Способ разделения водородсодержащей углеводородной смеси, сепарационная секция и олефиновая установка

РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2016 127 551 A (51) МПК B01D 53/14 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2016127551, 17.12.2014 (71) Заявитель(и): ЛИНДЕ АКТИНГЕЗЕЛЛЬШАФТ (DE) Приоритет(ы): (30) Конвенционный приоритет: 07.01.2014 EP 14000040.7 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 08.08.2016 R U (43) Дата публикации заявки: 13.02.2018 Бюл. № 05 (72) Автор(ы): ФРИЦ Хельмут (DE), ХЁФЕЛЬ Торбен (DE) (86) Заявка PCT: (87) Публикация заявки PCT: WO 2015/104153 (16.07.2015) R U (54) Способ разделения водородсодержащей углеводородной смеси, сепарационная секция и олефиновая установка (57) Формула изобретения 1. Способ разделения водородсодержащей углеводородной смеси (С2минус), которая, кроме водорода, по существу, содержит углеводороды с двумя атомами углерода и метан, с помощью перегонной колонны (10), в котором текучую среду (а, с, е) углеводородной смеси (С2минус) поэтапно охлаждают при первом уровне давления от первого уровня температуры через два или более промежуточных уровней температуры до второго уровня температуры, при этом из текучей среды (а, с, е) отделяют первые конденсаты (b, d) на каждом из промежуточных уровней температуры, текучую среду (е) углеводородной смеси (С2минус), которая остается газообразной при втором уровне температуры, подают при первом уровне давления в С2 поглотитель (7), в верхнюю часть которого добавляют жидкую флегму (r), при этом второй конденсат (f) извлекают из куба С2 поглотителя (7), а газообразный верхний поток (g), преимущественно содержащий метан и водород, извлекают из верхней части С2 поглотителя (7), текучую среду газообразного верхнего потока (g) из верхней части С2 поглотителя (7) охлаждают до третьего уровня температуры и перемещают при первом уровне давления в сепаратор водорода (8), в котором богатый метаном третий конденсат (i) отделяют от текучей среды газообразного верхнего потока (g), выходящий после газообразного, ...

Separation of lower hydrocarbons comprises operating de-ethanizer at no less than de-methanizer pressure and combines head fractions for at least an interval

A de-ethanizer (E) is operated at the same, or a higher pressure than the de-methanizer (M). At least some of the 2C-rich fraction (9) withdrawn at the head of the de-ethanizer is supplied for at least an interval to the 1C-rich fraction (11, 11') withdrawn at the head of the de-methanizer. Preferred Features: The fluid fraction (5) withdrawn from the sump of the de-methanizer, which is supplied to the de-ethanizer, is made available at least at a pressure permitting admixture of the head product (8, 9) of the de-ethanizer to the head product (11, 11') of the de-methanizer, without an additional compression of the former. For an interval , especially when recovered 2C-rich fraction is not extracted, one or more of the following measures is adopted. The temperature of the recycle stream (2, 3''') supplied to the demethanizer (M) is increased by up to 20 K, preferably by 10-15 K. The quantity of this recycle is reduced, or supply is interrupted. The temperature of the hydrocarbon-rich fraction ...

Process for seperating and recovering NGLS from hydrocarbon streams

Process for seperating and recovering NGLS from hydrocarbon streams

Process for seperating and recovering NGLS from hydrocarbon streams

PROCEDURE AND PLANT FOR THE RECUPERATION AND CLEANING OF ETHYLEN MANUFACTURED BY PYROLYSIS OF HYDROCARBON

Precooling for ethylene recovery in dual demethanizer fractionation systems

STAGE AND SYSTEM FOR COMPRESSION CRACKING - GAS

СПОСОБ И УСТАНОВКА ДЛЯ ИЗВЛЕЧЕНИЯ И ОЧИСТКИ ЭТИЛЕНА, ПРОИЗВЕДЕННОГО В РЕЗУЛЬТАТЕ ПИРОЛИЗА УГЛЕВОДОРОДОВ, И ГАЗ, ПОЛУЧЕННЫЙ ЭТИМ СПОСОБОМ

... 1. Способ для разделения на фракции газа, по существу, безводного газа (1), произведенного в результате пиролиза углеводородов, содержащего водород и углеводороды, в частности углеводороды от C1до C3 , включающие этилен, пропилен и ацетилен, по меньшей мере, на один поток , обогащенный водородом и/или метаном, по меньшей мере, на один поток, обогащенный этиленом, и с уменьшенным содержанием ацетилена и, по меньшей мере, на один поток, обогащенный пропиленом, отличающийся тем, что a) охлаждают и постепенно сжижают упомянутый газ (1), полученный в результате пиролиза углеводородов под давлением посредством пропускания через ряд зон теплообмена (2, 6, 9, 20), которые становятся все более и более холодными, отделяют от упомянутого газа пиролиза (1), по меньшей мере, один конденсат после его пропускания через каждую зону теплообмена, причем, по меньшей мере, один из конденсатов (15) обогащен пропиленом и, по меньшей мере, другой конденсат (23) обогащен этиленом и этаном и содержит в растворе ...

PROCESS FOR TREATING A STREAM OF CRACKED GAS COMING FROM A HYDROCARBON PYROLYSIS PLANT, AND ASSOCIATED PLANT

METHOD OF TREATMENT OF FLOW CRACKING GAS, OBTAINED ON PLANT PYROLYSIS OF HYDROCARBONS, AND INSTALLATION FOR ITS REALIZATION

A CURRENT PROCESS FOR THE RECOVERY OF ETHYLENE FROM A FEED STREAM RICH IN CARBON MONOXIDE, AND INSTALLATION

Ce procédé comprend les étapes suivantes : - traitement d'un courant de charge (12) pour obtenir un courant de gaz traité (60); - refroidissement du courant de gaz traité (60) dans un échangeur thermique (34) pour former au moins une fraction d'alimentation de colonne; - introduction de chaque fraction d'alimentation de colonne dans une colonne de distillation (50) ; - réchauffage d'au moins un flux aval (106) issu du courant de tête (104) de la colonne dans l'échangeur thermique (34). L'étape de traitement comporte la formation d'un courant intermédiaire (20) comportant au moins 20% en moles d'éthylène et au moins 20% en moles de monoxyde de carbone, le procédé comportant une étape d'élimination du monoxyde de carbone contenu dans le courant intermédiaire (20).

PROCEEDED OF TREATMENT Of a GAS CURRENT CRACKS RESULTING From an INSTALLATION FROM HYDROCARBON PYROLYSIS AND ASSOCIATED INSTALLATION.

Wasted heat driven refinery's petroleum gas recovery apparatus

A refinery petroleum gas recovery apparatus driven by normally wasted heat, comprising primarily the cooling system, the heat exchanging petroleum gas recovery system, and the appropriate peripheral equipment, wherein the wasted heat from the refining process is used as a power source for creating a vacuum cooling function to cool the water being heat exchanged with the petroleum gas down to the temperature of 12°-13° C. The heat in the gas is removed and the gas is condensed into liquid for reuse. The petroleum gases ethane, propane etc. which are ordinarily burned in the torch tower can now be recovered for reuse. The air pollution created from the burning of the gases in the torch tower is eliminated. Thus the apparatus has a high industrial value.

Process for separating and recovering NGLs from hydrocarbon streams

This process comprises using unconventional processing of hydrocarbons, e.g. natural gas, for recovering C2+ and NGL hydrocarbons that meet pipeline specifications, without the core high capital cost requirement of a demethanizer column, which is central to and required by almost 100% of the world's current NGL recovery technologies. It can operate in Ethane Extraction or Ethane Rejection modes. The process uses only heat exchangers, compression and simple separation vessels to achieve specification ready NGL. The process utilizes cooling the natural gas, expansion cooling, separating the gas and liquid streams, recycling the cooled streams to exchange heat and recycling selective composition bearing streams to achieve selective extraction of hydrocarbons, in this instance being NGLs. The compactness and utility of this process makes it feasible in offshore applications as well as to implementation to retrofit/revamp or unload existing NGL facilities. Many disparate processes and derivatives are anticipated for its use.

СПОСОБ ОБРАБОТКИ УГЛЕВОДОРОДНОГО СЫРЬЯ, СОДЕРЖАЩЕГО ВОДОРОД И УГЛЕВОДОРОДЫ C1-C4

FIELD: chemical or physical processes. SUBSTANCE: invention relates to a method of treating hydrocarbon feedstock containing hydrogen and hydrocarbons, including hydrocarbons C 1 -C 4 , in which: a) hydrocarbon feedstock is divided into gas phase (6), containing mainly hydrogen, and liquid phase (4) containing hydrocarbons; b) performing the first step of re-contacting first the gaseous phase obtained at step a) , with recirculating gas stream (23), obtained at step e) to extract gas (10), which is in contact with liquid phase (4) obtained at step (a), at temperature less than or equal to 55 °C; c) dividing flow from re-contact at step b) into gas phase (15), enriched with hydrogen, and liquid phase (16); d) performing a second re-contacting step of liquid phase (16) leaving step (c) with gas phase (21) coming from step (g) at a temperature lower than or equal to 55 °C; e) dividing the flow from re-contact at step d) into gas phase (23), which is returned to step b), and liquid phase (24) containing hydrocarbons; and f) fractionating liquid phase (24) from step e), in fractionation column (25) to separate gaseous head fraction (27) and liquid bottom fraction (26) containing hydrocarbons with carbon number greater than 4; g) condensing gaseous head fraction (27) from step f) and separating liquid phase (30) containing mainly hydrocarbons C 3 and C 4 , and gas phase (21), which is returned to step d). EFFECT: technical result is maximum increase in extraction of hydrogen and hydrocarbons C 3 and C 4 . 8 cl, 2 ex, 3 tbl, 1 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 722 590 C2 (51) МПК C10G 7/00 (2006.01) C10G 70/06 (2006.01) C01B 3/00 (2006.01) C10G 49/22 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК C10G 7/00 (2020.02); C10G 70/06 (2020.02); C01B 3/00 (2020.02); C10G 49/22 (2020.02) (21)(22) Заявка: 2016128731, 14.07.2016 (24) Дата начала отсчета срока действия патента: (73) Патентообладатель(и): ИФП ...

СПОСОБ КОНДИЦИОНИРОВАНИЯ ГАЗА И СИСТЕМА ДЛЯ ИЗВЛЕЧЕНИЯ КОНДЕНСИРУЮЩЕГОСЯ ПАРА ИЗ ПОДАВАЕМОГО ГАЗА

CONTINUOUS PRODUCTION OF AQUEOUS SOLUTIONS OF ALKALINE SALTSOF ARYLACETIC ACIDS

On décrit un procédé de dégazolinage par réfrigération d'un gaz contenant de s hydrocarbures condensables, effectué en présence de méthanol pour éviter la formation d'hydrates, ledit procédé permettant de récupérer au moins en part ie le méthanol entraîné dans le gaz, par lavage de celui-ci à l'aide d'une fraction hydrocarbure liquide. Le procédé décrit permet ainsi d'éviter d'avoir à compenser la perte en méthanol par un appoint permanent, comme c'est le cas dans les procédés conventionnels. Il présente de ce fait des performance s et une économie améliorées.

METHOD OF FRACTIONATION OF FLOW CRACKING GAS WITH THE USE OF INTERMEDIATE OF RECIRCULATION FLOW AND INSTALLATION FOR ITS REALIZATION

METHOD FOR SEPARATION AND EXTRACTION OF NGL OF CARBON FLOWS

Light hydrocarbon separation system and method

PROCESS FOR IMPROVING PROPYLENE RECOVERY FROM FCC RECOVERY UNIT

The present subject matter relates generally to processes for propylene recovery. More specifically, the present subject matter relates to processes for enhanced recovery of propylene and liquid petroleum gas (LPG) from the fuel gas produced in fluid catalytic cracking (FCC) units by minimizing the light ends and propylene in the unstabilized gasoline which is used as lean oil for the primary absorber of the FCC gas concentration unit. 1. A process for the recovery of propylene comprising:(i) contacting a hydrocarbon feed with a catalyst in a fluid catalytic cracking process to produce a product stream;(ii) distilling the product stream in a fractionator to obtain heavier liquid products as side/bottom draws and a gaseous top product;(iii) cooling and condensing the gaseous top product and thereafter, separating the obtained gas-liquid mixture in a receiver to obtain a liquid fraction and a lighter gaseous fraction;(iv) sequentially sending the gaseous fraction obtained from step (iii) to a wet gas compressor train;(v) feeding a first portion of the liquid fraction obtained in step (iii) back to the fractionator;(vi) feeding a second portion of the liquid fraction obtained in step (iii) to at least one heat exchanger to produce a heated stream; and(vii) feeding the heated stream to a flash drum to produce a flashed light ends stream to be sent back to the wet gas compressor in step (iv) and a bottoms liquid stream wherein the bottoms stream is sent to one or more heat exchangers in step (vi) before routing the liquid stream to FCC gas concentration absorber.2. The process of wherein the one or more heat exchangers heats the liquid fraction from about 38° C. to about 80° C.3. The process of wherein the flashed light ends stream contains nearly 70% of the propylene in the flash drum feed.4. The process of wherein one or more of the heat exchanges uses a waste heat process stream.5. The process of wherein two heat exchangers are used to heat the liquid fraction.6. A ...

Method for fractionating a stream of cracked gas, using an intermediate recirculation current, and related plant

The upstream, intermediate and downstream cooling steps is carried out without a heat exchanger respectively of an upstream stream of cracked gas (102), an intermediate stream of cracked gas (114) and a downstream stream of cracked gas (140) with an external refrigeration cycle.

Patent RU2018103076A3

``” ВУ“? 2018103076” АЗ Дата публикации: 26.12.2019 Форма № 18 ИЗ,ПМ-2011 Федеральная служба по интеллектуальной собственности Федеральное государственное бюджетное учреждение ж 5 «Федеральный институт промышленной собственности» (ФИПС) ОТЧЕТ О ПОИСКЕ 1. . ИДЕНТИФИКАЦИЯ ЗАЯВКИ Регистрационный номер Дата подачи 2018103076/04(0044ЗТ) 15.07.2016 РСТ/СВ2016/052163 15.07.2016 Приоритет установлен по дате: [ ] подачи заявки [ ] поступления дополнительных материалов от к ранее поданной заявке № [ ] приоритета по первоначальной заявке № из которой данная заявка выделена [ ] подачи первоначальной заявки № из которой данная заявка выделена [ ] подачи ранее поданной заявки № [Х] подачи первой(ых) заявки(ок) в государстве-участнике Парижской конвенции (31) Номер первой(ых) заявки(ок) (32) Дата подачи первой(ых) заявки(ок) (33) Код страны 1. 1512590.9 17.07.2015 СВ Название изобретения (полезной модели): [Х] - как заявлено; [ ] - уточненное (см. Примечания) СПОСОБ КОНДИЦИОНИРОВАНИЯ ГАЗА И СИСТЕМА ДЛЯ ИЗВЛЕЧЕНИЯ КОНДЕНСИРУЮЩЕГОСЯ ПАРА ИЗ ПОДАВАЕМОГО ГАЗА Заявитель: СЕЙДЖ ЭНД ТАЙМ ЭлЭлПи, СВ 2. ЕДИНСТВО ИЗОБРЕТЕНИЯ [Х] соблюдено [ ] не соблюдено. Пояснения: см. Примечания 3. ФОРМУЛА ИЗОБРЕТЕНИЯ: [Х] приняты во внимание все пункты (см. п см. Примечания [ ] приняты во внимание следующие пункты: [ ] принята во внимание измененная формула изобретения (см. Примечания) 4. КЛАССИФИКАЦИЯ ОБЪЕКТА ИЗОБРЕТЕНИЯ (ПОЛЕЗНОЙ МОДЕЛИ) (Указываются индексы МПК и индикатор текущей версии) С1ОГ. 3/10 (2006.01) 5. ОБЛАСТЬ ПОИСКА 5.1 Проверенный минимум документации РСТ (указывается индексами МПК) 5.2 Другая проверенная документация в той мере, в какой она включена в поисковые подборки: 5.3 Электронные базы данных, использованные при поиске (название базы, и если, возможно, поисковые термины): РУУРТ, Езрасепе, Соозе, РАТЕМТЗСОРЕ, Рабеагсв, ОЗРТО 6. ДОКУМЕНТЫ, ОТНОСЯЩИЕСЯ К ПРЕДМЕТУ ПОИСКА Кате- Наименование документа с указанием (где необходимо) частей, Относится к гория* относящихся к предмету поиска ...

