СПОСОБ ГАЗОФАЗНОЙ ПОЛИМЕРИЗАЦИИ ОЛЕФИНОВ

Изобретение относится к способу газофазной полимеризации олефинов и полимеризации, проводимой в реакторе, имеющем взаимосвязанные полимеризационные зоны. Способ газофазной полимеризации α-олефинов CH2=CHR, где R представляет собой водород или углеводородный радикал, имеющий 1-12 углеродных атомов, осуществляют в первой и второй взаимосвязанных полимеризационных зонах. Один или более α-олефинов подают в присутствии катализатора. Растущие полимерные частицы проходят через первую из указанных зон (труба, идущая вверх) в условиях быстрого псевдоожижения, выходят из трубы, идущей вверх, и поступают во вторую из указанных полимеризационных зон (труба, идущая вниз), через которую они проходят вниз в уплотненной форме, выходят из трубы, идущей вниз, и повторно вводятся в указанную трубу, идущую вверх. Газовая смесь, присутствующая в трубе, идущей вверх, полностью или частично предотвращается от поступления в трубу, идущую вниз. Газообразная композиция внутри части трубы, идущей вниз, поддерживается ...

СПОСОБ ПОЛУЧЕНИЯ УГЛЕВОДОРОДНЫХ СМОЛ И ПРОДУКТОВ ИХ ГИДРИРОВАНИЯ

Группа изобретений относится к углеводородной смоле из по меньшей мере одного циклического диолефинового компонента и по меньшей мере одного ароматического компонента с этиленовой ненасыщенностью и способу ее получения, а также к ее применению в качестве добавки к лаку, модификатора пластика, для улучшения механических и динамических характеристик каучуковых продуктов, добавки и/или гидрофобизатора в битуме, модификатора и/или гидрофобизатора в полипропиленовых пленках, в частности BOPP-пленках, в косметических средствах, в печатных красках, усилителя клейкости для термоклея для применения в промышленности гигиенических изделий и для использования в упаковках для пищевых продуктов. Способ включает смесь мономеров, которая содержит по меньшей мере один циклический диолефиновый компонент и по меньшей мере один ароматический компонент с этиленовой ненасыщенностью с 8-13 атомами углерода, нагревают со скоростью нагревания от 0,5 до 10°С/с до температуры по меньшей мере 180°С. Причем смесь мономеров ...

СПОСОБ ПОЛИМЕРИЗАЦИИ ОЛЕФИНА

Изобретение относится к способу полимеризации олефина. Способ включает подачу циркуляционного газа в реактор. Циркуляционный газ содержит по меньшей мере один альфа-олефин и инертный газ. В реакционной зоне реактора альфа-олефин полимеризуют в полиолефин. Полученный полиолефин отводят из реактора. Реактор полимеризации образован из цилиндрической секции "а" основания, расположенной в его нижней части, и конической верхней секции "b", расположенной сверху цилиндрической секции основания и имеющей открытый верх. Коническая верхняя секция "b" имеет угол наклона 4-7° относительно перпендикулярной линии. Внутреннее пространство реактора разделено на реакционную зону А, которая представляет собой зону с псевдоожиженным слоем, в которой происходит полимеризация олефина, и свободную зону В, расположенную сверху от реакционной зоны А и имеющую отделенные от газовой фазы твердые частицы полиолефина. Высота псевдоожиженного слоя по меньшей мере составляет высоту цилиндрической секции "а" основания ...

ГАЗОФАЗНЫЙ СПОСОБ ПОЛИМЕРИЗАЦИИ ПРОПИЛЕНА

Изобретение относится к способу газофазной полимеризации пропилена, необязательно в смеси с другими олефинами. Описан способ гомополимеризации или сополимеризации пропилена с прочими олефинами, осуществляемый в присутствии каталитической системы. Каталитическая система включает (а) твердый компонент катализатора, содержащий Mg, Ti, галоген, электронный донор, выбранный из 1,3-диэфиров, и 10-85 мас.% олефинового полимера; (b) алкилалюминиевое соединение; и (c) внешнее электронодонорное соединение, выбранное из соединения кремния. Компоненты (b) и (c) берутся в таких количествах, чтобы молярное соотношение Al/(ED) составляло 2-200. Твердый компонент имеет средний размер частиц 10-100 мкм. Способ пригоден для получения полипропиленового продукта, имеющего хорошие морфологические свойства, высокую стереорегулярность и обладающего свойствами самозатухания, выборочно решая или смягчая вредные воздействия, вызванные полимеризацией мелких частиц катализатора. 11 з.п. ф-лы, 1 табл., 18 пр.

СИСТЕМА ОТБОРА ПРОБ ИЗ ЖИДКО-ТВЕРДОЙ СМЕСИ ДЛЯ ПЕТЛЕВОГО СУСПЕНЗИОННОГО РЕАКТОРА

Изобретение относится к способу и системе измерения характеристик жидкости в двухфазной смеси жидкой и твердой фаз. Описан способ эксплуатации системы, содержащей единственный петлевой суспензионный реактор-полимеризатор или два или более петлевых суспензионных реактора-полимеризатора с интегрированными системами отбора проб смеси жидкой и твердой фаз. Также описаны система и способ измерения характеристик смеси жидкой и твердой фаз жидкости в сосуде. Технический результат - быстрое и эффективное разделение твердой и жидкой фаз с обеспечением потока жидкости, свободного от твердых частиц, которые могут закупоривать или отрицательно влиять на аналитическое оборудование. 3 н. и 17 з.п. ф-лы, 2 ил., 1 табл.

СПОСОБ НЕПРЕРЫВНОГО СИНТЕЗА ДИЕНОВОГО ЭЛАСТОМЕРА

Изобретение относится к способу синтеза диеновых эластомеров в непрерывном режиме при высокой степени конверсии. Способ непрерывного синтеза диенового эластомера характеризуется тем, что включает следующие одновременные этапы: a) непрерывное введение в полимеризационный реактор, снабженный газовой фазой и оборудованный по меньшей мере одним средством перемешивания и разгрузочным устройством, по меньшей мере: i. одного или нескольких мономеров, подлежащих полимеризации, из которых по меньшей мере один мономер является сопряженным диеном, и ii. от 0 до 70 масс. % органического растворителя, в расчете на общую массу мономеров и растворителя, b) непрерывную полимеризацию мономера или мономеров, c) перемешивание полимеризационной среды путем непрерывного движения по меньшей мере одного средства перемешивания вокруг оси вращения, d) непрерывную выгрузку эластомерной массы на выходе с этапа полимеризации, e) непрерывную подачу выгруженной эластомерной массы на устройство резки и резка ее на частицы ...

ПОЛИМЕРНАЯ КОМПОЗИЦИЯ ДЛЯ УКУПОРОЧНЫХ СРЕДСТВ ДЛЯ КОНТЕЙНЕРА

Изобретение относится к полимерной композиции для формования и укупорочному средству для контейнера, содержащего такую полимерную композицию. Композиция содержит гомополимер этилена и сополимер этилена, содержащий сомономер, представляющий собой 1-бутен, в количестве от 0,60 до 0,65 мол.% по отношению к общему количеству мономера в сополимере этилена. Сополимер этилена имеет более высокую средневесовую молекулярную массу, чем гомополимер этилена, причем полимерная композиция имеет плотность в диапазоне 0,9553-0,9560 г/см3, скорость течения расплава MFR2от 0,72 до 0,78 г/10 мин в условиях проведения испытания при 190°C с нагрузкой 2,16 кг, средневесовую молекулярную массу от 150000 до 200000 г/моль, вязкость при угловой частоте 0,01 [1/с], η0,01при 190°С от 22371 до 24420 Па*с. При этом массовое соотношение гомополимера этилена к сополимеру этилена в полимерной композиции находится в диапазоне от 45:55 до 55:45. Полимерная композиция имеет полупериод изотермической кристаллизации, который ...

МУЛЬТИМОДАЛЬНАЯ ПОЛИЭТИЛЕНОВАЯ ПЛЕНКА

Изобретение относится к мультимодальной полиэтиленовой композиции для формования, в частности для пленок или геомембран. Композиция включает: (А) от 40 до 65% по массе полиэтилена с низкой молекулярной массой, имеющего средневзвешенную молекулярную массу (Mw) от 20000 до 90000 г/моль, причем полиэтилен с низкой молекулярной массой имеет значение MI2от 500 до 1000 г/10 мин согласно стандарту ASTM D 1238, (В) от 5 до 17% по массе полиэтилена со сверхвысокой молекулярной массой, имеющего средневзвешенную молекулярную массу (Mw) от более 1000000 до 5000000 г/моль, и (С) от 30 до 50% по массе полиэтилена с высокой молекулярной массой, имеющего средневзвешенную молекулярную массу (Mw) от более 150000 до 1000000 г/моль. Причем плотность полиэтилена со сверхвысокой молекулярной массой и полиэтилена с высокой молекулярной массой составляет величину в одном и том же диапазоне, и обе плотности находятся в диапазоне от 0,910 до 0,940 г/см3. Молекулярно-массовое распределение мультимодальной полиэтиленовой ...

СПОСОБ ПОЛИМЕРИЗАЦИИ

Изобретение относится к способу полимеризации олефинов в реакторной системе. Описан способ полимеризации мономера в по меньшей мере первом и втором реакторах, работающих последовательно. Способ включает контактирование первого потока, содержащего пар, полученный из выходящего потока, выгружаемого из второго реактора, с потоком сырья для второго реактора. Указанный первый поток отделяют от полимера, выгружаемого из второго реактора, при давлении 0,5 МПа (5 бар) или выше. Также первый поток, включающий пар, полученный из выходящего потока, выгружаемого из последующего реактора, контактирует с потоком сырья для второго реактора. Указанный поток сырья включает выходящий поток из первого реактора. Описан также способ обработки первого потока. Технический результат – получение способа полимеризации, обладающего высокой эффективностью для желаемых компонентов конечного полимера, например мономера, но низкую эффективность для других компонентов, например водорода. 2 н. и 14 з.п. ф-лы, 1 пр.

СПОСОБ И УСТРОЙСТВО ДЛЯ ОЧИСТКИ ГАЗА СО ВСТАВКОЙ ДЛЯ ФОРМИРОВАНИЯ МАССОГО ПОТОКА

Изобретение относится к введению и/или удалению газа из смеси твердая фракция/газ. Описано устройство, содержащее защитную конструкцию, размещенный в ней обратный конус и размещенный под обратным конусом элемент, имеющий размеры, обусловливающие продольное прохождение твердой фазы между элементом и защитной конструкцией с приблизительно постоянным профилем скорости в сечении. Элемент включает выступающую наружу от него юбку и трубопровод для передачи газа к находящейся ниже юбки области или от нее и/или выступающую вовнутрь от него юбку и трубопровод для передачи газа к находящейся над этой юбкой области или от нее. Описан также способ очистки газа из смеси твердая фаза/газ. Технический результат - получение постоянной в сечении скорости потока полимера через очистной резервуар для достижения одинакового времени нахождения в нем полимера и более равномерного распределения очистного газа в полимере. 2 н. и 14 з.п. ф-лы, 5 ил.

СПОСОБ ПЕРЕХОДА

Изобретение относится к способу перехода от получения первого полимера к получению второго полимера в газофазном реакторе с псевдоожиженным слоем или в реакторе с перемешиваемым слоем. Предложенный способ включает стадии: a) проведения первой реакции полимеризации в реакторе с использованием первой каталитической системы для полимеризации с получением первого полимера, b) остановки первой реакции полимеризации и удаления по меньшей мере большей части полимера из реактора, c) введения в реактор слоя затравки, содержащего не менее 50 част./млн загрязнителей, где во время хранения содержание загрязнителей в слое затравки поддерживали равным не менее 50 част./млн, но менее 500 част./млн загрязнителей, d) обработки слоя затравки в реакторе для уменьшения количества загрязнителей и e) проведения второй реакции полимеризации в реакторе с получением второго полимера. Технический результат – предложенный способ позволяет сразу после запуска второй реакции получать кондиционный полимерный продукт ...

Способ получения водорастворимых гомо- или сополимеров, включающих (мет)акриламид

Изобретение относится к способу получения водорастворимых гомо- или сополимеров, включающих (мет)акриламид, которые могут быть использованы в качестве загустителя, флокулянта, армирующего материала для бумаги, для извлечения нефти или для применения в горнодобывающей промышленности. Способ получения водорастворимых гомо- или сополимеров заключается в том, что к охлажденному до менее 5°С мономерному водному раствору, включающему воду, от 25 до 45% мас. этилен-ненасыщенных мономеров (А), от 0,1 до 2% мас. стабилизатора (В), азоинициатор (С) со значением 10 ч tот 40°С до 75°С, добавляют окислительно-восстановительный инициатор радикальной полимеризации (D). При этом водный мономерный раствор имеет значение рН <7. Мономерный раствор инертизируют. Далее проводят гель-полимеризацию водного мономерного раствора в адиабатических условиях. Температура начала полимеризации составляет менее 5°С. Под воздействием тепла смесь нагревается до температуры от 60°С до 100°С, образуя полимерный гель. Полученный ...

СПОСОБ ПОЛУЧЕНИЯ ЭЛАСТИЧНЫХ СОПОЛИМЕРОВ ЭТИЛЕНА И АЛЬФА-ОЛЕФИНОВ

Настоящее изобретение относится к способу для получения сополимеров этилена и α-олефина и к сополимерам, полученным этим способом, которые могут быть адаптированы для широкого ряда разнообразных применений, включая пленку, электропровода и термоплавкие клеи. Сополимеры имеют содержание (С3-С18) α-олефина от 10 мас.% до 45 мас.% сополимера, молекулярно-массовое распределение (Mw/Mn) от 1,5 до 3,0, и плотность 0,850-0,900 г/см. Способ получения сополимеров этилена и (С3-С18) α-олефина осуществляют в растворе при температуре сополимеризации от 80°С до 140°С в единственном реакторе или в непрерывных реакторах, соединенных последовательно или параллельно для 2-стадийных реакций. Каталитический состав содержит активатор и катализатор, в состав которого входит соединение с переходным металлом, представленное химической формулой (1)где Xпредставляет собойа остальные значения радикалов указаны в формуле изобретения. Заявленный способ для сополимеризации этилена с α-олефином позволяет получать сополимер ...

СПОСОБ ПОЛУЧЕНИЯ ПОЛИМЕРНЫХ ПОЛИОЛОВ

Настоящее изобретение относится к способу получения полимерного полиола в периодическом или полупериодическом режиме, где способ включает смешение базового полиола, одного или более этиленненасыщенных мономеров, инициатора полимеризации, необязательно, макромера и, необязательно, агента переноса цепи и полимеризацию полученной смеси при температуре от 50 до 200°С, где одно или более смешиваемых соединений подаются с температурой, которая находится в диапазоне от 50 до 150% от температуры (в °С), при которой осуществляется полимеризация. Также описаны полиол, получаемый указанным выше способом, способ получения полиуретанового пенопласта вспениванием композиции, включающей полимерный полиол по настоящему изобретению, сам пенопласт, получаемый таким способом, а также формованное изделие, включающее полиуретановый пенопласт. Технический результат - существенное сокращение времени цикла периодического процесса, сокращение продолжительности пусковой фазы, а также разрешение проблемы накипи и ...

ТРУБА ИЗ МУЛЬТИМОДАЛЬНОГО ПОЛИЭТИЛЕНА

Настоящее изобретение относится к способу производства композиции мультимодального полиэтилена в реакторной системе, композиции мультимодального полиэтилена, получаемой данным образом, а также к применению трубы, содержащей композицию мультимодального полиэтилена. Реакторная система включает первый реактор, установку для удаления водорода, расположенную между первым реактором и вторым реактором и включающую по меньшей мере одну емкость, соединенную с оборудованием для сбрасывания давления, предпочтительно выбираемым из вакуумного насоса, компрессора, газодувки, эжектора или их комбинации, второй реактор и третий реактор. При этом оборудование для сбрасывания давления делает возможным доведение рабочего давления до значений в диапазоне 104-130 кПа (абс.). Техническим результатом является повышение механических свойств полиэтиленовых композиций. 4 н. и 13 з.п. ф-лы, 4 табл.

УСТАНОВКА ПРЕДВАРИТЕЛЬНОГО ОБРАЗОВАНИЯ КАТАЛИТИЧЕСКОЙ КОМПОЗИЦИИ ДЛЯ ПОЛУЧЕНИЯ КАТАЛИТИЧЕСКОЙ КОМПОЗИЦИИ ДЛЯ ОЛИГОМЕРИЗАЦИИ ЭТИЛЕНА

Изобретение относится к установке предварительного образования катализатора олигомеризации этилена. Описана установка предварительного образования катализатора олигомеризации этилена, содержащая:первую емкость с первым впускным отверстием для газа, содержащую раствор сокатализатора и модификатора; вторую емкость с вторым впускным отверстием для газа, содержащую соединение хрома и лиганд; смеситель, соединенный трубопроводами с первой и второй емкостями, причем каждый трубопровод имеет клапан-регулятор расхода, который независимо представляет собой тепловой массовый расходомер или расходомер Кориолиса; причем смеситель соединен посредством трубопровода, имеющего клапан-регулятор расхода, с реактором олигомеризации; причем каждое впускное отверстие для газа соединено с первой емкостью и со второй емкостью, и причем первая емкость, вторая емкость, смеситель и клапаны-регуляторы расхода, по меньшей мере частично находятся в корпусе с регулируемой температурой; причем клапаны-регуляторы расхода ...

СИСТЕМА ДЛЯ ПРОВЕДЕНИЯ РЕАКЦИИ ПОЛУЧЕНИЯ ПОЛИЭТИЛЕНА С УВЕЛИЧЕНИЕМ МИКРОПОВЕРХНОСТЕЙ С ИСПОЛЬЗОВАНИЕМ ПОЛИМЕРИЗАЦИИ В РАСТВОРЕ

Изобретение относится к области получения полиэтилена, в частности к системе для проведения реакции получения полиэтилена с увеличением микроповерхностей с использованием полимеризации в растворе. Описана система для проведения реакции получения полиэтилена с использованием полимеризации в растворе, содержащая: реактор предварительной полимеризации (10) и реактор полимеризации (20), соединенные последовательно, а также устройство циркуляционной сушки полиэтилена для удаления остаточной влаги из материала, при этом реактор предварительной полимеризации снабжен генератором межфазных микроповерхностей (101) при предварительной полимеризации для диспергирования и разделения этилена на микропузырьки, выпускной канал для форполимера расположен на дне реактора предварительной полимеризации; реактор полимеризации снабжен первым генератором межфазных микроповерхностей (201), который соединен с выпускным каналом для форполимера, установлен на входе в реактор полимеризации и предназначен для диспергирования ...

УСТРОЙСТВО И СПОСОБ ДЛЯ ГАЗОФАЗНОЙ ПОЛИМЕРИЗАЦИИ

Группа изобретений относится к устройству для каталитической газофазной полимеризации олефинов, содержащему первую зону полимеризации для восходящего течения растущих частиц полимера в условиях быстрого псевдоожижения и переноса, вторую зону полимеризации для нисходящего течения растущих частиц полимера и зону разделения газ/твердое тело. Вторая зона полимеризации имеет верхнюю часть, присоединенную к зоне разделения, и нижнюю часть, присоединенную к верхней части, причем отношение высоты Н01 зоны разделения к диаметру D01 зоны разделения составляет от 2,5 до 4,5, отношение диаметра D01 зоны разделения к диаметру D03 верхней части второй зоны полимеризации составляет от 1,02 до 1,5, отношение диаметра D03 верхней части второй зоны полимеризации к диаметру D04 нижней части второй зоны полимеризации составляет от 1,2 до 2. Описан также способ выполнения каталитической газофазной полимеризации олефинов в данном устройстве. Технический результат – обеспечение эффективного разделения газ/твердое ...

УГЛЕВОДОРОДНАЯ СМОЛА И СПОСОБ ЕЕ ПОЛУЧЕНИЯ

Изобретение относится к области получения углеводородных смол, а именно к получению смолы с помощью термической сополимеризации циклического диолефионового соединения, имеющего от 5 до 11 атомов углерода и ароматического соединения, содержащего инден и/или С1-4-алкилинден, а также с по меньшей мере одним винилароматическим соединением. Полученная после полимеризации смола обладает PDI от 1 до менее 2,3 и от 4 до 20 вес.%, в расчете на общую массу углеводородной смолы, структурных единиц индена и/или С1-4-алкилиндена. Предложенное изобретение позволяет получать светлые углеводородные смолы, имеющие высокую совместимость с базовыми полимерами различных термоклеев, что позволяет использовать их в качестве усилителя клейкости. 7 н. и 21 з.п. ф-лы, 1 ил., 3 табл., 5 пр.

СПОСОБ ПОЛИМЕРИЗАЦИИ ОЛЕФИНОВ В ГАЗОФАЗНОМ РЕАКТОРЕ С ТРЕМЯ ИЛИ БОЛЕЕ ЗОНАМИ ПОЛИМЕРИЗАЦИИ

Изобретение относится к способу получения олефинового полимера в присутствии водорода в газофазном реакторе полимеризации. Реактор полимеризации имеет три или более зон полимеризации, где по меньшей мере две из зон полимеризации являются подзонами установки полимеризации, в которой растущие полимерные частицы стекают вниз в уплотненной форме. По меньшей мере одна зона полимеризации имеет соотношение водорода к суммарному объему олефинов, которое в 1,5 раза ниже, чем соотношение водорода к суммарному объему олефинов в зоне полимеризации, имеющей самое высокое соотношение водорода к суммарному объему олефинов и которое в 1,5 раза выше, чем соотношение водорода к суммарному объему олефинов в зоне полимеризации, имеющей самое низкое соотношение водорода к суммарному объему олефинов. Способ полимеризации олефинов позволяет простым образом осуществлять полимеризацию в трех или более зонах полимеризации в одном реакторе полимеризации и получать гомогенные мультимодальные олефиновые полимеры с ...

САМООЧИЩАЮЩИЙСЯ КОМПОЗИТНЫЙ МАТЕРИАЛ ДЛЯ ПРОИЗВОДСТВА ФОРМОВАННЫХ ДЕТАЛЕЙ ИНТЕРЬЕРА КУХНИ И ВАННОЙ КОМНАТЫ

Изобретение относится к самоочищающемуся композитному материалу, предназначенному для производства формованных деталей интерьера кухни и ванной комнаты. Самоочищающийся композитный материал по изобретению содержит от 50 до 85% масс. минеральных наполнителей на основе тригидрата оксида алюминия (ATH); от 10 до 30% сшиваемого полимера, содержащего полиэфирную смолу; фотокаталитический диоксид титана (TiO), диспергированный в сшиваемом полимере с массовым процентным содержанием 0,05 - 5% относительно массы сшиваемого полимера; средство для улучшения совместимости для связывания между фотокаталитическим TiOи сшиваемым полимером, причём указанное средство для улучшения совместимости TiOпредставляет собой силан; и сшивающиеся мономеры, чтобы обеспечить поперечную сшивку сшиваемого полимера посредством термической или химической полимеризации, а также к способу его изготовления. Вышеуказанный состав самоочищающегося композитного материала обеспечивает получение материала, который легок в термоформовании ...

СУСПЕНЗИОННЫЙ СПОСОБ ПОЛУЧЕНИЯ СОПОЛИМЕРОВ ЭТИЛЕНА В КАСКАДЕ РЕАКТОРОВ

Изобретение относится к способам получения сополимеров этилена в суспензии в каскаде реакторов. Предложен способ получения мультимодального сополимера этилена в суспензии в каскаде реакторов, содержащем первый реактор полимеризации и один или несколько последующих реакторов полимеризации, включающий: разделение суспензии, образованной в каскаде реакторов, на частицы мультимодального сополимера этилена и рекуперированную суспензионную среду; очистку части рекуперированной суспензионной среды в секции очистки для получения очищенных компонентов рекуперированной суспензионной среды; повторную подачу по меньшей мере некоторых или части очищенных компонентов рекуперированной суспензионной среды в первый реактор полимеризации каскада реакторов; в котором очищенные компоненты рекуперированной суспензионной среды повторно подаются в первый реактор полимеризации, который содержит разбавитель, и подвергаются каталитической гидрогенизации перед подачей в первый реактор полимеризации. Предложено также ...

