СПОСОБ ПОЛУЧЕНИЯ ПОЛИМЕРОВ ЭТИЛЕНА

Описывается способ получения полимеров этилена в присутствии каталитической системы из этиленполимеризующих катализатора и сокатализатора в многостадийной реакционной последовательности, состоящей из последовательных жидкофазной и газофазной полимеризации, включающей, по крайней мере, одну непрерывную реакционную последовательность, в которой на первой стадии этилен и, необязательно, водород и сомономер полимеризуют в реакторе с циркуляцией в среде низкокипящего углеводорода в присутствии этиленполимеризующих катализатора и сокатализатора при температуре 75-100°С в течение, по крайней мере, 10 мин, затем реакционную смесь выводят из реактора с циркуляцией, по крайней мере, значительную часть реакционной среды удаляют и полимер поступает на конечную стадию, где полимеризацию осуществляют в газофазном реакторе в присутствии добавленных этилена и, необязательно, водорода, сомономеров и сокатализаторов. На первой стадии время пребывания и реакционную температуру выбирают так, что часть полимера ...

ПОЛУЧЕНИЕ МЕТАНОЛА С ИСПОЛЬЗОВАНИЕМ СВЕРХЧИСТОГО ВОДОРОДА ВЫСОКОГО ДАВЛЕНИЯ

Изобретение относится к способу получения метанола. Способ включает получение кислорода на установке разделения воздуха с воздушными компрессорами, приводимыми в действие газовой турбиной, нагревание потока углеводородного сырья с использованием отработанного в газовой турбине газа, экзотермическое взаимодействие первой части потока нагретого углеводородного сырья с паром или газообразным окислителем, включающим молекулярный кислород, с получением сингаза с экзотермическим выделением тепла, эндотермический риформинг второй части потока углеводородного сырья паром над катализатором в риформинг-установке с теплообменником с получением сингаза эндотермического риформинга, причем часть тепла, использованного при получении сингаза эндотермического риформинга, образуется при извлечении экзотермического тепла от образовавшегося сингаза и образовавшегося сингаза эндотермического риформинга, объединение образовавшегося с экзотермическим выделением тепла сингаза и образовавшегося сингаза эндотермического ...

СПОСОБ ПОЛУЧЕНИЯ АММИАКА И ПРОИЗВОДНЫХ СОЕДИНЕНИЙ, В ЧАСТНОСТИ МОЧЕВИНЫ

Изобретение относится к способу и установке получения аммиака и производных соединений аммиака, такого как мочевина, из природного газового сырья, а также к способу модернизации установки для синтеза аммиака и мочевины. Способ включает конверсию природного газа в синтез-газ во входной части, синтез аммиака из синтез-газа в контуре синтеза, использование по меньшей мере части аммиака для получения производного соединения аммиака. Кроме того, способ осуществляют с энергопотребителями и потребителями тепла. При этом часть природного газового сырья используют для снабжения топливом газовой турбины, а энергию, вырабатываемую газовой турбиной, используют для обеспечения, по меньшей мере частично, потребности энергопотребителей в энергии. Далее из отходящего газа газовой турбины рекуперируют тепло и по меньшей мере часть тепла рекуперируют в виде низкотемпературного тепла для обеспечения технологическим теплом по меньшей мере одного из указанных потребителей тепла. При этом низкотемпературное ...

РЕАКТОРНОЕ УСТРОЙСТВО С ОПТИМИЗИРОВАННЫМ НАГРЕВАНИЕМ И РАЗДЕЛЕНИЕМ ФАЗ

Группа изобретений относится к способу и устройству для этерификации и поликонденсации применяемых для производства сложных полиэфиров из расплавленной фазы. Способ получения сложного полиэфира включает нагревание первоначальной реакционной среды, протекающей в верхнем направлении через теплообменник, чтобы получить нагретую реакционную среду, и выведение паров из нагретой реакционной среды в вытянутый в горизонтальном направлении разделительный резервуар, чтобы получить преимущественно жидкий продукт. При этом по меньшей мере часть паров, являющихся побочным продуктом химической реакции, выводится в теплообменнике и/или в разделительном резервуаре. Разделительный резервуар имеет отношение длины к диаметру (L:D) в интервале от 1,25:1 до 8:1 и непосредственным образом соединен с теплообменником. Реакторное устройство для этерификации и поликонденсации содержит вертикальный теплообменник и горизонтально-расположенный разделительный резервуар. Теплообменник имеет впускное отверстие и выпускное ...

УСТАНОВКА С ОГНЕВЫМИ НАГРЕВАТЕЛЯМИ И СПОСОБ ВЫБОРА СХЕМЫ РАЗМЕЩЕНИЯ КОМПОНЕНТОВ УСТАНОВКИ

Раскрыты радиационные огневые нагреватели, используемые вместе с реакторами. Установка содержит по меньшей мере два ряда радиационных огневых нагревателей, при этом первый ряд расположен на второй высоте, которая меньше первой высоты. Каждый ряд радиационных огневых нагревателей содержит радиационный огневой нагреватель. Каждый радиационный огневой нагреватель содержит продуктовый змеевик, размещенный внутри нагревателя, горелки и выход для газообразных продуктов сгорания. Обеспечен входной коллектор с одним входом и множеством выходов, при этом каждый выход входного коллектора сообщается по текучей среде с одним входом продуктового змеевика. Выходной коллектор содержит множество входов и один выход, при этом указанное множество входов сообщается по текучей среде с выходами продуктового змеевика. 2 н. и 8 з.п. ф-лы, 19 ил.

СПОСОБ И УСТРОЙСТВО ГИДРИРОВАНИЯ

Настоящее изобретение относится к реакциям гидрирования различных фракций в переработке нефти. Изобретение раскрывает способ гидрирования углеводородного потока, содержащего олефиновые соединения, ароматические соединения или их комбинацию, включающий этапы: i) подачу углеводородного потока и водорода в первую реакционную зону установки гидрирования, ii) гидрирование в первой реакционной зоне по меньшей мере части ароматических соединений, олефиновых соединений или их комбинации в присутствии катализатора с получением первого промежуточного продукта, iii) охлаждение и разделение первого промежуточного продукта на первый промежуточный жидкий поток и первый промежуточный газовый поток, iv) перемещение первого промежуточного газового потока во вторую реакционную зону установки гидрирования, v) разделение первого промежуточного жидкого потока на первую часть первого промежуточного жидкого потока и вторую часть первого промежуточного жидкого потока и a) перемещение первой части первого промежуточного ...

СПОСОБ СОВМЕЩЕННОГО ПОЛУЧЕНИЯ МОЧЕВИНЫ И МЕЛАМИНА

... 1. Способ совмещенного получения мочевины и меламина, в котором мочевину получают на установке для получения мочевины, содержащей секцию синтеза мочевины при высоком давлении, где получают водный раствор, содержащий мочевину, карбамат аммония и аммиак, и секцию извлечения мочевины при низком давлении, а меламин получают на установке для получения меламина, отходящие газы которой, являющиеся побочными продуктами технологического процесса синтеза меламина, выходят из этой установки при среднем давлении и поступают на повторный цикл в секцию синтеза мочевины при высоком давлении, отличающийся тем, что он включает следующие этапы: ! подача по меньшей мере части упомянутого водного раствора, содержащего мочевину, карбамат аммония и аммиак, выходящего из секции синтеза мочевины, в секцию технологической обработки при среднем давлении установки для получения мочевины, для извлечения содержащихся в нем карбамата аммония и аммиака, ! подвергание упомянутой части водного раствора, содержащего мочевину ...

СПОСОБ И УСТРОЙСТВО ДЛЯ ПРЕВРАЩЕНИЯ ЦЕЛЛЮЛОЗНОГО МАТЕРИАЛА В ЭТАНОЛ

... 1. Способ превращения целлюлозного материала в этанол и другие продукты, причем целлюлозный материал содержит по меньшей мере целлюлозу, лигнин, гемицеллюлозу и золу, в котором целлюлозный материал очищают и подвергают непрерывной гидротермической предварительной обработке без добавления кислот или оснований, или других химических реактивов, которые требуется извлекать, причем получают жидкость и фракцию волокон, фракцию волокон подвергают ферментативному размягчению и осахариванию, причем способ включает ферментацию с получением этанола и извлечение продукта, где способ включает: ! осуществление гидротермической предварительной обработки, подвергая целлюлозный материал по меньшей мере одной операции вымачивания, и проведение целлюлозного материала через по меньшей мере один реактор высокого давления, задающий зону высокого давления реактора, работающую при повышенном давлении; целлюлозный материал нагревают до температуры от 170 до 230°С, и проводят по меньшей мере одну операцию отжима ...

СПОСОБЫ И УСТРОЙСТВО УЛУЧШЕННОГО ГАЗОРАСПРЕДЕЛЕНИЯ

... 1. Реактор, в котором имеется реакционная зона, при этом указанный реактор содержит: рассеиватель, расположенный в указанной реакционной зоне для введения текучей среды в реакционную зону, при этом указанный рассеиватель содержит, по меньшей мере, три радиально проходящих трубы распределения текучей среды,при этом в каждой трубе имеется, по меньшей мере, три отверстия выпуска текучей среды,при этом радиальный интервал между указанными отверстиями выпуска текучей среды каждой из указанных труб распределения текучей среды уменьшается наружу,при этом максимальный диаметр указанного рассеивателя составляет, по меньшей мере, 90% диаметра реакционной зоны на той высоте, где расположен указанный рассеиватель.2. Реактор по п. 1, в котором, если указанный рассеиватель теоретически разделить на четыре кольцевых области равной площади, суммарная площадь отверстий выпуска текучей среды, расположенных в одной из указанных кольцевых областей, составляет до 25% суммарной площади отверстий выпуска текучей ...