Способ очистки газа, обогащенного кислородом

WASTED HEAT DRIVEN REFINERY'S PETROLEUM GAS RECOVERY APPARATUS

PROCEDURE FOR THE HIGH TEMPERATURE SHORT TIME DISTILLATION OF RESIDUAL OIL

Method for fractionating a stream of cracked gas, using an intermediate recirculation current, and related plant

The invention relates to a method which includes the following steps: forming an expanded intermediate recirculation current (170) from a liquid (112, 128) obtained during an upstream cooling step and/or intermediate cooling step, upstream from the downstream cooling step; circulating the intermediate recirculation current (170) at least through an upstream heat exchanger (42) in order to cool an upstream stream of cracked gas (102); and injecting the reheated intermediate recirculation stream (170) back into a raw cracked gas (20) upstream from at least one compressor (36, 38) of a cooling and compression stage (24). The upstream, intermediate and downstream cooling steps are performed with no heat exchange, respectively, of an upstream stream of cracked gas (102), an intermediate stream of cracked gas (114) and a downstream stream of cracked gas (140) with an external cooling cycle, such as an ethylene cycle.

ENHANCED OLEFIN RECOVERY PROCESS

An enhanced method is disclosed for recovering olefins from a cracking furnace effluent stream in an olefins plant. In accordance with this method, a liquid hydrocarbon stream, preferably obtained from the compressor area drier liquids and/or from the deethanizer or depropanizer, is injected into the reaction effluent stream to condition the reaction effluent stream for enhanced condensation against propylene refrigeration. Also disclosed is an olefins plant utilizing liquid hydrocarbon injection and an improvement to existing olefins recovery process technology using liquid hydrocarbon injection for vapor stream conditioning.

CONTINUOUS PRODUCTION OF AQUEOUS SOLUTIONS OF ALKALINE SALTSOF ARYLACETIC ACIDS

On décrit un procédé de dégazolinage par réfrigération d'un gaz contenant des hydrocarbures condensables, effectué en présence de méthanol pour éviter la formation d'hydrates, ledit procédé permettant de récupérer au moins en partie le méthanol entraîné dans le gaz, par lavage de celui-ci à l'aide d'une fraction hydrocarbure liquide. Le procédé décrit permet ainsi d'éviter d'avoir à compenser la perte en méthanol par un appoint permanent, comme c'est le cas dans les procédés conventionnels. Il présente de ce fait des performances et une économie améliorées.

Recovery of ethylene and heavier hydrocarbons, from gas formed by pyrolysis of hydrocarbons, involves progressive condensation of gases and use of de-ethanizer and de-methanizer

Procédé pour la récupération à grand rendement de l'éthylène et des hydrocarbures plus lourds à partir de gaz produit par pyrolyse des hydrocarbures (1) dans lequel les produits liquides (12-15, 23) résultant de la condensation fractionnée du gaz de craquage (1) pour la récupération de presque tout l'éthylène, alimentent une colonne de distillation (C1), dite dééthaniseur à différents niveaux intermédiaires, au sommet de laquelle, la vapeur (31) du distillat de colonne est traitée directement dans un réacteur d'hydrogénation d'acétylène (R1), l'effluent ne contenant presque plus d'acétylène étant séparé par une colonne de distillation (C2) dite déméthaniseur, en un produit de queue (43) enrichi en éthylène et éthane tandis que le produit de tête (44) est recyclé par compression ou traité pour une récupération ultérieure de l'éthylène.

CYROGENIC SEPARATION OF LIGHT OLEFINS AND METHANE FROM SYNGAS

In accordance with the present invention, disclosed herein is a method comprising the steps for separating syngas and methane from C2-C4 hydrocarbons. Also disclosed herein, are systems utilized to separate syngas and methane from C2-C4 hydrocarbons.

LOW PRESSURE OLEFIN RECOVERY PROCESS

A low-pressure olefins recovery process and plant are described. The feed gas is compressed and distilled at a primary distillation pressure. The overhead stream is chilled at a pressure less than 30 kg/cm2 (430 psia) to partially condense the overheads. The primary distillation tower is refluxed with at least a portion of the condensate. The overhead vapor is further chilled and partially condensed and the condensate is fed to a demethanizer. The remaining vapor is cooled in a cold section and the resultant liquid is phase-separated and expanded to provide refrigeration for the cold section. The expanded vapor from the cold section is recycled to the process gas compressor. The bottoms streams from the primary distillation zone and the demethanizer are fractionated into respective streams consisting essentially of ethylene, ethane, propylene, propane, C4's, and C5+.

Способ разделения водородсодержащей углеводородной смеси, сепарационная секция и олефиновая установка

Способ разделения водородсодержащей углеводородной смеси (С2минус), которая, кроме водорода, по существу содержит углеводороды с двумя атомами углерода и метан, с помощью перегонной колонны. Текучую среду (а, с, е) углеводородной смеси (С2минус) охлаждают поэтапно при первом уровне давления, во время чего первые конденсаты (b, d) отделяют от текучей среды (а, с, е). Текучую среду (е) от углеводородной смеси (С2минус), которая после этого остается газообразной, подают при первом уровне давления в С2 поглотитель, в верхнюю часть которого добавляют жидкую флегму (r), в то время как второй конденсат (f) извлекают из куба С2 поглотителя, а газообразный верхний поток (g), преимущественно содержащий метан и водород, извлекают в верхней части С2 поглотителя. Текучую среду указанного выше газообразного верхнего потока (g) из верхней части С2 поглотителя охлаждают до третьего уровня температуры и перемещают при первом уровне давления в сепаратор водорода (8), в котором богатый метаном третий конденсат ...

СПОСОБ КОНДИЦИОНИРОВАНИЯ ГАЗА И СИСТЕМА ДЛЯ ИЗВЛЕЧЕНИЯ КОНДЕНСИРУЮЩЕГОСЯ ПАРА ИЗ ПОДАВАЕМОГО ГАЗА

FIELD: technological processes.SUBSTANCE: invention describes a method for extracting condensed steam from fed gas, comprising steps of: i) cooling the feed gas to a first condensation surface (41), wherein said first condensation surface is controlled by temperature to first temperature for condensation of portion of condensable steam in feed gas, so that the feed gas is divided into a pre-condensed fraction and a process gas, wherein preliminary condensed fraction is removed on first condensation surface by means of mechanical scraper means (56, 66); and ii) cooling process gas to second condensation surface (42), wherein second condensation surface is controlled by temperature to second temperature for condensation of additional portion of remaining condensing steam in process gas, so that process gas is divided into next condensed fraction and produced gas, wherein subsequent condensed fraction is removed on condensation surface by means of mechanical scraper means (56, 66); wherein the pre-condensed fraction has a higher condensation point temperature than the subsequent condensed fraction; and wherein the pre-condensed fraction has a higher viscosity than the subsequent condensed fraction at any given temperature below the second temperature, wherein the method further comprises steps of: a) collecting a remote successive condensed fraction at first location (92c), wherein first location is controlled by temperature to second temperature; and b) collecting the remote pre-condensed fraction at the second location, wherein second location is controlled by temperature to first temperature. Also disclosed is gas conditioning system (10) for extracting condensed steam.EFFECT: technical result in obtaining purified gas due to improved efficiency and reliability of condenser operation due to mechanical cleaning of condenser surface from accumulation of deposits (resin) on condensation surfaces, due to their improved fluidity.20 cl, 13 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU ...

METHOD AND SYSTEM FOR PURIFYING A GAS RICH IN HYDROCARBONS

Process for purifying a gas (1) rich in hydrocarbons and comprising at least 10 ppm by volume of hydrocarbons having at least six carbon atoms, comprising the following steps: Step a) Cooling said gas to a temperature between -20°C and -60°C by heat exchange with at least one coolant (3) in a heat exchanger (2); Step b) Scrubbing of compounds containing at least six carbon atoms from the gas partially liquefied in step a) in a washing column (5) containing a column (5) overhead (8) in its highest end and a column (5) bottom (7) in its lowest end in order to form, as washing column (5) overhead (8), a gas stream (9) containing less than 5 ppm by volume of compounds containing at least six carbon atoms and, as washing column (5) bottoms (7), a liquid stream (6) enriched in compounds containing at least five carbon atoms; Step c) At least partial condensation of said gas stream (9) resulting from step b) in a heat exchanger (10, 2) in order to form a two-phase stream (15); Step d) Separating said two-phase stream (15) resulting from step c) in a phase separator pot (16) at a temperature between -60°C and -80°C in order to form a gas stream (17) as pot overhead and a liquid stream (18) as pot bottoms (16); Step e) Use of the liquid stream (18) resulting from step d) as washing column (5) overhead (8) reflux; Step f) Condensation of the gas stream (17) resulting from step d) by heat exchange in a heat exchanger (20, 2) at a temperature below -100°C in order to form a liquefied gas (21) containing less than 5 ppm by volume of compounds containing at least six carbon atoms.

Precooling for Ethylene Recovery in Dual Demethanizer Fractionation Systems

Ethylene-containing feed gas to a cryogenic ethylene recovery system is cooled and condensed, prior to fractionation, by an improved method which utilizes a combination of one or more partial condensers followed by one or more dephlegmators. The improved method simplifies heat exchange equipment and reduces capital cost, and is particularly suited for processing a pressurized precooled feed gas from ethane cracking which contains less than about 1 mole% of propane plus propylene.

METHOD OF TREATING A HYDROCARBON FEEDSTOCK COMPRISING HYDROGEN AND HYDROCARBONS IN C1 HAS C4.

Patent RU2016127551A3

`7ВУ’” 2016127551” АЗ Дата публикации: 09.07.2018 Форма № 18 ИЗ,ПМ-2011 Федеральная служба по интеллектуальной собственности Федеральное государственное бюджетное учреждение 5 «Федеральный институт промышленной собственности» (ФИПС) ОТЧЕТ О ПОИСКЕ 1. . ИДЕНТИФИКАЦИЯ ЗАЯВКИ Регистрационный номер Дата подачи 2016127551/05(043192) 17.12.2014 РСТ/ЕР2014/078168 17.12.2014 Приоритет установлен по дате: [ ] подачи заявки [ ] поступления дополнительных материалов от к ранее поданной заявке № [ ] приоритета по первоначальной заявке № из которой данная заявка выделена [ ] подачи первоначальной заявки № из которой данная заявка выделена [ ] подачи ранее поданной заявки № [Х] подачи первой(ых) заявки(ок) в государстве-участнике Парижской конвенции (31) Номер первой(ых) заявки(ок) (32) Дата подачи первой(ых) заявки(ок) (33) Код страны 1. 14000040.7 07.01.2014 ЕР Название изобретения (полезной модели): [Х] - как заявлено; [ ] - уточненное (см. Примечания) Способ разделения водородсодержащей углеводородной смеси, сепарационная секция и олефиновая установка Заявитель: ЛИНДЕ АКТИНГЕЗЕЛЛЬШАФТ, ОЕ 2. ЕДИНСТВО ИЗОБРЕТЕНИЯ [Х] соблюдено [ ] не соблюдено. Пояснения: см. Примечания 3. ФОРМУЛА ИЗОБРЕТЕНИЯ: [Х] приняты во внимание все пункты (см. Примечания) [ ] приняты во внимание следующие пункты: [ ] принята во внимание измененная формула изобретения (см. Примечания) 4. КЛАССИФИКАЦИЯ ОБЪЕКТА ИЗОБРЕТЕНИЯ (ПОЛЕЗНОЙ МОДЕЛИ) (Указываются индексы МПК и индикатор текущей версии) ВОТ 53/14 (2006.01) 5. ОБЛАСТЬ ПОИСКА 5.1 Проверенный минимум документации РСТ (указывается индексами МПК) ВОО 53/00 - ВОО 53/14 5.2 Другая проверенная документация в той мере, в какой она включена в поисковые подборки: 5.3 Электронные базы данных, использованные при поиске (название базы, и если, возможно, поисковые термины): РУ\У/РТ, Ебрасепес, Рабеагсь, КОРТО, ИЗРТО 6. ДОКУМЕНТЫ, ОТНОСЯЩИЕСЯ К ПРЕДМЕТУ ПОИСКА Кате- Наименование документа с указанием (где необходимо) частей, Относится к гория* относящихся к предмету ...

Способ очистки газа, обогащенного углеводородами

FIELD: chemistry. SUBSTANCE: invention is intended for purification of gas enriched with hydrocarbons. Method of cleaning hydrocarbon-enriched gas and containing at least 10 ppm by volume of hydrocarbons, having at least six carbon atoms, comprises steps of: a) cooling said gas to temperature between -20 °C and -60 °C as a result of heat exchange with at least one coolant in heat exchanger; b) cleaning from compounds containing at least six carbon atoms, gas partially liquefied at step a) in a flushing column comprising an upper part of the column at its highest end and a capacity of the column at its lowest end, in order form a gas flow on the upper part of the flushing column, containing less than 5 ppm by volume of compounds having at least six carbon atoms, and in a flushing column a liquid stream enriched with compounds having at least five carbon atoms; c) at least partial condensation of said gas stream obtained at step b) in a heat exchanger in order to form a two-phase stream; d) separating the two-phase flow in the separator at a temperature in the range of -60 °C to -80 °C in order to form a gas stream in the upper part of the separator and a liquid stream in the vat of separator (16); e) using the stream of liquid obtained at step d) as reflux of the upper part of the flushing column; f) condensing the gas stream obtained at step d) by heat exchange in a heat exchanger at a temperature below -100 °C in order to form a liquefied gas containing less than 5 ppm by volume of compounds having at least six carbon atoms. EFFECT: technical result is reduction of content of heavy hydrocarbons in natural gas. 10 cl, 1 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 700 507 C1 (51) МПК F25J 3/00 (2006.01) C10G 5/06 (2006.01) C10L 3/10 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (52) СПК F25J 3/00 (2013.01); C10G 5/06 (2013.01); C10L 3/10 (2013.01) (21)(22) Заявка: 2016129126, 18.07.2016 (24) Дата начала отсчета ...

Petroleum gas recovery apparatus driven by refinery's normally wasted heat

A gas conditioning system

A process for extracting a condensable vapour (e.g. tars) from a supplied gas (e.g. methane), comprising the steps of: i) condensing the condensable vapour by cooling the supplied gas at a condensing surface, especially in a multi-step fashion, such that the supplied gas is divided into at least one condensed fraction and a product gas; while ii) removing the at least one condensed fraction from the condensing surface by mechanical scraping means, which may be the screw from a screw extruder. The condensing units may be those numbered 41-44.

PROCESS FOR SEPARATING AND RECOVERING NGLS FROM HYDROCARBON STREAMS

This process comprises using unconventional processing of hydrocarbons, e.g. natural gas, for recovering C2+ and NGL hydrocarbons that meet pipeline specifications, without the core high capital cost requirement of a demethanizer column, which is central to and required by almost 100% of the world's current NGL recovery technologies. It can operate in Ethane Extraction or Ethane Rejection modes. The process uses only heat exchangers, compression and simple separation vessels to achieve specification ready NGL. The process utilizes cooling the natural gas, expansion cooling, separating the gas and liquid streams, recycling the cooled streams to exchange heat and recycling selective composition bearing streams to achieve selective extraction of hydrocarbons, in this instance being NGLs. The compactness and utility of this process makes it feasible in offshore applications as well as to implementation to retrofit/revamp or unload existing NGL facilities. Many disparate processes and derivatives ...

LOW PRESSURE OLEFIN RECOVERY PROCESS

A low-pressure olefins recovery process and plant are described. The feed gas 300 is compressed 302, 304 and distilled 310 at a primary distillation pressure. The overhead stream 312 is chilled 318 at a pressure less than 30 kg/cm2 (430 psia) to partially condense the overheads. The primary distillation tower 310 is refluxed with at least a portion of the condensate 320. The overhead vapor is further chilled 318 and partially condensed and the condensate 322 is fed to a demethanizer 324. The remaining vapor 326 is cooled in a cold section 328 and the resultant liquid is phase-separated 330 and expanded 331, 334 to provide refrigeration for the cold ssection. The expanded vapor 332 from the cold section is recycled to the process gas compressor. The bottoms streams 338, 342 from the primary distillation zone and the demethanizer are fractionated into respective streams consisting essentially of ethylene 356, ethane 358, propylene 364, propane 366, C4's 346, and C5+ 348.