ПРОИЗВОДСТВЕННАЯ УСТАНОВКА ДЛЯ ПОЛИМЕРИЗАЦИИ ЭТИЛЕНА ПРИ ВЫСОКОМ ДАВЛЕНИИ И СПОСОБ АВАРИЙНОГО ОСТАНОВА

Настоящее изобретение относится к производственной установке для полимеризации этилена при высоком давлении и способу аварийного останова в указанной производственной установке. Предложена производственная установка для полимеризации этилена при высоком давлении, содержащая многослойный трубчатый реактор, включающий соединенные между собой первые трубчатые конструкции для переноса реакционной смеси высокого давления, в котором первые трубчатые конструкции представляют собой первые прямые трубы или первые колена, в котором соединенные между собой первые трубчатые конструкции образуют по меньшей мере один извилистый первый трубопровод и по меньшей мере один первый предохранительный клапан, присоединенный к указанному первому трубопроводу, многослойный трубчатый реактор, включающий соединенные между собой вторые трубчатые конструкции для переноса реакционной смеси высокого давления, в котором вторые трубчатые конструкции представляют собой вторые прямые трубы или вторые колена, в котором указанные ...

СПОСОБ ПРОИЗВОДСТВА α-ОЛЕФИНОВОГО НИЗКОМОЛЕКУЛЯРНОГО ПОЛИМЕРА И УСТАНОВКА ДЛЯ ПРОИЗВОДСТВА

Изобретение относится к способу и установке для производства α-олефинового низкомолекулярного полимера путем подвергания α-олефина низкомолекулярной полимеризации в присутствии катализатора в жидкофазной части в реакторе. Газ отбирают из газофазной зоны реактора, вводят его для охлаждения в кожухотрубный теплообменник и обеспечивают циркулирование и подачу полученной сконденсированной жидкости в реактор. Газ подают из отверстия для подачи газа с плотностью 20 кг/ми более при расходе газа 1 м/с и более. Теплообменник включает струйные сопла для подачи распыленных капель, расположенные между отверстием для подачи газа и трубной перегородкой. Струйные сопла расположены в пяти и более позициях при расчете на 1,00 мплощади поверхности трубной перегородки. Технический результат – подавление образования полимера на поверхности верхней трубной перегородки кожухотрубного теплообменника для теплоотвода для обеспечения стабильного проведения непрерывной операции в течение продолжительного периода ...

СПОСОБ ПОЛИМЕРИЗАЦИИ ОЛЕФИНОВ В ГАЗОФАЗНОМ РЕАКТОРЕ, ВКЛЮЧАЮЩЕМ РЕАКТОР ВОСХОДЯЩЕГО ПОТОКА И РЕАКТОР НИСХОДЯЩЕГО ПОТОКА

Изобретение относится к способу получения полимера этилена, включающему гомополимеризацию этилена или сополимеризацию этилена с одним или несколькими сомономерами в реакторе газофазной полимеризации. Реактор газофазной полимеризации имеет реактор восходящего потока, в котором растущие полимерные частицы движутся вверх в условиях псевдоожижения, быстрого псевдоожижения или других режимах транспортировки, и реактор нисходящего потока, в котором растущие частички полимера стекают вниз в уплотненной форме. В реакторе нисходящего потока остаточный объем полимерных частиц составляет 55- 80 мас.% от остаточного объема полимерных частиц в реакторе газофазной полимеризации. Технический результат – предотвращение и минимизация образования агломератов, комков или отложений на стенке реактора. 14 з.п. ф-лы, 1 ил., 1 табл., 3 пр.

СПОСОБ ПОЛИМЕРИЗАЦИИ, ВКЛЮЧАЮЩИЙ ДОЗИРОВКУ ИНИЦИАТОРОВ

... 1. Способ полимеризации, в котором, по меньшей мере, один пероксид с периодом полураспада от 1 до 0,001 ч при температуре полимеризации в момент добавления дозируют в реакционную смесь при температуре полимеризации, и в котором, по меньшей мере, в течение части периода дозирования пероксида i) охлаждающее устройство реактора поддерживают, по существу, при максимальной охлаждающей способности, и ii) добавляемое количество инициатора активно регулируют при помощи регулятора температуры, достигая, таким образом, желательной температуры полимеризации и поддерживая ее в пределах 0,3°C от указанной температуры полимеризации. 2. Способ полимеризации по п.1, в котором температуру полимеризации поддерживают в пределах 0,2°C, предпочтительно в пределах 0,1°C от указанной температуры полимеризации. 3. Способ полимеризации из п.1 или 2, в котором регулятор температуры регулирует температуру реакционной смеси, осуществляя текущий контроль температуры реакционной смеси и/или давления газовой фазы в полимеризационном ...

СПОСОБ СВОБОДНОРАДИКАЛЬНОЙ ПОЛИМЕРИЗАЦИИ ИЛИ СШИВАНИЯ В ПРИСУТСТВИИ ВЫБРАННОГО ОРГАНИЧЕСКОГО ПЕРОКСИДА, ПОЛУЧЕННОГО СПОСОБОМ EX SITU

... 1. Способ свободнорадикальной полимеризации или сшивания, в котором, по меньшей мере, один полимеризуемый мономер или, по меньшей мере, одно сшиваемое соединение взаимодействуют в присутствии, по меньшей мере, одного органического пероксида, выбранного из группы, состоящей из ди(н-пропил)пероксидикарбоната, ди(втор-бутил)пероксидикарбоната, ди(2-этилгексил)пероксидикарбоната, 1,1-диметил-3-гидроксибутилпероксинеодеканоата, α-кумилпероксинеодеканоата, α-кумилпероксинеогептаноата, трет-амилпероксинеодеканоата, трет-бутилпероксинеодеканоата, трет-амилпероксипивалата, трет-бутилпероксипивалата, 2,5-диметил-2,5-ди(2-этилгексаноилперокси)гексана, трет-амилперокси-2-этилгексаноата, трет-бутилперокси-2-этилгексаноата, трет-амилпероксиацетата, трет-бутилпероксиацетата, трет-амилпербензоата, трет-бутилпербензоата, OO-трет-амил-O-(2-этилгексил)монопероксикарбоната, ОО-трет-бутил-O-изопропилмонопероксикарбоната, OO-трет-бутил-1-(2-этилгексил)монопероксикарбоната, поли(трет-бутилпероксикарбонат)полиэфира ...

СПОСОБ ПОЛИМЕРИЗАЦИИ ЭТИЛЕНА С УСОВЕРШЕНСТВОВАННОЙ СИСТЕМОЙ ПОДАЧИ ЭТИЛЕНА

Изобретение относится к способу полимеризации этилена. Описан способ получения полиэтилена путем полимеризации в этиленовой суспензии в одном или нескольких С-Сальфа-олефинах. Полимеризация проходит при температуре 60-95°С и давлении 0,15-3 МПа. Полимеризация осуществляется в присутствии катализатора полимеризации в цилиндрическом реакторе полимеризации. Реактор имеет внутренний диаметр D и оснащен мешалкой для перемешивания содержимого реактора. Этилен подается в реактор системой впрыска этилена. Система впрыска содержит одно или несколько сопел, которые проходят через нижнюю крышку реактора или через стенку реактора и выступают внутрь реактора на величину 0,02-0,5 внутреннего диаметра D. Этилен выходит из сопла со скоростью на выходе 10-200 м/сек. Технический результат – уменьшение обрастания внутренних деталей реактора за счет усовершенствованной системы подачи этилена. 14 з.п. ф-лы, 5 ил.

СПОСОБ ПОЛИМЕРИЗАЦИИ В ПРИСУТСТВИИ ДОБАВКИ, СНИЖАЮЩЕЙ СТАТИСТИЧЕСКИЕ ЗАРЯДЫ

Изобретение относится к способу получения полиолефинов путем полимеризации олефинов в присутствии катализатора полимеризации. Полимеризацию осуществляют в присутствии добавки, снижающей статические заряды. Добавка, снижающая статический заряд, включает полимер, полученный из алкиленоксида, содержащего в среднем 10-200 повторяющихся звеньев -(CH-CHR-O)-. Полимер, полученный из алкиленоксида, представляет собой статистический сополимер этиленоксида и другие алкиленоксиды. Соотношение n:m повторяющихся звеньев –(CH-CH-O)–, полученных из этиленоксида, к повторяющимся звеньям–(CH-CHR'-O)–, полученным из других алкиленоксидов, составляет 6:1-1:1. Концевые группы полимера, полученного из алкиленоксида, представляют собой группы –OH. Технический результат – предотвращение электростатического заряда и уменьшение образование листового покрытия стенок или отложения полимерных агломератов в реакторе полимеризации. 14 з.п. ф-лы, 1 ил., 1 табл., 4 пр.

СПОСОБ ПОЛИМЕРИЗАЦИИ В ОБЪЕМЕ ДЛЯ ПОЛУЧЕНИЯ ПОЛИДИЕНОВ

Изобретение относится к способу полимеризации в массе для получения полидиенов. Способ осуществляют путем обеспечения по меньшей мере одного диенового мономера (DM) и необязательно по меньшей мере одного сомономера (СОМ). Проводят контактирование по меньшей мере одного диенового мономера (DM) и необязательно по меньшей мере одного сомономера (СОМ) с каталитической системой (CS) с образованием реакционной смеси (RM). Реакционную смесь (RM) полимеризуют по меньшей мере в одном корпусе реактора (RV). Реакционная смесь (RM) содержит растворитель, разбавитель и/или диспергатор в количестве ≤10 мас.% от общей массы реакционной смеси (RM). Коэффициент превращения диенового мономера (DM) и необязательно сомономера (СОМ) составляет ≥80%. Реакционная смесь (RM) содержит по меньшей мере один диеновый мономер (DM) в количестве ≥50,0 мас.%. Способ полимеризации в массе для получения диенов обеспечивает высокую степень превращения мономера по меньшей мере в 80% и приводит к выходу полидиенов с улучшенными ...

СПОСОБ ПОЛУЧЕНИЯ ГОМОПОЛИМЕРОВ ИЛИ СОПОЛИМЕРОВ ЭТИЛЕНА

Изобретение относится к способу получения гомополимеров или сополимеров этилена. Описан способ получения гомополимеров или сополимеров этилена в установке, содержащей трубчатый реактор высокого давления и предварительный нагреватель. Реакционная текучая среда, введенная в реактор, на входе в реактор нагревается в предварительном нагревателе, а средняя скорость реакционной текучей среды в предварительном нагревателе ниже, чем средняя скорость реакционной текучей среды в трубчатом реакторе на входе в реактор. Соотношение средней скорости реакционной текучей среды в трубчатом реакторе к средней скорости реакционной текучей среды в предварительном нагревателе составляет от 1,5:1 до 5:1. Технический результат - получение ПЭНП с более высокой глубиной превращения этилена за реакторный цикл и лучшими оптическими свойствами. 13 з.п. ф-лы, 1 табл., 3 пр., 3 ил.

ТРУБА ИЗ МУЛЬТИМОДАЛЬНОГО ПОЛИЭТИЛЕНА

Изобретение относится к композиции мультимодального полиэтилена. Композиция мультимодального полиэтилена содержит (А) 51-58 мас.ч. низкомолекулярного полиэтилена или среднемолекулярного полиэтилена, полученного путем полимеризации в первом реакторе, (В) 12-21 мас.ч. первого высокомолекулярного полиэтилена или первого сверхвысокомолекулярного полиэтилена, полученного путем полимеризации во втором реакторе, и (С) 27-33 мас.ч. второго высокомолекулярного полиэтилена или второго сверхвысокомолекулярного полиэтиленового сополимера, полученного путем полимеризации в третьем реакторе. Полиэтилен, полученный в каждом реакторе, обладает отличающейся молекулярной массой. Соотношение Mw/Mn между среднемассовой молекулярной массой Mw композиции мультимодального полиэтилена и среднечисленной молекулярной массой Mn композиции мультимодального полиэтилена находится в диапазоне 10-23. Композиция мультимодального полиэтилена характеризуется высокой стойкостью к ударным нагрузкам по Шарпи, улучшенным балансом ...

СПОСОБЫ ОПРЕДЕЛЕНИЯ ЗНАЧЕНИЯ ТЕМПЕРАТУРЫ, ХАРАКТЕРИЗУЮЩИЕ ЛИПКОСТЬ СМОЛЫ, НА ОСНОВЕ ДАННЫХ МОНИТОРИНГА РЕАКЦИИ ПОЛИМЕРИЗАЦИИ

... 1. Способ, включающий этапы, на которых ! а) осуществляют мониторинг реакции полимеризации, в результате которой в реакторе с псевдоожиженным слоем получают полимерную смолу, причем контрольная температура плавления в сухом состоянии является показателем характера изменений свойств в процессе плавления смолы в сухом состоянии, и ! б) на основе данных, отражающих по меньшей мере один подлежащий мониторингу параметр реакции, определяют в режиме реального времени пониженную контрольную температуру плавления, характеризующую изменение свойств полимерной смолы в процессе плавления в том виде, в котором она присутствует в реакторе, и по меньшей мере, по существу, равную разности между контрольной температурой плавления в сухом состоянии и величиной (D) понижения контрольной температуры плавления, представляющей собой температуру, на которую контрольная температура плавления в сухом состоянии понижается за счет присутствия в реакторе вместе со смолой разбавителя. ! 2. Способ по п.1, в котором ...

СПОСОБ И УСТАНОВКА ДЛЯ ПОЛУЧЕНИЯ ПОЛИМЕРОВ И СОПОЛИМЕРОВ НА ОСНОВЕ ЭТИЛЕНА

... 1. Способ получения полимеров и сополимеров этилена, включающий следующие стадии: сжатие этилена в первичном компрессоре, имеющем производительность по крайней мере 55 т/ч, за которым следует смешивание этого этилена с возвратным этиленом, дополнительное сжатие смешанного этилена до давления, составляющего по крайней мере 2300 бар, при производительности по крайней мере 120 т/ч во вторичном компрессоре; нагревание по крайней мере части сжатого этилена до температуры, составляющей, по крайней мере, 95°С, и введение этого нагретого этилена в переднюю часть трубчатого реактора, имеющего максимальный внутренний диаметр по крайней мере 65 мм и длину по крайней мере 1500 м, введение инициатора в трубчатый реактор по крайней мере в трех отдельных местах, что определяет по крайней мере три реакционные зоны; полимеризацию этилена, охлаждение реакционной смеси по крайней мере в первых двух реакционных зонах, так, что по крайней мере 28% мономера превращается в полимер; поддержание падения давления ...

КОНТЕЙНЕР ИЗ МУЛЬТИМОДАЛЬНОГО ПОЛИЭТИЛЕНА

СПОСОБ ПОЛУЧЕНИЯ ПОЛИОЛЕФИНОВ

СПОСОБ ЭФФЕКТИВНОЙ ПРОДУВКИ ПОЛИМЕРНЫХ ЧАСТИЦ

СПОСОБ И СИСТЕМА УПРАВЛЕНИЯ УСТАНОВКОЙ ПО НЕПРЕРЫВНОМУ ПРОИЗВОДСТВУ ПОЛИМЕРА

ПОЛУЧЕНИЕ ПОЛИМЕРОВ НА ОСНОВЕ ПРОПИЛЕНА С ВЫСОКИМ СОДЕРЖАНИЕМ СОМОНОМЕРА

СПОСОБ СОПОЛИМЕРИЗАЦИИ ЭТИЛЕНА И СЛОЖНЫХ ЭФИРОВ ВИНИЛОВОГО СПИРТА

ВВЕДЕНИЕ УЛАВЛИВАТЕЛЯ

СПОСОБ УЛУЧШЕННОГО ПОЛУЧЕНИЯ РЕАКЦИОННОСПОСОБНЫХ МОНОМЕРОВ ПОСРЕДСТВОМ МЕМБРАННОЙ ФИЛЬТРАЦИИ

СПОСОБЫ ПРИГОТОВЛЕНИЯ КАТАЛИЗАТОРОВ

СПОСОБ

... 1. Способ полимеризации, включающий следующие стадии:1) полимеризация мономера и сомономера по реакции полимеризации,2) отведение выходящего потока, включающего твердый полимер и смесь, включающую непрореагировавший мономер и непрореагировавший сомономер, и направление выходящего потока в систему извлечения при высоком давлении, причем давление в указанной системе извлечения при высоком давлении составляет, по крайней мере, 0,5 МПа, и указанная система извлечения при высоком давлении включает:а) стадию разделения при высоком давлении для отделения пара, включающего непрореагировавший мономер и непрореагировавший сомономер, от указанных твердых веществ иб) рециркуляционную систему при высоком давлении, где часть пара направляют в рециркуляционную систему реакции полимеризации,3) направление твердых веществ из системы извлечения при высоком давлении в систему извлечения при низком давлении, причем давление в указанной системе извлечения при низком давлении составляет менее 0,5 МПа, и указанная ...

СИСТЕМА И СПОСОБ ПОЛУЧЕНИЯ КАТАЛИЗАТОРА

... 1. Система, содержащаямешалку, расположенную внутри резервуара катализатора полимеризации и выполненную с возможностью смешивания или растворения по меньшей мере части или всего катализатора полимеризации и растворителя с образованием раствора катализатора полимеризации;нагревательную систему, соединенную с резервуаром катализатора полимеризации и выполненную с возможностью поддержания температуры раствора катализатора полимеризации выше определенного порога;реактор предварительного контакта, выполненный с возможностью приема сырьевых потоков, содержащих активатор и раствор катализатора полимеризации, из резервуара катализатора полимеризации с образованием каталитического комплекса; итрубопровод, выполненный с возможностью переноса каталитического комплекса из выпускного отверстия реактора предварительного контакта в реактор.2. Система по п. 1, отличающаяся тем, что реактор предварительного контакта содержитвторую мешалку, расположенную внутри реактора предварительного контакта и выполненную ...

OPAKES HOCHSCHLAGFESTES METHYLMETHACRYLAT-BUTADIEN-STYROL-POLYMER ZUR VERBESSERUNG DER SCHLAGFESTIGKEIT VON POLYVINYLCHLORID UND VERFAHREN ZU DESSEN HERSTELLUNG

Die vorliegende Erfindung gibt ein opakes hochschlagfestes Methylmethacrylat-Butadien-Styrol(MBS)-Polymer zur Verbesserung der Schlagfestigkeit von Polyvinylchlorid (PVC) und ein Herstellungsverfahren dafür an und gehört zum technischen Gebiet der Herstellung von PVC-Zusätzen. Das durch die vorliegende Erfindung angegebene MBS schließt, bezogen auf Masse, die folgenden Komponenten ein: 80-95 % Kernschicht;, 4-20 % Schalenschicht und 0,001-0,05 % Schutzkolloid, wobei die Kernschicht ein Polymer aus Butadien (B) und Styrol (S) ist; die Schalenschicht eines oder ein Copolymer aus zwei oder drei von S, Acrylat und Methylmethacrylat (MMA) ist; das Schutzkolloid eines oder eine Verbindung aus zwei oder drei von Polyvinylalkohol (PVA), Gelatine und Hydroxypropylmethylcellulose (HPMC) einschließt. Die vorliegende Erfindung löst die Probleme der geringen Schlagfestigkeit in dem heutigen MBS-Produkt und der schwierigen Koagulation oder Versprühung im Nachbehandlungsprozess.

VERFAHREN ZUM ANBRINGEN VON ANTIFOULINGMITTELN

Chemical reactions

PROCEDURE FOR THE CONTROLLING OF THE POLYMER RIVER DURING A POLYMERIZATION PROCESS

PROCEDURE FOR THE PRODUCTION OF WATER-ABSORBING POLYMER PARTICLES BY POLYMERIZATION OF DROPS OF A MONOMER SOLUTION

PROCEDURE FOR THE IMPROVEMENT OF THE COPOLYMERISATION OF ETHYLS AND OLEFIN MORE COMONOMER IN A LOOP POLYMERIZATION REACTOR

PROCEDURE FOR THE TRANSFORMATION OF A SCHLAUFENREAKTORS

SUSPENSION POLYMERIZATION PROCEDURE

PROCEDURE FOR THE GASEOUS PHASE POLYMERIZATION OF OLEFINEN

POLYMERIZATION PROCEDURE

POLYMERIZATION PROCEDURE

SEMIKONTINUIERLICH OPERATION PROCEDURE FOR THE PRODUCTION OF COPOLYMERS

PRODUCTION OF POLYMERS IN A CONICAL REACTOR

ARRANGEMENT FOR THE TREATMENT OF AN POLYMERIZATION-ABLE MATERIAL

PROCEDURE AND DEVICES FOR POLYMERIZING

PROCEDURE AND DEVICE FOR THE PRODUCTION OF POLYMERS

PROCEDURE FOR THE PRODUCTION MECHANICAL OF STABLE OF WATER-ABSORBING POLYMER PARTICLES

PROCEDURE AND DEVICE FOR THE EXECUTION OF POLYMERIZATION PROCESSES

POLYMERIZATION PROCEDURE WITH DOSAGE OF INITIATORS

Polymer composition for container closures

Abstract The present invention relates to a polymer composition comprising an ethylene homopolymer and an ethylene copolymer having a comonomer content comprising a comonomer in an amount of at least 0.55 mol% with respect to the total amount of monomer in the ethylene copolymer, wherein the ethylene copolymer has a higher weight average molecular weight than the ethylene homopolymer, the polymer composition has a density in the range of 0.950-0.965 g/cm, a melt flow rate (MFR2) of at least 0.3 g/10 minutes, a weight average molecular weight of at least 100,000 g/mol, a and viscosity at an angular frequency of 0.01 [1/s], n o.o1 of at least 20,000 Pa.s wherein; the polymer composition has an Isothermal Crystallization Half-Time, ICHT which is less than 10 minute at 123 C and a Full Notch Creep Test, FNCT of at least 60 hours.

Multimodal polyethylene thin film

The present invention relates to a reactor system for a multimodal polyethylene polymerization process, comprising; (a) a first reactor; (b) a hydrogen removal unit arranged between the first reactor and a second reactor comprising at least one vessel connected with a depressurization equipment, preferably selected from vacuum pump, compressor, blower, ejector or a combination, thereof, the depressurization equipment allowing to adjust an operating pressure to a pressure in a range of 100 - 200 kPa (abs); (c) the second reactor; and. (d) a third reactor and the use of a film thereof.

Method for producing vinyl chloride resin that prevents scaling

Scale forms inside piping that connects polymerization reactors for producing vinyl chloride resins. As scale growth increases, the interior of the piping becomes blocked, hindering the polymerization process. Reaction control is particularly difficult if the safety valve connection piping is blocked. Therefore, it is necessary to disassemble the connection piping and clean the interior thereof at regular intervals. Moreover, in such instances, there is a possibility that vinyl chloride monomer gas will escape from the system, which is undesirable. Provided is a method of production with which a countermeasure for preventing such events is performed. The connection piping in the upper portion of the polymerization reactor is consolidated, and nitrogen piping 21 is joined to the connection piping 20 and filled with an amount of nitrogen corresponding to the piping volume. It is thereby possible to cause vinyl chloride monomer gas, which is the substance that causes scale to form, to be forced ...

Two stage methods for processing adhesives and related compositions

Methods for forming melt processable, actinic radiation polymerizable and crosslinkable adhesives are described. In certain versions, the adhesives or pre-adhesive compositions include two initiators and are polymerized and/or crosslinked by exposure to actinic radiation such as UV light or electron beam radiation. Also described are pre-adhesive compositions including polymerizable monomers, articles including the adhesives, and various methods and systems related to the adhesives and their application. In addition, various apparatuses are described for polymerizing or crosslinking the compositions. Page 41 of 41 12366803 1 (GHMatters) P109455.AU.2 ...

Process for producing aqueous polyacrylamide solutions

Process for producing aqueous polyacrylamide solutions by polymerizing an aqueous solution comprising at least acrylamide thereby obtaining an aqueous polyacrylamide gel and dissolving said aqueous polyacrylamide gel in water, wherein the manufacturing steps are allocated to two different locations A and B and the process comprises the step of transporting an aqueous polyacrylamide gel hold in a transportable polymerization unit from a location A to a location B. Modular, relocatable plant for manufacturing aqueous polyacrylamide solutions wherein the units of the plant are located at two different locations A and B.

Manufacture of fully recyclable foamed polymer from recycled material

IMPROVED PUMPING APPARATUS AND PROCESS FOR SLURRY POLYMERIZATION IN LOOP REACTORS

Effervescent nozzle for catalyst injection

Apparatus for high throughput chemical reactions

Device and method for producing moulded bodies from thermoplastic polymers

Two stage methods for processing adhesives and related compositions

Methods for forming melt processable, actinic radiation polymerizable and crosslinkable adhesives are described. In certain versions, the adhesives or pre-adhesive compositions include two initiators and are polymerized and/or crosslinked by exposure to actinic radiation such as UV light or electron beam radiation. Also described are pre-adhesive compositions including polymerizable monomers, articles including the adhesives, and various methods and systems related to the adhesives and their application. In addition, various apparatuses are described for polymerizing or crosslinking the compositions.