СПОСОБ УЛУЧШЕННОГО ПОЛУЧЕНИЯ РЕАКЦИОННОСПОСОБНЫХ МОНОМЕРОВ ПОСРЕДСТВОМ МЕМБРАННОЙ ФИЛЬТРАЦИИ

PROCESS FOR THE PREPARATION OF TRIFLUOROMETHYL BENZENES FROM THE CORRESPONDING TRICHLORO OR TRIBROMO METHYL BENZENES

Verfahren zur Herstellung von Cyclohexanol und Cyclohexanon durch Oxydation von Cyclohexan

Industrielle Produktionsanlage mit minimalem Treibhausgasausstoß, insbesondere Kohlendioxidausstoß, und Verfahren zum Betrieb desselben

Bei einer industriellen Produktionsanlage (1), die eine aus einem kohlenstoffhaltigen Einsatzstoff ein CO2-armes und H2-reiches Abgas erzeugende erste Produktionsanlage (2) mit einer zugeordneten ersten Abgasreinigungsvorrichtung (3) und einer zugeordneten zweiten Abgasreinigungsvorrichtung (14) umfasst, soll eine Lösung geschaffen werden, mit der ein Carbon Capture and Utilisation-Verfahren effektiv und effizient durchführbar ist. Dies wird dadurch erreicht, dass die industrielle Produktionsanlage (1) weiterhin eine das Abgas in einen kohlenstoffhaltigen, zumindest im Wesentlichen H2-freien (6) und einen kohlenstofffreien, H2-reichen (7) Teilgasstrom aufteilende Gasaufbereitungsanlage (4) umfasst; eine Einrichtung (19) zur Erzeugung eines CO2-reichen Gasstroms umfasst, der zumindest ein Teil eines in einer Feuerungseinrichtung (11) entstehenden CO2-haltigen Abgasstroms (17) nach Durchströmen der zweiten Abgasreinigungsvorrichtung (14) zuführbar ist; und eine Wasserstoff (H2) und Sauerstoff ...

VERFAHREN ZUR HERSTELLUNG VON HOCHDRUCKPOLYAETHYLEN

REAKTOR ZUR OXIDATION VON ALKYLAROMATEN MIT SAUERSTOFFHALTIGEN GASEN IN FLUESSIGER PHASE

Verfahren zur Oxydation von Kohlenwasserstoffen

Vorrichtung und Verfahren zur Behandlung von Fest-Flüssig-Gemischen

Ein Laminarstromreaktor zur Herstellung von Werk- oder Brennstoffen, Humus, Maillard- oder ähnlichen Reaktionsprodukten aus einem Fest-Flüssig-Gemisch aus Wasser und einer kohlenstoffhaltigen Komponente, wobei das Fest-Flüssig-Gemisch bei einer Temperatur von über 100°C und einem Druck von über 5 bar behandelt wird, besteht aus Rohrreaktoreinheiten aus weitgehend senkrechten Haltestrecken (1, 3) und richtungsändernden Umlenkern (2, 4). Dabei werden die Haltestrecken von dem Fest-Flüssig-Gemisch langsamer durchströmt als die restlichen Rohrstrecken, weil sie größere Durchmesser aufweisen.

Fuel additive, fuel and method

Upgrading of a raw blend into a diesel fuel substitute:poly(dimethoxymethane)

Process

PYRIDINE MIXTURES

Production of polymeric polymethylene terephthalates

An apparatus for the continuous polycondensation of bis-hydroxyalkyl terephthalate comprises a number of closed heated chambers linked in series by heated ducts, a feed inlet for the first chamber for supplying bis-hydroxyalkyl terephthalate and a final outlet from the last chamber for discharging polycondensed material, the inlet orifice for each chamber being near the bottom of the chamber and the outlet orifice being higher than the inlet, the inlet and outlet orifices being offset in relation to each other, the final outlet being linked to a collection zone and means being provided for causing a pressure drop from the feed inlet to the final outlet. The arrangement is such that liquid undergoing polymerization from a previous chamber passes substantially through the whole depth of liquid in each chamber, thereby causing agitation of the polymerizing mass. Additional agitation may be effected by bleeding an inert gas through the chambers. The product may be further polycondensed in the ...

Integrated process

The present invention relates to a method for preparing polymers, in particular to a method for preparing recycled polymers from polyethylene terephthalate (PET). The method comprises producing a high quality BHET (bis(2-hydroxyethyl) terephthalate) product which is used as a monomer feedstock in an integrated polymerisation process. The PET is depolymerised, in a series of reactors, using ethylene glycol and a catalyst at a temperature of 150-230°C for a period of 20 minutes to 3 hours. Preferably, the PET is a copolymer comprising units chosen from isopthalic acid (IPA), diethylene glycol, butanediol, propanediol, cyclohexanedimethanol. The ethylene glycol is removed during the polymerisation by distillation and recycled to the depolymerisation reactors. The BHET is purified and crystallised and then passed to a polymerisation reactor in the form of a slurry or melt. In some embodiments, the BHET may be mixed with an additional BHET source. The recycled polymer may be extruded, or melt ...

Integrated stabilizer in deisobutanizer for isomerization of hydrocarbons and product separation

An isomerization method consists of a deisobutanizer column receives feed comprising n-butane. The deisobutanizer column delivers its bottoms a portion to a reboiler and another portion along with hydrogen is routed to a isomerization reactor and the reactor effluent is returned to the column. A stabilizer which is integrated with the column, an overhead stream used as a reflux and bottoms containing an iso-butane-rich stream that is the iso-butane product stream. The column overhead effluent is routed to separator, which splits the hydrocarbons and effluent, where the hydrocarbons are routed to deisobutanizer column and effluent recycled to stabilizer, where the stabilizer separates the reactor effluent into product streams contains an iso-butane product stream, a n-butane product stream, and a lighter hydrocarbon product stream.

Process and system for generating synthesis gas

Process and system for conversion of carbon dioxide to carbon monoxide

Process and system for conversion of carbon dioxide to carbon monoxide

METHOD AND PLANT FOR GENERATING SYNTHESIS GAS

METHOD AND APPARATUS FOR THE SYNTHESIS OF DIHYDROARTEMISININ AND ARTEMISININ DERIVATIVES

Process and system for generating synthesis gas

Process and system for conversion of carbon dioxide to carbon monoxide

METHOD AND APPARATUS FOR THE SYNTHESIS OF DIHYDROARTEMISININ AND ARTEMISININ DERIVATIVES

Process and system for conversion of carbon dioxide to carbon monoxide

Process and system for generating synthesis gas

METHOD AND APPARATUS FOR THE SYNTHESIS OF DIHYDROARTEMISININ AND ARTEMISININ DERIVATIVES

HOCHDRUCKVERFAHREN ZUR HERSTELLUNG VON REINEM MELAMIN

The invention relates to a high pressure method for producing pure melamine by pyrolyzing urea in a vertical synthesis reactor. The synthesis reactor has three stages above one another: a) in the first stage, the smaller portion of the total amount of urea is introduced into the central tube of a first tank reactor forming a first melamine-containing reaction medium; b) in the second stage, the first melamine-containing reaction medium and the larger portion of the total amount of urea is introduced into the central tube of a second tank reactor forming a second melamine-containing reaction medium; c) in the third stage, the second melamine-containing reaction medium is introduced into a vertical tubular flow reactor forming a raw melamine melt that is processed to obtain pure melamine.

VERFAHREN UND ANORDNUNG ZUM ERZIELEN EINES INNIGEN KONTAKTES ZWISCHEN EINEM GAS UND EINER FLUESSIGKEIT

ADSORBENT SYSTEM FOR SUBSTITUTION OF THE WATER GAUGE IN A POLYESTER PROCEDURE

PROCEDURE FOR THE OXIDATION OF LIQUID ORGANIC MATERIALS.

PROCEDURE AND ARRANGEMENT FOR OBTAINING AN INTIMATE CONTACT BETWEEN A GAS AND A LIQUID

DEVICE FOR WASTE WATER PURIFICATION.

CONTINUOUS PROCEDURE FOR THE PRODUCTION OF POLYTRIMETHYLENETHERGLYKOL

Procedure and device for the continuous transesterification of dicarbonic acid esters with alcohols, preferably of Dimethylterephthalat with ethylen glycol

Multimodal polyethylene thin film

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

A process for producing hydrogen and graphitic carbon from hydrocarbons

Abstract A process for producing hydrogen from a hydrocarbon gas comprising contacting at elevated temperature the hydrocarbon gas with a catalyst to catalytically convert the hydrocarbon gas to hydrogen and solid carbon; wherein, the catalyst comprises one or both of the following: (a) a calcined Fe-containing catalyst; or (b) a bimetallic MxNiy-type catalyst supported on a substrate.

Device for generating ultra pure 1-methylcyclopropene

The present invention relates to a device for generating ultra pure 1-methyl-cyclopropene (1 -MCP) by using an improved carrier gas flow control system. The invention also relates to the use of a 1-MCP generating device for inhibiting the action of ethylene which accelerates the ripening process of plants such as fruits, flowers, vegetables and the like. Furthermore the invention encompasses a method for treating and storing harvested agricultural products using said 1-MCP generating device.

High value organic-enhanced inorganic fertilizers

The invention is directed to the manufacture of fertilizer having commercial levels of nitrogen supplemented with organic substances, e.g., 16-0.5-2-17-3-14 (N-P- K-S-Fe-Organic by dry weight). The process causes treatment of organic matter with concentrated acid that heats a fertilizer mix causing the hydrolysis of various organic polymers that may be present. A biosolids mix is subsequently injected sequentially with a nitrogen base under controlled conditions. The resultant sterilized and liquefied organic matter is then disbursed over recycled material for the production of granules in a granulator before final drying to greater than 98 percent solids. Because the process allows for the controlled addition of acids and ammonia, desired levels of components can be achieved. For example, fertilizers with high nitrogen content can contain variable amounts of phosphate or iron. In addition, the process is both scalable, odor controlled and safe thereby allowing for the location of biosolid ...