METHOD FOR A HIGH TEMPERATURE SHORT-TIME DISTILLATION OF RESIDUAL OIL

The invention relates to a method for a high temperature short-time distillation of residual oil. The method according to the invention is characterized by a technically simple recovery of a small residual fraction from a gas and/or oil vapour mixture produced by a mixing apparatus (1). Said small residual fraction contains large quantities of undesirable polluting catalytic substances (CCR, Ni, V, asphaltenes). For this purpose, the gas and/or oil vapour mixture produced by the mixing apparatus (1) is diluted with gas or water vapour in a column (17) at a temperature of 450.degree.C in such a way that a high boiling fraction, which has a high content of the pollutant substances and whose initial boiling point is higher than 450.degree.C, is condensed and extracted. Another realization of the method consists in introducing a non condensed oil produced in the column (17) into a fractionating column (19), where said oil is decomposed in order to produce a depressurized gas oil fraction having ...

TARGETED HYDROGENATION HYDROCRACKING

This invention is directed to a process scheme in which a partial conversion hydrocracking (HCR) unit, preferably preceded by a hydrotreating unit, feeds unconverted oil to a FCC (fluid catalytic cracking ) unit. Most refineries run the FCC unit at the full capacity for optimal asset utilization. During shutdowns of Residue Desulfurization unit(s) which feed an FCC unit, it is desirable to reduce the conversion in the FCC feed hydrocracker. In this way, the feed to FCC unit is maximized. Jet and Diesel products that conform to specifications may be produced during low conversion HCR operation. Furthermore, undesirable over-saturation of the unconverted oil (UCO) from the HCR unit feeding the FCC unit can be avoided. Excess hydrogen consumption can also be avoided. Normally, further aromatic saturation of the middle distillate products from a low conversion HCR is achieved in a separate, post treatment, unit.

Stage and system for compressing cracked gas

A compression stage for the compression of cracked gas, the compression stage comprising a liquid separating means for separating liquid components from gaseous components of a cracked gas, a compressor connected to the liquid separating means, a gas cooling means connected to the compressor for cooling the compressed gas from the compressor, wherein the gas cooling means are cooled by a first cooling fluid from the cooling fluid source. The stage further comprises gas precooling means connected to the liquid separating means cracked gas, having an inlet for receiving the cracked gas.

A gas conditioning system

Improvements in or relating to the temperature treatment of fluids applicable to the recovery of volatile solvents

... In recovering vapours of solvents used in fabric-coating processes, a gas is directed by nozzles on to the fabric whilst subjected to heat, whereupon it is withdrawn through a heat-exchanger and then passes to a condenser, returning in closed cycle through the other side of the heat-exchanger to the nozzles. A fan 36 draws solvent-laden gas, e.g. air or carbon dioxide, from a casing 35 or forces it through a heat-exchanger 37, over a cooler 40, back through the other passage of the heat-exchanger, and then through a heater (not shown) to the casing 35 where it again takes up solvent vapour. The solvent condensed by the cooler 40 is drawn off by a tap (not shown). Valves may be provided to add to, or remove a portion from, the circulating gas. A suitable form of heat-exchanger consist of thin sheets of a well-conducting metal such as copper, alternately flat as at 25 and corrugated as at 26 in Fig. 3. The corrugated sheets act as spacers for the flat sheets, and the ...

Process for degaslining a gas containing condensable hydrocarbons

Method for separating a hydrocarbon mixture containing hydrogen, separating device, and olefin plant

The invention relates to a method for separating a hydrocarbon mixture containing hydrogen, which hydrocarbon mixture essentially contains, besides hydrogen, hydrocarbons having two carbon atoms and methane, by using a distillation column (10). Fluid (a, c, e) of the hydrocarbon mixture is cooled in stages at a first pressure level, wherein first condensates (b, d) are separated from the fluid (a, c, e). Fluid of the hydrocarbon mixture, which subsequently remains gaseous, is fed into a C2 absorber (7) at the first pressure level, to which C2 absorber a liquid return (r) is fed at the top, wherein a second condensate (f) is drawn from the bottom of the C2 absorber (7) and a gaseous top flow (g) predominantly containing methane and hydrogen is drawn at the top of the C2 absorber (7). Fluid of said gaseous top flow (g) from the top of the C2 absorber (7) is cooled to a third temperature level and is transferred at the first pressure level into a hydrogen separator (8), in which a methane-rich ...

PROCESS AND A PLANT FOR SEPARATING A HYDROCARBON MIXTURE

The invention relates to a process for separating a component mixture (K) which contains hydrogen, methane, hydrocarbons having two carbon atoms and hydrocarbons having three or more carbon atoms, wherein in a deethanization at least one portion of the component mixture (K) is subjected to a first partial condensation by cooling from a first temperature level to a second temperature level at a first pressure level to obtain a first gas fraction (G1) and a first liquid fraction (C1), at least one portion of the gas fraction (G1) is subjected to a second partial condensation by cooling from the second temperature level to a third temperature level at the first pressure level to obtain a second gas fraction (G4) and a second liquid fraction (C2) and at least a portion of the first liquid fraction (C1) and at least a portion of the second liquid fraction (C1) are subjected to a rectification to obtain a third gas fraction (G3) and a third liquid fraction (C3+). The first liquid fraction (C1 ...

NOX REMOVAL METHOD

The invention relates to mixtures comprising molecular hydrogen, hydrocarbons, and nitrogen oxides; to processes for removing at least a portion of the nitrogen oxides therefrom; to equipment useful in such processes; and to the use of such hydrocarbons for, e.g., chemical manufacturing.

PRECOOLING FOR ETHYLENE RECOVERY IN DUAL DEMETHANIZER FRACTIONATION SYSTEMS

Ethylene-containing feed gas to a cryogenic ethylene recovery system is cooled and condensed, prior to fractionation, by an improved method which utilizes a combination of one or more partial condensers followed by one or more dephlegmators. The improved method simplifies heat exchange equipment and reduces capital cost, and is particularly suited for processing a pressurized precooled feed gas from ethane cracking which contains less than about 1 mole% of propane plus propylene.

PROCESS OF EXTRACTION OF CRUDE Of a GAS CONTAINING OF CONDENSABLE HYDROCARBONS

PROCEEDED OF TREATMENT Of a GAS CURRENT CRACKS RESULTING From an INSTALLATION FROM HYDROCARBON PYROLYSIS AND ASSOCIATED INSTALLATION.

Ce procédé comporte la séparation d'un courant amont de gaz craqué partiellement condensé dans un séparateur intermédiaire (44B) pour récupérer un liquide intermédiaire (136) et un courant intermédiaire (138) de gaz craqué et l'introduction du liquide intermédiaire (140) dans une colonne intermédiaire (68) de déméthanisation. Le procédé comprend le prélèvement d'une partie du liquide intermédiaire (136) et la détente d'au moins une première fraction (194) obtenue à partir de la partie prélevée (190). Il comprend la mise en relation d'échange thermique de la première fraction détendue avec le courant intermédiaire de tête (146) issu de la colonne (68) pour condenser au moins partiellement le courant intermédiaire de tête (146). Le procédé comporte la séparation du courant intermédiaire de tête partiellement condensé dans un premier séparateur (76) de reflux pour former un courant liquide (148) introduit dans la colonne intermédiaire (68) et un courant gazeux de combustible (150).

Low pressure olefin recovery process

A low-pressure olefins recovery process and plant are described. The feed gas 300 is compressed 302, 304 and distilled 310 at a primary distillation pressure. The overhead stream 312 is chilled 318 at a pressure less than 30 kg/cm 2 (430 psia) to partially condense the overheads. The primary distillation tower 310 is refluxed with at least a portion of the condensate 320 . The overhead vapor is further chilled 318 and partially condensed and the condensate 322 is fed to a demethanizer 324 . The remaining vapor 326 is cooled in a cold section 328 and the resultant liquid is phase-separated 330 and expanded 331, 334 to provide refrigeration for the cold ssection. The expanded vapor 332 from the cold section is recycled to the process gas compressor. The bottoms streams 338, 342 from the primary distillation zone and the demethanizer are fractionated into respective streams consisting essentially of ethylene 356 , ethane 358 , propylene 364 , propane 366 , C 4 's 346 , and C 5+ 348.

Ethylene recovery method

NOX REMOVAL METHOD

The invention relates to mixtures comprising molecular hydrogen, hydrocarbons, and nitrogen oxides; to processes for removing at least a portion of the nitrogen oxides therefrom; to equipment useful in such processes; and to the use of such hydrocarbons for, e.g., chemical manufacturing.

PROCESS AND INSTALLATION FOR the RECOVERY AND the PURIFICATION OF the ETHYLENEPRODUIT BY PYROLYSIS Of HYDROCARBONS, AND GASES OBTAINED BY THIS PROCESS

PROCESS OF EXTRACTION OF CRUDE Of a GAS CONTAINING OF CONDENSABLE HYDROCARBONS

Le dégazolinage d'un gaz contenant des hydrocarbures condensables par réfrigération peut être effectué en présence de méthanol pour éviter la formation d'hydrates. Lors de la mise en oeuvre d'un procédé conventionnel une partie du méthanol est solubilisée dans le gaz après traitement. Cette perte en méthanol doit être compensée par un appoint permanent. La présente invention décrit un procédé permettant de récupérer le méthanol entraîné dans le gaz et présentant de ce fait des performances et une économie améliorées. The degasification of a gas containing condensable hydrocarbons by refrigeration can be carried out in the presence of methanol to prevent the formation of hydrates. During the implementation of a conventional process, part of the methanol is dissolved in the gas after treatment. This loss of methanol must be compensated by a permanent make-up. The present invention describes a process for recovering the methanol entrained in the gas and thereby exhibiting improved performance and economy.

METHOD OF TREATING A HYDROCARBON FEEDSTOCK COMPRISING HYDROGEN AND HYDROCARBONS IN C1 HAS C4.

La présente invention concerne un procédé de traitement d'une charge hydrocarbonée contenant de l'hydrogène et des hydrocarbures incluant des hydrocarbures en C1 à C4, mettant en œuvre une première et une seconde étapes de recontactage et dans lequel la l'effluent gazeux issu de la seconde étape de recontactage est recyclé à la première de recontactage. Le procédé s'applique en particulier au traitement d'une charge hydrocarbonée issue du reformage catalytique en vue de récupérer l'hydrogène et des hydrocarbures en C3 et C4. The present invention relates to a process for treating a hydrocarbon feedstock containing hydrogen and hydrocarbons including C1 to C4 hydrocarbons, implementing a first and a second recontacting step and wherein the gaseous effluent from the second recontacting step is recycled to the first recontacting. The process is particularly applicable to the treatment of a hydrocarbon feedstock from catalytic reforming for recovering hydrogen and C3 and C4 hydrocarbons.

탄화수소 스트림으로부터 NGL을 분리 및 회수하기 위한 공정

본 공정은, 세계의 현재 NGL 회수 기술의 중심이 되고 거의 100%로 요구되는 탈메탄화 컬럼의 핵심 고비용 요구 없이 파이프라인 사양들을 만족하는 C2+와 NGL 탄화수소를 회수하기 위한, 탄화수소, 예를 들어 천연 가스의 독특한 처리를 이용하는 것을 포함한다. 공정은 에탄 추출 또는 에탄 제거 모드에서 작동할 수 있다. 공정은 사양 준비 NGL을 얻기 위해 단지 열교환기, 압축 용기 및 단순한 분리 용기를 사용한다. 공정은 천연 가스를 냉각하는 것, 팽창 냉각, 가스 스트림과 액체 스트림을 분리하는 것, 냉각된 스트림을 열을 교환시키기 위해 재순환시키는 것, 그리고 탄화수소, 이 경우에 NGL의 선택적 추출을 얻기 위해 선택적 조성을 함유하는 스트림을 재순환시키는 것을 활용한다. 이러한 공정의 간결성 및 유용성은 공정을, 기존의 NGL 시설을 새로 장착/개조 또는 제거하기 위해 실행하는 것에 더해 역외의 응용들에서 실현 가능하게 만든다. 많은 상이한 공정들과 파생물이 이에 사용될 것으로 예상된다 The process is a process for the recovery of C2 + and NGL hydrocarbons that meet the pipeline specifications without the core high cost requirements of the demethanating columns that are at the center of the current NGL recovery technology in the world and which require almost 100% Gas < / RTI > The process may operate in an ethane extraction or ethane removal mode. The process uses only a heat exchanger, a compression vessel and a simple separation vessel to obtain a specially prepared NGL. The process may include cooling the natural gas, expanding cooling, separating the gas stream and the liquid stream, recirculating the cooled stream to exchange heat, and selectively extracting hydrocarbons, in this case selective extraction of NGL Lt; RTI ID = 0.0 > recycle < / RTI > The simplicity and availability of such a process makes the process feasible in applications outside of the country, in addition to executing to retrofit or retrofit existing NGL facilities. Many different processes and derivatives are expected to be used therefor

Hydrocarbon gas recovery methods

A method of recovery of rich gas where the rich gas is a hydrocarbon gas comprising less than 50 mole % methane is disclosed. The method comprises the steps of gathering the low pressure gas, compressing the gathered gas, cooling the compressed gas in a condenser so that a portion of the compressed gas condenses to form a liquefied gas and liquefied gas vapour in the condenser, and discharging the liquefied gas and liquefied gas vapour from the condenser, in which the cooling of the compressed gas is performed using at least one heat exchanger (40).

Process and installation for recovering and purifying of ethylen produced by hydrocarbon pyrolysis

Recovery of ethylene and heavier hydrocarbons, from gas formed by pyrolysis of hydrocarbons, involves progressive condensation of gases and use of de-ethanizer and de-methanizer The method involves the removal of acetylene by solvent extraction and selective hydrogenation. A final gaseous current enriched in hydrogen and methane and a liquid fraction enriched in ethylene and ethane are collected. A process for the fractionation of an anhydrous gas from hydrocarbons pyrolysis containing H2 and 1 - 3C hydrocarbons, including ethylene, propylene and acetylene into a current enriched in H2 and methane, a current enriched in ethylene and depleted in acetylene and a current enriched in propylene, involves: (a) cooling the pyrolysis gas and progressively liquefying it by passing through a succession of heat exchangers at decreasing temperatures; condensates are obtained one enriched in propylene and another enriched in ethylene and ethane with a proportion of H2, methane and acetylene in solution ...

A gas conditioning system

Process for degasolining a gas containing condensable hydrocarbons

Water and condensable hydrocarbon compounds are removed from natural/refinery gas using a process involving refrigeration in the presence of methanol to achieve simultaneous condensation of the hydrocarbon compounds and absorption of water by the methanol, followed by separation to obtain a gaseous purified product that will contain entrapped methanol, a liquid aqueous phase that is predominately methanol with absorbed water and a liquid hydrocarbon phase containing some methanol. The two liquid phases are separated, the C 1 and C 2 compounds are removed from the liquid hydrocarbon phase and the remaining higher molecular weight compounds (#C 3 ) are treated with water to remove the methanol. A portion of this methanol free hydrocarbon phase is then used to recover at least a portion of the entrapped methanol in the purified gaseous product and the solution thus obtained is then combined with the liquid hydrocarbon phase obtained from the separation step. A number of configurations of this ...

Process for separating and recovering NGLs from hydrocarbon streams

This process comprises using unconventional processing of hydrocarbons, e.g. natural gas, for recovering C2+ and NGL hydrocarbons that meet pipeline specifications, without the core high capital cost requirement of a demethanizer column, which is central to and required by almost 100% of the world's current NGL recovery technologies. It can operate in Ethane Extraction or Ethane Rejection modes. The process uses only heat exchangers, compression and simple separation vessels to achieve specification ready NGL. The process utilizes cooling the natural gas, expansion cooling, separating the gas and liquid streams, recycling the cooled streams to exchange heat and recycling selective composition bearing streams to achieve selective extraction of hydrocarbons, in this instance being NGLs. The compactness and utility of this process makes it feasible in offshore applications as well as to implementation to retrofit/revamp or unload existing NGL facilities. Many disparate processes and derivatives ...