Non-extrusion process for functionalization of low viscosity polyolefins

A process to form a first composition comprising a functionalized olefin-based polymer comprises: a) polymerizing a composition comprising an olefin to form a reaction product comprising an olefin-based polymer; b) subjecting at least a portion of the reaction product to at least one devolatilization to form a polymer-rich melt, wherein step b) occurs downstream from and in-line with step a); and c) reacting at least a portion of the polymer-rich melt with at least one functionalization agent and, optionally, at least one free-radical initiator to form the first composition, wherein step c) occurs downstream from and in-line with step b), wherein "the viscosity of the functionalized olefin-based polymer (177°C/350°F)" to "the viscosity of the olefin-based polymer (177°C/350°F)" is from 0.1 to 5.0.

Process and apparatus for manufacture of processable polyvinyl alcohol

The invention describes a method for the manufacture of a plasticised polyvinyl alcohol polymer mixture, the method comprising the steps of: introducing a polyvinyl alcohol polymer comprising at least 98wt% polyvinyl alcohol or a blend of the polymer into a mixing reactor; wherein the mixing reactor comprises a blending chamber having a primary inlet, a primary outlet and at least two inter-engaging components extending between the primary inlet and primary outlet, the components being arranged to apply a shearing force to the polymer while the polymer is conveyed by the components from the inlet through a reaction zone to the outlet; one or more secondary inlets located downstream from the primary inlet for introducing reactants comprising a processing agent and a plasticiser to the chamber to form a reaction mixture; wherein the blending chamber comprises a plurality of heated regions arranged so that the mixture is subjected to a controlled temperature profile; a secondary outlet located ...

Ethylene-vinyl acetate-acrylic acid graft copolymer production plant

Ethylene-vinyl acetate-acrylic acid graft copolymer production plant Abstract 5 Ethylene-vinyl acetate-acrylic acid graft copolymer production plant, including: mixing tank (DI01), kneader (D102), impregnation and penetration device (F101), reactor (D103), water scrubber (E101), filter (M10), dryer (LIO); among them, kneader (D102) is connected respectively to mixing tank (DI01) and impregnation and penetration device (F101), water scrubber (E10) is connected respectively to 10 reactor (D103) and filter (M101); among them, jacket capacity of mixing tank (D101) is 260-270 L. Figure 1 -- D KEl CIL* Figure ...

Acrylonitrile-styrene random copolymer production plant

Acrylonitrile-styrene random copolymer production plant Abstract 5 Acrylonitrile-styrene random copolymer production plant, including: preheater (LIO), filter (MIO), mixer (DI01), polymerizer (D102), condenser (ClOl), devolatilization device (L102), devolatilization device (L103), recovery tank (F101), material pump (JI01); among them, mixer (DI01) is connected respectively to filter (MIO) and polymerizer (D102), devolatilization device (L102) is connected 10 respectively to polymerizer (D102) and devolatilization device (L103); among them, nominal volume of mixer (DI01) is 330-360 L. Figure 1 :tl 4-4 L4 z L4-4 -a Figur I1- ...

APPARATUS FOR HIGH THROUGHPUT CHEMICAL REACTIONS

Apparatus, systems, chips, and methods of performing a large number of simultaneous chemical reactions are provided herein. The chips of the invention comprise addressable units that can be addressed according to the temperature of the reaction to be run. The subject apparatus, systems, and chips are particularly suited for performing polymerase chain reactions on thousands of nucleic acid sequences, up to and including sequences of an entire genome of an organism of interest.

PROCESS FOR THE CONTINUOUS PRODUCTION OF GEL FREE POLYMERS, AND POWDER AND LIQUID COATING APPLICATIONS CONTAINING GEL FREE POLYMERS

A process is disclosed for a continuous, high temperature polymerization process for preparing a gel free polymeric product. The process comprises continuously charging into a reactor at least one monomer such that the reactor is filled to 100 percent of its usable volume. The reactor is maintained at an effective temperature for an effective period of time to cause polymerization of the monomers into a polymeric product, such that the polymeric product is formed substantially free of gel particles.

CHEMICAL REACTIONS

The invention relates to a method of assembling apparatus (110) for containing reagents for a chemical reaction. The apparatus comprises an elongate housing (112) and a receptacle (114). The elongate housing (112) may include a cooling means (116), and end fittings (118, 120) which may include ports where fluids may be introduced and/or removed. Specifically, the method relates to the securement of a receptacle relative to the outwardly facing surface of the housing.

DUAL COMPOSITION BLOCK COPOLYMERS

Dual composition block copolymers made from conjugated diene and monovinyl aromatic monomers in batch organolithium initiated polymerization show advantageous performance in the production of crosslinked microcellular rubber compounds and pressure sensitive hot melt adhesives. The dual composition block copolymers are partially coupled with a coupling agent linking inner monovinyl aromatic blocks. Their un-coupled low molecular weight fraction has greater monovinyl aromatic repeating unit content than their coupled high molecular weight fraction. Crosslinked microcellular rubber articles made from these copolymers exhibit lower density, smaller and more homogeneous cell size, higher softness and higher resiliency than prior art block copolymers. Rubber compounding of formulations comprising the copolymers proceed at slightly lower torque and slightly lower temperature than with prior art block copolymers. Pressure sensitive hot melt adhesives formulated with the dual composition block copolymers ...

POLYETHYLENE COMPOSITION FOR FILMS

A polyethylene composition particularly suited for producing blown films, having the following features: 1) density from 0.948 to 0.960 g/cm3; 2) ratio MIF/MIP from 20 to 40; 3) MIF from 6 to less than 15 g/10 min.; 4) HMWcopo index from 0.5 to 3.5; ) long-chain branching index, LCBI, equal to or lower than 0.82; 6) ?0.02 of equal to or less than 150000.

METHOD OF OLEFIN POLYMERIZATION USING ALKANE-SOLUBLE NON-METALLOCENE PRECATALYST

A method of polymerizing an olefin monomer to make a polyolefin composition comprising a polyolefin polymer, the method comprising contacting a solution of an alkane-soluble non-metallocene precatalyst dissolved in an alkane solvent with an activator so as to make a trim catalyst comprising an alkane-soluble non-metallocene catalyst, feeding the trim catalyst, as a solution in an alkane solvent or supported on a support material as a dry powder or a slurry thereof in an alkane solvent, into a polymerization reactor, and polymerizing the olefin monomer with the trim catalyst in the polymerization reactor, thereby making the polyolefin composition.

IN-LINE BLENDING PROCESS

An in-line blending process for polymers comprising: (a) providing two or more reactor-low pressure separator units (1,7) in parallel configuration, each reactor-low pressure separator unit comprising one reactor (2,8) fluidly connected to one low pressure separator (3,9) downstream and further a recycling line (5,11) connecting the low pressure separator (3,9) back to the corresponding reactor (2,8); (b) polymerizing olefin monomers having two or more carbon atoms in each of the reactors (2,8) in solution polymerisation; (c) forming an unreduced reactor effluents stream including a homogenous fluid phase polymer-monomer-solvent mixture in each of the reactors (2,8), (d) passing the unreduced reactor effluents streams from each of the reactors (2,8) through the corresponding low pressure separators (3,9), whereby the temperature and pressure of the low pressure separators (3,9) is adjusted such that a liquid phase and a vapour phase are obtained, whereby yielding a polymer-enriched liquid ...

SOLID CATALYST FOR THE PREPARATION OF NUCLEATED POLYOLEFINS

The present invention is directed to solid catalyst particles comprising a Ziegler-Natta catalyst and a polymeric nucleating agent. Further, the present invention is also directed to a process for the preparation of said solid catalyst particles, the use of said solid catalyst particles in a process for the manufacture of a polymer and a polyolefin obtained in the presence of said solid catalyst particles.

OLEFIN POLYMERIZATION PROCESS IN A GAS-PHASE REACTOR HAVING THREE OR MORE POLYMERIZATION ZONES

Process for preparing an olefin polymer in the presence of hydrogen in a gas-phase polymerization reactor comprising three or more polymerization zones and at least two thereof are sub-zones of a polymerization unit, in which the growing polymer particles flow downward in a densified form, wherein at least one polymerization zone has a ratio of hydrogen to the sum of olefins which is by a factor of at least 1.5 lower than the ratio of hydrogen to the sum of olefins in the polymerization zone having the highest ratio of hydrogen to the sum of olefins and which is by a factor of at least.5 higher than the ratio of hydrogen to the sum of olefins in the polymerization zone having the lowest ratio of hydrogen to the sum of olefins.

BULKPOLYMERISATION PROCESS FOR THE PREPARATION OF POLYDIENES

The present invention is directed at a bulkpolymerisation process for the preparation of a polymer (P) comprising the steps of: (i) providing at least one diene monomer (DM) and optionally at least one comonomer (COM); (ii) contacting the at least one diene monomer (DM) and optionally the at least one comonomer (COM) with a catalyst system (CS) forming a reaction mixture (RM); (iii) polymerizing the reaction mixture (RM) comprising the at least one diene monomer (DM) and optionally the at least one comonomer (COM) in at least one reactor vessel (RV); (iv) isolating the polymer (P) obtained from the at least one reactor vessel (RV); wherein the reaction mixture (RM) comprises solvent, diluent and/or dispersant in an amount of = 10 wt.-%,based on the weight of the reaction mixture (RM); and wherein the conversion rate of the diene monomer (DM) and optionally the comonomer (COM) is =80 %.

METHODS FOR DETERMINING TEMPERATURE VALUE INDICATIVE OF RESIN STICKINESS FROM DATA GENERATED BY POLYMERIZATION REACTION MONITORING

In some embodiments, a method including the steps of monitoring a polymer ization reaction which produces a polymer resin in a fl.mu.id bed reactor, w here a dry melt reference temperature is characteristic of melting behavior of a dry version of the resin, and in response to data indicative of at leas t one monitored parameter of the reaction, determining in on-line fashion a reduced melt reference temperature that is at least substantially equal to t he difference between the dry melt reference temperature and a temperature b y which the dry melt reference temperature is depressed by the presence of c ondensable diluent gas with the resin in the reactor. Optionally, the method also includes the step of controlling the reaction in response to the reduc ed melt reference temperature or a stickiness parameter determined from the reduced melt reference temperature.

CATALYTIC OLEFIN BLOCK COPOLYMERS WITH CONTROLLED BLOCK SEQUENCE DISTRIBUTION

A process for the polymerization of one or more addition polymerizable monomers and the resulting polymer products, said process comprising: 1) contacting an addition polymerizable monomer or mixture of monomers under addition polymerization conditions in a reactor or reactor zone with a composition comprising at least one olefin polymerization catalyst and a cocatalyst and characterized by the formation of polymer chains from said monomer or monomers; 2) transferring the reaction mixture to a second reacto r or reactor zone and optionally adding one or more additional reactants, catalysts, monomers or other compounds prior to, commensurate with, or after said transfer; and 3) causing polymerization to occur in said second reactor or reactor zone to form polymer chains that are differentiated from the polymer chains formed in step 1); said process being characterized by additi on of a chain shuttling agent to the reaction mixture prior to, during, or subsequent to step 1) such that at least ...

A PROCESS FOR THE PRODUCTION OF POLYETHYLENE AND ETHYLENE COPOLYMERS

The invention provides a process and an apparatus for the high pressure p olymerization of ethylene in which a jet pump is used to pump a fluid into a polymer/monomer product mixture leaving a bumped tubular reactor. The fluid may be recycled monomer or another fluid such as a modifier.

SYSTEMS AND PROCESSES FOR POLYACRYLIC ACID PRODUCTION

Disclosed are systems and methods for the production of polyacrylic acid and superabsorbent polymers from ethylene oxidation to form ethylene oxide. Reacting the ethylene oxide with carbon monoxide to form to beta propiolactone (BPL) or polypropiolactone (PPL), or a combination thereof. An outlet configured to provide a carbonylation stream comprising the BPL or PPL, or a combination thereof and using one or more reactors to convert BPL to acrylic acid or to convert at least some of the BPL to PPL, and then to convert PPL to acrylic acid. An outlet configured to provide a PPL stream to a second reactor tm to convert at least some of the PPL to AA or a third reactor to convert at least some of the PPL to AA. The outlet configured to provide an AA stream to a fourth reactor to convert the AA to polyacrylic acid.

ACTIVITY MONITORING AND POLYMERIZATION PROCESS CONTROL

The present invention relates to a method to control a liquid feed stream carried out by measuring at least one spectrum of the liquid feed stream comprising an initiator or catalyst, determining its activity using a predictive model on the basis of said spectrum and adjusting the feed streams and/or the preparation conditions of the feed stream comprising the initiators or catalysts in order to attain or maintain a desired level of total activity. In a further aspect the invention relates to a controlled process for the preparation of polymers in a polymerization reactor by contacting liquid feed streams comprising monomers and initiators or catalysts, whereby the control of the feed streams entering the polymerization reactor and/ or the initiator or catalyst preparation is carried out by measuring at least one spectrum of the liquid feed stream comprising an initiator or catalyst, determining its activity using a predictive model on the basis of said spectrum and adjusting the feed streams ...

POLYETHYLENE PRODUCTION WITH MULTIPLE POLYMERIZATION REACTORS

A system and method for discharging a transfer slurry from a first polymerization reactor through a transfer line to a second polymerization reactor, the transfer slurry including at least diluent and a first polyethylene. A product slurry is discharged from the second polymerization reactor, the product slurry including at least diluent, the first polyethylene, and a second polyethylene. The velocity, pressure drop, or pressure loss due to friction in the transfer line is determined, and a process variable adjusted in response to the velocity, pressure drop, or pressure loss not satisfying a specified value.

CATALYST COMPOSITIONS FOR PRODUCING HIGH MZ/MW POLYOLEFINS

The present invention provides a polymerization process utilizing a dual ansa-metallocene catalyst system. Polymers produced from the polymerization process are also provided, and these polymers have a reverse comonomer distribution, a non-bimodal molecular weight distribution, a ratio of Mw/Mn from about 3 to about 8, and a ratio of Mz/Mw from about 3 to about 6.

Multiple Loop Reactor for Olefin Polymerization

The present invention provides a multiple loop reactor suitable for polymerizing olefins comprising at least two interconnected loop reactors, whereby said connection essentially consists of one or more transfer lines suitable for transferring polymer slurry from a reactor to another reactor and whereby said transfer line extends substantially horizontally. The invention further relates to a process for producing olefin polymers in a multiple loop react or according to the invention. The invention also relates to the use of a transfer line for transferring polymer slurry from a reactor to another reactor in a multiple loop reactor comprising at least two interconnected loop reactors, whereby said transfer line extends substantially horizontally.

Polyethylene Composition and Finished Products Made Thereof

Novel polyethylenes having defined molecular weight distribution and LCB structure are devised, for films or mouldings.

Process for preparing polyolefin

The invention relates to a process for preparing polyolefin in a loop reactor. The polymer is prepared by polymerizing olefin monomers in the presence of a catalyst to produce a polyolefin slurry while pumping said slurry through said loop reactor by means of a pump. The present process is characterized in that the catalyst is fed in the loop reactor at a distance to the pump. The invention allows production of the polymer with advantageous properties while leading to fewer blockages of the reactor.

INTERLOCK AND PROCESS

The present invention relates to production of polymer, and in particular provides an interlock for use in a process for production of a polymer in a reactor, which process comprises: a. polymerising a monomer and optionally a comonomer in the reactor to produce polymer, optionally in the presence of an inert hydrocarbon, and b. withdrawing produced polymer from the reactor, said interlock being based on the temperature in the reactor, and comprising: 1. measuring the temperature in the reactor or a temperature representative of the temperature in the reactor, and 2. comparing said measured temperature to a threshold temperature, said interlock being characterised in that withdrawal is allowed if the measured temperature is greater than the threshold temperature but is prevented if the measured temperature is lower than the threshold temperature. 114-. (canceled)15. An interlock for use in a process for production of a polymer in a reactor , which process comprises:a. polymerising a monomer and optionally a comonomer in the reactor to produce polymer, optionally in the presence of an inert hydrocarbon, andb. withdrawing produced polymer from the reactor, 1. measuring the temperature in the reactor or a temperature representative of the temperature in the reactor, and', '2. comparing said measured temperature to a threshold temperature,, 'said interlock being based on the temperature in the reactor, and comprisingsaid interlock being characterised in that withdrawal is allowed if the measured temperature is greater than the threshold temperature but is prevented if the measured temperature is lower than the threshold temperature.16. An interlock for use in a process for production of a polymer in a reactor , which process comprises:a. polymerising a monomer and optionally a comonomer in the reactor to produce polymer, optionally in the presence of an inert hydrocarbon, andb. withdrawing produced polymer from the reactor, 1. measuring the pressure in the reactor or a ...

INTERLOCK AND PROCESS

The present invention relates to the degassing of polymer powder, and in particular to an interlock for use in a process for degassing of a polymer powder in a degassing vessel, which interlock comprises: 1. measuring the temperature of the polymer powder within or exiting the degassing vessel, 2. comparing said measurement value to a threshold value in order to ascertain whether it is lower than the threshold value or not, and 3. if the measured temperature is lower than the threshold value taking one or more actions to reduce the concentration of hydrocarbons in the polymer powder exiting the degassing vessel and/or to stop the polymer powder withdrawal from that degassing vessel. 112-. (canceled)13. An interlock for use in a process for degassing of a polymer powder in a degassing vessel , which interlock comprises:1. measuring the temperature of the polymer powder within or exiting the degassing vessel,2. comparing said measured value to a threshold value in order to ascertain whether it is lower than the threshold value or not, and3. if the measured temperature is lower than said threshold value taking one or more actions to reduce the concentration of hydrocarbons in the polymer powder exiting the degassing vessel and/or to stop the polymer powder withdrawal from the degassing vessel.14. An interlock according to wherein the powder temperature is measured within the degassing vessel and in the half of the degassing vessel closest to the polymer powder exit.15. An interlock according to wherein the degassing vessel is a purge vessel in which polymer is contacted with a purge gas to remove monomers and other entrained hydrocarbons claim 13 , and the powder temperature is measured by measurement of the temperature of the purge gas after contact with the polymer powder.16. An interlock according to wherein the threshold value is adjusted depending on the polymer to be degassed and is defined by a fixed temperature differential between an upstream process condition ...

Process for the Gas-Phase Polymerization of Olefins

A process for the gas-phase copolymerization of: (a) propylene, (b) at least one C-Cα-olefin, and (c) optionally ethylene, 1. A process for the gas-phase copolymerization of:(a) propylene,{'sub': 4', '8, '(b) at least one C-Cα-olefin, and'}(c) optionally ethylene,the process being carried out in a reactor having two interconnected polymerization zones, wherein the growing polymer particles flow through the first of said polymerization zones (riser) under fast fluidization conditions, leave said riser and enter the second of said polymerization zones (downcomer) through which they flow downward in a densified form, leave said downcomer and are reintroduced into said riser, thus establishing a circulation of polymer between the riser and the downcomer,{'sub': 4', '8, 'the gas mixture present in the riser being at least partially prevented from entering the downcomer by introducing into the upper part of said downcomer a liquid barrier having a composition different from the gaseous mixture present in the riser and comprising at least one C-Cα-olefin in a total amount of from 0.1% to 35% by mol.'}2. The process according to claim 1 , wherein the partial evaporation of said liquid barrier generates in the upper part of the downcomer a flow of gas moving counter-currently to the flow of descendent polymer.3. The process according to claim 1 , wherein the C-Cα-olefin is 1-hexene and its amount ranges from 0.1% to 10% by mol.4. The process according to claim 3 , wherein the liquid barrier further comprises:from 70 to 90% by mol of propylene;from 5 to 15% by mol of propane; andfrom 0 to 5% by mol of ethylene;5. The process according to claim 4 , wherein the obtained polyolefin contains from 0.2 to 8.0% by weight of recurring units derived from 1-hexene.6. The process according to claim 1 , wherein the C-Cα-olefin is 1-butene and its amount ranges from 2% to 30% by mol.7. The process according to claim 6 , wherein the liquid barrier further comprises:from 50 to 90% by mol of ...

PROCESS FOR PRODUCING FUNCTIONALIZED POLYMERS

A method for preparing a functionalized polymer, the method comprising the steps of (a) polymerizing monomer in the presence of a coordination catalyst to form a polymer, (b) inhibiting said step of polymerizing with a Lewis base, and (c) reacting the polymer with a functionalizing agent. 1. A continuous polymerization method for preparing a functionalized polymer , the method comprising the steps of:(a) continuously introducing monomer and a coordination catalyst to form a polymerization mixture;(b) allowing at least a portion of the monomer to polymerize into a reactive polymer within a first zone;(c) continuously removing the polymerization mixture from the first zone and transferring the mixture to a second zone;(d) continuously introducing a Lewis base to the polymerization mixture after removal from the first zone;(e) continuously introducing a functionalizing agent to the polymerization mixture after removal from the first zone.2. The method of claim 1 , polymerization mixture includes less than about 20% by weight solvent.3. The method of claim 1 , where said step of introducing a Lewis base includes introducing the Lewis base in a sufficient amount to substantially cease the polymerization of monomer.4. The method of claim 1 , after said step of continuously introducing a Lewis base claim 1 , further comprising continuously removing the polymerization mixture from the second zone and transferring the mixture to a third zone.5. The method of claim 1 , where the reactive polymer has an active terminus.6. The method of claim 5 , where the functionalizing agent reacts with the reactive polymer at its active terminus.7. The method of claim 1 , where the polymerization mixture includes less than about 5% by weight solvent.8. The method of claim 1 , where said steps of continuously introducing monomer and said step of allowing at least a portion of the monomer to polymerize take place within an elongated reactor.9. The method of claim 1 , where said step of ...

PROCESS FOR IMPROVING THE DEVOLATILIZATION OF POLYMER SLURRY PRODUCED IN A POLYMERIZATION REACTOR

The present invention relates to a process for improving the devolatilization of polymer slurry produced in an olefin polymerization reactor. The process is characterized in that it involves an adjustment of the temperature of the interior surface of the flash line for periodically transferring polymer slurry from the polymerization reactor to a downstream processing unit. In particular, in accordance with the present process, the temperature of the interior surface of the flash line is adjusted to a temperature which is equal to or higher than the softening temperature of the polymer passing through said flash line whereby said temperature is higher in a first half of the length of the flash line than in the remaining length of the flash line. 113-. (canceled)15. The process of claim 14 , wherein the flash line comprises different flash line zones claim 14 , and wherein the temperature of the interior surface of the flash line varies in the different zones.16. The process of claim 14 , wherein the temperature of the interior surface of the flash line or a zone thereof is adjusted by adjusting temperature claim 14 , pressure and/or flow of the fluid heating the flash line or a zone thereof.17. The process of claim 14 , wherein the temperature of the interior surface of the flash line is up to 10% higher in the first half of the length of the flash line than in the remaining length of the flash line.18. The process of further comprising periodically withdrawing the polymer slurry from the polymerization reactor through one or more settling legs; and passing the withdrawn polymer slurry from the settling legs through one or more heated flash lines into a flash tank.19. The process of claim 19 , wherein the one or more settling legs comprise at least two settling legs.20. The process of claim 14 , wherein the flash tank is operated at a pressure of between 0.1 and 4 bar. The present invention relates to the field of olefin polymerization. In particular, the present ...

PUMPING APPARATUS AND PROCESS FOR POLYMERIZATION IN LOOP REACTORS

An olefin polymerization process and apparatus wherein a fluid slurry comprising monomer, diluent and catalyst is circulated in a continuous loop reactor by two or more pumps. The process and apparatus allow operating the reaction at significantly higher solids content in the circulating fluid slurry. In a preferred embodiment, the fluid slurry is circulated by two impellers arranged so that the downstream impeller benefits from the rotational energy imparted by the upstream impeller. An olefin polymerization process operating at higher reactor solids by virtue of more aggressive circulation has improved efficiencies, particularly in larger-volume reactors. 1. A loop slurry polymerization process comprising:introducing monomer, and catalyst to a loop reactor;polymerizing the monomer to form a slurry comprising solid polyolefin particles in a liquid medium;circulating the slurry using two impellers;imparting a first rotational motion to the slurry with a first of the impellers;imparting a second rotational motion to the slurry with a second of the impellers, wherein the second rotational motion is opposite to the first rotational motion.2. The loop slurry polymerization process of further comprising pre-swirling the slurry upstream of the first impeller claim 1 , in a direction opposite to the first rotational motion of the impeller of the first impeller.3. The loop slurry polymerization process of further comprising post-swirling the slurry downstream of the second pump claim 1 , in the same direction as the second rotational motion of the impeller of the second pump.4. A loop slurry polymerization process according to claim 1 , further comprising minimizing a clearance between at least one impeller and a portion of the loop reactor housing the impeller.5. A loop slurry polymerization process according to claim 1 , wherein the slurry has a concentration of the solid polyolefin particles of at least about 45 weight percent and at most about 75 weight percent.6. A ...