Systems and methods for solar-thermal gasification of biomass

A method, apparatus, and system for a solar-driven chemical plant that may include a solar thermal receiver having a cavity with an inner wall, where the solar thermal receiver is aligned to absorb concentrated solar energy from one or more of 1 ) an array of heliostats, 2) solar concentrating dishes, and 3) any combination of the two. Some embodiments may include a solar-driven chemical reactor having multiple reactor tubes located inside the cavity of solar thermal receiver, wherein a chemical reaction driven by radiant heat occurs in the multiple reactor tubes, and wherein particles of biomass are gasified in the presence of a steam (H2O) carrier gas and methane (CH4) in a simultaneous steam reformation and steam biomass gasification reaction to produce reaction products that include hydrogen and carbon monoxide gas using the solar thermal energy from the absorbed concentrated solar energy in the multiple reactor tubes.

Gasoline manufacturing system or method

Provided is a system or method for manufacturing gasoline from natural gas, said system or method being particularly effective in a place wherein water usable for steam reforming cannot be easily obtained, for example, in a desert which is a natural gas producing place, or on the sea. This system for manufacturing gasoline from natural gas via methanol includes: subjecting natural gas to steam reforming in a steam reformer (20) to form a reformed gas; synthesizing methanol from the reformed gas in a methanol synthesizer (30); synthesizing gasoline from the methanol in a gasoline synthesizer (50); and subjecting water generated in the gasoline synthesizer (50) to reuse in the steam reformer (20) for steam reforming.

Reactors for conducting thermochemical processes with solar heat input, and associated systems and methods

Reactors for conducting thermochemical processes with solar heat input, and associated systems and methods. A system in accordance with a particular embodiment include a reactor having a reaction zone, a reactant source coupled in fluid in communication with the reactant zone, and a solar concentrator having at least one concentrator surface positionable to direct solar energy to a focal area. The system can further include an actuator coupled to the solar concentrator to move the solar concentrator relative to the sun, and a controller operatively coupled to the actuator. The controller can be programmed with instructions that, when executed, direct the actuator to position the solar concentrator to focus the solar energy on the reaction zone when the solar energy is above a threshold level, and direct the actuator to position the solar concentrator to point to a location in the sky having relatively little radiant energy to cool an object positioned at the focal area when the solar energy ...

Method and system for synthesizing fuel from dilute carbon dioxide source

A method for producing a synthetic fuel from hydrogen and carbon dioxide comprises extracting hydrogen molecules from hydrogen compounds in a hydrogen feedstock to produce a hydrogen-containing fluid stream; extracting carbon dioxide molecules from a dilute gaseous mixture in a carbon dioxide feedstock to produce a carbon dioxide containing fluid stream; and processing the hydrogen and carbon dioxide containing fluid streams to produce a synthetic fuel. At least some thermal energy and/or material used for at least one of the steps of extracting hydrogen molecules, extracting carbon dioxide molecules, and processing the hydrogen and carbon dioxide containing fluid streams is obtained from thermal energy and/or material produced by another one of the steps of extracting hydrogen molecules, extracting carbon dioxide molecules, and processing the hydrogen and carbon dioxide containing fluid streams.

PROCESS FOR THE HIGH PRESSURE PRODUCTION OF POLYETHYLENE

A process for polymerizing ethylene under the high temperature and high pressure conditions by using a battery of two or more autoclave reactors connected in series by means of piping provided with a heat exchanger, each of said reactors having an upper reaction zone and a lower reaction zone. According to this process, the reaction yield of polyethylene is higher than attainable from the conventional two-zone polymerization methods, and the obtained polyethylene is improved in optical properties and processability.

APPARATUS AND METHOD FOR PREPARING POLYMER SOLUTIONS

Apparatus and method for the on-site, continuous preparation of aqueous solutions of polymers, especially aqueous solutions of partially hydrolyzed polyacrylamides, for use in secondary and tertiary oil recovery operations. The apparatus comprises a polymerization reactor and a post reactor. Successive batches of a pre-prepared reaction mixture are continuously fed into the polymerization reaction in a manner to form zones or layers in the reactor, each zone or layer comprising a reaction mixture which has reached a different stage or level of completion of the reaction than the zone or layer below and above it. The zones or layers are continuously moved through the polymerization reactor at a rate such that when a zone or layer reaches the outlet of the polymerization reactor, the reaction will have gone to substantial completion. The zones or layers are continuously conveyed from the polymerization reactor to the post reactor. Enroute to the post reactor, a polymer modifying agent is ...

ADSORBER SYSTEM TO REPLACE WATER COLUMN IN A POLYESTER PROCESS

The present invention provides a process for recovering a dihydroxy compound from a fluid stream that results from the preparation of a polyester by use of an adsorption system to selectively recover the dihydroxy compound.

LOW COST POLYESTER PROCESS USING A PIPE REACTOR

The invention is directed to polyester processes that utilizes a pipe reactor in the esterification, polycondensation, or both esterification and polycondensation processes. Pipe reactor processes of the present invention have a multitude of advantages over prior art processes including improved heat transfer, volume control, agitation and disengagement functions. The pipe reactor processes and apparatus of the present invention are built and operated at a much lower cost than conventional polyester processes.

SWEEP MEMBRANE SEPARATOR AND FUEL PROCESSING SYSTEMS

UPGRADING OF A RAW BLEND INTO A DIESEL FUEL SUBSTITUTE: POLY(DIMETHOXYMETHANE)

A method for forming poly(dimethoxymethane) includes a step of separating a formaldehyde-containing blend into a first bottom stream and a first top stream. The first formaldehyde-containing blend includes methanol, formaldehyde, and water while the first bottom stream includes water. The first top stream includes dimethoxymethane that is produced from the reaction between methanol and fomialdehyde. The first top stream is separated into a second bottom stream and a second top stream. The second bottom stream includes poly(dimethoxymethane) while the second top stream includes dimethoxymethane, methanol, and ethanol. The second top stream is separated into a third bottom stream and a third top stream. Third bottom stream includes methanol and ethanol while the third top stream includes dimethoxymethane. The third top steam can be recycled to fonn additional poly(dimethoxymethane). A system that implements the method is also provided.

METHOD FOR LIQUEFACTION OF INDUSTRIAL GAS BY INTEGRATION OF METHANOL PLANT AND AIR SEPARATION UNIT

A method for the liquefaction of an industrial gas by integration of a methanol plant and an air separation unit (ASU) is provided. The method can include the steps of: (a) providing a pressurized natural gas stream (24, 27), a pressurized purge gas stream (48) originating from a methanol plant, and a pressurized air gas stream (132) comprising an air gas originating from the ASU; (b) expanding three different pressurized gases to produce three cooled streams (32, 62, 142), wherein the three different pressurized gases are the pressurized natural gas stream, the pressurized purge gas stream, and the pressurized air gas stream; and (c) liquefying the industrial gas (44) in a liquefaction unit against the three cooled streams to produce a liquefied industrial gas stream (46). The industrial gas to be liquefied is selected from the group consisting of a first portion of the pressurized natural gas stream, a nitrogen gas stream, hydrogen and combinations thereof.

PROCESS AND APPARATUS FOR HYDROGENATION

The present invention relates hydrogenation reactions of different fractions in oil refining. It also relates to the process device applicable thereto and use of said device for hydrogenation of various feedstocks, especially relating to arrangements during campaign changes.

LIQUID FUEL PRODUCTION SYSTEM HAVING PARALLEL PRODUCT GAS GENERATION

A liquid fuel product system is configured to produce liquid fuels from carbonaceous materials. The liquid fuel product system includes a plurality of feedstock delivery systems, a plurality of first stage product gas generation systems, a plurality of second stage product gas generation systems, a plurality of third stage product gas generation systems, a primary gas clean-up system, a compression system, a secondary gas clean-up system, and a synthesis system that includes one or more from the group consisting of ethanol, mixed alcohols, methanol, dimethyl ether, and Fischer-Tropsch products.

PROCESS FOR THE CONTINUOUS PRODUCTION OF CONDENSATION RESINS

A PROCESS FOR PREPARING POLYMERS

INTEGRATED PROCESS FOR UREA AND MELAMINE PRODUCTION

In an integrated process for urea and melamine production, urea is produc ed in a urea plant (10) comprising a high pressure urea synthesis section (1 1) from which an aqueous solution comprising urea, ammonium carbonate and am monia is obtained and a urea recovery section (21) operating at low pressure , and melamine is produced in a melamine plant (40) wherein off-gases result ing as by-products of the melamine synthesis are discharged from said plant at a medium pressure and recycled to the high-pressure urea synthesis sectio n (11).

METHODS AND SYSTEMS FOR PROCESSING CELLULOSIC BIOMASS

Digestion of cellulosic biomass solids may be complicated by release of lignin therefrom. Methods and systems for processing a reaction product containing lignin-derived products, such as phenolics, can comprise hydrotreating the reaction product to convert the lignin-derived products to desired higher molecular weight compounds. The methods can further include separating the higher molecular weight compounds from unconverted products, such as unconverted phenolics, and recycling the unconverted phenolics for use as at least a portion of the digestion solvent and for further conversion to desired higher molecular weight compounds with additional hydrotreatment.

STARTING SYSTEM FOR STARTING REFORMING-BASED HYDROGEN PRODUCTION APPARATUS

The present invention discloses a start-up system for starting reforming hydrogen production device, the reforming hydrogen production device and the start-up system adopt methanol water as feedstock, comprising a feed riser pipe, a flame tray, an upper cover body and an igniter, wherein the flame tray and the upper cover body are disposed on the feed riser pipe from the bottom up; the middle part of the upper cover body is provided with an aperture in communication with the feed riser pipe, the methanol water feedstock may flow from the feed riser pipe up to the aperture and be exuded from the aperture and spread around along the upper side surface of the upper cover body until flowing into the flame tray; and an ignition position of the igniter corresponds to the upper side surface of the upper cover body.