RECOVERY AND PURIFICATION PROCESS AND INSTALLATION OF ETHYLENE MANUFACTURED THROUGH HYDROCARBON PYROLYSIS, AND GASES OBTAINED FROM THIS PROCESS

Procédé pour la récupération à grand rendement de l'éthylène et des hydrocarbures plus lourds à partir de gaz produit par pyrolyse des hydrocarbures (1) dans lequel les produits liquides (12-15, 23) résultant de la condensation fractionnée du gaz de craquage (1) pour la récupération de presque tout l'éthylène, alimentent une colonne de distillation (C1), dite dééthaniseur à différents niveaux intermédiaires, au sommet de laquelle, la vapeur (31) du distillat de colonne est traitée directement dans un réacteur d'hydrogénation d'acétylène (R1), l'effluent ne contenant presque plus d'acétylène étant séparé par une colonne de distillation (C2) dite déméthaniseur, en un produit de queue (43) enrichi en éthylène et éthane tandis que le produit de tête (44) est recyclé par compression ou traité pour une récupération ultérieure de l'éthylène.

The use of an intermediate recirculation flow fractionation cracking gas flow method and related apparatus

本发明涉及一种包括以下步骤的方法：‑在下游冷却步骤的上游，由在上游冷却和/或中间冷却步骤时获得的液体(112，128)形成膨胀的中间再循环流(170)；‑使中间再循环流(170)至少在上游热交换器(42)中流通以冷却上游裂化气体流(102)；‑将再加热的中间再循环流(170)再引入到冷却与压缩级(24)的至少一个压缩器(36，38)的上游的粗裂化气体(20)中。该上游、中间和下游冷却步骤的进行没有上游裂化气体流(102)、中间裂化气体流(114)和下游裂化气体流(140)与外部制冷循环如乙烯循环的各自的热交换。

A CURRENT PROCESS FOR THE RECOVERY OF ETHYLENE FROM A FEED STREAM RICH IN CARBON MONOXIDE, AND INSTALLATION

Low pressure olefin recovery process

A low-pressure olefins recovery process and plant are described. The feed gas 300 is compressed 302, 304 and distilled 310 at a primary distillation pressure. The overhead stream 312 is chilled 318 at a pressure less than 30 kg/cm 2 (430 psia) to partially condense the overheads. The primary distillation tower 310 is refluxed with at least a portion of the condensate 320. The overhead vapor is further chilled 318 and partially condensed and the condensate 322 is fed to a demethanizer 324. The remaining vapor 326 is cooled in a cold section 328 and the resultant liquid is phase-separated 330 and expanded 331, 334 to provide refrigeration for the cold ssection. The expanded vapor 332 from the cold section is recycled to the process gas compressor. The bottoms streams 338, 342 from the primary distillation zone and the demethanizer are fractionated into respective streams consisting essentially of ethylene 356, ethane 358, propylene 364, propane 366, C 4 's 346, and C 5+ 348.

METHOD FOR HIGH-TEMPERATURE DISTILLATION OF RESIDUAL OIL IN A LIMITED TIME

Method for separating a hydrocarbon mixture containing hydrogen, separating device, and olefin plant

The invention relates to a method for separating a hydrocarbon mixture containing hydrogen, which hydrocarbon mixture essentially contains, besides hydrogen, hydrocarbons having two carbon atoms and methane, by using a distillation column (10). Fluid (a, c, e) of the hydrocarbon mixture is cooled in stages at a first pressure level, wherein first condensates (b, d) are separated from the fluid (a, c, e). Fluid of the hydrocarbon mixture, which subsequently remains gaseous, is fed into a C2 absorber (7) at the first pressure level, to which C2 absorber a liquid return (r) is fed at the top, wherein a second condensate (f) is drawn from the bottom of the C2 absorber (7) and a gaseous top flow (g) predominantly containing methane and hydrogen is drawn at the top of the C2 absorber (7). Fluid of said gaseous top flow (g) from the top of the C2 absorber (7) is cooled to a third temperature level and is transferred at the first pressure level into a hydrogen separator (8), in which a methane-rich ...

RECOVERY AND PURIFICATION PROCESS AND INSTALLATION OF ETHYLENE MANUFACTURED THROUGH HYDROCARBON PYROLYSIS, AND GASES OBTAINED FROM THIS PROCESS

Procédé pour la récupération à grand rendement de l'éthylène et des hydrocarbures plus lourds à partir de gaz produit par pyrolyse des hydrocarbures (1) dans lequel les produits liquides (12-15, 23) résultant de la condensation fractionnée du gaz de craquage (1) pour la récupération de presque tout l'éthylène, alimentent une colonne de distillation (C1), dite dééthaniseur à différents niveaux intermédiaires, au sommet de laquelle, la vapeur (31) du distillat de colonne est traitée directement dans un réacteur d'hydrogénation d'acétylène (R1), l'effluent ne contenant presque plus d'acétylène étant séparé par une colonne de distillation (C2) dite déméthaniseur, en un produit de queue (43) enrichi en éthylène et éthane tandis que le produit de tête (44) est recyclé par compression ou traité pour une récupération ultérieure de l'éthylène.

LOW PRESSURE OLEFIN RECOVERY PROCESS

A low-pressure olefins recovery process and plant are described. The feed gas 300 is compressed 302, 304 and distilled 310 at a primary distillation pressure. The overhead stream 312 is chilled 318 at a pressure less than 30 kg/cm2 (430 psia) to partially condense the overheads. The primary distillation tower 310 is refluxed with at least a portion of the condensate 320. The overhead vapor is further chilled 318 and partially condensed and the condensate 322 is fed to a demethanizer 324. The remaining vapor 326 is cooled in a cold section 328 and the resultant liquid is phase-separated 330 and expanded 331, 334 to provide refrigeration for the cold ssection. The expanded vapor 332 from the cold section is recycled to the process gas compressor. The bottoms streams 338, 342 from the primary distillation zone and the demethanizer are fractionated into respective streams consisting essentially of ethylene 356, ethane 358, propylene 364, propane 366, C4's 346, and C5+ 348.

PROCESS FOR SEPARATING AND RECOVERING NGLS FROM HYDROCARBON STREAMS

This process comprises using unconventional processing of hydrocarbons, e.g. natural gas, for recovering C2+ and NGL hydrocarbons that meet pipeline specifications, without the core high capital cost requirement of a demethanizer column, which is central to and required by almost 100% of the world's current NGL recovery technologies. It can operate in Ethane Extraction or Ethane Rejection modes. The process uses only heat exchangers, compression and simple separation vessels to achieve specification ready NGL. The process utilizes cooling the natural gas, expansion cooling, separating the gas and liquid streams, recycling the cooled streams to exchange heat and recycling selective composition bearing streams to achieve selective extraction of hydrocarbons, in this instance being NGLs. The compactness and utility of this process makes it feasible in offshore applications as well as to implementation to retrofit/revamp or unload existing NGL facilities. Many disparate processes and derivatives are anticipated for its use.

PROCESS FOR TREATING A STREAM OF CRACKED GAS COMING FROM A HYDROCARBON PYROLYSIS PLANT, AND ASSOCIATED PLANT

Ce procédé comporte la séparation d'un courant amont de gaz craqué partiellement condensé dans un séparateur intermédiaire (44B) pour récupérer un liquide intermédiaire (136) et un courant intermédiaire (138) de gaz craqué et l'introduction du liquide intermédiaire (140) dans une colonne intermédiaire (68) de déméthanisation. Le procédé comprend le prélèvement d'une partie du liquide intermédiaire (136) et la détente d'au moins une première fraction (194) obtenue à partir de la partie prélevée (190). Il comprend la mise en relation d'échange thermique de la première fraction détendue avec le courant intermédiaire de tête (146) issu de la colonne (68) pour condenser au moins partiellement le courant intermédiaire de tête (146). Le procédé comporte la séparation du courant intermédiaire de tête partiellement condensé dans un premier séparateur (76) de reflux pour former un courant liquide (148) introduit dans la colonne intermédiaire (68) et un courant gazeux de combustible (150).

METHOD FOR FRACTIONATION OF A CRACKED GAS STREAM, IMPLEMENTING A CURRENT INTERMEDIATE RECYCLE, AND RELATED INSTALLATION

Ce procédé comprend les étapes suivantes : - formation d'un courant (170) de recycle intermédiaire détendu à partir d'un liquide (112, 128) obtenu lors d'une étape de refroidissement amont, ou/et de refroidissement intermédiaire, en amont d'une l'étape de refroidissement aval ; - circulation du courant de recycle intermédiaire (170) au moins dans un échangeur thermique amont (42) pour refroidir un courant amont de gaz craqué (102) ; - réintroduction du courant de recycle intermédiaire (170) réchauffé dans un gaz craqué brut (20) en amont d'au moins un compresseur (36, 38) d'un étage de refroidissement et de compression (24). Les étapes de refroidissement amont, intermédiaire et aval s'effectue sans échange thermique respectivement d'un courant amont de gaz craqué (102), d'un courant intermédiaire de gaz craqué (114) et d'un courant aval de gaz craqué (140) avec un cycle de réfrigération externe, tel qu'un cycle à l'éthylène. This process comprises the following steps: - formation of an intermediate recycle stream (170) expanded from a liquid (112, 128) obtained during an upstream cooling stage, and / or intermediate cooling, upstream a downstream cooling step; - circulating the intermediate recycle stream (170) at least in an upstream heat exchanger (42) for cooling an upstream stream of cracked gas (102); - reintroduction of the intermediate recycle stream (170) heated in a crude cracked gas (20) upstream of at least one compressor (36, 38) of a cooling stage and compression (24). The upstream, intermediate and downstream cooling stages are carried out without thermal exchange respectively of an upstream stream of cracked gas (102), an intermediate stream of cracked gas (114) and a downstream stream of cracked gas (140). ) with an external refrigeration cycle, such as an ethylene ring.

METHOD FOR FRACTIONATION OF A CRACKED GAS STREAM, IMPLEMENTING A CURRENT OF RECYCLED INTERMEDIATE, AND RELATED INSTALLATION

METHOD FOR FRACTIONATING A STREAM OF CRACKED GAS, USING AN INTERMEDIATE RECIRCULATION CURRENT, AND RELATED PLANT

RECOVERY OF ETHYLENE

PURPOSE: To efficiently obtain ethylene from a feed gas obtained from fractional distillation of ethane and ethane-propane. CONSTITUTION: In a method for recovering ethylene from a pressurized feed gas containing ethylene, hydrogen and a 1-3C hydrocarbon, a cooling and condensing step comprises (a) a step of partially condensing the pressurized feed gas in a partial condenser in a first condensing zone operated at a specific temperature or higher, (b) a step of separating the partially condensed feed gas of the step (a) into a first steam flow and a condensed flow, and (c) a step of obtaining a soft gas and a partially condensed liquid by partial condensation of the first steam flow in a second condensing zone operated at a specific temperature or lower so as to cool, partially condense and fractionate the same, and the condensed feed gas is supplied to a first demethanating tower as well as the partially condensed liquid is supplied to a second demethanating tower. COPYRIGHT: (C)1995,JPO ...

Verfahren zur Hochtemperatur-Kurzzeit-Destillation von Rückstandsöl

Ein Verfahren zur Hochtemperatur-Kurzzeit-Destillation von Rückstandsölen wird dahingehend verbessert, dass von dem Gas/Öldampf-Gemisch aus dem Mischwerk (1) eine kleine Rückstandsfraktion auf technisch einfache Weise gewonnen wird, in der die unerwünschten Katalysator-Schadstoffe (CCR, Ni, V, Asphaltene) weitgehend aufkonzentriert sind. Hierzu wird das in einem Mischreaktor (1) erzeugte Gas/Öldampf-Gemisch in einer Kolonne (17) soweit mit Gas oder Wasserdampf verdünnt, dass bei unter 450 DEG C eine schwer siedende schadstoffhaltige Fraktion mit einem Siedebeginn über 450 DEG C kondensiert und abgezogen wird, in der die Schadstoffe weitgehend aufkonzentriert sind. Nach einer weiteren Verbesserung wird das nicht kondensierte Produktöl aus Kolonne (17) einer Fraktionier-Kolonne (19) zugeführt, in der es in eine schadstoffarme Vakuum Gasöl sowie in eine Benzin/Gasöl-Fraktion zerlegt wird.

Verfahren zur Kälteversorgung der Tieftemperaturtrennungsstufe einer Olefinanlage

Es wird ein Verfahren zur Kältemittelversorgung einer Tieftemperaturversorgung in einer Tieftemperaturtrennungsstufe in einer Anlage zur Herstellung von Olefinen aus kohlenwasserstoffhaltigem Einsatz (Olefinanlage) beschrieben. Während der mit einem front end Deethanizer (3) nach Rohgasverdichtung (1), Vorkühlung und Trocknung (2) beginnenden Trennsequenz wird zuerst in einer Olefinfraktion mit höchstens zwei Kohlenstoffatomen und eine Olefinfraktion mit mindestens drei Kohlenstoffatomen getrennt. Die Fraktion mit mindestens drei Kohlenstoffatomen wird zur weiteren Trennsequenz für längerkettige Olefine geführt (4). Die Fraktion mit höchstens zwei Kohlenstoffatomen wird über eine zwischengeschaltete katalytische Hydrierungsstufe (5) zur Tieftemperaturtrennungsstufe (6) geführt, die drei Kondesationsstufen im Temperaturbereich von -50°C bis -100°C umfasst. Aus der Tieftemperaturtrennungsstufe werden gasförmiger Wasserstoff (9) und Methan (10) abgeleitet, während die Olefine mit höchstens ...

METHOD FOR HIGH-TEMPERATURE DISTILLATION OF RESIDUAL OIL IN A LIMITED TIME

The invention relates to a method for a high-temperature distillation of risidual oil in a limited time. The inventive method is improved by a technically simple recovery of a small residual fraction from a gas and/or oil vapour mixture produced by a mixing unit (1). Said small residual fraction contains large quantity of undesirable polluting catalytic substances (CCR, Ni, V, asphaltenes). For this purpose, the gas and/or oil vapour mixture produced by the mixing unit (1) is dissolved with gas or water vapour in a tower (17) at a temperature of 450 ~C in such a way that a high-boiling point fraction which has a high content of the pollutant substances and whose initial boiling point is higher than 450 ~C is condensed and extracted. Another improvement of the method consists in introducing a non-condensed oil produced in the tower (17) into a fractionating tower (19) where said oil is decomposed in order to produce a depressurised diesel fraction having a low content of the polluting substances ...

PROCESS FOR TREATING A STREAM OF CRACKED GAS COMING FROM A HYDROCARBON PYROLYSIS PLANT, AND ASSOCIATED PLANT

Ce procédé comporte la séparation d'un courant amont de gaz craqué partiellement condensé dans un séparateur intermédiaire (44B) pour récupérer un liquide intermédiaire (136) et un courant intermédiaire (138) de gaz craqué et l'introduction du liquide intermédiaire (140) dans une colonne intermédiaire (68) de déméthanisation. Le procédé comprend le prélèvement d'une partie du liquide intermédiaire (136) et la détente d'au moins une première fraction (194) obtenue à partir de la partie prélevée (190). Il comprend la mise en relation d'échange thermique de la première fraction détendue avec le courant intermédiaire de tête (146) issu de la colonne (68) pour condenser au moins partiellement le courant intermédiaire de tête (146). Le procédé comporte la séparation du courant intermédiaire de tête partiellement condensé dans un premier séparateur (76) de reflux pour former un courant liquide (148) introduit dans la colonne intermédiaire (68) et un courant gazeux de combustible (150).