Method and Apparatus for Monitoring and Restoring Electrical Properties of Polymerization Reactor Wall Film

Described herein are methods for monitoring and restoring electrical properties of polymerization reactor wall films. The method may comprise using a reactor wall monitor to monitor and determine an electrical property, such as the bed voltage or breakdown voltage, of the wall film The method may further comprise adding continuity additive to the reactor and/or adjusting the feed rate of continuity additive being added to the reactor in response to the measured electrical property. 1. A method for polymerizing olefins comprising: (i) during a first interval of time during the reaction in the reactor system, operating the static probe to generate high speed data indicative of bubbling in the fluid bed; and', '(ii) determining from the high speed data at least one electrical property of the coating;, '(a) during a polymerization reaction using at least one static probe in a fluid bed reactor system to monitor a coating comprising a film of polymer on a surface of the reactor system and a distal portion of each said static probe, wherein the coating is exposed to flowing fluid within the system, said monitoring including steps of(b) comparing the electrical property determined in step (a) with a reference breakdown voltage of the coating; and(c) if the electrical property is less than the reference breakdown voltage of the coating adding continuity additive to the polymerization reactor for a period of time until the determined electrical property of the coating is greater than or equal to the reference breakdown voltage of the coating.2. The method of claim 1 , wherein said surface of the reactor system is a bed wall and the coating is exposed to flowing fluid within the fluid bed during the reaction.3. The method of claim 1 , wherein the coating is a film of polymer.4. The method of claim 1 , wherein the high speed data include frequency components in a range from about 1 Hz to about 10 Hz claim 1 , and the first interval is at least one minute in duration.5. The ...

Process for preparing polyolefins

The present invention relates to a process of preparing a polyolefin in a loop reactor by introducing anti-fouling agent through a sleeve provided around at least part of the shaft of the pump. Also, the invention relates to the use of anti-fouling agent to prevent or reduce fouling by feeding the anti-fouling agent against the impeller of the pump upon introduction to the loop reactor. 1. Process of preparing a polyolefin in a loop reactor in the presence of anti-fouling agent , said loop reactor comprising interconnected pipes , defining a reactor path , and an axial pump comprising a motor , a shaft and an impeller , characterized in that at least part of the anti-fouling agent is introduced into said loop reactor through a sleeve provided around at least part of the shaft of said pump.2. Process according to claim 1 , wherein at least part of the anti-fouling agent is fed against the side of the impeller which is connected to the shaft of said pump.3. Process according to claim 1 , wherein all anti-fouling agent is fed through the sleeve into the reactor.4. Process according to claim 1 , wherein the anti-fouling agent is dissolved at a concentration of 0.1-10% by weight in a solvent.5. Process according to claim 1 , wherein the anti-fouling agent is fed under flushing with diluent.6. Process according to claim 1 , wherein the diluent comprises less than 15% by weight of monomer claim 1 , preferably less than 10% by weight claim 1 , more preferably less than 5% by weight claim 1 , most preferably less than 1% by weight of monomer.7. Process according to claim 1 , wherein said polyolefin is produced in slurry conditions.8. Process according to claim 1 , wherein said process is performed in a double loop reactor.9. Process according to claim 1 , wherein the anti-fouling agent is introduced into the first loop reactor of the double loop reactor through a sleeve provided around at least part of the shaft of the pump of the first loop reactor.10. Process according to ...

Pump for loop reactor

The present invention relates the use of a pump in a loop reactor for the production of polyethylene, as well as a reactor comprising such pump and methods for producing polyolefin by means of such reactor. The pump according to the invention is characterized in that it is an axial flow impeller circulation pump, wherein the impeller comprises 6 blades and wherein the pump is fixed on a spring supported frame. Use of the pump according to the present invention allows for preparation of homogeneous polyethylene products that meet high quality standards from the complicated ethylene polymerization mixtures while at the same time being produced with low energy consumption.

Process for preparing polyolefins and use of antifouling agents therein

The present invention relates to a process of preparing a polyethylene in a loop reactor in the presence of antifouling agent comprising the steps of: 1. Process of preparing polyethylene in a loop reactor in the presence of antifouling agent comprising the steps of:a) feeding into said loop reactor diluent, monomers, optionally hydrogen, and optionally one or more co-monomers to produce a liquid phase;b) introducing antifouling agent into said loop reactor,c) introducing a catalyst into the liquid phase to produce a slurry; andd) polymerizing the monomers and optional co-monomers to form the polyethylene, characterized in that the time difference between introduction of the antifouling agent and introduction of the catalyst is at most 3 hours.2. Process according to claim 1 , wherein said polyethylene is produced in slurry conditions.33. Process according to or claim 1 , wherein antifouling agent is introduced in said loop reactor at most hours before introduction of the catalyst of step c) in the liquid phase.4. Process according to any of to claim 1 , wherein antifouling agent is introduced in said loop reactor at least 1 minute before introduction of the catalyst of step c) in the liquid phase.5. Process according to any of to claim 1 , wherein antifouling agent is introduced in said loop reactor at most 1 hour after introduction of the catalyst of step c) in said liquid phase.6. Process according to any of to claim 1 , wherein antifouling agent is introduced in said loop reactor at least 1 minute after introduction of the catalyst of step c) in said liquid phase.7. Process according to any of to claim 1 , wherein in step c) the catalyst is introduced into the liquid phase when the concentration of antifouling agent is ranging from 0 to less than 0.3 ppm.8. Process according to any of to claim 1 , wherein said polyolefin is polyethylene.9. Process according to any of to claim 1 , wherein the process further comprises the step of (e) subsequently increasing the ...

METHOD FOR PRODUCING POLYETHYLENE

The present invention relates to a method for consecutively producing at least two different polyethylene resins in one slurry loop reactor, comprising producing a first polyethylene resin in the presence of a Ziegler-Natta and/or a Chromium catalyst, and consecutively producing a second polyethylene resin in the presence of a metallocene catalyst, characterized in that the ratio of the melt flow index of the first produced polyethylene resin to the melt flow index of the second produced polyethylene resin is at least 0.3. 1. Method for consecutively producing at least two different polyethylene resins in one slurry loop reactor , comprising the steps of producing a first polyethylene resin in the presence of a Ziegler-Natta and/or a Chromium catalyst , and consecutively producing a second polyethylene resin in the presence of a metallocene catalyst , characterized in that the ratio of the melt flow index of the first produced polyethylene resin to the melt flow index of the second produced polyethylene resin is at least 0.3.2. Method according to claim 1 , wherein said production is performed continuously.3. Method according to claim 1 , wherein the ratio of the melt flow index of the first produced polyethylene to the melt flow index of the second produced polyethylene is at least 1.4. Method according to claim 1 , wherein the ratio of the melt flow index of the first produced polyethylene to the melt flow index of the second produced polyethylene is at least 3.5. Method according to claim 1 , wherein the ratio between the melt flow index of said first resin and the melt flow index of said second resin is between 0.3 and 15.6. Method according to claim 1 , wherein the first polyethylene resin is produced in the presence of a Ziegler-Natta catalyst.7. Method of transition between polyethylene resins of different grades comprising the steps of producing in a loop reactor a first polyethylene resin in the presence of a Ziegler-Natta and/or a Chromium catalyst claim 1 ...

Method for Continuously Producing Thermoplastic Resin From Conjugated Diene and Thermoplastic Resin Produced by the Same

A method for continuously producing a thermoplastic resin from a conjugated diene includes: primarily polymerizing a conjugated diene monomer with an aromatic vinyl monomer in a first solvent in a first reactor, and feeding a hydroxyl group-containing polymerization inhibitor and a polar hydrocarbon to the first reactor to prepare a rubber solution; and adding an aromatic vinyl monomer and a monomer copolymerizable with the aromatic vinyl monomer to the rubber solution, and subjecting the mixture to secondary polymerization in a second solvent of the same kind as the first solvent in a second reactor. The method can provide a thermoplastic resin that can have excellent color and low gloss characteristics. 1. A method for continuously producing a thermoplastic resin from a conjugated diene , the method comprising:primarily polymerizing a conjugated diene monomer with an aromatic vinyl monomer in a first solvent in a first reactor, and feeding a hydroxyl group-containing polymerization inhibitor and a polar hydrocarbon to the first reactor to prepare a rubber solution; andadding an aromatic vinyl monomer and a monomer copolymerizable with the aromatic vinyl monomer to the rubber solution, and subjecting the mixture to secondary polymerization in a second solvent of the same kind as the first solvent in a second reactor.2. The method as claimed in claim 1 , wherein the conjugated diene monomer is butadiene claim 1 , isoprene or a combination thereof.3. The method as claimed in claim 1 , wherein the polymerization in the first reactor is carried out using an organometallic catalyst.4. The method as claimed in claim 1 , wherein a vinyl modifier is added for the polymerization in the first reactor.5. The method as claimed in claim 1 , wherein the rubber solution prepared by the polymerization in the first reactor is concentrated by extrusion before being fed into the second reactor.6. The method as claimed in claim 1 , wherein the first and second solvents are aromatic ...

Catalyst compositions for the polymerization of olefins

Catalyst compositions containing N,N-bis[2-hydroxidebenzyl]amine transition metal compounds are disclosed. Methods for making these transition metal compounds and for using such compounds in catalyst compositions for the polymerization of olefins also are provided.

Ethylene-Based Interpolymers and Processes to Make the Same

Ethylene-based interpolymers, e.g., ethylene-acrylic acid copolymers, are made by a process comprising the steps of: A. Injecting a first feed comprising a chain transfer agent system (CTA system) and ethylene into a first autoclave reactor zone to produce a first zone reaction product, the CTA system of the first reactor zone having a transfer activity Z1; and B. (1) Transferring at least part of the first zone reaction product to a second reactor zone selected from a second autoclave reactor zone or a tubular reactor zone, and (2) at least one of transferring or freshly injecting a feed comprising a CTA system into the second reactor zone to produce a second zone reaction product, the CTA system of the second reactor zone having a transfer activity of Z2; and with the proviso that the ratio of Z1:Z2 is greater than 1. The comonomer comprises at least one carboxylic acid group or an anhydride group. 2. The process of claim 1 , further comprising one or more steps of transferring a zone reaction product produced in an (ith−1) reaction zone to an (ith) reaction zone claim 1 , where 3≦i≦n claim 1 , and n≧3 claim 1 , each zone operating at polymerization conditions claim 1 , and injecting an (ith) feed comprising a CTA system into the (ith) reaction zone claim 1 , the CTA system of the (ith) reaction zone having a transfer activity of Zi; andwith the proviso that the ratio of Z1/Zi is greater than 1.3. The process of claim 1 , in which the second feed further comprises ethylene.4. The process of claim 1 , in which the at least one comonomer is selected from acrylic acid claim 1 , methacrylic acid claim 1 , or a combination thereof.5. The process of claim 1 , in which at least part of the first zone reaction product is transferred to a second autoclave reactor zone.6. The process of claim 1 , in which at least part of the first zone reaction product is transferred to a tubular reactor zone.7. The process of claim 1 , in which each feed to each reactor zone contains the ...

CONTINUOUS PROCESS FOR PREPARING POLYFLUOROACRYLATE PARTICLES

The present invention is directed to a continuous process for preparing a crosslinked polymer comprising a fluoro group. 4. The process of wherein the polymer comprises structural units corresponding to Formulae 1 claim 1 , 2 and 3.5. The process wherein either:(i) the structural units corresponding to Formula 1 constitute at least about 85 wt. % based on the total weight of structural units of Formulae 1, 2, and 3 in the polymer calculated from the amounts of monomers used in the polymerization reaction, and the weight ratio of the structural unit corresponding to Formula 2 to the structural unit corresponding to Formula 3 is from about 4:1 to about 1:4, or(ii) the mole fraction of the structural unit of Formula 1 in the polymer is at least about 0.87 based on the total number of moles of the structural units of Formulae 1, 2, and 3 calculated from the amounts of monomers used in the polymerization reaction, and the mole ratio of the structural unit of Formula 2 to the structural unit of Formula 3 is from about 0.2:1 to about 7:1.6. The process of wherein the polymer comprises structural units corresponding to Formulae 1 and 2.7. The process of wherein the polymer comprises structural units corresponding to Formulae 1 and 3.10. The process of wherein the polymerization mixture further comprises a polymerization initiator.11. The process of claim 1 , further comprising a continuous reactor claim 1 , with an aqueous phase and an organic phase fed to the reactor.12. The process of claim 11 , wherein the organic phase comprises a mixture of monomers that are mixed in a mixer prior to being fed to the reactor.13. The process of claim 11 , wherein the aqueous phase comprises a mixture of water claim 11 , surfactant and salts are mixed prior to being fed to the reactor.14. The process of claim 11 , wherein the reactor is a plug flow reactor.15. The process of claim 14 , wherein the plug flow reactor additionally comprises an orifice plate.16. The process of claim 15 , ...

Method For Controlling Bubble Formation In Polymerization Reactors

Disclosed herein are methods for controlling bubble formation in a polymerization reactor. The method includes: (a) determining a concentration of at least one component at a location in the reactor using a mathematical model; (b) determining a vapor pressure of the composition based at least in part upon the concentration of the component; (c) determining an operating pressure of the reactor at the location; (d) determining a pressure difference as ΔP =P-P, wherein Pis the operating pressure and Pis the vapor pressure; (e) comparing the ΔP to a threshold value; and (f) implementing an effect when the ΔP is less than the threshold value. 1. A method for controlling bubble formation in a polymerization reactor , the reactor containing a composition comprising at least one component , the method comprising:(a) determining a concentration of the at least one component in the composition at a location in the reactor using a mathematical model;(b) determining a vapor pressure of the composition based at least in part upon the concentration of the at least one component;(c) determining an operating pressure of the reactor at the location;{'sub': X', 'V', 'X', 'V, '(d) determining a pressure difference as ΔP=P−P, wherein Pis the operating pressure and Pis the vapor pressure;'}(e) comparing the ΔP to a threshold value, wherein the threshold value reflects a desired difference between the vapor pressure and operating pressure, and wherein a ΔP that is greater than the threshold value produces an acceptable amount of bubble formation; and(f) implementing an effect when the ΔP is less than the threshold value.2. The method of claim 1 , wherein one or more of (a) through (f) are conducted on a real-time basis.3. The method of claim 1 , wherein the method is conducted during change of a reactant supplied to the reactor during a grade transition.4. The method of claim 1 , wherein steps (a) through (f) are conducted at more than one location within the reactor.5. The method of ...

CONTINUOUS FLOW POLYMERISATION PROCESS

The present invention relates to a process for continuously preparing polymer by RAFT solution polymerisation, the process comprising: introducing into a flow reactor a reaction solution comprising one or more ethylenically unsaturated monomers, RAFT agent, non-reactive solvent and free radical initiator; and promoting RAFT polymerisation of the one or more ethylenically unsaturated monomers within the reactor so as to form a polymer solution that flows out of the reactor. 1. A process for continuously preparing polymer by RAFT solution polymerisation , the process comprising:introducing into a flow reactor a reaction solution comprising one or more ethylenically unsaturated monomers, RAFT agent, non-reactive solvent and free radical initiator; andpromoting RAFT polymerisation of the one or more ethylenically unsaturated monomers within the reactor so as to form a polymer solution that flows out of the reactor.2. The process according to claim 1 , wherein the flow reactor is in the form of a tubular flow reactor.3. The process according to claim 2 , wherein the flow reactor is in the form of a capillary tubular flow reactor.4. The process according to claim 1 , wherein the flow reactor comprises one or more flow lines through which the reaction solution passes claim 1 , the one or more flow lines having an internal diameter of about 1 mm.5. The process according to claim 1 , wherein the flow reactor comprises multiple flow lines through which the reaction solution passes claim 1 , each flow line having an internal diameter of about 1 mm.6. The process according to claim 1 , wherein the flow reactor comprises one or more flow lines through which the reaction solution passes claim 1 , the one or more flow lines being made of metal.7. The process according to which further comprises introducing the resulting polymer solution into a flow reactor or a region of a flow rector claim 1 , together with a reaction solution comprising one or more ethylenically unsaturated ...

CONTINUOUS PROCESS FOR THE SYNTHESIS OF GRAFT POLYMERS BASED ON POLYETHERS

The invention relates to a continuous process for the preparation of amphiphilic graft polymers, wherein a vinyl ester component (B) composed of vinyl acetate and/or vinyl propionate (B1) and, if desired, a further ethylenically unsaturated monomer (B2), is polymerized in the presence of a polyalkylene oxide (A), a free radical-forming initiator (C) and, if desired, an additive (D), at a mean polymerization temperature at which the initiator (C) has a decomposition half-time of from 1 to 500 min, in at least one tubular reactor segment with a feed side and an outlet side, through which the reaction mixture comprising at least a part of component (A) to (C), and if desired (D), streams, a tubular reactor segment and the use of the inventive amphiphilic graft polymer. The invention further relates to an inventive amphiphilic graft polymer and the use thereof. 123.-. (canceled)24. A continuous process for the preparation of amphiphilic graft polymers , wherein a vinyl ester component (B) composed of vinyl acetate and/or vinyl propionate (B 1) and , optionally , a further ethylenically unsaturated monomer (B2) , is polymerized in the presence of a polyalkylene oxide (A) , a free radical-forming initiator (C) and , optionally , an additive (D) , at a mean polymerization temperature at which the initiator (C) has a decomposition half-time of from 1 to 500 min , in at least one tubular reactor segment with a feed side and an outlet side , through which the reaction mixture comprising at least a part of component (A) to (C) , and optionally (D) , streams.25. The continuous process according to claim 24 , wherein the polymerization takes place in at least two tubular reactor segments connected in series.26. The continuous process according to claim 25 , wherein at least two tubular segments are connected in series claim 25 , wherein the first tubular reactor segment has a first feed side and a first outlet side claim 25 , wherein the first tubular reactor segment is ...

Copolymer Production System and Process

In a process for making a copolymer, a first product stream comprising a semi-crystalline polymer and a chain terminating agent is produced in a first reactor system. The first product is provided to a second reactor system wherein a low crystallinity polymer is produced in the presence of the semi-crystalline polymer. At least a portion of the chain terminating agent is removed from the second reactor system by an in-situ process. 1. A process for making a copolymer , the process comprising:a. producing in a first reactor system a first product stream comprising a semi-crystalline polymer and a chain terminating agent;b. providing at least a portion of the first product stream to a second reactor system;c. producing in the second reactor system a low crystallinity polymer in the presence of the semi-crystalline polymer; andd. removing at least a portion of the chain terminating agent introduced with the first product stream from the second reactor system by an in-situ process.2. The process of claim 1 , wherein the in-situ process comprises a catalytic hydrogenation reactor to consume hydrogen via reaction with monomer claim 1 , or a membrane unit to selectively remove the chain terminating agent from the reaction system.3. The process of claim 1 , wherein the copolymer has an intrinsic viscosity ratio (IVR) of greater than 4.4. The process of claim 1 , wherein the chain terminating agent is hydrogen.5. The process of claim 1 , wherein the monomer is selected from ethylene and propylene.6. The process of claim 1 , wherein the semi-crystalline polymer has a matrix claim 1 , and at least a portion of the low crystallinity polymer is formed within the pores of the matrix.7. The process of claim 1 , wherein the semi-crystalline polymer is polypropylene homopolymer and the low crystallinity polymer is ethylene propylene rubber (EPR).8. The process of claim 1 , wherein the first reactor system comprises a slurry loop reactor or a plurality of slurry loop reactors in ...

PROCESS FOR OPERATING A MIXING KNEADER

The invention relates to a process for operating a mixing kneader, comprising one or more shafts on whose surfaces are disposed kneading bars and which are surrounded by a casing, comprising the following steps:

Polymers, Method of Producing the Same, and Articles Made Therefrom

A virgin granular polymer comprising polymer particles wherein at least 90% by weight of the granular polymer particles, have an I 21 that is within two standard deviations of a mean I 21 of the granular polymer, the ratio of the standard deviation of I 21 to the mean of the granular polymer is less than 0.2 and the ratio of the standard error of a linear fit to the mean of the granular polymer is less than 0.1, and further wherein the virgin granular polymer has an I 21 less than or equal to 70 and/or further wherein at least 90% by weight of the granular polymer particles, have a density that is within two standard deviations of a mean density of the granular polymer, the ratio of the standard deviation of the mean density of the granular polymer to the mean density of the granular polymer is less than 0.002 and the ratio of the standard error of a linear fit to the mean of the density is less than 0.001, and further wherein the virgin granular polymer has an I 21 less than or equal to 70 is provided.

Process for Producing Water-Absorbing Polymer Particles in a Polymerization Reactor with At Least Two Axially Parallel Rotating Shafts

A process for producing water-absorbing polymer particles by polymerizing an aqueous monomer solution in a polymerization reactor with at least two axially parallel rotating shafts, wherein the polymerization is performed in the presence of an inert gas and under positive pressure.

Double Loop Technology

A method for the copolymerization of ethylene and a C olefin in a loop reactor and polymers formed therefrom are described herein. The method generally includes introducing an ethylene monomer, a C olefin and a diluent carrier liquid into a loop reactor. A catalyst system can be supplied to said loop reactor. The diluent liquid, ethylene monomer, and C olefin can be circulated through said loop reactor, while copolymerizing said ethylene and C olefin in the presence of said catalyst system to produce a slurry. The slurry can be diverted into a settling leg, and sequentially discharged therefrom and withdrawn from said loop reactor. An ethylene monomer co-feed can be introduced into said loop reactor at spaced locations downstream of the ethylene and diluent. The ethylene co-feed can be introduced in an amount effective to reduce the variation in the ratio of ethylene and C olefin. 111-. (canceled)12. A method for controlling the injection of catalyst slurry in a polymerization reactor , wherein polyethylene is prepared , said catalyst slurry comprising solid catalyst in a hydrocarbon diluent , the method comprising:providing solid catalyst and a hydrocarbon diluent in one or more storage vessels such that a catalyst slurry is obtained in said one or more storage vessels,transferring said catalyst slurry from said one or more storage vessels to a mixing vessel wherein said catalyst slurry is diluted for obtaining a suitable concentration for use in a polymerization reaction,pumping said diluted catalyst slurry at a controlled flow rate from said mixing vessel to said polymerization reactor through one or more conduits, by means of a pumping means, provided in each of said conduits, and the dilution being adapted to the pumping means.13. The method according to wherein said catalyst is a metallocene catalyst.14. The method of wherein the metallocene catalyst is a supported metallocene catalyst.15. The method according to wherein said catalyst slurry is diluted with ...

ENERGY EFFICIENT POLYOLEFIN PROCESS

A manufacturing system for producing polyolefin includes a polymerization reactor, a flash chamber, and a purge column. In certain embodiments, the purge column may receive a solids stream directly from the flash chamber. Further, the purge column may function as a feed tank for an extruder within an extrusion/loadout system. According to certain embodiments, the manufacturing system may be configured to consume less than 445 kilowatt-hours of energy per metric ton of polyolefin produced based on consumption of electricity, steam, and fuel gas. 1. A system , comprising:a first polymerization reactor configured to produce a slurry comprising first polyolefin particles and a diluent;a separation vessel configured to receive the slurry to produce a lights stream comprising light components and a solids stream comprising the first polyolefin particles and residual diluent; anda second polymerization reactor configured to receive the solids stream and produce second polyolefin particles.2. The system of claim 1 , wherein the separation vessel comprises a flash chamber.3. The system of claim 1 , wherein the first and second polyolefin particles are mixed in the second polymerization reactor to produce a product polyolefin particle stream.4. The system of claim 3 , comprising a flash chamber configured to receive the product polyolefin particle stream and separate a portion of the diluent to produce a flash stream comprising separated diluent and an additional solids stream comprising the product polyolefin particle stream.5. The system of claim 4 , comprising a solids discharge conduit configured to convey the additional solids stream from the flash chamber claim 4 , wherein the solids discharge conduit does not comprise a low-pressure flash vessel or a low-pressure flash compressor or blower.6. The system of claim 1 , wherein the second polymerization reactor comprises a gas phase polymerization reactor.7. The system of claim 1 , wherein the second polymerization reactor ...