AN INTEGRATED METHOD AND SYSTEM FOR THE CHLORINE DIOXIDE PRODUCTION COUPLED WITH A RELATIVELY INDEPENDENT SODIUM CHLORATE ELECTROLYTIC PRODUCTION

An integrated method and system for chlorine dioxide production coupled with a relatively independent electrolytic sodium chlorate production unit is disclosed. The system is consisted of the following features: an electrolytic production unit of sodium chlorate (NaClO3) and crystallization unit, a chlorine dioxide (ClO2) production unit and a hydrochloric acid (HCl) synthesis unit. The system feeds an electrolyte solution into a solid-liquid filter, wherein the electrolyte solution contains sodium chlorate crystal, to filter out the crystal from sodium chloride and sodium dichromate. The sodium chlorate crystal is then fed into a chlorine dioxide generator after dissolving, while sodium chloride and sodium dichromate solution separated returns back to the electrolyzer for the electrolysis process, recycling the intermediate chemicals in the sodium chlorate production system, rather than entering chlorine dioxide production unit. Whereas sodium chloride constantly formed as a byproduct ...

MICROWAVE INDUCED PLASMA CLEANING DEVICE AND METHOD FOR PRODUCER GAS

A device and method for cleaning producer gas includes a filter bed chamber, a microwave chamber, a first catalytic chamber and a second catalytic chamber. The filter bed chamber comprises an inlet for carbon-based material and a spent carbon outlet. The microwave chamber comprises a permeable top and wave guides around the perimeter through which microwaves can be introduced into the device using magnetrons. The first catalytic chamber is connected to the microwave chamber, and the second catalytic chamber is connected to the first catalytic chamber. The method comprises using the device by filling the filter bed chamber with carbon-based material, introducing microwaves into the microwave chamber using the magnetrons and wave guides, dissociating heavy carbons entrained within the gas by passing the gas through carbon-based material in the filter bed chamber, the microwave chamber, the first catalytic chamber and the second catalytic chamber.

MULTILAYER REACTOR UTILIZING HEAT EXCHANGE

An end surface of each first side wall, an end surface of each first intermediate wall, and an end surface of each first regulating wall are joined, by diffusion bonding, to an adjacent second structure, and an end surface of each second side wall, an end surface of each second intermediate wall, and an end surface of each second regulating wall are joined, by diffusion bonding, to an adjacent first structure or a cover structure. The thickness dimension of the first side walls is greater than or equal to the thickness dimension of the first intermediate walls, and the thickness dimension of the second side walls is greater than or equal to the thickness dimension of the second intermediate walls.

SYSTEM AND METHODS OF TRIM DEWAXING DISTILLATE FUELS

Systems and methods are provided for dewaxing a distillate fuel oil by subjecting an at least partially hydroprocessed distillate fuel oil to cavitation to reduce the pour point, reduce the cloud point, reduce the cold filter plugging point, or a combination thereof of the distillate fuel oil.

A PROCESS FOR PRODUCING HYDROGEN AND GRAPHITIC CARBON FROM HYDROCARBONS

In accordance with the present invention, there is provided a process for producing hydrogen and graphitic carbon from a hydrocarbon gas comprising: contacting at a temperature between 600 °C and 1000 °C the catalyst with the hydrocarbon gas to catalytically convert at least a portion of the hydrocarbon gas to hydrogen and graphitic carbon, wherein the catalyst is a low grade iron oxide. Also provided is a method for the beneficiation of catalytic metal containing ore, the method comprising contacting at a temperature between 600 °C and 1000 °C the catalytic metal containing ore with a hydrocarbon gas to form a carbon-coated metal species.

HIGH VALUE ORGANIC-ENHANCED INORGANIC FERTILIZERS

The invention is directed to the manufacture of fertilizer having commercial levels of nitrogen supplemented with organic substances, e.g., 16-0.5-2-17-3-14 (N-P- K-S-Fe-Organic by dry weight). The process causes treatment of organic matter with concentrated acid that heats a fertilizer mix causing the hydrolysis of various organic polymers that may be present. A biosolids mix is subsequently injected sequentially with a nitrogen base under controlled conditions. The resultant sterilized and liquefied organic matter is then disbursed over recycled material for the production of granules in a granulator before final drying to greater than 98 percent solids. Because the process allows for the controlled addition of acids and ammonia, desired levels of components can be achieved. For example, fertilizers with high nitrogen content can contain variable amounts of phosphate or iron. In addition, the process is both scalable, odor controlled and safe thereby allowing for the location of biosolid ...

SUBSTANCE CONTAINER FOR A CHEMICAL REACTION

In a method for carrying out a chemical reaction in a reactor (R), at least one substance is present in a container (2; 3; 4) that is closed in a gas-tight manner, is introduced into the reactor in said container, and is released by breaking open the container. The container (2; 3; 4) is designed in such a way that the container breaks open when a specified bursting pressure difference between the internal pressure and the external pressure is exceeded. The breaking open of the container and thus the release of the substance in the container occur as a result of the deliberate application of a pressure difference in the reactor (R), which exceeds the bursting pressure difference. The method has the advantage that substances to be added in a metered manner can be introduced into the reactor before the start of the reaction and are kept ready there until said substances are needed in the course of the reaction process and are released in a pressure-induced manner. This enables novel reaction ...

SYSTEM OR METHOD FOR PRODUCING GASOLINE

Provided is a system or method for manufacturing gasoline from natural gas, said system or method being particularly effective in a place wherein water usable for steam reforming cannot be easily obtained, for example, in a desert which is a natural gas producing place, or on the sea. This system for manufacturing gasoline from natural gas via methanol includes: subjecting natural gas to steam reforming in a steam reformer (20) to form a reformed gas; synthesizing methanol from the reformed gas in a methanol synthesizer (30); synthesizing gasoline from the methanol in a gasoline synthesizer (50); and subjecting water generated in the gasoline synthesizer (50) to reuse in the steam reformer (20) for steam reforming.

PREPARATION OF 18F-FLUCICLOVINE

The present invention provides a method for the production of [18F]-FACBC which has advantages over know such methods. Also provided by the present invention is a system to carry out the method of the invention and a cassette suitable for carrying out the method of the invention on an automated radiosynthesis apparatus.

INTEGRATED PROCESS TO RECOVER HIGH QUALITY NATIVE CO2 FROM A SOUR GAS COMPRISING H2S AND CO2

The invention concerns a method for treating a hydrocarbon feed gas stream containing at least CO2 and H2S to recover a high quality purified CO2 gas stream, comprising the following steps: a. Separating said hydrocarbon feed gas stream into (i) a sweetened hydrocarbon gas stream, and (ii) an acid gas stream comprising at least CO2 and H2S; b. Introducing said gas stream (ii) into a Claus unit, thereby recovering (iii) a liquid stream of elemental sulfur and (iv) a tail gas mainly comprising N2, CO2, SO2 and H2S; c. Introducing the tail gas (iv) into a hydrogenation reactor and then into a quench contactor of the Tail Gas Treatment Unit (TGTU) thereby recovering (v) a hydrogenated tail gas stream mainly comprising N2, H2, CO, CO2 and H2S; d. Contacting said tail gas stream (v) with a non-selective amine-based solvent into a non-selective acid gas absorption unit of the TGTU thereby recovering (vi) an off gas mainly comprising N2, H2 and CO and (vii) a gas stream enriched in CO2 and H2S; ...

AMMONIA GAS GENERATION FROM UREA FOR LOW TEMPERATURE PROCESS REQUIREMENTS

A process for providing an ammonia feed includes (i) a thermal gasification stage and (ii) a controlled catalyzed hydrolysis stage. In stage (i) urea, water and heated gases are introduced into a gasification chamber upstream at a temperature and for a time sufficient to gasify the solution to a first stage gas stream comprising ammonia and isocyanic acid. The first stage gas stream is introduced to a stage (ii) catalytic hydrolysis reactor wherein the isocyanic acid) is hydrolyzed to ammonia with carbon dioxide as a byproduct. The process is provides ammonia for a low-temperature operation as needed.

PROCESS FOR THE CONTINUOUS PREPARATION OF ARYL CARBONATES

Process for the continuous preparation of aryl carbonates A b s t r a c t Organic carbonates which contain at least one aromatic ester group can be obtained continuously from carbonates, which contain at least one aliphatic ester group, and a phenolic compound in the presence of a transesterification catalyst known per se in that the reaction is carried out in a bubble column reactor or in a cascade of at least two bubble column reactors in such a way that the phenolic compound is metered into the first bubble column and the carbonate containing at least one aliphatic ester group is metered into each individual bubble column, but preferably only into the last bubble column. The carbonate containing at least one aromatic ester group is taken off in the liquid state from the last bubble column. Volatile reaction products, for example eliminated alcohol or a dialkyl carbonate are taken off at the upper end of each individual bubble column, preferably at the upper end of the first bubble column ...

REACTOR CONTAINER, PLANT AND PROCESS FOR THE PRODUCTION OF SULFURIC ACID

A new chemical reaction container (43) is provided which is suitable for a process plant the production of sulfuric acid according to the contact process. It comprises a cylindrical envelope surface and is divided by vertical separation walls into at least two sections usually three. Each section has an inlet and an outlet, the separation walls at their bottom parts having one or several openings for making contact possible between the different sections. The advantage of this is that both the drying of the process gas, the interpass absorption step and the final absorption step may be conducted in one and the same reactor, instead of three separate reactors as done previously. This saves both space and material. Further are provided a plant and a process for the production of sulfuric acid according to the contact process, which plant and which process comprise the above reactor container.

Procédé continu de préparation d'hydrocarbures chlorés et/ou bromés liquides, et appareil pour la mise en oeuvre de ce procédé

Vorrichtung zur kontinuierlichen Durchführung von Reaktionen unter Rückflusskühlung

Appareil pour effectuer de manière continue une réaction de polycondensation

Procédé d'oxydation d'hydrocarbures

Verfahren zur kontinuierlichen Herstellung von vernetzten Amino-Harz-Polymerisaten

Verfahren zur kontinuierlichen Umesterung von Dicarbonsäureestern mit Alkoholen

Procédé de préparation d'un oligomère à terminaisons hydroxyles

Procédé de préparation de dihalogénures d'oléfines normalement gazeuses et appareil pour la mise en oeuvre dudit procédé

PROCEDURE FOR THE PRODUCTION OF A MIXTURE OF LOW-MOLECULAR ONES, MULTI-VALUED ALCOHOLS, HYDROXYALDEHYDEN AND HYDROXYKETONEN.