From the carbon monoxide-rich feed stream and recovering ethylene stream and related equipment

METHOD OF PURIFYING HYDROCARBON-RICH GAS

Procédé de purification d'un gaz (1) riche en hydrocarbures, et comprenant au moins 10 ppm en volume d'hydrocarbures ayant au moins six atomes de carbone, comprenant les étapes suivantes : Etape a) Refroidissement dudit gaz à une température comprise entre -20°C et -60°C par échange thermique avec au moins un réfrigérant (3) dans un échangeur de chaleur (2) ; Etape b) Epuration en composés contenant au moins six atomes de carbone du gaz partiellement liquéfié à l'étape a) dans une colonne (5) de lavage contenant une tête (8) de colonne (5) dans son extrémité la plus haute et une cuve (7) de colonne (5) dans son extrémité la plus basse pour former, en tête (8) de colonne de lavage (5), un courant (9) gazeux contenant moins de 5 ppm en volume de composés contenant au moins six atomes de carbone et, en cuve (7) de colonne de lavage (5), un courant (6) liquide enrichi en composés contenant au moins cinq atomes de carbone ; Etape c) Condensation au moins partielle dudit courant (9) gazeux issu de l'étape b) dans un échangeur (10, 2) de chaleur pour former un courant diphasique (15) ; Etape d) Séparation dudit courant diphasique (15) issu de l'étape c) dans un pot (16) séparateur de phases à une température comprise entre -60°C et -80°C pour former un courant (17) gazeux en tête de pot et un courant (18) liquide en cuve de pot (16) ; Etape e) Utilisation du courant liquide (18) issu de l'étape d) comme reflux en tête (8) de colonne de lavage (5) ; Etape f) Condensation du courant (17) gazeux issu de l'étape d) par échange thermique dans un échangeur de chaleur (20, 2) à une température inférieure à -100°C pour former un gaz (21) liquéfié contenant moins de 5 ppm en volume de composés contenant au moins six atomes de carbone. A process for purifying a gas (1) rich in hydrocarbons, and comprising at least 10 ppm by volume of hydrocarbons having at least six carbon atoms, comprising the following steps: Step a) cooling said gas to a temperature ...

PROCESS FOR TREATING A STREAM OF CRACKED GAS COMING FROM A HYDROCARBON PYROLYSIS PLANT, AND ASSOCIATED PLANT

Process for treating a stream of cracked gas coming from a hydrocarbon pyrolysis plant, and associated plant. This process comprises the separation of an upstream partially condensed cracked gas stream in an intermediate separator (44B) so as to recover an intermediate liquid (136) and an intermediate cracked gas stream (138) and the injection of the intermediate liquid (140) into an intermediate demethanization column (68). The process includes sampling a portion of the intermediate liquid (136) and expanding at least a first fraction (194) obtained from the sampled portion (190). The process comprises bringing the expanded first fraction into heat exchange relationship with the overhead intermediate stream (146) from the column (68) in order for the overhead intermediate stream (146) to be at least partially condensed. The process includes the separation of the partially condensed overhead intermediate stream in a reflux first separator (76) so as to form a liquid stream (148) fed into ...

Method for cold supply to the low-temperature separation stage of an olefin plant

A method is described for refrigerant supply of a low-temperature separation stage in a plant for producing olefins from hydrocarbon-containing feed (olefin plant). During the separation sequence beginning with a front end deethanizer (3) downstream of raw gas compressor (1), precooler and dryer (2), first separation is performed into an olefin fraction having at most two carbon atoms and an olefin fraction having at least three carbon atoms. The fraction having at least three carbon atoms is conducted to the further separation sequence for longer-chain olefins (4). The fraction having at most two carbon atoms is conducted via a catalytic hydrogenation stage (5) connected in between to the low-temperature separation stage (6) which comprises three condensation stages in the temperature range from −50° C. to −100° C. From the low-temperature separation stage, gaseous hydrogen (9) and methane (10) are drawn off, while the olefins having at most two carbon atoms are conducted to a further ...

Method for providing refrigeration to the cryogenic separation stage of an olefin plant

Es wird ein Verfahren zur Kältemittelversorgung einer Tieftemperaturtrennungsstufe in einer Anlage zur Herstellung von Olefinen aus kohlenwasserstoffhaltigem Einsatz (Olefinanlage) beschrieben. Während der, mit einem front end Deethanizer (3) nach Rohgasverdichtung (1), Vorkühlung und Trocknung (2) beginnenden, Trennsequenz wird zuerst in eine Olefinfraktion mit höchstens zwei Kohlenstoffatomen und eine Olefinfraktion mit mindestens drei Kohlenstoffatomen getrennt. Die Fraktion mit mindestens drei Kohlenstoffatomen wird zur weiteren Trennsequenz für längerkettige Olefine geführt (4). Die Fraktion mit höchstens zwei Kohlenstoffatomen wird über eine zwischengeschaltete katalytische Hydrierungsstufe (5) zur Tieftemperaturtrennungsstufe (6) geführt, die drei Kondensationsstufen im Temperaturbereich von -50°C bis -100°C umfasst. Aus der Tieftemperaturtrennungsstufe werden gasförmiger Wasserstoff (9) und Methan (10) abgeleitet, während die Olefine mit höchstens zwei Kohlenstoffatomen zu einer weiteren Fraktionierungsstufe geführt werden (7). Die Kälteleistung für die Tieftemperaturtrennungsstufe wird durch die Verdampfung eines Teils der im front end Deethanizer entstehenden flüssigen Ethylenfraktion (8) über Wärmetauschern zur Verfügung gestellt. Die verdampfte Ethylenfraktion wird zur Rohgasverdichtung zurückgeführt (11). The invention relates to a process for the supply of a cryogenic separation stage in a plant for the production of olefins from hydrocarbon-containing feedstock (olefin plant). During the separation sequence beginning with a front end deethanizer (3) after crude gas compression (1), pre-cooling and drying (2), first an olefin fraction having at most two carbon atoms and an olefin fraction having at least three carbon atoms are separated. The fraction with at least three carbon atoms is led to the further separation sequence for longer-chain olefins (4). The fraction of at most two carbon atoms is passed through an intermediate catalytic hydrogenation ...

PRODUCING OLEFINS BY PYROLYTIC CRACKING OF REFINERY OFF-GAS

Process for the separation of C2/C3 hydrocarbons in ethylene production plants

Removal of specific hydrocarbon(s) in ethylene@ plants Removal of 2C-/3C+ hydrocarbons in ethylene plants is claimed, in which crude gas (5) contg. the hydrocarbons is compressed where a gaseous stream (44) and a condensate stream (26, 36) are produced from the precooler (31) connected to crude gas compressor (C). The 2C- (60) and 3C+ (8) hydrocarbons are removed using two columns (27, 45) operating at different pressure. The novelty is that the gaseous stream (44) from the precooler (31) is injected into the column (45) operating at higher pressure, and each condensate stream (26, 36) from the precooler (31) is injected into the column (27) operating at lower pressure.

Recovering refinery petroleum gases

A refinery petroleum gas recovery apparatus driven by waste heat comprises a water cooling system and a heat exchanging petroleum gas recovery system. Waste heat from the refining process in the form of steam is fed to ejectors 3, 4, 5, which are associated with an evaporator 1 so as to create a negative pressure therein by high speed discharge into a condenser 2. As a result of the reduced pressure within the evaporator 1 water passing therethrough is cooled to 12 - 13 DEG C. This cooled water is fed to a heat exchanger 20 for condensing a liquid petroleum gas for reuse. Thus petroleum gases, such as ethane and propane, previously flared off can now be recovered for reuse. ...

수소 함유 탄화수소 혼합물의 분리 방법, 분리 장치 및 올레핀 플랜트

... 본 발명은 증류탑(10)을 사용하여, 기본적으로 2개의 탄소 원자와 메탄으로 구성된 탄화수소 및 수소를 포함하는 수소 함유 탄화수소 혼합물(C2 마이너스)을 분리하는 방법에 관한 것이다. 탄화수소 혼합물(C2 마이너스)로 구성된 유체(a, c, e)는 제1압력 레벨에서 단계적으로 냉각되며, 이 때 제1응축수(b, d)가 상기 유체(a, c, e)로부터 분리된다. 이후에 가스 상태로 남아 있는 탄화수소 혼합물(C2 마이너스)로 구성된 유체(e)는 제1압력 레벨에서 C2 흡수기(7)로 공급되고, 그 상단에 환류액(r)이 첨가되며, 제2응축수(f)는 C2 흡수기(7)의 섬프로부터 인출되고, 주로 메탄 및 수소를 포함하는 가스 상태의 상단 스트림(g)은 C2 흡수기(7)의 상단에서 인출된다. C2 흡수기(7)의 상단에서 나온 상술된 가스 상태의 상단 스트림(g)으로 구성된 유체는 제3온도 레벨로 냉각된 후 제1압력 레벨에서 수소 분리기(8)로 이송되고, 수소 분리기의 가스 상태의 상단 스트림(g)으로 구성된 유체로부터 메탄 함량이 풍부한 제3응축수(i)가 분리되는 한편 가스 상태의 수소 함량이 풍부한 스트림(h)이 남도록 구성된다. 제1응축수(b, d)로 구성된 유체 및 제2응축수(f)로 구성된 유체는 제1압력 레벨에서 제1압력 레벨 이하의 제2압력 레벨로 감압된 후 제2압력 레벨에서 작동되는 증류탑(10)으로 공급된다. 수소 분리기(8)에서 C2 흡수기(7)로부터 나온 가스 상태의 상단 스트림(g)으로부터 분리된 제3응축수(i)로 구성된 유체는 환류액(r)으로 사용되어 C2 흡수기(7)의 상단에 첨가되는데, 수소 분리기에서 단지 중력에 의해서만 C2 흡수기로 이송된다. 본 발명은 또한 이에 관련된 분리 유닛 및 올레핀 기구에 관한 것이다.

Process for treating a stream of cracked gas coming from a hydrocarbon pyrolysis plant, and associated plant

Process for treating a stream of cracked gas coming from a hydrocarbon pyrolysis plant, and associated plant. This process comprises the separation of an upstream partially condensed cracked gas stream in an intermediate separator (44B) so as to recover an intermediate liquid (136) and an intermediate cracked gas stream (138) and the injection of the intermediate liquid (140) into an intermediate demethanization column (68). The process includes sampling a portion of the intermediate liquid (136) and expanding at least a first fraction (194) obtained from the sampled portion (190). The process comprises bringing the expanded first fraction into heat exchange relationship with the overhead intermediate stream (146) from the column (68) in order for the overhead intermediate stream (146) to be at least partially condensed. The process includes the separation of the partially condensed overhead intermediate stream in a reflux first separator (76) so as to form a liquid stream (148) fed into ...

Method for purifying a gas rich in hydrocarbons

Process for purifying a gas (1) rich in hydrocarbons and comprising at least 10 ppm by volume of hydrocarbons having at least six carbon atoms, comprising the following steps: Step a) Cooling said gas to a temperature between -20°C and -60°C by heat exchange with at least one coolant (3) in a heat exchanger (2); Step b) Scrubbing of compounds containing at least six carbon atoms from the gas partially liquefied in step a) in a washing column (5) containing a column (5) overhead (8) in its highest end and a column (5) bottom (7) in its lowest end in order to form, as washing column (5) overhead (8), a gas stream (9) containing less than 5 ppm by volume of compounds containing at least six carbon atoms and, as washing column (5) bottoms (7), a liquid stream (6) enriched in compounds containing at least five carbon atoms; Step c) At least partial condensation of said gas stream (9) resulting from step b) in a heat exchanger (10, 2) in order to form a two-phase stream (15); Step d) Separating ...

Method for purifying a gas rich in hydrocarbons

Process for purifying a gas (1) rich in hydrocarbons and comprising at least 10 ppm by volume of hydrocarbons having at least six carbon atoms, comprising the following steps: Step a) Cooling said gas to a temperature between -20°C and -60°C by heat exchange with at least one coolant (3) in a heat exchanger (2); Step b) Scrubbing of compounds containing at least six carbon atoms from the gas partially liquefied in step a) in a washing column (5) containing a column (5) overhead (8) in its highest end and a column (5) bottom (7) in its lowest end in order to form, as washing column (5) overhead (8), a gas stream (9) containing less than 5 ppm by volume of compounds containing at least six carbon atoms and, as washing column (5) bottoms (7), a liquid stream (6) enriched in compounds containing at least five carbon atoms; Step c) At least partial condensation of said gas stream (9) resulting from step b) in a heat exchanger (10, 2) in order to form a two-phase stream (15); Step d) Separating ...

Cat cracker gas plant process for increased olefins recovery

The invention relates to a new process for more efficient separation and recovery of light olefins such as ethylene and propylene from a fluid catalytic cracking unit. The new process invention for recovering olefins from a mixture of cracked hydrocarbons from a fluid catalytic cracker comprises the steps of: (a) providing a mixture of cracked hydrocarbons including methane, ethylene, ethane, propylene, propane, butylene, butane and heavier hydrocarbons such as naphtha produced in a fluid catalytic cracker; (b) separating said mixture into (i) a first stream comprising substantially all of said ethane, ethylene, and methane and a major portion of said propane and propylene and (ii) a second stream comprising a portion of said butylene and butane, and a major portion of said heavier hydrocarbons; and (c) processing said first stream to recover the ethylene and propylene therefrom, and the details of such process described herein.

PROCESS FOR THE RECOVERY OF CRUDE

A method for the production of stabilized crude oil, the method comprising the steps of: providing a stream of crude oil; injecting steam into said stream and so stripping C3− from said stream; providing a gas stream; extracting C4+ from the gas stream, and so; producing a stream from the extracted C4+; co-mingling the stripped stream with the C4+ stream, and so; producing a stream of stabilized crude oil. 1. A method for the production of crude oil , the method comprising the steps of:providing a stream of crude oil;injecting steam into said stream and so stripping C3− from said stream;providing a gas stream;extracting C4+ from the gas stream, and so;producing a stream from the extracted C4+;co-mingling the stripped stream with the C4+ stream.2. The method according to wherein the extracting step comprises the step of condensing the C4+ from the gas stream.3. The method of wherein the condensing step comprises applying dew-point control to the gas stream to condenses the C4+ from the gas stream.4. The method according to further including the step of introducing the crude stream to a steam stripping column claim 1 , within which injecting of steam to the crude stream is effected.5. The method according to further including claim 1 , after the co-mingling step claim 1 , the step of separating vapour and liquid from the co-mingled stream to produce a stream of stabilized crude oil.6. The method according to wherein an offgas rate for vapour separated from the stabilized crude oil stream is maintained at a preset value.7. A system for the production of stabilized crude oil comprising:a steam injection station arranged to receive a stream of unstabilised crude oil, said station arranged to subject said stream to an injection of steam;said steam injection station including a first outflow to deliver a stripped stream of crude to a stabilizer section and a second outflow to deliver a flow of gas to a condensation station;said condensation station arranged to condense the ...

Cyclonic Cooling System

Fractionation, the process used by refineries to break down carbon chains of petroleum compounds so that the desired carbon compound can be achieved. This process typically involves high heat, distillation, re-boiling, and energy intensive cooling processes. This application discloses an invention that will condense vapor produced by a pyrolysis reactor. This system uses one standard cyclone; three cascading cyclones with internal cyclonic rotation fins that force incoming vapor to maintain a fixed amount of rotation regardless of the vapor's velocity, heat sinks that increase condensation, reversing fins that force gases to reverse direction inside the cyclone decreasing vapor velocity to increase heat loss; a main collection tank that allows for the controlling of the fuel flash point; a compact low temperature coil cooler that uses 100 percent of the cooling surface that allows for the production of higher quality fuel; and, bubblers/scrubbers that produce back pressure into the pyrolysis reactor.

STAGE AND SYSTEM FOR COMPRESSING CRACKED GAS

A compression stage for the compression of cracked gas, the compression stage comprising a liquid separating means for separating liquid components from gaseous components of a cracked gas, a compressor connected to the liquid separating means, a gas cooling means connected to the compressor for cooling the compressed gas from the compressor, wherein the gas cooling means are cooled by a first cooling fluid from the cooling fluid source. The stage further comprises gas precooling means connected to the liquid separating means cracked gas, having an inlet for receiving the cracked gas. 1. A compression stage for the compression of cracked gas , the compression stage comprising:a liquid separating means for separating liquid components from gaseous components of a cracked gas;a compressor connected to the liquid separating means;a gas cooling means connected to the compressor for cooling the compressed gas from the compressor, wherein the gas cooling means are cooled by a first cooling fluid from the cooling fluid source;the stage further comprisinggas precooling means connected to the liquid separating means, having an inlet for receiving the cracked gas.2. The stage according to claim 1 , whereinthe gas precooling means comprises a heat exchanging means and an absorption cooling means, whereinthe heat exchanging means is cooled by a second cooling fluid from the absorption cooling means, whereinthe absorption cooling means is arranged for generating the second cooling fluid using first cooling fluid from the cooling fluid source and hot water from a heating fluid source.3. The stage according to claim 1 , whereinthe first cooling fluid for the absorption cooling means is supplied from a primary gas cooler of the gas cooling means of the stage, and whereinthe first cooling fluid from the absorption cooling means is supplied to the secondary gas cooler.4. The stage according to claim 1 , whereinthe first cooling fluid for the absorption cooling means of the stage is ...