Blow Moulded Articles of Bimodal Polyethylene

The invention relates to A process for the polymerisation of ethylene to produce a polyethylene resin in at least two slurry loop reactors connected to each other in series, the resin having a bimodal molecular weight distribution, a molecular weight distribution MWD of at least 7.0, an HLMI of from 1 to 100 g/10 min, and a density of from 0.935 to 0.960 g/cm 3 , wherein in one reactor 30 to 47 wt % based on the total weight of the polyethylene resin of a high molecular weight (HMW) polyethylene fraction is produced having an HL275 of from 0.05 to 1.8 g/10 min (the equivalent of HLMI of from 0.01 to 1.56 g/10 min), a density of from 0.925 to 0.942 g/cm 3 and an MWD of at least 5.0, and in the other reactor a low molecular weight (LMW) polyethylene fraction is produced having an HLMI of from 10 to 1500 g/10 min and a density of from 0.960 to 0.975 g/cm 3 , in the presence of a Ziegler-Natta catalyst system.

POLYMERIZATION REACTOR FOR BUTYL RUBBER PRODUCTION

A low temperature polymerization reactor for the production of butyl rubber by catalytic polymerization of isobutylene with small amount of a conjugated diolefin such as isoprene includes: an extended upper head with fluid deflector fixed to the top tube-sheet, the shapes of the head and deflector being optimized in order to reach a very homogeneous slurry velocity in the rows of tubes and to minimize the pressure drop due to the inversion of flow from up-flow to down-flow and to the entrance of the slurry in the tubes; an hemispheric bottom head with fluid deflectors placed between the impeller and the bottom itself and designed to minimize the pressure drop due to the inversion of flow from down-flow to up-flow; and straightening baffles inside the draft tube, which shape and dimensions are optimized to turn the radial velocity components produced by the rotation of the impeller into axial velocity components. 110-. (canceled)11151119426) A single pass shell and tubes type polymerization reactor () , used to produce butyl rubber in slurry , copolymerizing at least 95 wt % of isobutylene with not more than about 5 wt % of isoprene , in concentration of about 35% to 45% by vol. in a solvent , preferably methyl chloride , in presence of 0.015% to 0.15% by weight of catalyst , preferably aluminum chloride , and at a temperature within the range of −104° C. to −90° C. , wherein the velocity in the tubes is in the range from 2.4 to 4.5 m/sec , wherein the reaction mixture is introduced from the bottom side near an impeller shaft () and the outflow () is in the top , with the reaction in tube side and a cooling media in the shell side () to remove the heat of reaction , and a circulation pump installed at the bottom () , to permit high velocity of the rubber slurry in the central draft tube () and in downflow smaller tubes () , the reactor comprising:{'b': 3', '15', '6', '6, 'a—an extended upper head (), containing a fluid deflector (), having an inclined bottom up drop ...

Reactor and process for preparing polyolefin

The invention relates to a process for preparing polyolefin in a loop reactor. The polymer is prepared by polymerizing olefin monomers in the presence of a catalyst to produce a polyolefin slurry while pumping said slurry through said loop reactor by means of a pump. The present process is characterized in that the catalyst is fed in the loop reactor at a distance to the pump. The invention allows production of the polymer with advantageous properties while leading to fewer blockages of the reactor.

SCC EQUIPPED WITH FOAM REMOVAL UNIT

The present invention provides a SCC (Spinning Cone Column) equipped with a foam removal unit comprising: a housing having a rotation axis; a supply part of at least one reactant formed inside of the housing; at least two spinning cones that are installed so as to have a constant gradient from the upper part to the lower part to the rotation axis, move supplied reactants through the reactant supply part, and rotate around the rotation axis; a fixed cone that is fixed and formed on the inner side of the housing, and provides a pathway for sequentially moving reactant from a spinning cone at the upper part to a spinning cone at the lower part; a product collection part for collecting reactants moved through the spinning cone and the fixed cone; and a driving part for rotating the spinning cone, wherein a foam removal unit is installed on one side of the housing. The SCC according to the present invention solves the problems that foam is generated when separating material to be removed to decrease removal yield and lower stability of the product, and may improve removal yield and product stability because a foam removal unit is for removing generated foam is installed. 1. A SCC (Spinning Cone Column) equipped with a foam removal unit comprisinga housing having a rotation axis;a supply part of at least one reactant formed inside of the housing;at least two spinning cones that are installed so as to have a constant gradient from the upper part to the lower part to the rotation axis, move reactants supplied through the reactant supply part, and rotate around the rotation axis;a fixed cone that is fixed and formed on the inner side of the housing, and provides a pathway for sequentially moving reactant from a spinning cone at the upper part to a spinning cone at the lower part;a product collection part for collecting reactants moved through the spinning cone and the fixed cone; anda driving part for rotating the spinning cone,wherein a foam removal unit is installed on one ...

Heat Transfer in a Polymerization Reactor

A process comprises polymerizing an olefin monomer in a loop reactor in the presence of a catalyst and a diluent, and producing a slurry comprising solid particulate olefin polymer and diluent. The Biot number is maintained at or below about 3.0 within the loop reactor during the polymerizing process. The slurry in the loop reactor forms a slurry film having a film coefficient along an inner surface of the reactor wall, and the film coefficient is less than about 500 BTU·hr·ft·° F.. 1. A reactor comprising:{'sup': −1', '−2', '−1, 'a continuous tubular shell comprising a thickness and a thermal conductivity, wherein the continuous tubular shell defines a continuous loop; wherein a ratio of the thermal conductivity to the thickness is greater than or equal to about 120 BTU·hr·ft·° F.; and'}a slurry disposed within the continuous tubular shell, wherein the slurry comprises solid particulate olefin polymer and a diluent, and wherein the volume fraction of the solids in the slurry is greater than about 0.65.2. The reactor of claim 1 , wherein the ratio of the thermal conductivity to the thickness is greater than or equal to about 160 BTU·hr·ft·° F..3. The reactor of claim 1 , wherein the ratio of the thermal conductivity to the thickness is greater than or equal to about 250 BTU·hr·ft·° F..4. The reactor of claim 1 , wherein the ratio of the thermal conductivity to the thickness is greater than or equal to about 300 BTU·hr·ft·° F..5. The reactor of claim 1 , wherein the thermal conductivity of the shell is between about 20 and about 40 BTU·hr·ft·° F..6. The reactor of claim 1 , wherein the shell comprises a steel selected from the group consisting of: A106 Gr 8 (60) claim 1 , A516 Gr 70 claim 1 , A537 Cl 2 claim 1 , A106 Gr C (40) claim 1 , A202 Gr 8 claim 1 , A285 Gr C claim 1 , A514 Gr 8 claim 1 , A/SA516 Gr 70 claim 1 , A515 Gr 70 claim 1 , A517 Gr A claim 1 , A517 Gr 8 claim 1 , A533 Ty A C13 claim 1 , A542 Ty A C12 claim 1 , A678 Gr C claim 1 , AISI 1010 claim 1 , ...

POLYOLEFIN PRODUCTION WITH MULTIPLE POLYMERIZATION REACTORS

A polyolefin production system including: a first reactor configured to produce a first discharge slurry having a first polyolefin; a second reactor configured to produce a second discharge slurry having a second polyolefin; and a post-reactor treatment zone having at least a separation vessel configured to receive the second discharge slurry or both the first discharge slurry and the second discharge slurry. 1. A polyolefin production system comprising:a first reactor configured to produce a first reactor discharge comprising a first polyolefin;a second reactor configured to produce a second reactor discharge comprising a second polyolefin; anda post-reactor treatment zone configured to receive the first reactor discharge and the second reactor discharge, wherein the first and second reactors are configured to allow the first reactor discharge to be (a) transferred to the second reactor and, alternatively, (b) diverted to by-pass the second reactor and fed into the post-reactor treatment zone wherein to the first and second polyolefins are first contacted in the post-reactor treatment zone,wherein the first polyolefin is 30 weight % to 70 weight % of the second polyolefin.2. The polyolefin production system of claim 1 , wherein the first reactor and the second reactor each comprise a loop reactor.3. The polyolefin production system of claim 1 , wherein:the post-reactor treatment zone comprises a separation vessel; andthe first and second polyolefins are transferred to the separation vessel such that the first and second polyolefins are first contacted in the separation vessel.4. The polyolefin production system of claim 1 , wherein:the post-reactor treatment zone comprises a purge column; andthe first and second polyolefins are transferred to the purge column such that the first and second polyolefins are first contacted in the purge column.5. The polyolefin production system of claim 1 , wherein:the post-reactor treatment zone comprises an extruder feed tank; ...

SYNTHESIS OF AN ACRYLATE POLYMER IN FLOW REACTOR

An improved process for synthesizing acrylic polymers, which is highly controllable to achieve high molecular weight, high conversion rate, and low polydispersity involves continuously introducing initiator(s), acrylic monomer(s), and optionally other monomers capable of polymerizing with the acrylic monomer(s), into a microchannel of a microreactor having an integral micromixer and an integral heat exchanger. 1. A process for synthesizing a polymer , comprising:continuously introducing a fluid stream including at least one radical initiator and at least one monomer into a channel of a reactor having an integral mixer and an integral heat exchanger to effect simultaneous and substantially continuous mixing of the fluid stream, reaction of the monomers, and heat transfer from the resulting polymer product.2. The process of claim 1 , in which the fluid stream includes at least one acrylate.3. The process of claim 1 , in which the fluid stream includes at least one alkyl acrylate and a nitrogen containing monomer copolymerizable with the alkyl acrylate.4. The process of claim 1 , in which the fluid stream includes butyl acrylate and acrylamide.5. The process of claim 1 , in which at least one monomer that is introduced into the microchannel is dissolved in a solvent in which the monomer is miscible.6. The process of claim 1 , in which at least one radical initiator is an azo compound.7. The process of claim 1 , in which at least one radical initiator is azobisisobutyronitrile.8. The process of claim 1 , in which at least one radical initiator that is introduced into the microchannel is dispersed in a solvent in which the radical initiator is miscible.9. The process of claim 1 , in which at least one radical initiator is introduced into the microchannel via a first pump and at least one acrylic monomer is introduced into the microchannel via a second pump.10. The process of claim 1 , in which the copolymer product is poly(butyl acrylate-co-acrylamide).11. The process of ...

Recovery of hydrocarbons from a hydrocarbon recycle

The invention relates to a process for the polymerization of olefins comprising the comprising the steps of a. Polymerizing olefins in a reaction mixture comprising monomers, diluent, processing as aids to prepare a product stream comprising polyolefins, monomers and diluent; b. Removing the polyolefins from the product stream to obtain a purge stream; c. Removing gaseous components from the purge stream to obtain a liquid fraction; d. Treating the liquid fraction with at least one ionic liquid to obtain a fraction containing unsaturated hydrocarbons; e. Recycling the fraction containing unsaturated hydrocarbons to the reaction mixture, optionally after purification of said fraction containing unsaturated hydrocarbons. The invention also relates to an olefin polymerization system comprising a polymerization reactor, a purge vessel, a vent gas recovery and an ionic liquid separator for separating liquid alkenes from liquid alkanes, wherein the liquid alkenes which are separated from the alkanes in the ionic liquid separator can be recycled to the polymerization reactor.

Systems and processes for polyacrylic acid production

Disclosed are systems and methods for the production of polyacrylic acid and superabsorbent polymers from ethylene oxidation to form ethylene oxide. Reacting the ethylene oxide with carbon monoxide to form to beta propiolactone (BPL) or polypropiolactone (PPL), or a combination thereof. An outlet configured to provide a carbonylation stream comprising the BPL or PPL, or a combination thereof and using one or more reactors to convert BPL to acrylic acid or to convert at least some of the BPL to PPL, and then to convert PPL to acrylic acid. An outlet configured to provide a PPL stream to a second reactor tm to convert at least some of the PPL to AA or a third reactor to convert at least some of the PPL to AA. The outlet configured to provide an AA stream to a fourth reactor to convert the AA to polyacrylic acid.

SYSTEM AND METHOD FOR RAPID TRANSITIONING OF POLYOLEFIN PROCESSES FROM ONE PRODUCT TO ANOTHER

A gas-phase polyolefin reactor system for rapidly transitioning from one polyolefin product to another is disclosed. The reactor system comprises a steady-state control valve, a high-flow valve, a polyolefin reactor, a flow meter, a totalizer, an online analyzer and an empirical model. During a transition, the on-line analyzer measures an initial concentration of a reaction component, the empirical model predicts a required amount based upon the measured initial concentration and a selected ending concentration, the flow meter measures a flow rate, the totalizer determines a totalized amount when the flow rate of the first stream reaches the required amount based upon the measured flow rate and outputs the totalized amount to the empirical model, and the empirical model compares the required amount to the totalized amount and determines a transition endpoint. A method of rapidly transitioning the reactor system from one polyolefin product to another is also disclosed. 1. A gas-phase polyolefin reactor system , comprising:a) a steady-state control valve, wherein a first stream is connected to an input end of the steady-state control valve and to an input end of a high-flow valve and a second stream is connected to an output end of the steady-state control valve and the high-flow valve, wherein the second stream is connected to a third stream, wherein the third stream is connected to an input of a gas-phase polyolefin reactor;b) wherein the first, second and third streams comprise a reaction component, wherein an on-line analyzer measures an initial concentration of the reaction component in the third stream upstream from the gas-phase polyolefin reactor, wherein an empirical model predicts a required amount of a reaction component based upon the measured initial concentration and a selected ending concentration, wherein a flow meter measures a flow rate of the first stream near the input end of the high-flow valve and outputs the measured flow rate to a totalizer, ...

SOLUTION POLYMERIZATION PROCESS

Disclosed herein is a system for solution polymerization comprising a reactor system that is operative to receive an anti-solvent, a monomer, and a solvent, and to react the monomer to form a polymer; where the anti-solvent is not a solvent for the polymer and is operative to reduce the lower critical solution temperature; a plurality of devolatilization vessels located downstream of the reactor system, where each devolatilization vessel operates at a lower pressure than the preceding devolatilization vessel and wherein the plurality of devolatilization vessels receives a polymer solution from the reactor system; and a liquid-liquid separator that is operative to receive a polymer solution from the reactor system and to facilitate a separation between the polymer and volatiles by reducing the pressure and temperature of the polymer solution in the liquid-liquid separator. 1. A system for solution polymerization comprising:a reactor system that is operative to receive an anti-solvent, a monomer, and a solvent, and to react the monomer to form a polymer; where the anti-solvent is not a solvent for the polymer and is operative to reduce the lower critical solution temperature;a plurality of devolatilization vessels located downstream of the reactor system, where each devolatilization vessel operates at a lower pressure than the preceding devolatilization vessel and wherein the plurality of devolatilization vessels receives a polymer solution from the reactor system; anda liquid-liquid separator that is operative to receive a polymer solution from the reactor system and to facilitate a separation between the polymer and volatiles by reducing the pressure and temperature of the polymer solution in the liquid-liquid separator, with the polymer is present in a polymer-rich phase and the volatiles are present in a solvent-rich phase.2. The system of claim 1 , where the anti-solvent is ethane claim 1 , the monomer is an α-olefin and where the solvent is methylcyclohexane.3. ...

PROCESS

The invention provides a process for separating hydrogen from a gaseous feed stream in a polymerisation process, comprising the steps i) polymerising an olefin monomer and optionally at least one olefin comonomer, in the presence of a solvent optionally in the presence of hydrogen, so as to form a polymerisation reaction mixture comprising a polyolefin polymer, unreacted monomer(s), solvent and hydrogen; ii) separating said polyolefin polymer from said unreacted monomer(s), solvent and hydrogen; iii) feeding said unreacted monomer(s) and hydrogen to a condenser so as to form said gaseous feed stream; iv) contacting said gaseous feed stream with a hydrogen separating membrane so as to form a hydrogen-rich gaseous stream and a hydrogen-lean gaseous stream. 1. A process for separating hydrogen from a gaseous feed stream in a polymerisation process , comprising the steps:i. polymerising an olefin monomer and optionally at least one olefin comonomer, in the presence of a solvent, optionally in the presence of hydrogen, so as to form a polymerisation reaction mixture comprising a polyolefin polymer, unreacted monomer(s), solvent and hydrogen;ii. separating said polyolefin polymer from said unreacted monomer(s), solvent and hydrogen;iii. feeding said unreacted monomer(s), solvent and hydrogen to a separator so as to form said gaseous feed stream;iv. contacting said gaseous feed stream with a hydrogen separating membrane so as to form a hydrogen-rich gaseous stream and a hydrogen-lean gaseous stream.2. The process as claimed in or , wherein said polymerisation process is a solution polymerisation process.3. The process as claimed in any of to , further comprisingv. recycling the hydrogen-lean gaseous stream from step iv to step i.4. The process as claimed in any of to , wherein said polyolefin is polyethylene.5. The process as claimed in claim 5 , wherein said polyethylene is a polyethylene homopolymer or a polyethylene copolymer of ethylene and at least one alpha-olefin ...

Methods of Making Polyethylene Polymer Comprising Polar Comonomer and Polymer Compositions

A continuous process for producing high pressure polyethylene is described. The process includes contacting first amounts of ethylene, an optional polar comonomer, and a first Cto Cmodifier in the presence of a first amount of initiator in a reaction system under polymerization conditions to form a reaction system effluent comprising a first polyethylene resin having a first concentration of unreacted monomer therein; and directing an ethylene stream and the reaction system effluent to a pressure separation unit operated at separation conditions thereby removing at least a portion of the unreacted monomer from the reaction system effluent. 1. A continuous process for producing high pressure polyethylene , comprising:{'sub': 2', '12, 'contacting a first amount of ethylene and a first amount of a Cto Cmodifier in the presence of a first amount of initiator in a reaction system under polymerization conditions to form a reaction system effluent comprising a first polyethylene resin having a first concentration of an unreacted monomer therein; and'}directing an ethylene stream and the reaction system effluent to a pressure separation unit operated at separation conditions thereby removing at least a portion of the unreacted monomer from the reaction system effluent.2. The process of claim 1 , further including providing a first amount of polar monomer claim 1 , and contacting the first amount of ethylene claim 1 , the first amount of a Cto Cmodifier and the first amount of polar monomer claim 1 , wherein the unreacted monomer comprises unreacted polar monomer.3. The process of claim 2 , further including providing a second amount of ethylene claim 2 , a second amount of polar monomer claim 2 , and a second amount of a Cto Cmodifier to the reaction system.4. The process of claim 1 , wherein the first amount of a Cto Cmodifier includes at least one saturated or unsaturated modifier claim 1 , preferably a linear or branched claim 1 , substituted or unsubstituted aldehyde or ...

Pressure Management for Slurry Polymerization

Processes and systems for the production for pressure management of a polymerization product flowing from a loop polymerization reactor to a separation vessel in a slurry polymerization system are disclosed herein. For example, a process comprises withdrawing a polymerization product slurry from a loop polymerization reactor, conveying the polymerization product slurry through a first line comprising a continuous take-off valve to yield a mixture comprising a vapor phase, wherein the mixture exits the continuous take-off valve, and conveying the mixture through a second line comprising a flashline heater so that the mixture has a Froude number in a range from about 5 to about 100. 1. A process for pressure management of a polymerization product in slurry polymerization , the process comprising:withdrawing a polymerization product slurry from a loop polymerization reactor;conveying the polymerization product slurry through a first line comprising a continuous take-off valve to yield a mixture comprising a vapor phase, wherein the mixture exits the continuous take-off valve; andconveying the mixture through a second line comprising a flashline heater so that the mixture has a Froude number in a range from about 5 to about 100.2. The process of claim 1 , wherein a drop in pressure of the first line is less than a drop in pressure of the second line.3. The process of claim 1 , wherein a drop in pressure of the first line is greater than a drop in pressure of the second line.4. The process of claim 1 , wherein the Froude number of the mixture conveyed through the flashline heater is in a range of about 10 to about 60.5. The process of claim 1 , wherein the flashline heater comprises a plurality of segments.6. The process of claim 5 , wherein the conveying the mixture through the second line comprising the flashline heater comprises:conveying the mixture through at least one segment of the plurality of segments of the flashline heater so that the mixture has a Froude ...

Cooling between multiple polyolefin polymerization reactors

A system and method for a first reactor to produce a transfer slurry having a first polyolefin polymerized in the first reactor, a heat-removal zone to remove heat from the transfer slurry, and a second reactor to receive the transfer slurry cooled by the heat-removal zone, the second reactor to produce a product slurry having a product polyolefin which includes the first polyolefin and a second polyolefin polymerized in the second reactor.

POLYMERIC MATERIALS

Apparatus for undertaking a chemical reaction includes an elongate housing and a receptacle. The elongate housing may include a cooling means, and end fittings, which may include ports where fluids may be introduced and/or removed. In use of the apparatus, a chemical reaction product is formed within the receptacle. Subsequently the receptacle containing the chemical reaction product is withdrawn from the elongate housing. 127-. (canceled)28. An Apparatus for undertaking a polymerisation reaction to produce a drag reducing polymer , the apparatus comprising:(a) an elongate housing; and(b) an elongate receptacle within the housing, said receptacle being arranged to receive reagents for reaction in the apparatus to produce a drag reducing polymer.29. The apparatus according to claim 28 , wherein said receptacle comprises a plastic film material which has a thickness of at least 20 μm (preferably at least 50 μm) and a thickness of less than 2000 μm (preferably less than 1000 μm); and/or wherein the internal wall area of the receptacle is defined as the area of the receptacle which is arranged to contain material (e.g. polymer in use) claim 28 , wherein at least 50% (preferably about 100%) of the internal wall area is defined by a said plastic film material which consists of a single layer.30. The apparatus according to claim 29 , wherein said plastic material of said film comprises an optionally-substituted polyolefin polymer claim 29 , for example polyethylene.31. The apparatus according to claim 29 , wherein said receptacle includes a first end and a second end which are spaced apart along the elongate extent of the receptacle claim 29 , wherein said first end is a closed end and includes a sealed region claim 29 , wherein said receptacle is formed from lay-flat tubing.32. The apparatus according to claim 31 , wherein the length of the receptacle is the linear distance between said first end and said second end claim 31 , wherein the diameter of the receptacle is ...

On-Line Adjustment of Mixed Catalyst Ratio and Olefin Polymerization

The present disclosure provides processes for polymerizing olefin(s). In at least one embodiment, a method for producing a polyolefin is provided. The method includes contacting a first composition and a second composition in a line to form a third composition. The first composition includes a contact product of a first catalyst, a second catalyst, a support, a first activator, and a diluent, and the mol ratio of first catalyst to second catalyst is from 90:10 to 40:60. The second composition includes a contact product of the second catalyst, a second activator, and a second diluent. The third composition includes a mol ratio of first catalyst to second catalyst of from 89:11 to 10:90. The method includes introducing the third composition from the line into a gas-phase fluidized bed reactor, exposing the third composition to polymerization conditions, and obtaining a polyolefin.

On-Line Adjustment of Mixed Catalyst Ratio By Trim and Olefin Polymerization with the Same

In an embodiment, a method for producing a polyolefin is provided. The method includes: contacting a first composition and a second composition in a line to form a third composition, wherein: the first composition comprises a contact product of a first catalyst, a second catalyst, a support, and a diluent, wherein the mol ratio of second catalyst to first catalyst is from 60:40 to 40:60, the second composition comprises a contact product of the second catalyst and a second diluent; introducing the third composition from the line into a gas-phase fluidized bed reactor; exposing the third composition to polymerization conditions; and obtaining a polyolefin.