Substance container for a chemical reaction.

Bei einem Verfahren zur Durchführung einer chemischen Reaktion in einem Reaktor (R) liegt mindestens eine Substanz in einem gasdicht verschlossenen Behältnis (2; 3; 4) vor, wird in diesem Behältnis in den Reaktor eingebracht und durch Aufbrechen des Behältnisses freigesetzt. Das Behältnis (2; 3; 4) ist so ausgebildet, dass es bei Überschreiten einer spezifizierten Berst-Druckdifferenz zwischen Innendruck und Aussendruck aufbricht. Das Aufbrechen des Behältnisses und damit die Freisetzung der im Behältnis befindlichen Substanz erfolgt durch gezielte Anwendung einer die Berst-Druckdifferenz überschreitenden Druckdifferenz im Reaktor (R). Das Verfahren hat den Vorteil, dass zuzudosierende Substanzen bereits vor Reaktionsbeginn in den Reaktor eingebracht werden können und dort dann bereitgehalten werden, bis sie im Zuge des Reaktionsablaufs benötigt und druckinduziert freigesetzt werden. Dies ermöglicht neue Reaktionsführungen und macht diese signifikant einfacher.

The device for performing [...], multistage industrial process.

Die Erfindung betrifft eine Anlage (1) zur Durchführung eines kontinuierlichen, mehrstufigen Industrieprozesses, umfassend mindestens einen ersten Raum (2a) und einen zweiten Raum (2b), wobei in diesen Räumen (2a, 2b) während des Prozessverlaufs verschiedene Prozessbedingungen vorherrschen. Diese zwei Räume (2a, 2b) sind durch einen ersten Verbindungskanal (3a) miteinander verbunden. Ein Prozessgut (4) kann bei einem Prozessablauf den ersten Raum (2a), den ersten Verbindungskanal (3a) und den zweiten Raum (2b) nacheinander durchlaufen. Erfindungsgemäss ist ein Fliessgut (5a) im ersten Verbindungskanal (3a) vorgesehen, in welchem oder mit welchem bei einem Prozessablauf das Prozessgut (4) den ersten Verbindungskanal (3a) durchlaufen kann, wobei das Fliessgut (5a) zusammen mit dem Prozessgut (4) eine rieselfähige Dichtzone (6) im Verbindungskanal (3a) bildet, welche die Aufrechterhaltung der unterschiedlichen Prozessbedingungen in den beiden Räumen (2a, 2b) gewährleistet. Die Erfindung betrifft ...

COMPLEX METHOD OF EXTRACTION OF NATURAL COVYSOKOGO QUALITY FROM ACID GAS, INCLUDING HS AND CO

COMBINED PRODUCTION OF CARBAMIDE AND MELAMINE

МОДУЛЬНОЕ УСТРОЙСТВО ДЛЯ НЕПРЕРЫВНОЙ ДЕГАЗАЦИИ И ПОЛУЧЕНИЯ ПОЛИМЕРНЫХ ФОРКОНДЕНСАТОВ С РЕАКЦИОННО-ТЕХНИЧЕСКИ ВЫСОКИМ СООТНОШЕНИЕМ МЕЖДУ ПЛОЩАДЬЮ ПОВЕРХНОСТИ ПРОДУКТА И ЕГО ОБЪЁМОМ ПРИ ЩАДЯЩЕЙ ОБРАБОТКЕ ПРОДУКТА РЕАКЦИИ

В изобретении описано модульное устройство для непрерывной дегазации продуктов реакции карбоновой кислоты или дикарбоновых кислот с полифункциональным спиртом, которое может использоваться для получения форконденсатов (или же форполимеров) и в котором благодаря особой конструкции и особому расположению модульных днищ обеспечивается реакционно-технически высокое соотношение между площадью поверхности продукта и его объемом, при котором (соотношении) характеристическая вязкость продукта реакции составляет от 0,20 до 0,35 дл/г. Такое устройство имеет стандартизированную модульную конструкцию и состоит по меньшей мере из 3 модулей, которые обеспечивают небольшой перепад температур между массой продукта и теплоносителем и которыми являются загрузочный модуль для подачи продукта в реактор, нагреваемый кубовый модуль для сбора в нем и отбора из него продукта и головной модуль для сбора и выпуска выпара. Реактор при необходимости последующего повышения его производительности можно дооснащать неглубокими ...

METHOD OF PRODUCING HYDROGEN AND GRAPHITE CARBON FROM HYDROCARBONS

COMBINED PRODUCTION OF CARBAMIDE AND MELAMINE

METHOD AND INSTALLATION OF UREA SYNTHESIS

СПОСОБ ПРОИЗВОДСТВА ПОЛИМЕРА СЛОЖНОГО ПОЛИЭФИРА, СПОСОБ ПОЛИКОНДЕНСАЦИИ И РЕАКТОРНОЕ УСТРОЙСТВО

Реакторное устройство способно функционировать таким образом, что оно способствует химической реакции в реакционной среде, протекающей через него. Реакторное устройство содержит теплообменник для нагрева реакционной среды и разделительный резервуар для удаления пара из нагретой реакционной среды.

Methods and Apparatus for Enhanced Gas Distribution

Methods and apparatus for introducing a gas into the reaction zone of a reactor. Such methods and apparatus can more evenly distribute the gas throughout the reaction zone. Spargers for introducing a gas into the reaction zone of a reactor can be employed in systems and methods for carrying out the liquid-phase oxidation of an oxidizable compound, such as para-xylene.

Component Separations in Polymerization

A process for component separation in a polymer production system, comprising separating a polymerization product stream into a gas stream and a polymer stream, wherein the gas stream comprises ethane and unreacted ethylene, distilling the gas stream into a light hydrocarbon stream, wherein the light hydrocarbon stream comprises ethane and unreacted ethylene, contacting the light hydrocarbon stream with an absorption solvent system, wherein at least a portion of the unreacted ethylene from the light hydrocarbon stream is absorbed by the absorption solvent system, and recovering a waste gas stream from the absorption solvent system, wherein the waste gas stream comprises ethane, hydrogen, or combinations thereof.

Hydrotreating of Aromatic-Extracted Hydrocarbon Streams

Deep desulfurization of hydrocarbon feeds containing undesired organosulfur compounds to produce a hydrocarbon product having low levels of sulfur, i.e., 15 ppmw or less of sulfur, is achieved by first subjecting the entire feed to an extraction zone to separate an aromatic-rich fraction containing a substantial amount of the aromatic refractory and sterically hindered sulfur-containing compounds and an aromatic-lean fraction containing a substantial amount of the labile sulfur-containing compounds. The aromatic-rich fraction is contacted with isomerization catalyst, and the isomerized aromatic-rich fraction and the aromatic-lean fraction are combined and contacted with a hydrotreating catalyst in a hydrodesulfurization reaction zone operating under mild conditions to reduce the quantity of organosulfur compounds to an ultra-low level.

CONTINUOUS TAKE OFF TECHNIQUE AND PRESSURE CONTROL OF POLYMERIZATION REACTORS

A polymerization reactor system includes features for operating two or more reactors in series or parallel. The system includes a discharge line coupled to an outlet of a first polymerization reactor, a first conduit connecting the first polymerization reactor to a second polymerization reactor via the discharge line, a second conduit connecting the first polymerization reactor to a flashline apparatus via the discharge line, and a diverter valve coupling the first and second conduits to the discharge line. The diverter valve is configured to selectively open the discharge line to the first conduit and close the discharge line to the second conduit in a first valve state and to selectively open the discharge line to the second conduit and close the discharge line to the first conduit in a second valve state. The diverter valve is capable of switching between the first and second valve states. 1. A polymerization reactor system , comprising:a discharge line coupled to an outlet of a first polymerization reactor;a first conduit connecting the first polymerization reactor to a second polymerization reactor via the discharge line;a second conduit connecting the first polymerization reactor to a flashline apparatus via the discharge line; anda diverter valve coupling the first and second conduits to the discharge line, wherein the diverter valve is configured to selectively open the discharge line to the first conduit and close the discharge line to the second conduit in a first valve state, and is configured to selectively open the discharge line to the second conduit and close the discharge line to the first conduit in a second valve state, wherein the diverter valve is capable of switching between the first and second valve states.2. The system of claim 1 , wherein the first valve state is configured to place the first and second polymerization reactors in a series configuration.3. The system of claim 1 , wherein the second valve state is configured to enable one or ...

Method and system for acoustically treating material

Methods and systems for acoustically treating material using a continuous process in which material may be caused to flow in a continuous or intermittent fashion into/out of an acoustic treatment chamber where the material is exposed to focused acoustic energy. The methods and systems may be arranged to permit continuous processing for extended periods while an acoustic energy source operates at a relatively high power output. Treatment chambers may include features such as an acoustic window, a heat exchanger, inlet/outlet flow arrangements, an inspection window, insert elements that define a treatment volume size or shape, etc. Treatment system configurations relating to arrangements of a treatment chamber relative to an acoustic source and coupling medium, material flow paths, and others are provided.

Method and system for acoustically treating material

Methods and systems for acoustically treating material using a continuous process in which material may be caused to flow in a continuous or intermittent fashion into/out of an acoustic treatment chamber where the material is exposed to focused acoustic energy. The methods and systems may be arranged to permit continuous processing for extended periods while an acoustic energy source operates at a relatively high power output. Treatment chambers may include features such as an acoustic window, a heat exchanger, inlet/outlet flow arrangements, an inspection window, insert elements that define a treatment volume size or shape, etc. Treatment system configurations relating to arrangements of a treatment chamber relative to an acoustic source and coupling medium, material flow paths, and others are provided.

Vapor-liquid contacting apparatuses and methods for removing contaminants from gas streams

Vapor-liquid contacting apparatuses and methods for removing contaminants from gas streams are provided. In an embodiment, a vapor-liquid contacting apparatus includes a vortex contacting stage having a contacting zone bound by a wall and defining an axis, a radially inner region surrounding the axis, and a radially outer region adjacent the wall. The vapor-liquid contacting apparatus also includes a feed conduit configured to direct flow of a feed gas into the radially outer region of the contacting zone in a direction tangential to the axis to form a vortex. Further, the vapor-liquid contacting apparatus includes a liquid conduit configured to deliver a liquid absorbent stream to the radially inner region in the contacting zone.