Process and plant for separation of a hydrocarbon mixture

The invention relates to a process for separating a component mixture (K) comprising hydrogen, methane, hydrocarbons having two carbon atoms and hydrocarbons having three or more carbon atoms, wherein in a deethanization at least a portion of the component mixture (K) is subjected to a first partial condensation by cooling from a first temperature level to a second temperature level at a first pressure level to obtain a first gas fraction (G) and a first liquid fraction (C), at least a portion of the first gas fraction (G) is subjected to a second partial condensation by cooling from the second temperature level to a third temperature level at the first pressure level to obtain a second gas fraction (G) and a second liquid fraction (C), and at least a portion of the first liquid fraction (C) and at least a portion of the second liquid fraction (C) are subjected to a rectification to obtain a third gas fraction (G) and a third liquid fraction (C). The first liquid fraction (C) or its part subjected to the rectification and the second liquid fraction (C) or its part subjected to the rectification are expanded to a second pressure level and the rectification is carried out at the second pressure level, the first pressure level being 25 to 35 bar and the second pressure level being 14 to 17 bar. An overhead gas formed during the rectification is cooled to −25 to −35° C. and partially condensed, wherein a condensed portion of the overhead gas is used partially or completely as a reflux in the rectification and an uncondensed portion of the overhead gas is provided partially or completely as the third gas fraction (G). The present invention likewise provides a corresponding plant (). 1. Process for separating a component mixture (K) comprising hydrogen , methane , hydrocarbons having two carbon atoms and hydrocarbons having three or more carbon atoms , comprising a deethanization and a demethanization subsequent to the deethanization , wherein{'b': 1', '1, 'in the ...

GAS CONDITIONING PROCESS AND SYSTEM FOR EXTRACTING A CONDENSABLE VAPOUR FROM A SUPPLIED GAS

A process for extracting a condensable vapour from a supplied gas, comprising the steps of: i) condensing the condensable vapour by cooling the supplied gas at a condensing surface, such that the supplied gas is divided into at least one condensed fraction and a product gas; while ii) removing the at least one condensed fraction from the condensing surface by mechanical scraping means. 2. The process as claimed in claim 1 , wherein the supplied gas is a product of coal gasification or pyrolysis of a carbonaceous feed ; and wherein the condensable vapor comprises hydrocarbon which has a non-gaseous phase at a standard ambient temperature of 25° C. and pressure of 1 atm.3. The process as claimed in claim 2 , wherein the supplied gas comprises methane; and wherein the condensable vapor comprises tars.4. The process as claimed in claim 1 , further comprising a step of controlling supplied gas temperature with a supplied gas heat exchanger prior to the step of cooling the supplied gas; wherein the supplied gas prior to the cooling step is substantially free from the at least one condensed fraction.5. The process as claimed in claim 1 , further comprising a step of filtering supplied gas with a filter prior to the step of cooling said supplied gas.61. The process as claimed in claim 1 , further comprising a step of scrubbing the product gas with a scrubber; wherein the scrubbed product gas is subsequently dried using a gas dryer.7. The process as claimed in claim 1 , wherein step ii) is repeated at further condensing surfaces using the product gas of the previous step as an input gas claim 1 , and steps c)-d) are repeated at further locations using a condensed fraction a further condensing surfaces and/or the heated condensed fraction of the previous step as input material claim 1 ,8. A gas conditioning system for carrying out the process as claimed in claim 1 , comprising at least one condensing unit claim 1 , wherein a thermally controlled conveying means is provided ...

HYDROCARBON GAS RECOVERY METHODS

A method of recovery of rich gas where the rich gas is a hydrocarbon gas comprising less than 50 mole % methane is disclosed. The method comprises the steps of gathering the low pressure gas, compressing the gathered gas, cooling the compressed gas in a condenser so that a portion of the compressed gas condenses to form a liquefied gas and liquefied gas vapour in the condenser, and discharging the liquefied gas and liquefied gas vapour from the condenser, in which the cooling of the compressed gas is performed using at least one heat exchanger (). 124-. (canceled)25. A method of recovery of rich gas , the method comprising:gathering the rich gas, wherein the rich gas is a hydrocarbon gas comprising less than 50 mole % methane;compressing the gathered gas;cooling the compressed gas in a condenser so that a portion of the compressed gas condenses to form a liquefied gas and liquefied gas vapour in the condenser, wherein the cooling of the compressed gas is performed using at least one heat exchanger; anddischarging the liquefied gas and liquefied gas vapour from the condenser26. The method of claim 25 , wherein the rich gas has a gauge pressure of less than or equal to 1379.0 kPa (200 psi).27. The method of claim 25 , wherein the liquefied gas and liquefied gas vapour is discharged into one or more storage means.28. The method of claim 27 , wherein the at least one storage means is a storage tank.29. The method of claim 25 , wherein the at least one heat exchanger is a fan-cooled condenser.30. The method of claim 25 , wherein the rich gas is gathered from a source comprising a two-phase separator claim 25 , a treater unit claim 25 , a vapour recovery tower claim 25 , an oil storage tank claim 25 , or a combination thereof.31. The method of claim 25 , wherein the step of compressing the gas is performed using at least one compression pump.32. The method of claim 31 , wherein:each compression pump is controlled by a control unit,the control unit comprises a central ...

Method for purifying a gas rich in hydrocarbons

A process for the purification of a gas rich in hydrocarbons and comprising at least 10 ppm by volume of hydrocarbons having at least six carbon atoms nitrogen.

METHOD FOR FRACTIONATING A STREAM OF CRACKED GAS, USING AN INTERMEDIATE RECIRCULATION CURRENT, AND RELATED PLANT

This method comprises: 1. A method for fractionating a stream of cracked gas from a hydrocarbon pyrolysis plant to obtain an ethylene-rich cut and a C hydrocarbon-lean fuel stream , the method comprising:compressing the stream of raw cracked gas in at least one compressor a cooling and compression stage to form a compressed cracked gas stream;upstream cooling and partial condensing, in at least one upstream heat exchanger, of an upstream stream of cracked gas, obtained from the compressed cracked gas stream, and separation of an upstream liquid in at least one upstream balloon to form an intermediate stream of cracked gas pre-cooled at first temperature;intermediate cooling and partial condensing of the intermediate stream of cracked gas in an intermediate heat exchanger and separation of an intermediate liquid in an intermediate separating balloon to form a downstream stream of cracked gas cooled to a second temperature lower than the first temperature;downstream cooling and partial condensing of the downstream stream of cracked gas in at least one downstream heat exchanger to a third temperature lower than the second temperature;introducing of the downstream stream of partially condensed cracked gas from the downstream heat exchanger in a downstream separator;{'sub': 2', '2, 'sup': +', '+, 'recovering, at the head of the downstream separator a gas stream of high-pressure fuel, lean in C hydrocarbons, and recovering, at the bottom of the downstream separator, a downstream liquid, rich in C hydrocarbons;'}passing of the stream of high-pressure fuel through the downstream exchanger and the intermediate exchanger to form a heated high-pressure fuel stream;expanding of the heated high-pressure fuel stream in at least one first dynamic expansion device to obtain a stream of partially expanded fuel;heating of the stream of partially expanded fuel through the downstream exchanger and the intermediate exchanger;treating of at least one liquid stream obtained during the ...

NOx Removal Method

The invention relates to mixtures comprising molecular hydrogen, hydrocarbons, and nitrogen oxides; to processes for removing at least a portion of the nitrogen oxides therefrom; to equipment useful in such processes; and to the use of such hydrocarbons for, e.g., chemical manufacturing.

PROCESS AND SYSTEM FOR CRACKING A HYDROCARBON FEED

A process for hydrocracking a hydrocarbon feed is provided. The process comprises hydrocracking the hydrocarbon feed to produce a first hydrocracking product stream, separating the first hydrocracking product stream to form a gas stream and a liquid stream, hydrocracking the liquid stream to produce a second hydrocracking product stream, separating the second hydrocracking product stream to form a first light stream and a first heavy stream comprising benzene, toluene, xylene, C hydrocarbon, or a combination comprising at least one of the foregoing, purifying the gas stream to form a purified gas stream, and separating the purified gas stream to form at least two of a hydrogen stream, Cstream, Cstream, Cstream, Cstream, C stream, or a combination comprising at least one of the foregoing. 1. A process for hydrocracking a hydrocarbon feed , comprising:hydrocracking the hydrocarbon feed to produce a first hydrocracking product stream;separating the first hydrocracking product stream to form a gas stream and a liquid stream;hydrocracking the liquid stream to produce a second hydrocracking product stream;{'sub': '9+', 'separating the second hydrocracking product stream to form a first light stream and a first heavy stream comprising benzene, toluene, xylene, C hydrocarbon, or a combination comprising at least one of the foregoing;'}purifying the gas stream to form a purified gas stream; and{'sub': 1', '2', '3', '4', '5+, 'separating the purified gas stream to form at least two of a hydrogen stream, Cstream, Cstream, Cstream, Cstream, C stream, or a combination comprising at least one of the foregoing.'}2. The process of claim 1 , wherein the gas stream comprises hydrogen and C-Chydrocarbons and the liquid stream comprises C hydrocarbons.3. The process of claim 1 , wherein the second hydrocracking product stream comprises a C hydrocarbon claim 1 , benzene claim 1 , toluene claim 1 , xylene claim 1 , C hydrocarbon claim 1 , or a combination comprising at least one of the ...

Method for quenching pyrolysis product

A method for quenching a pyrolysis product, including: supplying a discharge stream from a liquid decomposition furnace to a first quench tower; supplying an upper discharge stream from the first quench tower to a second quench tower; supplying a discharge stream from a first gas decomposition furnace to the second quench tower; and supplying a discharge stream from a second gas decomposition furnace to the second quench tower.

CYROGENIC SEPARATION OF LIGHT OLEFINS AND METHANE FROM SYNGAS

In accordance with the present invention, disclosed herein is a method comprising the steps for separating syngas and methane from C2-C4 hydrocarbons. Also disclosed herein, are systems utilized to separate syngas and methane from C2-C4 hydrocarbons. 1. A method comprising the steps of:a) providing a first product stream comprising syngas, methane, and C2-C4 hydrocarbons, wherein the first product stream has a first temperature;b) lowering the first temperature of the first product stream to a second temperature in a first heat exchange unit;c) separating at least a portion of the syngas from the first product stream in a cryogenic separation unit, thereby producing a second product stream comprising methane and C2-C4 hydrocarbons;d) separating at least a portion of the methane in the second product stream in a demethanizer, thereby producing a third product stream comprising C2-C4 hydrocarbons;e) recycling the at least a portion of the separated syngas to a Fischer-Tropsch reactor; andf) recycling the at least a portion of the separated methane to a syngas generation unit.2. The method of , further comprises the step of separating at least a portion of Hfrom the at least a portion of the separated syngas in a methane wash unit , thereby producing a methane wash product comprising methane and carbon monoxide , wherein at least a portion of separated methane in the method of is used to wash the at least a portion of the separated syngas in the methane wash unit.3. The method of claim 1 , wherein the separated syngas has a third temperature claim 1 ,wherein the method further comprises the steps of:{'sub': '2', 'lowering the third temperature of at least a portion of the separated syngas to a fourth temperature via a Nrefrigeration loop and a second heat exchange unit; and'}recycling energy from the portion of the separated syngas with the fourth temperature to the first product stream comprising syngas, methane, and C2-C4 hydrocarbons via the first heat exchange unit ...

Enhanced olefin recovery method

An enhanced method is disclosed for recovering olefins from a cracking furnace effluent stream in an olefins plant. In accordance with this method, a liquid hydrocarbon stream, preferably obtained from the compressor area drier liquids and/or from the deethanizer or depropanizer, is injected into the reaction effluent stream to condition the reaction effluent stream for enhanced condensation against propylene refrigeration. Also disclosed is an olefins plant utilizing liquid hydrocarbon injection and an improvement to existing olefins recovery process technology using liquid hydrocarbon injection for vapor stream conditioning.

Cat cracker gas plant process for increased olefins recovery

The invention relates to a new process for more efficient separation and recovery of light olefins such as ethylene and propylene from a fluid catalytic cracking unit. The new process invention for recovering olefins from a mixture of cracked hydrocarbons from a fluid catalytic cracker comprises the steps of: (a) providing a mixture of cracked hydrocarbons including methane, ethylene, ethane, propylene, propane, butylene, butane and heavier hydrocarbons such as naphtha produced in a fluid catalytic cracker; (b) separating said mixture into (i) a first stream comprising substantially all of said ethane, ethylene, and methane and a major portion of said propane and propylene and (ii) a second stream comprising a portion of said butylene and butane, and a major portion of said heavier hydrocarbons; and (c) processing said first stream to recover the ethylene and propylene therefrom, and the details of such process described herein.

Cyclonic cooling system

Fractionation, the process used by refineries to break down carbon chains of petroleum compounds so that the desired carbon compound can be achieved. This process typically involves high heat, distillation, re-boiling, and energy intensive cooling processes. This application discloses an invention that will condense vapor produced by a pyrolysis reactor. This system uses one standard cyclone; three cascading cyclones with internal cyclonic rotation fins that force incoming vapor to maintain a fixed amount of rotation regardless of the vapor's velocity, heat sinks that increase condensation, reversing fins that force gases to reverse direction inside the cyclone decreasing vapor velocity to increase heat loss; a main collection tank that allows for the controlling of the fuel flash point; a compact low temperature coil cooler that uses 100 percent of the cooling surface that allows for the production of higher quality fuel; and, bubblers/scrubbers that produce back pressure into the pyrolysis reactor.

Precooling for ethylene recovery in dual demethanizer fractionation systems

Ethylene-containing feed gas to a cryogenic ethylene recovery system is cooled and condensed, prior to fractionation, by an improved method which utilizes a combination of one or more partial condensers followed by one or more dephlegmators. The improved method simplifies heat exchange equipment and reduces capital cost, and is particularly suited for processing a pressurized precooled feed gas from ethane cracking which contains less than about 1 mole % of propane plus propylene.

Verfahren zur Kälteversorgung der Tieftemperaturtrennungsstufe einer Olefinanlage

Es wird ein Verfahren zur Kältemittelversorgung einer Tieftemperaturtrennungsstufe in einer Anlage zur Herstellung von Olefinen aus kohlenwasserstoffhaltigem Einsatz (Olefinanlage) beschrieben. Während der, mit einem front end Deethanizer (3) nach Rohgasverdichtung (1), Vorkühlung und Trocknung (2) beginnenden, Trennsequenz wird zuerst in eine Olefinfraktion mit höchstens zwei Kohlenstoffatomen und eine Olefinfraktion mit mindestens drei Kohlenstoffatomen getrennt. Die Fraktion mit mindestens drei Kohlenstoffatomen wird zur weiteren Trennsequenz für längerkettige Olefine geführt (4). Die Fraktion mit höchstens zwei Kohlenstoffatomen wird über eine zwischengeschaltete katalytische Hydrierungsstufe (5) zur Tieftemperaturtrennungsstufe (6) geführt, die drei Kondensationsstufen im Temperaturbereich von -50°C bis -100°C umfasst. Aus der Tieftemperaturtrennungsstufe werden gasförmiger Wasserstoff (9) und Methan (10) abgeleitet, während die Olefine mit höchstens zwei Kohlenstoffatomen zu einer weiteren Fraktionierungsstufe geführt werden (7). Die Kälteleistung für die Tieftemperaturtrennungsstufe wird durch die Verdampfung eines Teils der im front end Deethanizer entstehenden flüssigen Ethylenfraktion (8) über Wärmetauschern zur Verfügung gestellt. Die verdampfte Ethylenfraktion wird zur Rohgasverdichtung zurückgeführt (11).

Precooling for ethylene recovery in dual demethanizer fractionation systems

Olefin recovery method

Olefin recovery from hydrocarbon streams.