On-Line Adjustment of Catalysts by Trim and Olefin Polymerization

In an embodiment, a method for producing a polyolefin includes contacting a first composition and a second composition in in a line to form a third composition, wherein: the first composition comprises a contact product of a first catalyst, a second catalyst, a support, a first activator, and a diluent, wherein the mol ratio of second catalyst to first catalyst is from 60:40 to 40:60, the second composition comprises a contact product of the third catalyst, a second activator, and a second diluent, and the third composition comprises a mol ratio of the third catalyst to the second catalyst to the first catalyst of from 10:35:55 to 60:15:25, such as 30:20:30; introducing the third composition from the line into a gas-phase fluidized bed reactor; exposing the third composition to polymerization conditions; and obtaining a polyolefin. 1. A method for producing a polyolefin comprising: the first composition comprises a contact product of a first catalyst, a second catalyst, a support, a first activator, and a diluent, wherein the mol ratio of second catalyst to first catalyst is from 60:40 to 40:60,', 'the second composition comprises a contact product of a third catalyst, a second activator, and a second diluent, and', 'the third composition comprises a mol ratio of third catalyst to second catalyst to first catalyst of from 10:35:55 to 60:15:25;, 'contacting a first composition and a second composition in a line to form a third composition, whereinintroducing the third composition from the line into a gas-phase fluidized bed reactor;exposing the third composition to polymerization conditions; andobtaining a polyolefin.2. The method of claim 1 , wherein the first catalyst is a metallocene catalyst and the second catalyst is a metallocene catalyst.3. The method of claim 2 , wherein the third catalyst is a metallocene catalyst.4. The method of claim 1 , wherein the first composition further comprises a wax.5. (canceled)6. The method of claim 1 , wherein a mol ratio of ...

Polyolefin production with chromium-based catalysts

A method including contacting a chromium-based catalyst with a reducing agent in a solvent to lower an oxidation state of at least some chromium in the chromium-based catalyst to give a reduced chromium-based catalyst, drying the reduced chromium-based catalyst at a temperature, and adjusting the temperature to affect the flow index response of the reduced chromium-based catalyst.

POLYETHYLENE PRODUCTION WITH MULTIPLE POLYMERIZATION REACTORS

A system and method for discharging a transfer slurry from a first polymerization reactor through a transfer line to a second polymerization reactor, the transfer slurry including at least diluent and a first polyethylene. A product slurry is discharged from the second polymerization reactor, the product slurry including at least diluent, the first polyethylene, and a second polyethylene. The velocity, pressure drop, or pressure loss due to friction in the transfer line is determined, and a process variable adjusted in response to the velocity, pressure drop, or pressure loss not satisfying a specified value. 1. A method of operating a polyethylene reactor system , comprising:discharging continuously a transfer slurry from a first polymerization reactor through a transfer line to a second polymerization reactor, the transfer slurry comprising diluent and a first polyethylene;discharging a product slurry from a second polymerization reactor, the product slurry comprising diluent, the first polyethylene, and a second polyethylene;calculating a pressure loss due to friction in the transfer line to determine a calculated pressure loss; andmeasuring a pressure differential through the transfer line to determine a measured pressure differential and adjusting a process variable in response to the measured pressure differential exceeding the calculated pressure loss by a specified amount.2. The method of claim 1 , wherein the first polymerization reactor and the second polymerization reactor each comprise a liquid-phase reactor.3. The method of claim 1 , wherein the first polymerization reactor and the second polymerization reactor each comprise a loop reactor.4. The method of claim 1 , comprising:feeding ethylene, diluent, and catalyst to the first polymerization reactor;polymerizing ethylene in the first polymerization reactor to form the first polyethylene, wherein the transfer slurry comprises active catalyst; andpolymerizing ethylene in the second polymerization ...

POLYETHYLENE PRODUCTION WITH MULTIPLE POLYMERIZATION REACTORS

A system and method for discharging a transfer slurry from a first polymerization reactor through a transfer line to a second polymerization reactor, the transfer slurry including at least diluent and a first polyethylene. A product slurry is discharged from the second polymerization reactor, the product slurry including at least diluent, the first polyethylene, and a second polyethylene. The velocity, pressure drop, or pressure loss due to friction in the transfer line is determined, and a process variable adjusted in response to the velocity, pressure drop, or pressure loss not satisfying a specified value. 1. A method of operating a polyethylene reactor system , comprising:discharging continuously a transfer slurry from a first polymerization reactor through a transfer line to a second polymerization reactor, the transfer slurry comprising diluent and a first polyethylene;discharging a product slurry from a second polymerization reactor, the product slurry comprising diluent, the first polyethylene, and a second polyethylene;calculating a pressure loss due to friction in the transfer line to determine a calculated pressure loss; andmeasuring a pressure differential through the transfer line to determine a measured pressure differential and adjusting a process variable in response to the measured pressure differential exceeding the calculated pressure loss by a specified amount.2. The method of claim 1 , wherein the first polymerization reactor and the second polymerization reactor each comprise a liquid-phase reactor.3. The method of claim 1 , wherein the first polymerization reactor and the second polymerization reactor each comprise a loop reactor.4. The method of claim 1 , comprising:feeding ethylene, diluent, and catalyst to the first polymerization reactor;polymerizing ethylene in the first polymerization reactor to form the first polyethylene, wherein the transfer slurry comprises active catalyst; andpolymerizing ethylene in the second polymerization ...

Continuous reaction apparatus and method of continuous polymerization using the same

The present invention includes a first raw material feeding unit, a second raw material feeding unit, a reactor unit, and a controller configured to control the amount of a first raw material being fed from the first raw material feeding unit to the reactor unit, the amount of a second raw material being fed from the second raw material feeding unit to the reactor unit, the temperature of the first raw material being fed from the first raw material feeding unit to the reactor unit, and the temperature of the second raw material being fed from the second raw material feeding unit to the reactor unit. The first raw material is raw material monomer solution containing a raw material monomer. The second raw material is polymerization initiator solution containing a polymerization initiator. A reaction product is polymer compound resulting from a living anionic polymerization reaction of the raw material monomer.

Process for Forming Polyolefins

Processes of forming polyolefins are described herein. One or more specific embodiments of the processes generally include introducing olefin monomer selected from C 2 -C 3 olefins into a first reaction zone under first polymerization conditions to form a first polyolefin; withdrawing a transfer effluent from the first reaction zone, the transfer effluent including first polyolefin and unreacted olefin monomer; introducing the transfer effluent, a comonomer selected from C 4 -C 8 olefins, and additional olefin monomer to a second reaction zone under second polymerization conditions to form a second reactor product; maintaining an essentially constant comonomer:olefin monomer ratio in the second reaction zone; and withdrawing at least a portion of the second reactor product, wherein the second reactor product includes a bimodal polyolefin.

USE OF AT LEAST ONE HEMI-PEROXYACETAL, ALONE OR IN COMBINATION WITH OTHER PEROXIDES, TO PROMOTE POLYMERISATION OR COPOLYMERISATION OF ETHYLENE UNDER HIGH PRESSURE

The present invention relates to the use of at least one peroxide selected from the group consisting of hemiperoxyacetals, alone or in combination with one or more distinct additional peroxides, for the radical polymerization or copolymerization of ethylene under high pressure. 121-. (canceled)22. An organic peroxide , for use alone or in combination with one or more distinct additional organic peroxides , selected from the group consisting of hemiperoxyacetals for the radical polymerization or copolymerization of ethylene under high pressure.23. The organic peroxide of claim 22 , which is selected from the group consisting of hemiperoxyacetals having a half-life temperature at one minute and at atmospheric pressure of from 125° C. to 160° C.25. The organic peroxide of claim 22 , wherein the organic peroxide is selected from the group consisting of 1-methoxy-1-tert-amylperoxycyclohexane (TAPMC) claim 22 , 1-methoxy-1-t-butylperoxycyclohexane (TBPMC) claim 22 , 1-methoxy-1-t-amylperoxy-3 claim 22 ,3 claim 22 ,5-trimethylcyclohexane claim 22 , 1-methoxy-1-t-butylperoxy-3 claim 22 ,3 claim 22 ,5-trimethylcyclohexane claim 22 , 1-ethoxy-1-t-amylperoxycyclohexane claim 22 , 1-ethoxy-1-t-butylperoxycyclohexane claim 22 , 1-ethoxy-1-t-butyl-3 claim 22 ,3 claim 22 ,5-peroxycyclohexane and mixtures thereof.26. The organic peroxide of claim 22 , wherein the organic peroxide is 1-methoxy-1-tert-amylperoxycyclohexane.27. The organic peroxide of claim 22 , wherein the additional peroxide or peroxides is or are selected from the group consisting of peroxyacetals.28. The organic peroxide of claim 22 , wherein the additional peroxide or peroxides is or are selected from the group consisting of peroxyacetals capable of initiating the radical polymerization or copolymerization of ethylene under high pressure in a temperature range of from 190° C. to 250° C.30. The organic peroxide of claim 22 , wherein the additional peroxide or peroxides is or are selected from the group consisting ...

METHOD FOR ISOMER REDUCTION DURING POLYMERIZATION AND SYSTEM FOR ACCOMPLISHING THE SAME

Disclosed herein is a method for reducing isomerization during the copolymerization of ethylene with an α-olefin comprising adding to a reactor a reaction mixture comprising hydrogen, ethylene, an α-olefin, a solvent and a catalyst; where the catalyst does not include a chain shuttling agent that comprises dialkyl zinc; heating the reactor to a first temperature to react the ethylene with the α-olefin to form a copolymer; discharging from the reactor a first product stream to a heat exchanger; where the product stream comprises the copolymer; adding to the product stream prior to the heat exchanger a first additive that is operative to reduce isomerization of the α-olefin; and discharging from the heat exchanger a second product stream. 1. A method for reducing isomerization during the copolymerization of ethylene with an α-olefin comprising:adding to a reactor a reaction mixture comprising hydrogen, ethylene, an α-olefin, a solvent and a catalyst; where the catalyst does not include a chain shuttling agent that comprises dialkyl zinc;heating the reactor to a first temperature to react the ethylene with the α-olefin to form a copolymer;discharging from the reactor a first product stream to a heat exchanger; where the product stream comprises the copolymer;adding to the product stream prior to the heat exchanger a first additive that is operative to reduce isomerization of the α-olefin; anddischarging from the heat exchanger a second product stream.2. The method of claim 1 , further comprising adding a second additive to the reactor claim 1 , where the second additive is operative to reduce isomerization of the α-olefin.3. The method of claim 2 , further comprising adding a third additive to the second product stream claim 2 , where the third additive is operative to reduce isomerization of the α-olefin.4. The method of claim 3 , where the first additive is the same or different from the second additive and where the first additive and the second additive are the ...

REACTOR

A polymerization device that includes: a reaction vessel that houses a polymerization solution and in which a polymerization reaction is performed; a stirring blade that stirs the polymerization solution housed in the reaction vessel; a plurality of heat transfer pipes that transfer heat to the polymerization solution in order to start the polymerization reaction and cause the polymerization reaction to proceed, and that remove, from the polymerization solution, heat generated by the polymerization reaction; and a baffle arranged between a vessel wall of the reaction vessel and the heat transfer pipes. 1. A reactor comprising:a reaction vessel that houses a polymerization solution and in which a polymerization reaction is performed;a stirring blade configured to stir the polymerization solution housed in the reaction vessel;a plurality of heat transfer pipes configured to transfer heat to the polymerization solution in order to start the polymerization reaction and cause the polymerization reaction to proceed, and to remove, from the polymerization solution, heat generated by the polymerization reaction; anda baffle arranged between a vessel wall of the reaction vessel and the heat transfer pipes; whereinthe plurality of heat transfer pipes are arranged in a circumferential shape around the stirring blade, include heat transfer pipes whose lower ends are arranged in a position higher than a bottom face of the reaction vessel, and restrict an amount of the polymerization solution circulated from an inner side to a vessel wall side of the reaction vessel, at a depth at which the heat transfer pipes are arranged, andthe baffle changes a flow direction of the polymerization solution that has flowed between the vessel wall of the reaction vessel and the heat transfer pipes arranged in the circumferential shape, and generates a flow of the polymerization solution to an inward direction of the reaction vessel.2. The reactor according to claim 1 , whereina plurality of the ...

Single-Site Catalyst Polyolefin Polymerization Process

Disclosed is a method for polymerizing olefins comprising passing a heterogeneous single-site catalyst to a solution or slurry polymerization reactor in the absence of pre-polymerization, wherein the polymerization reactor operates at a temperature of at least 50° C. The heterogeneous single-site catalyst may be suspended and/or dissolved in a solvent selected from the group consisting of oils, aliphatic hydrocarbons and mixtures thereof. Also, the heterogeneous single-site catalyst may be passed to the polymerization reactor at a velocity of greater than 1 m/s or 3 m/s.

Methods for Determining Transition Metal Compound Concentrations in Multicomponent Liquid Systems

Methods for determining the concentration of transition metal compounds in a solution containing more than one transition metal compound are described. Polymerization reactor systems providing real-time monitoring and control of the concentrations of the transition metal components of a multicomponent catalyst system are disclosed, as well as methods for operating such polymerization reactor systems and for improving methods of preparing the multicomponent catalyst system.

Methods for Scale-Up From a Pilot Plant to a Larger Production Facility

Methods for scale-up from a pilot plant to full production of a bimodal polymer product having a density, melt index, and a melt index ratio are provided herein. The methods provide for adjusting reactor conditions and catalyst ratio of a bimodal catalyst system to optimize the transition from single catalyst to bimodal polymer compositions on a full-scale process plant consistent with pilot plant development. 1. A method for scale-up from a pilot plant to a larger production facility of a bimodal polymer product having a density and a melt index comprising the steps of:producing a bimodal polymer product in a first reactor in a pilot plant with a bimodal catalyst system under a first set of operating conditions, wherein the bimodal catalyst system comprises a first catalyst and a second catalyst and the bimodal polymer product has a bimodal polymer product density and a bimodal polymer product melt index;producing a single catalyst polymer composition in the first reactor in the pilot plant with a single catalyst system under a second set of operating conditions, wherein the single catalyst polymer composition has a single catalyst polymer composition density and a single catalyst polymer composition melt index, and the single catalyst polymer composition is produced in the first reactor before or after the step of producing the bimodal polymer product in the first reactor;producing the single catalyst polymer composition in a second reactor in a full-scale process plant with the single catalyst system, wherein the second set of operating conditions to produce the single catalyst polymer composition are adjusted to provide a third set of operating conditions;determining a fourth set of operating conditions, wherein each operating condition of the fourth set of operating conditions equals a ratio of the operating condition of the third set of operating conditions to the operating condition of the second set of operating conditions and the operating condition of the ...

REDUCTION OF FOULING IN HIGH PRESSURE REACTORS

The Application of equations of state to experimental and literature data permits the formation of a model and phase diagram(s) that show under what conditions polyethylene is likely to precipitate out of a high pressure solution of polyethylene in supercritical ethylene. This then permits a better definition to run a high pressure reactor to reduce the likelihood of phase separation, loss of cooling and potentially decomposition of the reactor contents. 1. A method to determine the curve of the liquid liquid equilibrium boundary as a function of molecular weight distribution (MWD) for a multitude of different products comprising from about 80 to about 100 wt. % of ethylene and about 0 up to about 20 weight % of one or more Calpha olefins having a molecular weight from about 8 ,000 to about 500 ,000 produced in super critical ethylene in a high pressure reactor at temperatures from about 80° C. to about 350° C. and pressures from about 100 MPa to about 350 MPa comprising:a) modeling experimental or literature data for the liquid liquid equilibrium using an equation of state model to describe the effects of the molecular weight and the polydispersity of the polyethylene on the liquid liquid equilibrium curveb) determining the composition-specific parameters of the model from a); and,c) applying an equation of state model selected from TPT1, TPT1-MSA and TPT1-RHNC to the temperature, pressure and composition conditions of the reaction to generate the liquid liquid equilibrium boundary and optionally the critical polymer concentration.2. The process according to wherein the reactor is a tubular reactor.3. A process to prepare a liquid polymer lean/liquid polymer rich and liquid liquid phase diagram for a reactor for polymerizing a system comprising a polymer having a weight average molecular weight from about 8 claim 1 ,000 to about 500 claim 1 ,000 comprising from about 80 to about 100 wt % of ethylene and about 0 to about 20 wt % of one or more Calpha olefins in ...

Method for producing water-soluble homopolymers or copolymers which comprise (meth)acrylamide

A process for preparing water-soluble homo- or copolymers comprising (meth)acrylamide by free-radical polymerization of an aqueous solution of monoethylenically unsaturated monomers comprising at least (meth)acrylamide in the presence of at least one stabilizer for prevention of polymer degradation by molecular oxygen. The stabilizer is preferably one selected from the group of sulfur compounds, sterically hindered amines, N-oxides, nitroso compounds, aromatic hydroxyl compounds and ketones, more preferably 2-mercaptobenzothiazole or a salt thereof.

CONTINUOUS EMULSION POLYMERIZATION PROCESS AND INITIATION SYSTEM

In a continuous emulsion polymerization process, at least one monomer, an aqueous phase, and at least two different redox initiators are added to a continuous polymerization reactor comprising a first zone and a second zone. At least one redox initiator is added to the first zone and at least one redox initiator is added to the second zone. 1. A continuous emulsion polymerization process comprising:adding at least one monomer, an aqueous phase, and at least two different redox initiators to a continuous tubular reactor comprising (1) a circulating loop section and (2) a secondary line section having one end connected to a discharge opening of the loop section and a polymer outlet at its other end; andpolymerizing the at least one monomer.2. The process of claim 1 , wherein each redox initiator comprises a reducing agent and an oxidizing agent.3. The process of claim 1 , wherein the at least two different redox initiators are added to the tubular reactor at different locations.4. The process of claim 2 , wherein at least one of the at least two different redox initiators is added to the circulating loop section of the tubular reactor.5. The process of claim 4 , wherein the reducing agent from at least one of the at least two different redox initiators is added to the secondary line section of the tubular reactor.6. The process of claim 4 , wherein oxidizing agent from at least one of the at least two different redox initiators is added to the secondary line section of the tubular reactor.7. The process of claim 2 , wherein at least one of the at least two different redox initiators is water soluble and at least one of the at least two different redox initiators is oil soluble.8. The process of claim 7 , wherein the water soluble initiator is added to the reactor upstream of where the oil soluble initiator is added.9. The process of claim 7 , wherein the oxidizing agent from the oil soluble redox initiator is added to the circulating loop section of the tubular ...

HIGH-PRESSURE POLYMERIZATION PROCESS OF ETHYLENICALLY UNSATURATED MONOMERS

A process for polymerizing or copolymerizing ethylenically unsaturated monomers in the presence of free-radical polymerization initiators, wherein the polymerization is carried out at temperatures from 100° C. to 350° C. and pressures in the range of from 110 MPa to 500 MPa in a continuously operated polymerization reactor which is controlled by a pressure control valve at the outlet of the polymerization reactor, the process comprising continuously monitoring the pressure within the polymerization reactor, feeding a pressure signal to a controller for controlling the control valve and having the controller altering the opening of the pressure control valve to control the pressure within the polymerization reactor, wherein the controller starts an emergency shutdown program when the pressure control valve closes more than a preset threshold value and the pressure within the polymerization reactor decreases below a preset pressure threshold. 1. A process for polymerizing or copolymerizing ethylenically unsaturated monomers in the presence of free-radical polymerization initiators , wherein the polymerization is carried out at temperatures from 100° C. to 350° C. and pressures in a range of from 110 MPa to 500 MPa in a continuously operated polymerization reactor which is controlled by a pressure control valve at the outlet of the polymerization reactor and the monomer mixture is brought to the polymerization pressure by a combination of a primary compressor and a secondary compressor ,the process comprising continuously monitoring the pressure within the polymerization reactor by one or more pressure sensors creating a pressure signal indicative of the pressure within the polymerization reactor, feeding the pressure signal to a controller for controlling the control valve and having the controller altering the opening of the pressure control valve to control the pressure within the polymerization reactor,wherein the controller starts an emergency shutdown program ...

Olefin-Based Polymer

An olefin-based polymer and method of making the same is disclosed herein. In some embodiments, the olefin-based polymer has multiple crystallinity and satisfies the following: (1) two or more peaks in a temperature range of −20° C. to 120° C. when measured by cross-fractionation chromatography (CFC), and T(90)−T(50)<8.0° C., (2) a soluble fraction (SF) of 1 wt % or less at −20° C. in CFC, (3) 15° C. Подробнее

WATER-ABSORBENT RESIN PRODUCTION APPARATUS

In a water-absorbent resin production apparatus for producing a water-absorbent resin by polymerizing a water-soluble ethlenically unsaturated monomer, a water-absorbent resin powder obtained by drying a water-absorbent resin composition with a dryer passes through a first powder flow path pipe, is discharged therefrom toward a classifier while a flow rate is regulated so as to a predetermined value by a powder flow rate regulating discharge member composed of a hopper and a rotary valve, and is classified by the classifier. In the water-absorbent resin production apparatus, a collector for collecting a powder aggregate composed of aggregated particles of the water-absorbent resin powder is disposed in the first powder flow path pipe. Accordingly, a water-absorbent resin in the form of a particulate powder from which the powder aggregate is removed can be produced at a high production efficiency. 1. A water-absorbent resin production apparatus , comprising:a polymerization reactor provided with a resin composition outflow opening portion, in the polymerization reactor a water-soluble ethylenically unsaturated monomer being polymerized to obtain a water-absorbent resin composition including a water-absorbent resin as a polymer of the water-soluble ethylenically unsaturated monomer, the water-absorbent resin composition flowing out from the polymerization reactor through the resin composition outflow opening portion;a resin composition flow path member having one end portion connected to the resin composition outflow opening portion, the resin composition flow path member functioning as a flow path through which the water-absorbent resin composition flowing out from the resin composition outflow opening portion passes; the dryer being provided with a resin composition inflow opening portion which is connected to the other end portion of the resin composition flow path member, and a powder outflow opening portion,', 'the water-absorbent resin composition passing ...

APPARATUS FOR PRODUCING WATER-ABSORBENT RESIN

In an apparatus for producing the water-absorbent resin, gas heated by the polymerization heat accompanied by a polymerization reaction in a reactor main body flows through a first pipe into a heat exchanging structure, and a cooled fluid obtained by the cooling flows through a second pipe into the reactor main body. In the apparatus, a first pipe temperature adjusting portion adjusts a temperature of the first pipe to fall within a predetermined temperature range, and a polymerization reactor temperature adjusting portion adjusts a temperature of an upper portion of the reactor main body to fall within a predetermined temperature range. 1. An apparatus for producing a water-absorbent resin , comprising: a reactor main body in which the water soluble ethylenically unsaturated monomer and the liquid medium is contained and an upper portion of which is left for a gaseous phase portion, and', 'a gas discharging portion which is connected to the reactor main body and discharges gas of the gaseous phase portion from the reactor main body;, 'a polymerization reactor in which a water-absorbent resin is produced by polymerization reaction on a water soluble ethylenically unsaturated monomer in a liquid medium, the polymerization reactor including'}a first channel portion having a first channel which is connected to the gas discharging portion and through which the gas discharged from the reactor main body by the gas discharging portion flows;a first channel portion temperature adjusting portion which adjusts a temperature of the first channel portion to fall within a predetermined temperature range in which the gas flowing through the first channel of the first channel portion is not condensed; a cooler main body which is connected to the first channel portion, into which the gas flowing through the first channel of the first channel portion flows, and which cools inflow gas, and', 'a cooled fluid discharging portion which is connected to the cooler main body and discharges ...

APPARATUS FOR PREPARING POLYBUTADIENE

Provided is an apparatus for preparing polybutadiene which may improve productivity by minimizing a plugging phenomenon occurred during the preparation of polybutadiene and increasing a conversion rate. The apparatus for preparing polybutadiene includes two first polymerization reactors arranged in parallel to reduce the plugging phenomenon in which butadiene (reaction raw material), a polymerization catalyst, and a solvent are respectively supplied and polymerized, at least one second polymerization reactor arranged in series with the first polymerization reactors in which a first polymerization solution containing a butadiene polymer discharged from the first polymerization reactors is supplied and a butadiene polymerization reaction is performed, and one or more condensers which condense gases discharged from the first polymerization reactors and the second polymerization reactor and supply a condensate to the first polymerization reactors and/or the second polymerization reactor. 1. An apparatus for preparing polybutadiene , the apparatus comprising:two first polymerization reactors arranged in parallel to reduce a plugging phenomenon in which butadiene (reaction raw material), a polymerization catalyst, and a solvent are respectively supplied and polymerized;at least one second polymerization reactor arranged in series with the first polymerization reactors in which a first polymerization solution containing a butadiene polymer discharged from the first polymerization reactors is supplied and a butadiene polymerization reaction is performed; andone or more condensers which condense gases discharged from the first polymerization reactors and the second polymerization reactor and supply a condensate to the first polymerization reactors and/or the second polymerization reactor.2. The apparatus for preparing polybutadiene of claim 1 , wherein a conversion rate into the butadiene polymer is increased when a residence time of a feedstock in the parallel-arranged ...