NOVEL REACTOR FOR IONIC LIQUID CATALYZED ALKYLATION BASED ON MOTIONLESS MIXER

Systems and apparatus for ionic liquid catalyzed hydrocarbon conversion may comprise a modular reactor comprising a plurality of mixer modules. The mixer modules may be arranged in series. One or more feed modules may be disposed between the mixer modules. Such systems may be used for ionic liquid catalyzed alkylation reactions. Processes for ionic liquid catalyzed hydrocarbon conversion are also disclosed. 1. A system for ionic liquid catalyzed hydrocarbon conversion , the system comprising:a modular reactor comprising a plurality of static mixer modules and one or more feed modules, wherein:said static mixer modules are arranged in series,each said static mixer module and each said feed module is vertically aligned,said static mixer modules are arranged alternately with said feed modules such that each feed module is disposed between two of said static mixer modules, andeach said static mixer module is arranged coaxially with each said feed module.2. The system according to claim 1 , wherein the number of said static mixer modules is n claim 1 , and the number of said feed modules is (n−1).3. The system according to claim 2 , wherein the number of said static mixer modules claim 2 , n claim 2 , is in the range from two (2) to 10.4. The system according to claim 1 , wherein:each said static mixer module is in contact with at least one of said feed modules, andeach said feed module is in contact with two of said static mixer modules.5. The system according to claim 1 , wherein:each said static mixer module and each said feed module has a circular cross-section, andeach said static mixer module and each said feed module has the same internal diameter.6. The system according to claim 1 , wherein each said static mixer module occupies essentially the entire cross-sectional area of the modular reactor.7. The system according to claim 1 , further comprising a feed supply line claim 1 , wherein:each said feed module includes a feed conduit,each said feed conduit is in ...

Heat Transfer in a Polymerization Reactor

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

POLYOLEFIN PRODUCTION WITH MULTIPLE POLYMERIZATION REACTORS

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

PROCESS AND APPARATUS FOR PRODUCING AN AQUEOUS SOLUTION CONTAINING CHLORINE DIOXIDE

The present invention relates to a process for producing an aqueous solution containing chlorine dioxide from gaseous chlorine dioxide and from an aqueous phase. The invention additionally relates to an apparatus for producing an aqueous solution containing chlorine dioxide and/or for carrying out the process of the invention. Finally, the invention also relates to the use of an apparatus according to the invention for carrying out a process according to the invention. In the following, all statements made in respect of the process of the invention also apply correspondingly to the apparatus of the invention and the use according to the invention, and vice versa, unless indicated otherwise in the individual case. 1. A process for producing an aqueous solution containing chlorine dioxide from gaseous chlorine dioxide and from an aqueous phase ,comprising the following steps:(a) production of a first aqueous solution comprising dissolved chlorine dioxide and further dissolved constituents,(b) transfer of dissolved chlorine dioxide from the first aqueous solution produced into a first gas stream comprising a carrier gas, resulting in a second gas stream which comprises carrier gas and is enriched in gaseous chlorine dioxide,(c) transfer of gaseous chlorine dioxide from the second gas stream into an aqueous phase, with chlorine dioxide being dissolved in the aqueous phase to form the aqueous solution containing chlorine dioxide and a third gas stream which is depleted in chlorine dioxide being formed, from the third gas stream', 'or', 'from a chlorine dioxide-containing fraction of the third gas stream and further added gaseous compounds, '(d) production of further amounts of the first gas stream'}and repetition or continuation of the above process steps (b) and (c) so that further amounts of chlorine dioxide are dissolved in the aqueous phase,where acid-chlorite process,', 'hydrochloric acid-chlorite process,', 'acid-hypochlorite-chlorite process,', 'peroxodisulfate- ...

Conversion of Metal Carbonate into Metal Chloride

A method for producing metal chloride MClx− includes reacting metal carbonate in solid form using phosgene, diphosgene and/or triphosgene to form metal chloride MClx−, wherein the metal M is selected from the group containing alkali metals, alkaline earth metals, Al and Zn, Li and Mg, or Li, for example, and x corresponds to the valency of the metal cations. An apparatus for performing such method is also disclosed. 1. A method for producing metal chloride MCl , the method comprising:providing phosgene, diphosgene and/or triphosgene,{'sup': x+', '−, 'sub': 'x', 'reacting metal carbonate as solid with the phosgene, diphosgene and/or triphosgene to produce metal chloride MCl,'}wherein the metal M is selected from the group consisting of the alkali metals, alkaline earth metals, Al and Zn, Li and Mg, and Li, andwherein x indicates the valence of the metal cation.2. The method of claim 1 , further comprising adding M as an additional reactant.3. The method of claim 2 , wherein at least one of:the metal M is used together with the metal carbonate, orphosgene, diphosgene and/or triphosgene is prepared in situ by reaction of chlorine with carbon monoxide.4. The method of claim 1 , further comprising subsequently reacting the metal chloride to produce metal M.5. The method of claim 4 , further comprising reacting the produced metal M at least partly with carbon dioxide to produce metal carbonate claim 4 , to thereby form a metal circuit.6. The method of claim 1 , wherein the reaction is performed in a grid reactor or a mechanically moved fixed-bed reactor or in a cyclone reactor.7. The method of claim 1 , wherein the phosgene claim 1 , diphosgene and/or triphosgene is prepared by the reaction of carbon monoxide and chlorine.8. The method of claim 7 , wherein the carbon monoxide is produced by a reaction of metal carbonate with the metal M and/or from an electrolysis of carbon dioxide.9. An apparatus for reacting metal carbonate as solid with phosgene claim 7 , diphosgene ...

Method for producing carbonates

In an embodiment, a method of producing a carbonate comprises reacting carbon monoxide and chlorine in a phosgene reactor in the presence of a catalyst to produce a first product comprising phosgene; wherein carbon tetrachloride is present in the first product in an amount of 0 to 10 ppm by volume based on the total volume of phosgene; and reacting a monohydroxy compound with the phosgene to produce the carbonate; wherein the phosgene reactor comprises a tube, a shell, and a space located between the tube and the shell; wherein the tube comprises one or more of a mini-tube section and a second tube section; a first concentric tube concentrically located in the shell; a twisted tube; an internal scaffold; and an external scaffold.

SYSTEM AND METHOD FOR THE MATERIAL USE OF HYDROGEN

A system for the material use of hydrogen includes a transfer-hydrogenation facility with a transfer-hydrogenation unit for the hydrogenation of a material for hydrogenation and a hydrogen-provision device for the provision of hydrogen for the transfer-hydrogenation facility, where, via the hydrogen-provision device, hydrogen in bound form is provided for the transfer-hydrogenation facility, and the hydrogen-provision device includes a loading unit for the loading of a carrier medium with hydrogen. 1. A system for a material use of hydrogen comprising:a transfer-hydrogenation facility comprising a transfer-hydrogenation unit for hydrogenation of a material for hydrogenation;a hydrogen-provision device for provision of hydrogen for the transfer-hydrogenation facility, wherein, by means of the hydrogen-provision device, hydrogen is provided in bound form for the transfer-hydrogenation facility, and the hydrogen-provision device comprises a loading unit for loading a carrier medium with hydrogen.2. A system according to claim 1 , wherein a catalyst is provided in the transfer-hydrogenation unit in order to promote the hydrogenation by contacting the material for hydrogenation with the hydrogen provided in bound form.3. A system according to claim 2 , wherein the transfer-hydrogenation unit comprises a stirring device claim 2 , wherein the catalyst is present as a suspension of a finely distributed claim 2 , solid catalyst in a mixture of liquid carrier medium and material for hydrogenation.4. A system according to claim 1 , wherein the hydrogen-provision device comprises a carrier-medium storage unit for storage of loaded carrier medium.5. A system according to claim 1 , wherein the hydrogen-provision device comprises a hydrogen-generating unit for generating hydrogen.6. A system according to claim 1 , further comprising:a separating device connected with the transfer-hydrogenation facility for separation of a mixture of at least partially unloaded carrier medium and ...

Salt Byproduct Separation During Formation of Polyarylene Sulfide

Methods of forming a polyarylene sulfide and systems as may be utilized in carrying out the methods are described. Included in the formation method is a filtration process for treatment of a mixture, the mixture including a polyarylene sulfide, a salt byproduct of the polyarylene sulfide formation reaction, and a solvent. The filtration process includes maintaining the downstream side of the filter medium at an increased pressure. The downstream pressure can such that the boiling temperature of the mixture at the downstream pressure can be higher than the temperature at which the polyarylene sulfide is insoluble in the solvent. 1. A method for forming a polyarylene sulfide comprising:reacting a dihaloaromatic compound with an alkali metal sulfide or an alkali metal hydrosulfide in an organic amide solvent to form a polyarylene sulfide and a salt;subjecting a mixture including the polyarylene sulfide, the salt, and the organic amide solvent to a filtration process in which the mixture flows to a filter medium from upstream of the filter medium and in which a filtrate flows away from the filter medium in a downstream direction, the salt being retained on the filter medium during the filtration process and forming a filter cake, the filtration process having a downstream pressure, the downstream pressure being elevated above atmospheric pressure, the boiling temperature of the mixture at the downstream pressure being greater than the minimum temperature at which the polyarylene sulfide is fully soluble in the solvent, the filtration having an upstream pressure, the upstream pressure being greater than the downstream pressure for at least a portion of the filtration process, the filtration being carried out in a temperature range that is less than the boiling temperature of the mixture at the downstream pressure and that is greater than the minimum temperature at which the polyarylene sulfide is fully soluble in the solvent.2. The method of claim 1 , further comprising ...