Improved recovery of olefins

올레핀 플랜트에서 분해노 유출물 스트림으로 부터 올레핀을 회수하기 위한 개선된 방법이 개시되어 있다. 본 방법에 따라, 바람직하게는 압축기 부위의 건조기 액체 및/또는 탈 에탄기 또는 탈 프로판 기로 부터 수득한 액체 탄화수소 스트림을 반응 유출물 스트림에 주입하여 프로필렌 냉각에 의한 개선된 응축을 위해 반응 유출물 스트림을 조절한다. An improved process for recovering olefins from cracking furnace effluent streams in an olefin plant is disclosed. According to the method, the reaction effluent stream is preferably injected into the reaction effluent stream by pouring a liquid hydrocarbon stream from the dryer liquid and / or the deethane or depropane groups at the compressor site to the reaction effluent stream. Adjust 또한 액체 탄화수소 주입을 사용하는 올레핀 프랜트 및 증기 스트림 조절을 위해 액체 탄화수소 주입을 사용하는 현존의 올레핀 회수 공정 기술의 기선 등이 기재되어 있다. Also described are olefin plants using liquid hydrocarbon injection and baselines of existing olefin recovery process techniques using liquid hydrocarbon injection for vapor stream control.

Olefin recovery method

An enhanced method is disclosed for recovering olefins from a cracking furnace effluent stream in an olefins plant. In accordance with this method, a liquid hydrocarbon stream, preferably obtained from the compressor area drier liquids and/or from the deethanizer or depropanizer, is injected into the reaction effluent stream to condition the reaction effluent stream for enhanced condensation against propylene refrigeration. Also disclosed is an olefins plant utilizing liquid hydrocarbon injection and an improvement to existing olefins recovery process technology using liquid hydrocarbon injection for vapor stream conditioning.

개선된 올레핀의 회수방법

올레핀 플랜트에서 분해노 유출물 스트림으로부터 올레핀을 회수하기 위한 개선된 방법이 개시되어 있다. 본 방법에 따라, 바람직하게는 압축기 부위의 건조기 액체 및/또는 탈 에탄기 또는 탈 프로판기로부터 수득한 액체 탄하수소 스트림을 반응 유출물 스트림에 주입하여 프로필렌 냉각에 의한 개선된 응축을 위해 반응 유출물 스트림을 조절한다. 또한 액체 탄화수소 주입을 사용하는 올레핀 플랜트 및 증기 스트림 조절을 위해 액체 탄화수소 주입을 사용하는 현존의 올레핀 회수 공정 기술의 개선 등이 기재되어 있다.

Process for recovering ethylene comprising a precooling step

Process for improving propylene recovery from FCC recovery unit

The present subject matter relates generally to processes for propylene recovery. More specifically, the present subject matter relates to processes for enhanced recovery of propylene and liquid petroleum gas (LPG) from the fuel gas produced in fluid catalytic cracking (FCC) units by minimizing the light ends and propylene in the unstabilized gasoline which is used as lean oil for the primary absorber of the FCC gas concentration unit.

Method for improving propylene recovery from fluid catalytic cracker unit

The present invention relates to a method for treating a cracked stream stemming from a fluid catalytic cracker unit (FCCU) in order to improve propylene recovery. The present invention also relates to the corresponding installation to implement the method.

Low pressure chilling train for olefin plants

A method of processing a cracked gas feedstream containing hydrogen and C 1 to C 6 and heavier hydrocarbons is described using a relatively low pressure as compared to conventional cryogenic separation processes. At pressures below 27 bars, the feedstream is dried and cooled in a series of steps to initially separate out essentially all of the C 6 and heavier hydrocarbons forming a vapor stream containing the hydrogen, the C 1 to C 3 hydrocarbons and at least some of the C 4 and C 5 hydrocarbons. The C 4 and C 5 components act as an absorption liquid to lower the light ends partial pressure permitting the condensation of C 2 and C 3 components at higher temperature levels and permitting the operation at lower pressures. The vapor stream is then further cooled and separated in another series of steps and processed in a demethanizer column in a manner to provide a high pressure hydrogen and methane overhead product and a high recovery of C 2 and C 3 components in the bottoms.

Low pressure olefin recovery process

A low-pressure olefins recovery process and plant are described. The feed gas 300 is compressed 302, 304 and distilled 310 at a primary distillation pressure. The overhead stream 312 is chilled 318 at a pressure less than 30 kg/cm 2 (430 psia) to partially condense the overheads. The primary distillation tower 310 is refluxed with at least a portion of the condensate 320. The overhead vapor is further chilled 318 and partially condensed and the condensate 322 is fed to a demethanizer 324. The remaining vapor 326 is cooled in a cold section 328 and the resultant liquid is phase-separated 330 and expanded 331, 334 to provide refrigeration for the cold ssection. The expanded vapor 332 from the cold section is recycled to the process gas compressor. The bottoms streams 338, 342 from the primary distillation zone and the demethanizer are fractionated into respective streams consisting essentially of ethylene 356, ethane 358, propylene 364, propane 366, C 4 's 346, and C 5+ 348.

使用中间再循环流分馏裂化气体流的方法及相关设备

本发明涉及一种包括以下步骤的方法：?在下游冷却步骤的上游，由在上游冷却和/或中间冷却步骤时获得的液体(112，128)形成膨胀的中间再循环流(170)；?使中间再循环流(170)至少在上游热交换器(42)中流通以冷却上游裂化气体流(102)；?将再加热的中间再循环流(170)再引入到冷却与压缩级(24)的至少一个压缩器(36，38)的上游的粗裂化气体(20)中。该上游、中间和下游冷却步骤的进行没有上游裂化气体流(102)、中间裂化气体流(114)和下游裂化气体流(140)与外部制冷循环如乙烯循环的各自的热交换。

Method for fractionating a stream of cracked gas using an intermediate recirculation stream, and related plant

The provided method includes the following steps: forming an expanded intermediate recirculation current (170) from a liquid (112, 128) obtained during an upstream cooling step and/or intermediate cooling step, upstream from the downstream cooling step; circulating the intermediate recirculation stream (170) at least through an upstream heat exchanger (42) in order to cool an upstream stream of cracked gas (102); injecting the reheated intermediate recirculation stream (170) back into a raw cracked gas (20) upstream from at least one compressor (36, 38) of a cooling and compression stage (24). The upstream, intermediate and downstream cooling steps are performed with no heat exchange, respectively, of an upstream stream of cracked gas (102), an intermediate stream of cracked gas (114) and a downstream stream of cracked gas (140) with an external cooling cycle, such as an ethylene cycle.

Procédé de fractionnement d'un courant de gaz craqué, mettant en oeuvre un courant de recycle intermédiaire, et installation associée

Ce procédé comprend les étapes suivantes : - formation d'un courant (170) de recycle intermédiaire détendu à partir d'un liquide (112, 128) obtenu lors d'une étape de refroidissement amont, ou/et de refroidissement intermédiaire, en amont d'une l'étape de refroidissement aval; - circulation du courant de recycle intermédiaire (170) au moins dans un échangeur thermique amont (42) pour refroidir un courant amont de gaz craqué (102); - réintroduction du courant de recycle intermédiaire (170) réchauffé dans un gaz craqué brut (20) en amont d'au moins un compresseur (36, 38) d'un étage de refroidissement et de compression (24). Les étapes de refroidissement amont, intermédiaire et aval s'effectue sans échange thermique respectivement d'un courant amont de gaz craqué (102), d'un courant intermédiaire de gaz craqué (114) et d'un courant aval de gaz craqué (140) avec un cycle de réfrigération externe, tel qu'un cycle à l'éthylène.

Cat cracker gas plant process for increased olefins recovery

The invention relates to a new process for more efficient separation and recovery of light olefins such as ethylene and propylene from a fluid catalytic cracking unit. The new process invention for recovering olefins from a mixture of cracked hydrocarbons from a fluid catalytic cracker comprises the steps of: (a) providing a mixture of cracked hydrocarbons including methane, ethylene, ethane, propylene, propane, butylene, butane and heavier hydrocarbons such as naphtha produced in a fluid catalytic cracker; (b) separating said mixture into (i) a first stream comprising substantially all of said ethane, ethylene, and methane and a major portion of said propane and propylene and (ii) a second stream comprising a portion of said butylene and butane, and a major portion of said heavier hydrocarbons; and (c) processing said first stream to recover the ethylene and propylene therefrom, and the details of such process described herein.

Process for separating and recovering NGLs from hydrocarbon streams

This process comprises using unconventional processing of hydrocarbons, e.g. natural gas, for recovering C2+ and NGL hydrocarbons that meet pipeline specifications, without the core high capital cost requirement of a demethanizer column, which is central to and required by almost 100% of the world's current NGL recovery technologies. It can operate in Ethane Extraction or Ethane Rejection modes. The process uses only heat exchangers, compression and simple separation vessels to achieve specification ready NGL. The process utilizes cooling the natural gas, expansion cooling, separating the gas and liquid streams, recycling the cooled streams to exchange heat and recycling selective composition bearing streams to achieve selective extraction of hydrocarbons, in this instance being NGLs. The compactness and utility of this process makes it feasible in offshore applications as well as to implementation to retrofit/revamp or unload existing NGL facilities. Many disparate processes and derivatives are anticipated for its use.

Method for improving propylene recovery from fluid catalytic cracker unit

The present invention relates to a method for treating a cracked stream stemming from a fluid catalytic cracker unit (FCCU) in order to improve propylene recovery. The present invention also relates to the corresponding installation to implement the method.

用于改进fcc回收单元的丙烯回收率的方法

本主题大体上涉及丙烯回收方法。更具体地，本主题涉及通过将用作FCC气体浓缩单元的初级吸收塔的贫油的未稳定汽油中的轻馏分和丙烯减至最少而增强从流体催化裂化(FCC)单元中生成的燃料气中回收丙烯和液化石油气(LPG)的方法。

Low pressure olefin recovery process

A low-pressure olefins recovery process and plant are described. The feed gas is compressed and distilled at a primary distillation pressure. The overhead stream is chilled at a pressure less than 30 kg/cm2 (430 psia) to partially condense the overheads. The primary distillation tower is refluxed with at least a portion of the condensate. The overhead vapor is further chilled and partially condensed and the condensate is fed to a demethanizer. The remaining vapor is cooled in a cold section and the resultant liquid is phase-separated and expanded to provide refrigeration for the cold section. The expanded vapor from the cold section is recycled to the process gas compressor. The bottoms streams from the primary distillation zone and the demethanizer are fractionated into respective streams consisting essentially of ethylene, ethane, propylene, propane, C4's, and C5+.

Low pressure olefin recovery process

A low-pressure olefins recovery process and plant are described. The feed gas is compressed and distilled at a primary distillation pressure. The overhead stream is chilled at a pressure less than 30 kg/cm2 (430 psia) to partially condense the overheads. The primary distillation tower is refluxed with at least a portion of the condensate. The overhead vapor is further chilled and partially condensed and the condensate is fed to a demethanizer. The remaining vapor is cooled in a cold section and the resultant liquid is phase-separated and expanded to provide refrigeration for the cold section. The expanded vapor from the cold section is recycled to the process gas compressor. The bottoms streams from the primary distillation zone and the demethanizer are fractionated into respective streams consisting essentially of ethylene, ethane, propylene, propane, C4's, and C5+.

Low pressure olefin recovery process

A low-pressure olefins recovery process and plant are described. The feed gas 300 is compressed 302, 304 and distilled 310 at a primary distillation pressure. The overhead stream 312 is chilled 318 at a pressure less than 30 kg/cm 2 (430 psia) to partially condense the overheads. The primary distillation tower 310 is refluxed with at least a portion of the condensate 320 . The overhead vapor is further chilled 318 and partially condensed and the condensate 322 is fed to a demethanizer 324 . The remaining vapor 326 is cooled in a cold section 328 and the resultant liquid is phase-separated 330 and expanded 331, 334 to provide refrigeration for the cold section. The expanded vapor 332 from the cold section is recycled to the process gas compressor. The bottoms streams 338, 342 from the primary distillation zone and the demethanizer are fractionated into respective streams consisting essentially of ethylene 356 , ethane 358 , propylene 364 , propane 366 , C 4 's 346 , and C 5+ 348.

用于分离烃混合物的方法和设备

本发明涉及一种用于分离包含氢气、甲烷、具有两个碳原子的烃类和具有三个或更多个碳原子的烃类的组分混合物的方法，其中在脱乙烷中，在第一压力水平下，通过从第一温度水平冷却至第二温度水平，使至少一部分组分混合物经历第一部分冷凝，以获得第一气体馏分和第一液体馏分；在第一压力水平下，通过从第二温度水平冷却至第三温度水平，使至少一部分气体馏分经历第二部分冷凝，以获得第二气体馏分和第二液体馏分；且使至少一部分第一液体馏分和至少一部分第二液体馏分经历精馏以获得第三气体馏分和第三液体馏分。将经历精馏的第一液体馏分或其部分和经历精馏的第二液体馏分或其部分减压至第二压力水平，并在第二压力水平下进行精馏。

旋风凝结和冷却系统

提供一种用于处理可重复使用燃料的装置，包括具有第一配置的第一类型旋风冷却器。该装置还设置有一个或多个第二类型旋风冷却器，其中每一个或多个第二类型旋风冷却器具有与相应的其他一个或多个第二类型旋风冷却器基本相同的第二配置，其中第二配置与第一配置不同。该装置还可以设置有空气冷却热交换器、盘管凝结器和一个或多个起泡器。第一类型旋风冷却器和一个或多个第二类型旋风冷却器连接。一个或多个第二类型旋风冷却器中的一个连接到空气冷却热交换器。空气冷却热交换器连接到盘管凝结器。盘管凝结器连接到一个或多个起泡器。

低压烯烃回收方法

描述了低压烯烃回收方法和设备。原料气300在初级蒸馏压下，经过压缩302、304并经过蒸馏310。塔顶流312在低于30kg/cm 2 (430psia)的压力下冷却318，以使塔顶流部分冷凝。初级蒸馏塔310采用至少部分冷凝物320进行回流。塔顶蒸汽进一步冷却318并部分冷凝，冷凝物322供给脱甲烷塔324。剩余的蒸汽326在冷区328中冷却，得到的液体进行相分离330并膨胀331和334，从而提供冷区所需的冷量。来自冷区的膨胀的蒸汽332重新循环进入工艺气体压缩器。来自初级蒸馏区和脱甲烷塔的塔底流338、342分馏成分别基本上由乙烯356、乙烷358、丙烯364、丙烷366、C 4 346和C 5+ 358组成的各流。

冷供应至烯烃装置的低温分离阶段的方法

本发明描述了在从含有烃类的进料制造烯烃的装置(烯烃装置)中的低温分离阶段的制冷供应的方法。在分离顺序中，首先分离成具有最多两个碳原子的馏份及具有至少三个碳原子的馏份。将具有至少三个碳原子的馏份送至长链烯烃的其他分离顺序(4)。将具有最多两个碳原子的馏份经过催化氢化阶段(5)送至包括在－50℃至－100℃的温度范围内的三个冷凝阶段的低温分离阶段(6)。从低温分离阶段抽取气态的氢(9)及甲烷(10)，同时将具有最多两个碳原子的烯烃送至其他的分馏阶段(7)。通过一部分来自前端乙烷馏除塔(3)的液体乙烯馏份(8)的蒸发经过热交换器提供低温分离阶段的制冷功率。将蒸发的乙烯馏份再循环至原料气体压缩机。

Pre-cooling Method for Ethylene Recovery in Dual Demethanizer Fractionation Systems

본 발명은 하나 또는 그 이상의 부분 응축기, 이어서 하나 또는 그 이상의 분류기를 결합하여 사용하므로써 저온 에털렌 회수 시스템에 대한 에틸렌-함유 공급 기체를 냉각 및 응축시키는 개선된 방법에 관한 것으로서, 상기 방법은 열 교환기를 단순화시키고, 또한 비용을 절감시키며, 약 1몰% 이하의 프로판과 프로필렌을 함유하는 에탄 분해물로 부터 압축 및 예비 냉각된 공급 기체를 처리하는데 특히 적합하다.