REACTOR

A polymerization device that includes: a reaction vessel that houses a polymerization solution and in which a polymerization reaction is performed; a stirring blade that stirs the polymerization solution housed in the reaction vessel; a plurality of heat transfer pipes that transfer heat to the polymerization solution in order to start the polymerization reaction and cause the polymerization reaction to proceed, and that remove, from the polymerization solution, heat generated by the polymerization reaction; and a baffle arranged between a vessel wall of the reaction vessel and the heat transfer pipes. 1. A manufacturing method for a reaction product comprising:housing a polymerization solution in a reaction vessel in which a polymerization reaction is performed;stirring the polymerization solution housed in the reaction vessel using a stirring blade;transferring heat to the polymerization solution in order to start the polymerization reaction and cause the polymerization reaction to proceed, and to remove, from the polymerization solution, heat generated by the polymerization reaction using a plurality of heat transfer pipes; whereinthe plurality of heat transfer pipes are arranged in a circumferential shape around the stirring blade, include a heat transfer pipe whose lower end is arranged in a position higher than a bottom face of the reaction vessel, and restrict an amount of the polymerization solution circulated from an inner side to a vessel wall side of the reaction vessel, at a depth at which the heat transfer pipes are arranged,the method further comprising changing a flow direction of the polymerization solution that has flowed between the vessel wall of the reaction vessel and the heat transfer pipes arranged in the circumferential shape using a baffle arranged between a vessel wall of the reaction vessel and the heat transfer pipes, thereby generating a flow of the polymerization solution to an inward direction of the reaction vessel, and whereinthe ...

Pressure Management for Slurry Polymerization

Processes and systems for the production for pressure management of a polymerization product flowing from a loop polymerization reactor to a separation vessel in a slurry polymerization system are disclosed herein. For example, a process comprises withdrawing the polymerization product from a loop polymerization reactor, and conveying the withdrawn polymerization product to a separation vessel via a first pressure differential and a second pressure differential. The withdrawn polymerization product may flow through the first pressure differential before flowing through the second pressure differential, and the first pressure differential may be less than the second pressure differential. 1. A process for pressure management of a polymerization product in slurry polymerization , the process comprising:withdrawing the polymerization product from a loop polymerization reactor; andconveying the withdrawn polymerization product to a separation vessel via a first pressure differential and a second pressure differential, wherein the withdrawn polymerization product flows through the first pressure differential before flowing through the second pressure differential, wherein the first pressure differential is less than the second pressure differential.2. The process of claim 1 , wherein the first pressure differential has a drop in pressure between about 5% to about 50% of a total pressure differential between the loop polymerization reactor and the separation vessel claim 1 , wherein the second pressure differential has a drop in pressure between about 50% to about 95% of the total pressure differential between the loop polymerization reactor and the separation vessel.3. The process of claim 2 , wherein the drop in pressure of the first pressure differential is greater than 40% and less than 50% of the total pressure differential claim 2 , wherein the drop in pressure of the second pressure differential is greater than 50% and less than 60% of the total pressure ...

Pressure Management for Slurry Polymerization

Processes and systems for the production for pressure management of a polymerization product flowing from a loop polymerization reactor to a separation vessel in a slurry polymerization system are disclosed herein. For example, a process comprises withdrawing the polymerization product from a loop polymerization reactor, and conveying the withdrawn polymerization product to a separation vessel via a first pressure differential and a second pressure differential. The withdrawn polymerization product may flow through the first pressure differential before flowing through the second pressure differential, and the first pressure differential may be less than the second pressure differential.

HETEROGENEOUS, CO-CONTINUOUS COPOLYMERS OF VINYLIDENE FLUORIDE

The invention relates to a heterogeneous, co-continuous copolymer composition of vinylidene fluoride and at least one other comonomer. Preferred comonomers are hexafluoropropylene and perfluoroalkylvinyl ether. The co-continuous morphology is provide by first forming a first phase polymer, then adding one or more comonomers before half of the original monomer stream has been added, and at an effective level to cause phase separation of the copolymer. The co-continuous morphology provides a means for incorporating a high level of comonomer into the copolymer with little or no adverse effect on the melting temperature. The morphology also provides the copolymer composition with a unique combination of properties, including a high melting point, good flexibility and good low temperature impact resistance. The unique properties of the polymer make it useful in end-use application where those properties provide performance advantages, such as in the wire and cable market, and in oil and gas applications. 1. A melt-processable heterogeneous copolymer composition comprising two or more co-continuous phases , wherein said co-continuous phases comprise:a) from 25 to 50 weight percent of a first co-continuous phase comprising 90 to 100 weight percent of vinylidene fluoride monomer units and 0 to 10 weight percent of other fluoromonomers units, andb) from greater than 50 weight percent to 75 weight percent of a second co-continuous phase comprising from 65 to 95 weight percent of vinylidene fluoride monomer units and an effective amount of one or more comonomers selected from the group consisting of hexafluoropropylene and perfluoroalkylvinyl ether to cause the second co-continuous phase to phase separate from the first continuous phase.2. The heterogeneous copolymer composition of claim 1 , wherein said copolymer composition comprises from 2.5 to 31 weight percent of one or more fluoromonomer units claim 1 , based on the total weight of monomer units in the copolymer ...

POLYMERIZATION REACTOR

The present invention relates to a polymerization reactor. The polymerization reactor according to one aspect of the present invention comprises: a housing including a supply part for supplying a reactant; a tube which is provided inside the housing and extends along the height direction of the housing; a first impeller including a blade which spirally surrounds the tube along the height direction of the housing; a second impeller which is provided inside the housing in order to enable the reactant to flow into the tube; and a partition wall which is provided to surround the second impeller along the circumferential direction. 1. A polymerization reactor comprisinga housing including a supply part for supplying a reactant;a tube which is provided inside the housing and extends along the height direction of the housing;a first impeller including a blade which spirally surrounds the tube along the height direction of the housing;a second impeller which is provided inside the housing in order to enable the reactant to flow into the tube; anda partition wall which is provided to surround the second impeller along the circumferential direction.2. The polymerization reactor according to claim 1 , whereinthe second impeller is provided in a lower region of the housing, andthe supply part is provided in the lower region of the housing such that the reactant is fed into the partition wall.3. The polymerization reactor according to claim 2 , whereinthe farther the partition wall is from the tube, it is provided to have the higher diameter.4. The polymerization reactor according to claim 3 , whereinthe partition wall is provided such that an edge having a maximum diameter is spaced from an inner peripheral surface of the housing.5. The polymerization reactor according to claim 3 , whereinthe partition wall is provided such that its minimum diameter is equal to the diameter of the tube.6. The polymerization reactor according to claim 3 , whereinthe partition wall is provided ...

Methods for Scale-Up From a Pilot Plant to a Larger Production Facility

Methods for scale-up from a pilot plant to a larger production facility of a bimodal polymer product having a density, a melt index and melt index ration are provided herein.

Process for Making Crosslinked Cable Insulation Using High Melt Strength Ethylene-Based Polymer Made in a Tubular Reactor and Optionally Modified with a Branching Agent

An insulated wire or cable is made by a process comprising the steps of: 16-. (canceled)7. A process of making an insulated wire or cable , the process comprising the steps of: (1) a high melt strength ethylene-based polymer made in a tubular reactor and modified with at least one of PPG AEMA, a di- or higher functional (meth)acrylate, a monomeric chain transfer agent, or an asymmetrical polyene, and', '(2) a peroxide, and, '(A) extruding onto a covered or uncovered metal conductor or optical fiber a composition having a DF measured at 130° C. (60 Hz, 2 kV) or 120° C. (60 Hz, 8 kV) or 100° C. (60 Hz, 8 kV) of ≤0.5% and comprising(B) crosslinking the modified, high melt strength ethylene-based polymer.9. A process of making an insulated wire or cable , the process comprising the steps of: [{'sup': 'th', '(1) a branch modified, high melt strength ethylene homopolymer made in a tubular reactor by a process using (A) a tubular reactor comprising i (i≥3) reaction zones in which (1) the peak temperature of the first reaction zone is greater than the peak temperature in the ireaction zone, and (2) the pressure in each reactor zone is less than or equal to (≤) 300 MPa, and (B) a chain transfer agent (CTA) that has a chain transfer constant (Cs) less than or equal to (≤) 0.5, and'}, '(2) a peroxide, and, '(A) extruding onto a covered or uncovered metal conductor or optical fiber a composition having a DF measured at 130° C. (60 Hz, 2 kV) or 120° C. (60 Hz, 8 kV) or 100° C. (60 Hz, 8 kV) of ≤0.5% and comprising(B) crosslinking the branch modified, high melt strength ethylene homopolymer.10. The process of in which the chain transfer agent (CTA) has a chain transfer constant (Cs) less than or equal to (≤) 0.017.11. The process of in which the peroxide is an organic peroxide.12. A low- claim 7 , medium claim 7 , high or extra-high voltage wire or cable comprising:a metal conductor or an optical fiber;an insulation sheath extruded onto the metal conductor or optical fiber, the ...

POLYETHYLENE COPOLYMERS HAVING A PARTICULAR COMONOMER DISTRIBUTION

Novel polyethylene copolymers having a relatively high comonomer partitioning tendency are disclosed as are methods for their preparation. The comonomer partitioning tendency is the tendency for a copolymer to have comonomer in the higher molecular weight chains. Novel metrics for describing the comonomer partitioning tendency are also disclosed. 1. A method for preparing a polyethylene copolymer having a comonomer partitioning tendency of greater than 1.16 by polymerizing ethylene and one or more comonomers in the presence of one or more catalyst compositions.2. A method according to claim 1 , wherein the one or more catalyst compositions comprises a catalyst compound having a titanium claim 1 , a zirconium or a hafnium atom.3. A method according to claim 2 , wherein the catalyst composition comprises two or more catalyst compounds comprising a titanium claim 2 , a zirconium or a hafnium atom.4. A method according to any one of to claim 2 , wherein the catalyst composition further comprises one or more activators or co-catalysts.9. A method according to any one of to wherein the catalyst composition comprises two or more of the catalyst compounds according to any one of to in any ratio.10. A method according to any one of to claim 2 , wherein the comonomer is one or more comonomers containing 3 to 16 carbon atoms.11. A method according to any one of to claim 2 , wherein the polymerization is performed in gas phase claim 2 , slurry phase claim 2 , solution phase claim 2 , high pressure or combinations thereof.12. A method according to any one of to claim 2 , wherein the polymerization is performed in a single gas phase reactor. This application is a Divisional of U.S. National Stage Application Ser. No. 15/568,662 filed Oct. 23, 2017 and published as U.S. Publication No. 2018-0155473 A1 on Jun. 7, 2018, which claims priority to International Application Number PCT/US2016/028545, filed Apr. 21, 2016 and published as WO 2016/172279 on Oct. 27, 2016, which claims the ...

SULFONATED POLYMER

Copolymer compositions and methods of making copolymer compositions with enhanced stability in high temperature and high salinity environments. The copolymers include hydrophobic monomers and sulfonated monomers. The sulfonated monomers can include 2-acrylamido-2-methylpropane sulfonic acid and allyl sulfonate. The sulfonated monomers increase the stability of the polymers in harsh conditions, and in high temperature, high salinity environments. The sulfonated monomers also reduce or prevent the hydrolysis of acrylamide groups, and therefore enhance the stability of the copolymer. The copolymer compositions can be made with free radical polymerization and an initiation complex. 2. The compound of claim 1 , wherein a mole ratio of Rto Rto Ris 100 moles Rto 2-15 moles Rto 0.05-0.2 moles R.3. The compound of claim 2 , wherein the mole ratio of Rto Rto Ris 100 moles Rto 2 moles Rto 0.1 moles R.4. The compound of claim 2 , wherein the mole ratio of Rto Rto Ris 100 moles Rto 10 moles Rto 0.05 moles R.5. The compound of claim 1 , wherein the compound has a Tvalue as measured by thermal gravimetric analysis that is greater than 300° C.6. The compound of claim 1 , wherein the compound has a Tvalue as measured by thermal gravimetric analysis that is greater than 320° C.7. The compound of claim 1 , wherein the compound has a molecular weight of 1-10 MDa.8. The compound of claim 1 , wherein the compound has a viscosity averaged molecular weight of the compound is 1-10 MDa.9. The compound of claim 1 , wherein the compound has a number average molar mass of 40-400 MDa.10. The compound of claim 1 , wherein the compound has a polydispersity index of 1-3.11. The compound of claim 1 , wherein the compound has a C* value of about 1290 at 25° C.12. The compound of claim 1 , wherein the compound has a C* value of about 1510 at 90° C.13. The compound of claim 1 , wherein the compound has a viscosity of greater than 20 mPa·s at 25° C.14. The compound of claim 1 , wherein the compound has ...

PROCESS FOR PREPARATION OF POLYETHYLENE

The invention relates to a process for the preparation of an ethylene-based polymer, the process comprising: a) suspension polymerizing ethylene and an optional comonomer to obtain a suspension () comprising the ethylene-based polymer and wax in a suspension medium comprising a diluent, b) separating the ethylene-based polymer () from the suspension () to obtain a liquid stream () comprising the diluent and the wax, c) feeding at least part of the liquid stream () to a forced circulation reboiler (Q) for separating the diluent and the wax to obtain an evaporated stream () comprising the diluent, wherein the evaporated stream () is recycled to step a). 1. A process for the preparation of an ethylene-based polymer , the process comprising:{'b': '11', '#text': 'a) suspension polymerizing ethylene and an optional comonomer to obtain a suspension () comprising the ethylene-based polymer and wax in a suspension medium comprising a diluent,'}{'b': ['13', '11', '12'], '#text': 'b) separating the ethylene-based polymer () from the suspension () to obtain a liquid stream () comprising the diluent and the wax,'}{'b': ['25', '27', '27'], '#text': 'c) feeding at least part of the liquid stream () to a forced circulation reboiler (Q) for separating the diluent and the wax to obtain an evaporated stream () comprising the diluent, wherein the evaporated stream () is recycled to step a).'}2. The process according to claim 1 , wherein the ethylene-based polymer is selected from an ethylene homopolymer and an ethylene copolymer of ethylene and C3-C12 α-olefin.3. The process according to claim 1 , wherein the polymerization in step a) is carried out at pressures of 0.1 to 20 MPa and temperatures of 40° C. to 130° C.4. The process according to claim 1 , wherein step a) is performed in in a series of polymerization reactors comprising at least a first polymerization reactor (A) and a second polymerization reactor (H) claim 1 , wherein the suspension subjected to step b) is obtained in ...

SLURRY PHASE POLYMERISATION PROCESS

A process comprising polymerizing in a loop reactor an olefin monomer optionally together with an olefin commoner in the presence of a polymerisation catalyst in a diluent to produce a slurry comprising solid particulate olefin polymer and the diluent wherein the Froude number is maintained at or below 20 is disclosed. 121-. (canceled)22. A process comprising polymerizing in a loop reactor an olefin monomer optionally together with an olefin comonomer in the presence of a polymerization catalyst in a diluent to produce a slurry comprising solid particulate olefin polymer and the diluent wherein the Froude number is maintained at or below 20 , wherein the loop reactor has an internal diameter of over 500 millimeters , wherein the solids concentration of the slurry in the loop reactor is above 20 vol % and wherein the loop reactor is one of two or more reactors connected in series and being used to produce a multimodal polymer , and at least one of the following applies:i) hydrogen is maintained at a low (or zero) concentration in the reactor(s) manufacturing the high molecular weight components and hydrogen is maintained at a high concentration in the reactor(s) manufacturing the low molecular weight components,ii) there is being produced a polymer with molecular weight less than 50 kDaltons,iii) there is being produced a polymer with molecular weight greater than 200 kDaltons,iv) there is being produced a polymer with a melt index below 0.1,v) there is being produced a polymer with a melt index above 50.23. A process as claimed in wherein the Froude number is in the range 2 to 15.24. A process as claimed in wherein the Froude number is in the range 3 to 10.25. A process as claimed in wherein the solids concentration of the slurry in the loop reactor is above 30 vol %.26. A process as claimed in wherein the solids concentration of the slurry in the loop reactor is in the range 40-60 wt % based on the total weight of the slurry.27. A process as claimed in wherein the ...

SYSTEMS AND PROCESSES FOR POLYACRYLIC ACID PRODUCTION

Disclosed are systems and methods for the production of polyacrylic acid and superabsorbent polymers from ethylene oxidation to form ethylene oxide. Reacting the ethylene oxide with carbon monoxide to form to beta propiolactone (BPL) or polypropiolactone (PPL), or a combination thereof. An outlet configured to provide a carbonylation stream comprising the BPL or PPL, or a combination thereof and using one or more reactors to convert BPL to acrylic acid or to convert at least some of the BPL to PPL, and then to convert PPL to acrylic acid. An outlet configured to provide a PPL stream to a second reactor tm to convert at least some of the PPL to AA or a third reactor to convert at least some of the PPL to AA. The outlet configured to provide an AA stream to a fourth reactor to convert the AA to polyacrylic acid. 1. A system for producing polyacrylic acid (PAA) from ethylene , comprising: an inlet configured to receive ethylene,', 'an oxidative reaction zone configured to convert at least some of the ethylene to ethylene oxide (EO), and', 'an outlet configured to provide an EO stream comprising the EO;, 'an oxidative reactor, comprising an inlet configured to receive EO from the EO stream of the oxidative reactor, and carbon monoxide (CO) from a CO source,', 'a central reaction zone configured to convert at least some of the EO to beta propiolactone (BPL) or polypropiolactone (PPL), or a combination thereof, and', 'an outlet configured to provide a carbonylation stream comprising the BPL, or a carbonylation stream comprising the PPL, or a combination thereof;, 'a central reactor, comprising [ an inlet configured to receive BPL from the carbonylation stream of the central reactor,', 'a first reaction zone configured to convert at least some of the BPL to acrylic acid (AA), and', 'an outlet configured to provide an AA stream comprising the AA,, '(i) a first reactor, comprising, an inlet configured to receive BPL from the carbonylation stream of the central reactor,', 'a ...

PROCESS FOR FORMING POLYOLEFINS

Processes of forming polyolefins are described herein. One or more specific embodiments of the processes generally include introducing olefin monomer selected from C-Colefins into a first reaction zone under first polymerization conditions to form a first polyolefin; withdrawing a transfer effluent from the first reaction zone, the transfer effluent including first polyolefin and unreacted olefin monomer; introducing the transfer effluent, a comonomer selected from C-Colefins, and additional olefin monomer to a second reaction zone under second polymerization conditions to form a second reactor product; maintaining an essentially constant comonomer:olefin monomer ratio in the second reaction zone; and withdrawing at least a portion of the second reactor product, wherein the second reactor product includes a bimodal polyolefin. 131.-. (canceled).32. A process of forming polyolefins comprising:{'sub': 2', '3, 'introducing olefin monomer selected from C-Colefins into a first reaction zone under first polymerization conditions to form a first polyolefin;'}withdrawing a transfer effluent from the first reaction zone, the transfer effluent comprising first polyolefin and unreacted olefin monomer;{'sub': 4', '8, 'introducing the transfer effluent, a comonomer selected from C-Colefins, and additional olefin monomer to a second reaction zone under second polymerization conditions to form a second reactor product;'}maintaining an essentially constant comonomer:olefin monomer ratio in the second reaction zone; andwithdrawing at least a portion of the second reactor product, wherein the second reactor product comprises a bimodal polyolefin,wherein the first reaction zone and second reaction zone are connected in series, the first reaction zone comprises one or more loop slurry reaction vessels, and the second reaction zone comprises a gas phase reactor.331. The process of claim , further comprising introducing hydrogen or a first comonomer into the first reaction zone under the ...

Linear Alpha Olefin Process Using Temperature Control in Oligomerization Reactor

The present disclosure provides assemblies for producing linear alpha olefins and methods for producing linear alpha olefins. In at least one embodiment, a method for producing a linear alpha olefin includes providing an olefin, a catalyst, and a process solvent to a first tubular reactor; obtaining an effluent from the first tubular reactor; and transferring the effluent to a second tubular reactor. In at least one embodiment, an assembly for producing linear alpha olefins includes a first tubular reactor having a first end and a second end; an effluent line having a first end and a second end, the first end coupled with the second end of the first tubular reactor; and a second tubular reactor having a first end and a second end, the first end coupled with the second end of the effluent line. 1. A method for producing a linear alpha olefin , comprising:providing an olefin, a catalyst, and a process solvent to a first tubular reactor under oligomerization conditions;obtaining an effluent produced in the first tubular reactor;transferring the effluent to a second tubular reactor under oligomerization conditions; andobtaining an effluent produced in the second tubular reactor.2. The method of claim 1 , further comprising providing steam to a first steam jacket disposed around the first tubular reactor and providing steam to a second steam jacket disposed around the second tubular reactor.3. The method of claim 2 , further comprising controlling the pressure of steam in the first steam jacket with a valve disposed on the outlet of the steam jacket to provide a temperature (T1) within the first steam jacket.4. The method of claim 3 , further comprising controlling the pressure of steam in the second steam jacket with a valve disposed on the outlet of the steam jacket to provide a temperature (T2) within the second steam jacket.5. The method of claim 4 , wherein temperature (T1) is greater than temperature (T2).6. The method of claim 4 , wherein temperature (T1) and ...

Linear Alpha Olefin Process Using Solvent Flash Drum for Olefin Separation

The present disclosure provides assemblies for producing linear alpha olefins and methods for producing linear alpha olefins. In at least one embodiment, a method for producing a linear alpha olefin includes providing an olefin, a catalyst, and a process solvent to a reactor under oligomerization conditions; obtaining an effluent produced in the reactor; and transferring the effluent to a solvent-containing portion of a flash drum via a first effluent line coupled with the flash drum. In at least one embodiment, an assembly for producing linear alpha olefins includes a configuration to provide olefin, catalyst and process solvent coupled with a reactor; a flash drum; a first effluent line coupled with the reactor at a first end and coupled with the flash drum at a second end; and a second effluent line coupled with the flash drum at a first end and coupled with the first effluent line at a second end. 1. A method for producing a linear alpha olefin , comprising:providing an olefin, a catalyst, and a process solvent to a reactor;obtaining an effluent produced in the reactor; andtransferring the effluent to a solvent-containing portion of a flash drum via a first effluent line coupled with the flash drum.2. The method of claim 1 , further comprising controlling the flow rate of effluent transferred to the flash drum with a V-Ball valve.3. The method of claim 1 , further comprising providing heat to the effluent line using one or more heaters coupled with the effluent line.4. The method of claim 1 , wherein the temperature in the flash drum is 130° C. or greater.5. The method of claim 4 , further comprising transferring an effluent from the flash drum to a knockout drum via an effluent line and cooling the effluent using a chiller coupled with the effluent line.6. The method of claim 5 , further comprising transferring a first effluent from the knockout drum to the reactor and transferring a second effluent from the knockout drum to the flash drum.7. The method of ...

METHOD OF PREPARING AROMATIC VINYL COMPOUND-VINYL CYANIDE COMPOUND POLYMER AND APPARATUS FOR PREPARING THE SAME

A method of preparing an aromatic vinyl compound-vinyl cyanide compound polymer includes polymerizing a reaction mixture containing an aromatic vinyl compound, a vinyl cyanide compound, and an organic solvent in a reactor and transferring the vaporized reaction mixture present in the upper space of the reactor to a heat exchanger via a pipe and condensing the vaporized reaction mixture. The condensed reaction mixture is transferred to one side of the pipe and sprayed into the pipe, the flow velocity of the reaction mixture vaporized in the reactor is reduced, and temperature is lowered. Accordingly, a phenomenon wherein polymer particles in a reactor are sucked into a heat exchanger is prevented, and occurrence of polymerization in the heat exchanger is suppressed. Therefore, productivity and quality may be improved. 1. A method of preparing an aromatic vinyl compound-vinyl cyanide compound polymer , comprising:polymerizing a reaction mixture containing an aromatic vinyl compound, a vinyl cyanide compound, and an organic solvent in a reactor; andtransferring the vaporized reaction mixture present in an upper space of the reactor to a heat exchanger via a pipe and condensing the vaporized reaction mixture,wherein the condensed reaction mixture is transferred to one side of the pipe and sprayed into the pipe.2. The method according to claim 1 , wherein the spraying is performed so that a flow of the condensed reaction mixture is countercurrent to a flow of the vaporized reaction mixture.3. The method according to claim 1 , wherein the reaction mixture contains 40 to 80% by weight of the aromatic vinyl compound claim 1 , 10 to 35% by weight of the vinyl cyanide compound claim 1 , and 5 to 35% by weight of the organic solvent.4. The method according to claim 1 , wherein the spray comprises all or a portion of the reaction mixture transferred to the heat exchanger.5. The method according to claim 1 , wherein a temperature of the reaction mixture transferred to the heat ...