CONTINUOUS POLYMERIZATION DEVICE, METHOD FOR PRODUCING POLYMER COMPOSITION, AND INJECTION VALVE

A continuous polymerization apparatus uses at least a first reactor and a second reactor (). Each of the reactors () comprises a supply port () and an effluent port (). The supply port () of the first reactor () is connected to supply sources () of a raw material monomer and a polymerization initiator, and the effluent port () thereof is connected to the supply port () of the second reactor () by a connection line (). The connection line () is combined with a replenishing line () through an injection valve () at a combining part. The injection valve () comprises, in a full closure state thereof, a clearance that may cause a fluid comprising at least the raw material monomer to flow from the replenishing line () to the connection line (). 1. A continuous polymerization apparatus at least comprisinga first reactor and a second reactor, whereineach of the reactors comprises a supply port and an effluent port, whereinthe supply port of the first reactor is connected to supply sources of a raw material monomer and a polymerization initiator, whereinthe effluent port of the first reactor is connected to the supply port of the second reactor by a connection line, whereinthe connection line is combined with a replenishing line through an injection valve at a combining part located between the effluent port of the first reactor and the supply port of the second reactor, and whereinthe injection valve in a full closure state thereof comprises a clearance capable of causing a fluid comprising at least the raw material monomer to flow from the replenishing line to the connection line.2. The continuous polymerization apparatus of claim 1 , whereinthe injection valve comprises:a plug;a body comprising a space that accommodates the plug; anda shaft that supports and operates the plug in the space, and whereinin the full closure state, the clearance is formed between an inner wall face of the body and a surface of the plug.3. The continuous polymerization apparatus of claim 1 , ...

SCALABLE HEAT EXCHANGER REFORMER FOR SYNGAS PRODUCTION

Heat exchanger-reformer for use in a hydrogen production plant for producing syngas, for instance by means of a steam methane reforming method, wherein the reformer comprises vessel with a first inlet for supplying feed and a second inlet for supplying hot reformer effluent, preferably coming from a main steam methane reformer, wherein the heat exchanger-reformer further comprises a heat exchanging section that is arranged in fluid connection with the first and second inlets for exchanging heat between the feed and reformer effluent to effectuate steam reforming of hydrocarbon to produce syngas, wherein the heat exchanging section comprises a plate heat exchanger assembly for heat exchange between said feed and said reformer effluent. 1. A heat exchanger reformer for convective steam reforming of a hydrocarbon feed , wherein the heat exchanger reformer comprises a vessel having a plate assembly section placed therein comprising of several plates positioned at a distance from each other to provide at least alternating first and second channels between adjacent plates , which vessel comprises a first inlet at a first end of the plate assembly section for supplying a mixture of a hydrocarbon feed and steam to the first channels and causing the mixture to flow in a direction toward a second end of the plate assembly section , which vessel also comprises a second inlet close to the second end of the plate assembly for supplying hot reformer effluent as a heating gas flow to the second channels , wherein the second channels comprise a first and a second section which are connected to each other , wherein the first section is provided for conducting the hot reformer effluent in a direction towards the first end of the plate assembly counter current to the flow of the hydrocarbon feed and steam mixture in the first channels , and the second section is provided for conducting the hot reformer effluent to flow in cross direction of the first channels , which second channels ...

PROCESS AND SYSTEM FOR PRODUCING DIMETHYL ETHER

The invention relates to an improved process and system for the synthesis of dimethyl ether (DME) from a feedstock comprising Hand CO, wherein x=1-2. The process according to the invention comprises (a) subjecting the gaseous mixture comprising synthesis gas originating from step (c) to DME synthesis by contacting it with a catalyst capable of converting synthesis gas to DME to obtain a gaseous mixture comprising DME; (b) subjecting a gaseous mixture comprising the gaseous mixture originating from step (a) to a separation-enhanced reverse water gas shift reaction; and (c) subjecting the gaseous mixture originating from step (b) to DME/synthesis gas separation to obtain DME and a gaseous mixture comprising synthesis gas, which is recycled to step (a). Herein, the feedstock is introduced in step (a) or step (b) and the molar ratio of Hto COin the gaseous mixture which is subjected to step (b) is at least (x+0.8). Also a system for performing the reaction according to the invention is disclosed. 116-. (canceled)18. The process according to claim 17 , wherein the feedstock comprises CO claim 17 , wherein x is 1.5-2 and the feedstock is introduced in step (b).19. The process according to claim 17 , wherein the feedstock comprises CO claim 17 , wherein x is 1.9-2 and the feedstock is introduced in step (b).20. The process according to claim 19 , wherein the feedstock comprises CO claim 19 , wherein x is 1-1.5 and the feedstock is introduced in step (a).21. The process according to claim 20 , wherein the feedstock comprises CO claim 20 , wherein x is 1-1.2 and the feedstock is introduced in step (a).22. The process according to claim 17 , wherein the molar ratio of Hto COin the feedstock is in the range of (x+1) to (x+10).23. The process according to claim 17 , wherein step (a) and/or step (b) is performed in a separation-enhanced DME synthesis (SEDMES) reaction zone.24. The process according to claim 23 , wherein the SEDMES reaction zone is sorption-enhanced and comprises ...

CONVERSION OF WASTE PLASTIC THROUGH PYROLYSIS TO HIGH VALUE PRODUCTS LIKE BENZENE AND XYLENES

A process for producing benzene and xylenes comprising introducing hydrocarbon liquid stream to hydroprocessor to yield first gas stream and hydrocarbon product (C+); optionally introducing hydrocarbon product to first aromatics separating unit to produce saturated hydrocarbons (C+) and first aromatics stream (C+); feeding hydrocarbon product and/or saturated hydrocarbons to reformer to produce reformer product, second gas stream, and hydrogen stream; introducing reformer product to second aromatics separating unit to produce a non-aromatics recycle stream and second aromatics stream comprising C+ aromatics; recycling non-aromatics recycle stream to reformer; introducing first aromatics stream and/or second aromatics stream to third aromatics separating unit to produce first Caromatics (benzene), Caromatics (toluene), Caromatics (xylenesðylbenzene), C 1. A process for producing benzene and xylenes comprising:{'sub': '5', '(a) contacting a hydrocarbon liquid stream with a hydroprocessing catalyst in the presence of hydrogen in a hydroprocessing unit to yield a hydrocarbon product and a first gas stream, wherein the hydrocarbon product comprises C+ hydrocarbons;'}{'sub': 5', '6, '(b) optionally introducing at least a portion of the hydrocarbon product to a first aromatics separating unit to produce a saturated hydrocarbons stream and a first aromatics stream, wherein the saturated hydrocarbons stream comprises C+ saturated hydrocarbons, and wherein the first aromatics stream comprises C+ aromatic hydrocarbons;'}{'sub': 6', '8', '6', '8, '(c) feeding at least a portion of the hydrocarbon product and/or at least a portion of the saturated hydrocarbons stream to a reforming unit to produce a reforming unit product, a second gas stream, and a hydrogen stream, wherein the reforming unit comprises a reforming catalyst, and wherein an amount of Cto Caromatic hydrocarbons in the reforming unit product is greater than an amount of Cto Caromatic hydrocarbons in the saturated ...

TWO-STAGE ENERGY-INTEGRATED PRODUCT GAS GENERATION SYSTEM AND METHOD

A multi-stage product gas generation system converts a carbonaceous material, such as municipal solid waste, into a product gas which may subsequently be converted into a liquid fuel or other material. One or more reactors containing bed material may be used to conduct reactions to effect the conversions. Unreacted inert feedstock contaminants present in the carbonaceous material may be separated from bed material using a portion of the product gas. A heat transfer medium collecting heat from a reaction in one stage may be applied as a reactant input in another, earlier stage. 144.-. (canceled)45. A method for converting a carbonaceous material into at least one liquid fuel , the method comprising:(a) combining a carbonaceous material and carbon dioxide in a feedstock delivery system;(b) introducing the combined carbonaceous material and carbon dioxide into a first reactor containing a first particulate heat transfer material;(c) introducing steam into the first reactor;(d) reacting the carbonaceous material with steam and carbon dioxide in an endothermic thermochemical reaction to generate a first reactor product gas containing char;(e) introducing a portion of the char into a second reactor containing a second particulate heat transfer material;(f) introducing an oxygen-containing gas into the second reactor;(g) reacting the char with the oxygen-containing gas in the second reactor, in an exothermic thermochemical reaction to generate a second reactor product gas;(h) transferring heat, via a second reactor heat exchanger, from the exothermic thermochemical reaction to a first heat transfer medium in thermal contact with the second reactor, the heat transfer medium comprising steam;(i) introducing at least a portion of the heated first heat transfer medium into the first reactor for use as the source of steam in (c);(j) compressing the first and/or second reactor product gas to thereby form a compressed product gas;(k) removing carbon dioxide from the compressed ...

Method for hydrogen production

The present invention relates to a method for hydrogen production and to a method of hydrogen and/or carbon dioxide production from syngas. The method comprises the steps of: (i) providing a gas stream comprising hydrogen and carbon monoxide, (ii) separating at least part of hydrogen from the stream yielding a hydrogen-depleted stream, (iii) subjecting the hydrogen-depleted stream to a water-gas shift reaction, and (iv) separating hydrogen from the stream resulting from step (iii). The method according to the invention improves the conversion of carbon monoxide in the water gas shift reaction and allows to increase the hydrogen production by 10-15% and to increase the overall energy efficiency of the system by 5-7%. The invention further relates to a plant for hydrogen and/or carbon dioxide production suitable for the method of the invention.