Method for recovering an ethylene stream from carbon monoxide rich feed stream, and associated installation

根据本发明的方法包括以下步骤：-处理进料物流(12)以获得经处理气体物流(60)；-在热交换器(34)中冷却经处理气体物流(60)以形成至少一个塔供料级分；-将每个塔供料级分引入到蒸馏塔(50)中；-在热交换器(34)中加热源自于塔顶物流(104)的至少一个下游物流(106)。该处理步骤包括形成中间物流(20)，所述中间物流(20)包含至少20％摩尔的乙烯和至少20％摩尔的一氧化碳，该方法包括去除中间物流(20)中所含的一氧化碳的去除步骤。

Gas conditioning process and system for extracting condensable vapors from a supplied gas

一种从供应的气体提取可冷凝蒸汽的过程，包括以下步骤：i)通过在冷凝表面处冷却供应的气体来使可冷凝蒸汽冷凝，使得供应的气体分成至少一个冷凝馏分和产物气体；同时ii)由机械刮擦器件使该至少一个冷凝馏分从冷凝表面移除。

Method for improving propylene recover from fluid catalytic cracker unit

본 발명은 프로필렌 회수를 개선하기 위하여 유체촉매분해장치(FCCU)로부터 나오는 분해된 스트림을 처리하는 방법에 관한 것이다. 본 발명은 또한 상기 방법을 구현하기 위한 대응하는 장치에 관한 것이다.

Process for recovering ethylene comprising precooling step

본 발명은 하나 또는 그 이상의 부분 응축기, 이어서 하나 또는 그 이상의 분류기를 결합하여 사용하므로써 저온 에틸렌 회수 시스템에 대한 에틸렌-함유 공급 기체를 냉각 및 응축시키는 개선된 방법에 관한 것으로서, 상기 방법은 열 교환기를 단순화시키고, 또한 비용을 절감시키며, 약 1몰% 이하의 프로판과 프로필렌을 함유하는 에탄 분해물로부터 압축 및 예비 냉각된 공급 기체를 처리하는데 특히 적합하다. The present invention is directed to an improved method of cooling and condensing an ethylene-containing feed gas for a low temperature ethylene recovery system by using one or more partial condensers, followed by one or more fractionators. It simplifies, reduces costs, and is particularly suitable for treating compressed and precooled feed gases from ethane decomposition products containing up to about 1 mole percent propane and propylene.

Oil circulation-treatment method and oil circulation-treatment apparatus for pyrolysis equipment, and pyrolysis treatment equipment comprising the same

본 발명은 열분해 처리 설비로부터 발생한 고온의 유증기를 효율적으로 처리하여 고온의 유증기에 대한 냉각효율을 향상시킬 수 있고, 오일을 개질할 수 있을 뿐만 아니라, 가스 생산량을 증대시킬 수 있는, 열분해 처리 설비용 오일 순환처리 방법과 오일 순환처리 장치 및 이를 포함하는 열분해 처리 설비에 관한 것이다. 본 발명에 따르면, 열분해 처리 설비에서 발생하는 오일과 유증기를 처리하기 위한 장치로서, 열분해 처리 설비에서 발생된 오일을 공급받는 오일 저장 탱크; 상기 오일 저장 탱크에 저장된 오일을 공급받고, 열분해 처리 설비에서 발생된 유증기를 공급받아 상기 유증기를 이용하여 오일을 개질하도록 구성되며, 개질된 오일을 상기 오일 저장 탱크로 배출하도록 구성되는 오일 개질 장치; 상기 오일 저장 탱크와 오일 개질 장치 간을 연결하는 오일 공급 관로; 상기 오일 공급 관로 상에 구비되어 상기 오일 저장 탱크의 오일을 상기 오일 개질 장치로 공급하도록 작동하는 오일 공급 펌프; 및 상기 오일 개질 장치의 오일 배출구와 상기 오일 저장 탱크의 오일 유입구 간에 연결되어 상기 오일 개질 장치에서 배출되는 오일을 상기 오일 저장 탱크로 회수되도록 하는 순환 관로;를 포함하는 것을 특징으로 하는 열분해 처리 설비용 오일 순환처리 장치가 제공된다. The present invention is for a pyrolysis treatment facility that can efficiently treat high-temperature oil vapor generated from a pyrolysis treatment facility to improve the cooling efficiency of the high-temperature oil vapor, and can reform oil as well as increase gas production It relates to an oil circulation treatment method, an oil circulation treatment apparatus, and a pyrolysis treatment facility including the same. According to the present invention, there is provided an apparatus for treating oil and oil vapor generated in a pyrolysis treatment facility, comprising: an oil storage tank receiving oil generated in a pyrolysis treatment facility; an oil reforming device configured to receive oil stored in the oil storage tank, receive oil vapor generated from a pyrolysis treatment facility, and reform the oil using the oil vapor, and discharge the reformed oil to the oil storage tank; an oil supply pipe connecting the oil storage tank and the oil reforming device; an oil supply pump provided on the oil supply pipe and operated to supply oil from the oil storage tank to the oil reformer; and a circulation pipe connected between the oil outlet of the oil reformer and the oil inlet of the oil storage tank to recover the oil discharged from the oil reformer to the oil storage tank. An oil circulation treatment device is provided. ...

Stages and systems for compressing cracked gas

분해된 가스의 압축을 위한 압축 스테이지로서, 상기 압축 스테이지는 분해된 가스의 가스 성분으로부터 액체 성분을 분리하기 위한 액체 분리 수단, 상기 액체 분리 수단에 연결된 압축기, 상기 압축기로부터 압축된 가스를 냉각시키기 위해 압축기에 연결되고, 냉각 유체 공급원으로부터의 제1 냉각 유체에 의해 냉각되는 가스 냉각 수단을 포함한다. 상기 스테이지는 상기 액체 분리 수단에 연결되고, 분해된 가스를 수용하기 위한 주입구를 갖는 가스 사전 냉각 수단을 더 포함한다.

METHOD OF PURIFYING HYDROCARBON-RICH GAS

Procédé de purification d'un gaz (1) riche en hydrocarbures, et comprenant au moins 10 ppm en volume d'hydrocarbures ayant au moins six atomes de carbone, comprenant les étapes suivantes : Etape a) Refroidissement dudit gaz à une température comprise entre -20°C et -60°C par échange thermique avec au moins un réfrigérant (3) dans un échangeur de chaleur (2) ; Etape b) Epuration en composés contenant au moins six atomes de carbone du gaz partiellement liquéfié à l'étape a) dans une colonne (5) de lavage contenant une tête (8) de colonne (5) dans son extrémité la plus haute et une cuve (7) de colonne (5) dans son extrémité la plus basse pour former, en tête (8) de colonne de lavage (5), un courant (9) gazeux contenant moins de 5 ppm en volume de composés contenant au moins six atomes de carbone et, en cuve (7) de colonne de lavage (5), un courant (6) liquide enrichi en composés contenant au moins cinq atomes de carbone ; Etape c) Condensation au moins partielle dudit courant (9) gazeux issu de l'étape b) dans un échangeur (10, 2) de chaleur pour former un courant diphasique (15) ; Etape d) Séparation dudit courant diphasique (15) issu de l'étape c) dans un pot (16) séparateur de phases à une température comprise entre -60°C et -80°C pour former un courant (17) gazeux en tête de pot et un courant (18) liquide en cuve de pot (16) ; Etape e) Utilisation du courant liquide (18) issu de l'étape d) comme reflux en tête (8) de colonne de lavage (5) ; Etape f) Condensation du courant (17) gazeux issu de l'étape d) par échange thermique dans un échangeur de chaleur (20, 2) à une température inférieure à -100°C pour former un gaz (21) liquéfié contenant moins de 5 ppm en volume de composés contenant au moins six atomes de carbone. A process for purifying a gas (1) rich in hydrocarbons, and comprising at least 10 ppm by volume of hydrocarbons having at least six carbon atoms, comprising the following steps: Step a) cooling said gas to a temperature ...

Method for purifying a gas rich in hydrocarbons

A process for the purification of a gas rich in hydrocarbons and comprising at least 10 ppm by volume of hydrocarbons having at least six carbon atoms nitrogen.

Method for providing refrigeration to the cryogenic separation stage of an olefin plant

Process with a pre-cooling stage for the recovery of ethylene

A kind of method of separating plant saturation dry gas

本发明涉及干气处理领域，公开了一种分离炼厂饱和干气的方法，包括：将饱和干气依次进行压缩、冷却和第一气液分离处理，将第一气液分离处理得到的气相和凝液分别进行碳四吸收和汽油稳定处理，将碳四吸收处理得到的气相和液相分别进行汽油吸收和碳四解吸处理；回收碳四解吸处理得到的气相，并将碳四解吸处理得到的液相返回至碳四吸收处理；将汽油吸收处理得到的液相进行汽油稳定处理，将汽油稳定处理得到的液相返回至汽油吸收处理，将汽油稳定处理得到的气相依次进行冷凝和第二气液分离处理，将第二气液分离处理得到的气相和液相分别返回至压缩处理和汽油稳定处理、碳四吸收处理。本发明的方法，流程简单，投资小，能耗低，C2C3回收率高。

Method for separating coking dry gas

本发明涉及干气处理领域，公开了一种分离焦化干气的方法，该方法包括：将焦化干气依次进行催化加氢处理、冷却处理和碳四吸收剂吸收处理，然后将碳四吸收剂吸收处理得到的气相物料和液相物料分别进行汽油吸收剂吸收处理和碳四解吸处理，回收碳四解吸处理得到的气相物料，并将碳四解吸处理得到的液相物料返回至碳四吸收剂吸收处理。本发明的方法具有投资小、能耗低、碳四吸收剂循环量小等特点。

Gas regulation process and system for the gas extraction condensable vapours from supply

一种从供应的气体提取可冷凝蒸汽的过程，包括以下步骤：i)通过在冷凝表面处冷却供应的气体来使可冷凝蒸汽冷凝，使得供应的气体分成至少一个冷凝馏分和产物气体；同时ii)由机械刮擦器件使至该少一个冷凝馏分从冷凝表面移除。

System and method for recovering NGLS using dual compression

A system includes a first separator that separates water from a fluid material. The water settles on the bottom of the water knock-out tank. The system includes multiple compressors to boost the pressure of the fluid material. The system includes a second separator that separates condensate from the fluid material. The system includes a mixing pipe that mixes glycol with the fluid material and a first heat exchanger that cools the mixed fluid material and glycol. The system includes a third separator that separates gaseous components and liquid components of the mixed fluid material and glycol and a fourth separator that separates the liquid components of the mixed fluid material and glycol. The system includes a fractional distillation column that heats a first liquid from the fourth separator, gasifying a first portion of the first liquid. A second portion of the first liquid remains liquid and is natural gas liquids.

Low pressure olefin recovery process

描述了低压烯烃回收方法和设备。原料气300在初级蒸馏压下，经过压缩302、304并经过蒸馏310。塔顶流312在低于30kg/cm 2 (430psia)的压力下冷却318，以使塔顶流部分冷凝。初级蒸馏塔310采用至少部分冷凝物320进行回流。塔顶蒸汽进一步冷却318并部分冷凝，冷凝物322供给脱甲烷塔324。剩余的蒸汽326在冷区328中冷却，得到的液体进行相分离330并膨胀331和334，从而提供冷区所需的冷量。来自冷区的膨胀的蒸汽332重新循环进入工艺气体压缩器。来自初级蒸馏区和脱甲烷塔的塔底流338、342分馏成分别基本上由乙烯356、乙烷358、丙烯364、丙烷366、C 4 346和C 5+ 358组成的各流。

Process for the separation of C2 / C3 hydrocarbons in ethylene plants

Process and equipment for recovering and purifying ethylene produced by pyrolysis of hydrocarbons

NOx removal method

The invention relates to mixtures comprising molecular hydrogen, hydrocarbons, and nitrogen oxides; to processes for removing at least a portion of the nitrogen oxides therefrom; to equipment useful in such processes; and to the use of such hydrocarbons for, e.g., chemical manufacturing.

Whirlwind coagulation and cooling system

提供一种用于处理可重复使用燃料的装置，包括具有第一配置的第一类型旋风冷却器。该装置还设置有一个或多个第二类型旋风冷却器，其中每一个或多个第二类型旋风冷却器具有与相应的其他一个或多个第二类型旋风冷却器基本相同的第二配置，其中第二配置与第一配置不同。该装置还可以设置有空气冷却热交换器、盘管凝结器和一个或多个起泡器。第一类型旋风冷却器和一个或多个第二类型旋风冷却器连接。一个或多个第二类型旋风冷却器中的一个连接到空气冷却热交换器。空气冷却热交换器连接到盘管凝结器。盘管凝结器连接到一个或多个起泡器。

Novel process of absorption stabilizing unit and comprehensive utilization method of product thereof

本发明涉及一种吸收稳定单元的新工艺，其包括S1富气一次压缩、S2富气二次压缩、S3干气吸收及S4汽油稳定等操作步骤；来自催化分馏单元的富气经一次压缩、脱重塔精馏和二次压缩等操作后，脱重塔塔顶以C 3 为主的气相与来自催化分馏单元的粗汽油在吸收塔内进行吸收操作，吸收塔顶出未吸收组份干气；吸收塔塔釜的富吸收油和来自脱重塔塔釜以C 4 为主的液相进稳定塔进行稳定操作。本发明吸收稳定单元的新工艺，通过分步压缩能够明显降低吸收稳定单元的能耗，便于吸收稳定单元产物进一步利用。本发明还涉及一种吸收稳定单元产物的综合利用方法，其将吸收稳定新工艺后的稳定汽油、液化气和干气中的有效组份最大化转化为丙稀等高附加值化工产品。

Procedure for treating a stream of cracked gas from a hydrocride pyrolysis installation and associated installation

Este procedimiento comprende la separación de una corriente, corriente arriba de gas craqueado parcialmente condensado en un separador intermedio (44B) para recuperar un líquido intermedio (136) y una corriente intermedia (138) de gas craqueado y la introducción del líquido intermedio (140) en una columna intermedia (68) de desmetanización.El procedimiento comprende la extracción de una parte del líquido intermedio (136) y la expansión de al menos una primera fracción (194) obtenida a partir de la parte extraída (190). Comprende la puesta en relación de intercambio térmico de la primera fracción expandida con la corriente intermedia superior (146) proveniente de la columna (68) para condensar al menos parcialmente la corriente intermedia superior (146).El procedimiento comprende la separación de la corriente intermedia superior parcialmente condensada en un primer separador (76) de reflujo para formar una corriente líquida (148) introducida en la columna intermedia (68) y una corriente gaseosa de combustible (150). This method comprises the separation of a stream, upstream of partially condensed cracked gas in an intermediate separator (44B) to recover an intermediate liquid (136) and an intermediate stream (138) of cracked gas and the introduction of the intermediate liquid (140) in an intermediate demetanization column (68). The method comprises the extraction of a part of the intermediate liquid (136) and the expansion of at least a first fraction (194) obtained from the extracted part (190). It comprises the setting in thermal exchange relation of the first expanded fraction with the upper intermediate stream (146) from the column (68) to at least partially condense the upper intermediate stream (146). The method comprises the separation of the intermediate stream upper partially condensed in a first reflux separator (76) to form a liquid stream (148) introduced into the intermediate column (68) and a gaseous fuel stream (150).

Process for separating and recovering ngls from hydrocarbon streams

This process comprises using unconventional processing of hydrocarbons, e.g. natural gas, for recovering C2+ and NGL hydrocarbons that meet pipeline specifications, without the core high capital cost requirement of a demethanizer column, which is central to and required by almost 100% of the world's current NGL recovery technologies. It can operate in Ethane Extraction or Ethane Rejection modes. The process uses only heat exchangers, compression and simple separation vessels to achieve specification ready NGL. The process utilizes cooling the natural gas, expansion cooling, separating the gas and liquid streams, recycling the cooled streams to exchange heat and recycling selective composition bearing streams to achieve selective extraction of hydrocarbons, in this instance being NGLs. The compactness and utility of this process makes it feasible in offshore applications as well as to implementation to retrofit/revamp or unload existing NGL facilities. Many disparate processes and derivatives are anticipated for its use.

Method for cooling pyrolysis product

The present invention relates to a method for cooling a pyrolysis product and, more specifically, provides a method for cooling a pyrolysis product, comprising the steps of: supplying a liquid-phase decomposition furnace discharge stream to a first rapid cooling tower; supplying a first rapid cooling tower upper discharge stream to a second rapid cooling tower; supplying a first gas-phase decomposition furnace discharge stream to the second rapid cooling tower; and supplying a second gas-phase decomposition furnace discharge stream to the second rapid cooling tower.