Multimodal polyethylene pipe

The present invention relates to a reactor system for a multimodal polyethylene polymerization process, comprising; (a) first reactor; (b) a hydrogen removal unit arranged between the first reactor and a second reactor comprising at least one vessel connected with a depressurization equipment, preferably selected, from vacuum pump, compressor, blower, ejector or a combination thereof, the depressurization equipment allowing to adjust an operating pressure to a pressure in a range of 100-200 kPa (abs); (c) the second reactor; and (d) a third reactor and use thereof as a pipe.

Process

The present invention relates to the treatment and recycle of effluent streams from a polymerisation process, and in particular provides a polymerisation process comprising the steps of: 1) Polymerising a monomer and a comonomer in a polymerisation reaction, 2) Withdrawing an effluent stream comprising solid polymer and a mixture comprising unreacted monomer and unreacted comonomer, and passing the effluent to a high pressure recovery system comprising a. a high pressure separation step for separating a vapour comprising unreacted monomer and unreacted comonomer from said solids, and b. a high pressure recycle system for recycling a portion of the vapour to the polymerisation reaction, 3) Passing the solids from the high pressure recovery system to a low pressure recovery system comprising a. a low pressure separation step for separating further unreacted monomer and unreacted comonomer from said solids, and b. a low pressure recycle system for recycling at least a portion of the unreacted monomer and unreacted comonomer to the polymerisation reaction, characterised in that a portion of the vapour separated in step 2(a) is passed to the low pressure recovery system.

Process for Preparing Polyolefins

The present invention relates to a process of preparing a polyolefin in a loop reactor by introducing anti-fouling agent in by-pass pipes. Also, the invention relates to the use of anti-fouling agent to prevent blockage by feeding the anti-fouling agent into the by-pass pipes of the loop reactor.

SLURRY PHASE POLYMERISATION PROCESS

A slurry process for the polymerisation of ethylene is disclosed, which takes place in a reactor system comprising one or more reactors in series, having a characteristic such that the average polymerisation productivity [kg PE/kgcata] per unit ethylene per hour aI during operation at any first residence time rI is less than 1.7 (a2r2 −aIrI)/(r2−rI), where a2 is the average polymerisation productivity [kgPE/kgcata] per unit ethylene per hour during operation at any second residence time r2 where r2>rI, a2 and r2 being measured either in the same reactor in the case of a single reactor polymerisation, or in a reactor subsequent to the reactor in which aI and rI are measured in the case where the polymerisation takes place in more than one reactor, and wherein the specific yield of the reactor system is greater than 0.3 tonnes/m, specific yield being the production rate of the final reactor (kg/h) in the reactor system divided by the total volume of all the reactors in the reactor system (m) multiplied by the total residence time in all the reactors in the reactor system (h). Operating the system under the above conditions results in improved productivity/unit ethylene. 115-. (canceled)16. Slurry process for the polymerisation of ethylene in a reactor system comprising one or more reactors in series , having an average polymerisation productivity [kgPE/kgcata] per unit ethylene per hour a1 during operation at any first residence time r1 is less than 1.7 (a2r2−a1r1)/(r2−r1) , where a2 is the average polymerisation productivity [kgPE/kgcata] per unit ethylene per hour during operation at any second residence time r2 where r2>r1 , r2 and the value a2r2 being determined either in the same reactor in the case of a single reactor polymerisation , or in a reactor subsequent to the reactor in which a1 and r1 are measured in the case where the polymerisation takes place in more than one reactor , the residence time r2 and value a2r2 in this latter case corresponding to the ...

METHOD FOR PRODUCING POLYOLEFIN

A method for producing a polyolefin is provided. The method includes steps of polymerizing an olefin in a first gas-phase polymerization tank to obtain polyolefin-containing particles, transferring the polyolefin-containing particles to a second gas-phase polymerization tank through a transfer pipe, and polymerizing an olefin in the presence of the transferred polyolefin-containing particles in the second gas-phase polymerization tank. A connection place between the first gas-phase polymerization tank and the transfer pipe is higher than a connection place between the second gas-phase polymerization tank and the transfer pipe. 130 kPa≥P−P≥0 is satisfied, where Prepresents the pressure in the first gas-phase polymerization tank and Prepresents the pressure in the second gas-phase polymerization tank. 1. A method for producing a polyolefin with use of a polyolefin production system equipped with a first gas-phase polymerization tank and a second gas-phase polymerization tank connected to the first gas-phase polymerization tank through a transfer pipe , the method comprising the following steps 1 to 3 and satisfying the following requirements 1 and 2:Step 1; a step of polymerizing an olefin in the first gas-phase polymerization tank to obtain polyolefin-containing particles;Step 2: a step of transferring the polyolefin-containing particles obtained in the step 1 to the second gas-phase polymerization tank through the transfer pipe; andStep 3: a step of polymerizing an olefin in the presence of the polyolefin-containing particles transferred in the step 2 in the second gas-phase polymerization tank; andRequirement 1: the connection place “a” between the first gas-phase polymerization tank and the transfer pipe is higher than the connection place “b” between the second gas-phase polymerization tank and the transfer pipe; and{'sub': 1', '2', '1', '2, 'Requirement 2: when Prepresents the pressure in the first gas-phase polymerization tank and Prepresents the pressure in ...

POLYMER PRODUCTION METHOD

A polymer production method whereby: a flow reactor comprising a flow path wherein a plurality of liquids can be mixed is used; and a monomer is anionically polymerized in the presence of an initiator. The flow reactor comprises a mixer for mixing two liquids, said mixer comprising either a joint member having a double pipe therein or a static mixer member. 1. A polymer production method comprising the step of anionically polymerizing a monomer in the presence of an initiator by using a flow reactor having a flow channel capable of mixing a plurality of liquids ,wherein the flow reactor is equipped with a mixer for mixing two liquids that comprises a joint member having a double tube at the interior or a static mixer member.2. The polymer production method of claim 1 , wherein the static mixer member comprises a tubular body and an element body inserted at the interior of the tubular body.3. The polymer production method of claim 1 , wherein the mixer for mixing two liquids comprises a joint member having a double tube at the interior and a static mixer member.4. The polymer production method of claim 3 ,wherein the mixer for mixing two liquids comprises a joint member having a double tube at the interior and a static mixer member;the static mixer member comprises a tubular body and an element body inserted at the interior of the tubular body; andthe joint member and the static mixer member are connected in such manner that a double tube side endface of the tubular body is in touching contact with a static mixer member side endface of the double tube.5. The polymer production method of claim 4 , wherein the static mixer member side end of the double tube is situated at the interior of the joint member.6. The polymer production method of claim 1 , wherein the joint member has an insertion hole for inserting an inner tube through which flows an initiator solution and claim 1 , in the inner tube-inserted state claim 1 , the double tube is formed of claim 1 , at least ...

METHOD FOR PRODUCING POLYOLEFIN AND POLYOLEFIN PRODUCTION SYSTEM

A polyolefin production system is provided. The polyolefin production system includes a plurality of gas-phase polymerization tanks configured to polymerize an olefin gas to form a polyolefin, a gas transfer series line connecting the plurality of the gas-phase polymerization tanks to each other in series, a compressor having an inlet and an outlet and being configured to compress an olefin-containing gas, a gas main feed line disposed at the frontmost gas-phase polymerization tank and configured to guide the gas fed from the outlet of the compressor to the frontmost gas-phase polymerization tank, a gas discharge line disposed at the rearmost gas-phase polymerization tank, and a first valve installed in the gas main feed line. 1. A polyolefin production system comprising:a plurality of gas-phase polymerization tanks configured to polymerize an olefin gas to form a polyolefin ;a gas transfer series line connecting the plurality of the gas-phase polymerization tanks to each other in series;a compressor comprising an inlet and an outlet and being configured to compress an olefin-containing gas;a gas main feed line disposed at the frontmost gas-phase polymerization tank, configured to guide the gas fed from the outlet of the compressor to the frontmost gas-phase polymerization tank;a gas discharge line disposed at the rearmost gas-phase polymerization tank; anda first valve installed in the gas main feed line.2. The polyolefin production system according to claim 1 , wherein the first valve is a butterfly valve or an eccentric rotary plug valve.3. The polyolefin production system according to claim 1 , further comprising a second valve installed in the gas transfer series line connecting at least one pair of the gas-phase polymerization tanks to each other.4. The polyolefin production system according to claim 1 , further comprising a second valve installed in the gas discharge line.5. The polyolefin production system according to claim 3 , wherein the second valve is a ...

APPARATUS FOR PRODUCING PULVERULENT POLY(METH)ACRYLATE

An apparatus for producing pulverulent poly(meth)acrylate in a reactor for droplet polymerization having an apparatus for dropletization of a monomer solution for the production of the poly(meth)acrylate having holes through which the monomer solution is introduced, an addition point for a gas above the apparatus for dropletization, at least one gas withdrawal point on the circumference of the reactor and a fluidized bed, and above the gas withdrawal point the reactor has a region having a constant hydraulic internal diameter and below the gas withdrawal point the reactor has a hydraulic internal diameter that steadily decreases. The reactor has a heating means in the region having a steadily decreasing hydraulic internal diameter. 18.-. (canceled)9151351911119119131. An apparatus for producing pulverulent poly(meth)acrylate , comprising a reactor () for droplet polymerization comprising an apparatus () for dropletization of a monomer solution for the production of the poly(meth)acrylate comprising holes through which the monomer solution is introduced , an addition point () for a gas above the apparatus () for dropletization , at least one gas withdrawal point () on the circumference of the reactor () and a fluidized bed () , wherein above the gas withdrawal point () the reactor () comprises a region having a constant hydraulic internal diameter and below the gas withdrawal point () the reactor has a hydraulic internal diameter that steadily decreases , wherein the reactor () comprises a heating means () in the region having a steadily decreasing hydraulic internal diameter.1031. The apparatus according to claim 9 , wherein the heating means () supplies a heat output in the range of from 20 to 5000 W/m.1131. The apparatus according to claim 9 , wherein the heating means () is an electric heater.123131. The apparatus according to claim 9 , wherein the heating means is a double shell or takes the form of heating coils () applied to the outside of the reactor shell ...

Linear Alpha Olefin Process Including Solvent Purification Using Dividing Wall Distillation Column

The present disclosure provides assemblies for producing linear alpha olefins and methods for producing linear alpha olefins. In at least one embodiment, a method for forming a linear alpha olefin, includes providing an olefin, a catalyst, and a process solvent to a reactor; obtaining an effluent from the reactor; and transferring the effluent to a distillation tower comprising a dividing wall. In at least one embodiment, an assembly for producing linear alpha olefins includes a distillation tower comprising a dividing wall having a height that is from 25% to 95% of the height of the distillation tower. In at least one embodiment, a method for forming a linear alpha olefin comprises providing an olefin, a catalyst, and orthoxylene to a tubular reactor; obtaining an effluent from the tubular reactor; and transferring the effluent to a distillation tower. 1. A method for forming a linear alpha olefin , comprising:providing an olefin, a catalyst, and a process solvent to a reactor, under oligomerization conditions;obtaining an effluent produced in the reactor; andtransferring the effluent to a distillation tower comprising a dividing wall.2. The method of claim 1 , further comprising obtaining a process solvent from the distillation tower.3. The method of claim 2 , wherein the process solvent has an olefin content of less than 0.5 wt %.4. The method of claim 3 , wherein the obtained process solvent has an olefin content of less than 0.05 wt %.5. The method of claim 2 , wherein the obtained process solvent has a water content of less than 10 ppm.6. The method of claim 2 , wherein the obtained process solvent has a water content of less than 25 ppb.7. The method of claim 2 , further comprising recycling the process solvent by providing the process solvent to a process solvent source.8. The method of claim 1 , wherein the dividing wall is configured to block flow of the effluent entering the distillation tower on a first side of the distillation tower from contacting a ...

Linear Alpha Olefin Process Using Catalyst Deactivation with High Product Purity

The present disclosure provides assemblies for producing linear alpha olefins and methods for producing linear alpha olefins. In at least one embodiment, a method for producing a linear alpha olefin includes providing an olefin, a catalyst, and a process solvent to a reactor under oligomerization conditions; obtaining an effluent produced in the reactor; transferring the effluent through an effluent line; and providing a quench agent to the effluent line via a quench agent line coupled with the effluent line. In at least one embodiment, an assembly for producing linear alpha olefins includes a configuration to provide olefin, catalyst and process solvent coupled with a reactor; an effluent line coupled with the reactor at a first end and coupled with a mixer or a flash drum at a second end; and a quench agent line coupled with the effluent line at a first end. 1. A method for producing a linear alpha olefin , comprising:providing an olefin, a catalyst, and a process solvent to a reactor under oligomerization conditions; 'transferring the effluent through an effluent line; and', 'obtaining an effluent produced in the reactor;'}providing a quench agent to the effluent line via a quench agent line coupled with the effluent line.2. The method of claim 1 , further comprising controlling the flow rate of effluent transferred through the effluent line using a V-Ball valve coupled with the effluent line.3. The method of claim 1 , wherein transferring the effluent comprises transferring the effluent through the effluent line to a mixer.4. The method of claim 1 , wherein transferring the effluent comprises transferring the effluent through the effluent line to a flash drum.5. The method of claim 4 , wherein the flash drum has a pressure from 300 psi to 400 psi and a temperature from 100° C. to 150° C.6. The method of claim 1 , wherein the quench agent is provided to the effluent line via a dip tube coupled with a first end of the quench agent line and disposed within the ...

METHOD FOR MANUFACTURING POLYMER

Object: To provide a method for manufacturing a polymer, which is a method for forming a polymer having a homogeneous copolymer composition and a narrow molecular weight distribution. 1. A method for manufacturing a polymer using a microreactor comprising a flow path capable of mixing a plurality of liquids to perform radical polymerization of a monomer component containing two or more types of monomers in the presence of a polymerization initiator;wherein the microreactor comprises a first inlet port configure to feed the monomer component and an additional inlet port located downstream of the first inlet port; andthe method comprises feeding the monomer component through the first inlet port and the additional inlet port.2. The method for manufacturing a polymer according to claim 1 , wherein the monomer component to be fed through the first inlet port and the additional inlet port contains two or more types of (meth)acrylic-based monomers.3. The method for manufacturing a polymer according to claim 1 , wherein the monomers contained in the monomer component to be fed through the first inlet port and the additional inlet port are the same claim 1 , and a difference between the contents of each monomer is within ±5%.4. The method for manufacturing a polymer according to claim 2 , wherein the monomers contained in the monomer component to be fed through the first inlet port and the additional inlet port are the same claim 2 , and a difference between the contents of each monomer is within ±5%.5. The method for manufacturing a polymer according to claim 1 , wherein the radical polymerization is performed in the presence of the polymerization initiator and a chain transfer agent.6. The method for manufacturing a polymer according to claim 2 , wherein the radical polymerization is performed in the presence of the polymerization initiator and a chain transfer agent.7. The method for manufacturing a polymer according to claim 3 , wherein the radical polymerization is ...

METHOD OF PREPARING AROMATIC VINYL COMPOUND-VINYL CYANIDE COMPOUND POLYMER AND APPARATUS FOR PREPARING THE SAME

The present invention relates to a method of preparing an aromatic vinyl compound-vinyl cyanide compound polymer including a step of separating volatile components from a polymerization product containing an aromatic vinyl compound-vinyl cyanide compound polymer, a residual aromatic vinyl monomer, a residual vinyl cyanide monomer, and an organic solvent using a volatilization tank, and a step of condensing the separated volatile components using a condenser, wherein an organic solvent or an aromatic vinyl monomer is sprayed onto the volatile components being transferred to the condenser. Volatile components may be fully condensed in a condenser, thereby significantly reducing the amount of volatile components discharged to the outside without being condensed. Therefore, wastewater treatment costs consumed in treating the volatile components may be reduced, and the amount of vinyl cyanide monomers harmful to the human body discharged into the atmosphere may be significantly reduced. 1. A method of preparing an aromatic vinyl compound-vinyl cyanide compound polymer , comprising:separating volatile components from a polymerization product containing an aromatic vinyl compound-vinyl cyanide compound polymer, residual aromatic vinyl monomer, residual vinyl cyanide monomer, and an organic solvent using a volatilization tank; andcondensing the separated volatile components using one condenser or two or more condensers connected in series,wherein the method comprises spraying an organic solvent onto the separated volatile components being transferred from the volatilization tank to the condenser; orspraying an organic solvent or an aromatic vinyl monomer onto the volatile components not being condensed in a first condenser and being transferred to a second condenser when the two or more condensers connected in series are used.2. The method according to claim 1 , wherein the method comprises spraying the organic solvent onto the volatile components being transferred to the ...

IMPROVED PROCESS AND SYSTEM FOR VAPOR PHASE POLYMERIZATION OF OLEFIN MONOMERS

The present invention relates to a continuous vapor phase olefin polymerization process comprising polymerization of at least one olefin monomer in at least two serial polymerization reactors containing an agitated bed of forming polymer particles, wherein forming polymer particles are transferred from an upstream reactor to a downstream reactor, wherein the upstream reactor is a horizontal stirred reactor containing multiple reaction zones, each reaction zone having at least one inlet for a gaseous stream and optionally additionally an inlet for a liquid stream, wherein said process reduces the carry-over of undesired reactive gases from the upstream reactor to the downstream reactor. The present invention further relates to a system suitable for the present continuous vapor phase olefin polymerization process. The present invention further relates to the use of the present process and system for producing heterophasic polypropylene. 1. A continuous vapor phase olefin polymerization process comprising polymerization of at least one olefin monomer in at least two serial vapor phase polymerization reactors containing an agitated bed of forming polymer particles ,wherein forming polymer particles are transferred from an upstream reactor to a downstream reactor,wherein the upstream reactor is a horizontal stirred reactor containing multiple reaction zones, each reaction zone having at least one inlet for a gaseous stream and optionally additionally an inlet for a liquid stream and,{'sub': 2', 'discharge zone', 'discharge zone', '2', 'receding zone', 'preceding zone, 'wherein one reaction zone comprised in the upstream reactor vessel is a polymer discharge reaction zone from which forming polymer particles are discharged and subsequently transported to the downstream reactor and wherein the ratio of the hydrogen concentration to the olefin monomer concentration in the polymer discharge reaction zone ([H]/[Olefin monomer]) is reduced compared to the ratio of the hydrogen ...

Pressure relief for multiple polyolefin polymerization reactors

A polyolefin manufacturing system and method including polymerizing olefin in a first reactor to form a polyolefin, transferring the polyolefin to a second reactor, polymerizing olefin in the second reactor, and discharging a product polyolefin from the second reactor. The system and method including operating the first reactor with a first reactor pressure relief system and the second reactor with a second reactor pressure relief system, both pressure relief systems to discharge to a flare system, and wherein a relief instrumented system (RIS) is configured to direct at least one process interlock that mitigates an excess reaction scenario as an overpressure relief scenario.

Polymerization reactor and method for producing water absorbent resin

A polymerization reactor of the present invention includes a container body 1 and a jacket 2 covering the outer surface of the container body 1 and defining a passage for passing a cooling/heating medium between itself and the outer surface of the container body. The container body 1 is made of a clad metal plate including a support metal layer 11 a having an inner surface at an inner side of the container body and an outer surface at an outer side of the container body, and an inner corrosion-resistant metal skin layer 11 b bonded to the inner surface of the support metal layer and being smaller in thickness than the support metal layer.

Vent Gas Purge Optimizer for Slurry Loop Polyethylene Reactors

A method for minimizing the amount of catalyst inactivating agent that is present in a liquid fraction recovered from a slurry-based polymer production process, the liquid fraction comprising diluent used in the polymer production process, is disclosed. The method includes steps for controlling the pressure over the liquid fraction collected during diluent recovery so as to minimize the concentration of catalyst inactivating agent that is retained in the recovered liquid fraction. Embodiments of apparatus suitable for conducting the disclosed method are also provided. 1. A method for minimizing catalyst inactivating agent in a recycled diluent comprising: i(a). the gas flow f if measured, is measured via a flow rate sensor that is operatively connected to send a gas flow signal to a flow controller operatively linked to a temperature control valve disposed in a coolant flow line that provides coolant to a heat exchanger in operative connection to a recycle condenser configured to contact a vapor received from a flash tank and condense at least a portion of the vapor to liquid; and/or', 'i(b). the pressure p, if measured, is measured via a pressure sensor that is operatively connected to send a pressure signal indicating the measured pressure p to a pressure controller;, 'i. measuring either or both of (a) gas flow f and/or (b) pressure p in a purge line in fluid connection with an accumulator tank that stores a condensate comprising the diluent under an overhead gas comprising a diluent so as to withdraw gas from the accumulator tank; wherein'}{'sub': sp', 'sp, 'ii. either or both of (a) comparing the measured flow f to a desired gas flow rate set point fset in the flow controller and/or (b) comparing the measured pressure p to a desired pressure set point pin the pressure controller; and'} [{'sub': sp', 'sp, 'iii(a). controlling the temperature control valve via the flow controller such that the temperature control valve is opened to lower the temperature of the ...

Slurry Loop Reactor Bad Catalyst Range Control

A process for maintaining an optimum polymerization process in a continuous loop polymerization reactor by driving a catalyst feed range set-point around a bad catalyst set-point range using a bad catalyst feed rate program to vary the catalyst feed rate for differing periods of time between previously determined good catalyst feed rates. 1. A process for maintaining an optimum polymerization conditions in a continuous loop polymerization reactor by driving a catalyst feed range set-point around a bad catalyst set-point range , comprising:if there is a non-optimum polymerization condition requiring a change in a catalyst feed rate, calculating a desired catalyst feed rate to return the process to optimum conditions;sending the desired catalyst feed rate to a bad catalyst program for determining whether the desired catalyst feed rate falls within a bad catalyst feed rate set-point range;if the desired catalyst feed rate is determined to fall within the bad catalyst feed rate set-point range, turning over control of the catalyst feed rate to the bad catalyst program,wherein the bad catalyst program controls and incrementally changes the catalyst feed rate set-point delivered by a semi-continuous shot feeder between previously established first and second good catalyst feed rate set-points, above and below the bad catalyst feed rate set-point range, so that an average catalyst feed rate is equivalent to the desired catalyst feed rate set-point within the bad catalyst feed rate set-point range.2. The process of claim 1 , wherein the bad catalyst program determines a first period of time required for the catalyst feed rate to remain at the first good catalyst feed rate set-point claim 1 , and a second period of time required for the catalyst feed rate to remain at the second good catalyst feed rate set-point claim 1 , to establish a time-weighted average catalyst feed rate which is equivalent to the desired catalyst feed rate set-point within the bad catalyst feed rate ...

Processes and Apparatus for Bimodal Slurry Polymerization

Processes and apparatus for preparing bimodal polymers are provided. In some embodiments, processes include introducing a monomer, a first diluent, a catalyst, hydrogen, at a first hydrogen concentration, and optional comonomer, to a first loop reactor to produce, under polymerization conditions, a first slurry of polymer solids. Processes may also include continuously discharging the first slurry of polymer solids from the loop reactor as a first polymerization effluent to a first flash tank; separating the first polymerization effluent in the first flash tank to provide a first concentrated polymer slurry with significantly lower hydrogen concentration; and transferring the first concentrated polymer slurry from the flash tank to a re-slurry mixer. Processes may further include introducing a re-slurry mixer diluent to the first concentrated polymer slurry to form a second concentrated polymer slurry in the re-slurry mixer that can be pumped to a second slurry loop reactor.

Olefin polymerization processes

A process for producing an olefin polymer employs a gas phase polymerization reactor having a product discharge system comprising first and second pairs of lock hoppers, wherein each pair comprises an upstream lock hopper connected by valve means to the reactor and a downstream lock hopper connected by valve means to the upstream lock hopper and by further valve means to a product recovery system, and wherein a first cross-tie is provided between the upstream lock hoppers of the first and second pairs of lock hoppers and a second cross-tie is provided between the downstream lock hoppers of the first and second pairs of lock hoppers. Operation of the second cross-tie during product removal cycles is controlled in accordance with reactor pressure.