POLYETHYLENE PRODUCTION WITH MULTIPLE POLYMERIZATION REACTORS

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

POLYETHYLENE PRODUCTION WITH MULTIPLE POLYMERIZATION REACTORS

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

System and Method for Preparing High-Purity Vanadium Pentoxide Powder

The present invention provides a system and method for preparing high-purity vanadium pentoxide powder. Industrial grade vanadium pentoxide is converted to vanadium oxytrichloride by low temperature fluidizing chlorination, wherein chlorinating gas is preheated via heat exchange between fluidizing gas and chlorination flue gas, and an appropriate amount of air is added to enable a part of carbon powder to combust so as to achieve a balanced heat supply during the chlorination, thereby increasing the efficiency of chlorination and ensuring good selectivity in low temperature chlorination. The vanadium oxytrichloride is subjected to purification by rectification, ammonium salt precipitation and fluidized calcination, thereby obtaining high-purity vanadium pentoxide, wherein the ammonia gas produced during calcination is condensed and then recycled for ammonium salt precipitation. The system and method have advantages of favorable adaptability to raw material, less pollution, low energy consumption in production, low operation cost, stable product quality, etc. 1. A system for preparing high-purity vanadium pentoxide powder , comprising a feeding device , a low temperature chlorination fluidized bed , a rectification and purification device , an ammonium salt precipitation device , an ammonium salt feeding device , a calcination fluidized bed , a tail gas washing absorber , an induced draft fan and a chimney;wherein the feeding device comprises an industrial grade vanadium pentoxide hopper, an industrial grade vanadium pentoxide screw feeder, a carbon powder hopper and a carbon powder screw feeder;the low temperature chlorination fluidized bed comprises a chlorination bed feeder, a chlorination fluidized bed body, a chlorination bed cyclone separator, a flue gas heat exchanger, a flue gas condenser, a chlorination bed acid-seal tank and a chlorination bed spiral slag-discharging device;the rectification and purification device comprises a distilling still, a rectifying ...

PROCESS FOR PRODUCING 1-(4-ISOBUTYLPHENYL)ETHANOL BY HYDROGENATION OF 1-(4-ISOBUTYL-PHENYL)ETHANONE IN THE PRESENCE OF A CATALYST COMPOSITION COMPRISING COPPER

Described is a process for producing 1-(4-isobutylphenyl)ethanol by reacting 1-(4-isobutyl-phenyl)ethanone with hydrogen in the presence of a catalyst composition comprising cop-per and one or more metals other than copper, and a use of a respective composition and/or of a pre-composition, the pre-composition comprising a mixture of oxides of copper and oxides of one or more metals other than copper, in a catalytic hydrogenation process for producing 1-(4-isobutylphenyl)ethanol from 1-(4-isobutylphenyl)ethanone. 1. A process for producing 1-(4-isobutylphenyl)ethanol comprising 'wherein the catalyst composition comprises the copper in a total amount in a range of from 30 mass-% to 98 mass-%, relative to a total mass of metals present in the catalyst composition.', 'S3) reacting 1-(4-isobutylphenyl)ethanone with hydrogen in the presence of a catalyst composition comprising copper and one or more metals other than copper,'}2. The process according to claim 1 , wherein the catalyst composition comprises the copper in a total amount in the range of from 45 mass-% to 98 mass-% relative to the total mass of metals present in the catalyst composition.3. The process according to claim 1 , wherein the catalyst composition comprises in addition to the copper: 'wherein a total amount of aluminium, silicon, zirconium and carbon in the catalyst composition, relative to the total mass of copper present in the catalyst composition, is in a range of from 2.5 mass-% to 60.0 mass-%;', 'c2) a carrier component comprising one or more substance selected from the group consisting of aluminium, aluminium compounds, silicon, silicon compounds, zirconium, zirconium compounds, carbon, and carbon compounds,'}and/or 'wherein the total amount of the one or more metal different from the group consisting of copper, aluminium, and zirconium in the catalyst composition, relative to the total mass of metals present in the catalyst composition, is in the range of from 0.1 mass-% to 55.0 mass-%.', 'c3) ...

Fuel Oil Conversion

A system for processing a stream including fuel oil includes an atmospheric flash column for receiving the stream as feedstock and separate the stream into an atmospheric flash distillate stream and an atmospheric flash residue stream. The system includes a vacuum flash column for receiving the atmospheric flash residue stream and separating the atmospheric flash residue stream into a vacuum flash distillate stream, a vacuum flash residue stream, and a vacuum gas oil stream. The system includes a first hydrocracking unit for receiving and processing at least a portion of the vacuum flash residue stream to produce an intermediate stream and a slurry. The system includes a second hydrocracking unit for receiving and processing the vacuum gas oil stream and the intermediate stream to produce a naphtha product and a light ends product. The system includes a pelletization unit for receiving and processing the slurry to produce a pelletized product. 1. A system for processing a stream comprising fuel oil , the system comprising:a flash column configured to receive the stream as feedstock and separate the stream into a flash distillate stream and a flash residue stream;a vacuum column configured to receive the flash residue stream and separate the flash residue stream into a vacuum distillate stream, a vacuum gas oil stream, and a vacuum residue stream;a first hydrocracking unit configured to receive and process at least a portion of the vacuum residue stream to produce an intermediate stream and a slurry;a second hydrocracking unit configured to receive and process the vacuum gas oil stream and the intermediate stream to produce a naphtha product, a light ends product, and an unconverted oil stream recycled to the first hydrocracking unit; anda pelletization unit configured to receive and process the slurry to produce a pelletized product and a recovered oil stream recycled to the first hydrocracking unit.2. The system of claim 1 , wherein the first hydrocracking unit is ...

SYSTEMS, METHODS, AND APPARATUSES FOR FISCHER-TROPSCH REACTOR CASCADE

Methods, systems and apparatuses are disclosed for a Fischer-Tropsch (“FT”) operation including a first FT stage comprising at least one FT reactor having a first FT catalyst and a first heat transfer surface area to catalyst volume configured to receive a first feed comprising synthesis gas and to convert a first portion of the synthesis gas in the first feed into first FT products. The disclosure also provides for a separation apparatus configured to separate the first FT products into first liquid FT hydrocarbons and first FT tail gas comprising unreacted syngas and for a second FT stage comprising at least one second FT reactor, having a second FT catalyst and a second heat transfer surface area to catalyst volume different from the first heat transfer surface area to catalyst volume, and configured to receive a second feed comprising the first FT tail gas and to convert at least a portion of the second feed into a second FT products. 1. A Fischer-Tropsch (“FT”) reactor system , the system comprising:a. a first FT reactor having a first FT catalyst and a first heat transfer surface area to catalyst volume ratio, the first FT reactor configured to receive a first feed comprising synthesis gas and, operating at first FT conditions, to convert a first portion of the synthesis gas in the first feed into first FT products comprising FT hydrocarbons and leave unconverted a second portion of the synthesis gas;b. a first separation apparatus configured to receive the first FT products as at least part of its feed and to separate the first FT products into first liquid FT hydrocarbons and first FT tail gas stream comprising unreacted syngas; andc. a second FT reactor, having a second FT catalyst and a second heat transfer surface area to catalyst volume ratio that is different from the first heat transfer surface area to catalyst volume ratio, in series with the first FT reactor and configured to receive a second feed comprising the first FT tail gas stream and, ...

APPARATUS AND METHOD FOR CONTINUOUS PRODUCTION OF POLYETHYLENE GLYCOL DINITRATE

An apparatus for producing polyethylene glycol dinitrate. The apparatus includes providing continuously an acid composition and a glycol composition to a reaction apparatus; reacting the acid composition and the glycol composition in the reaction apparatus in a continuous manner to generate a reaction composition; using an alkaline composition to at least partially neutralize the reaction composition to cause at least a portion of the polyethylene glycol dinitrate to deposit from a solution of the reaction composition; and extracting the deposit of polyethylene glycol dinitrate. 113-. (canceled)14. A reaction apparatus for producing in a continuous manner polyethylene glycol dinitrate (PEGDN) , characterized in that the reaction apparatus includesa series of reaction cells spatially disposed in one or more planar structures, the plurality of reaction cells constitute;a feed preparation section having feedstreams for continuously providing an acid composition and a glycol composition to reaction cells thereof, wherein the acid composition includes a mixture of dilute nitric acid and concentrated sulphuric acid;a nitration section in which the acid composition and the glycol composition react in reaction cells in a continuous manner to generate a reaction composition;a quench and neutralization section having a feed for a cooling arrangement for cooling reaction cells to avoid spatial reaction hotspots and thereby preventing thermal runaway occurring within the reaction apparatus, and a plurality of feeds for providing an alkaline composition to at least partially neutralize the reaction composition to cause at least a portion of the polyethylene glycol dinitrate to deposit from a solution of the reaction composition; anda separation arrangement for extracting the deposit of polyethylene glycol dinitrate.15. The reaction apparatus of claim 14 , characterized in that the dilute nitric acid has a concentration in a range of 50-70 weight %.16. The reaction apparatus of ...

FLEXIBLE CHEMICAL PRODUCTION PLATFORM

Disclosed are integrated systems and methods for the conversion of epoxides to beta lactones and to multiple Cproducts and/or Cproducts. 1. A system for the production of Cand Cproducts , comprising:an epoxide source;a carbon monoxide (CO) source; an inlet configured to receive epoxide from the epoxide source and CO from the CO source,', 'a central reaction zone configured to convert at least some of the epoxide to a beta lactone, and', 'an outlet configured to provide an outlet stream comprising the beta lactone,, 'a central reactor, comprising [{'sub': '3', 'claim-text': an inlet configured to receive the outlet stream comprising beta lactone of the central reactor,', {'sub': 3', '3, 'a first Creaction zone configured to convert at least some of the beta lactone to a first Cproduct, and'}, {'sub': '3', 'an outlet configured to provide an outlet stream comprising the first Cproduct,'}], '(i) a first Creactor, comprising, {'sub': '3', 'claim-text': an inlet configured to receive the outlet stream comprising beta lactone of the central reactor,', {'sub': 3', '3, 'a second Creaction zone configured to convert at least some of the beta lactone to a second Cproduct, and'}, {'sub': '3', 'an outlet configured to provide an outlet stream comprising the second Cproduct, and'}], '(ii) a second Creactor, comprising, {'sub': '4', 'claim-text': an inlet configured to receive the outlet stream comprising beta lactone of the central reactor,', {'sub': 4', '4, 'a first Creaction zone configured to convert at least some of the beta lactone to a first Cproduct, and'}, {'sub': '4', 'an outlet configured to provide an outlet stream comprising the first Cproduct, and'}], '(iii) a first Creactor, comprising], 'two or more of (i)-(iii)a controller to independently modulate production of the beta lactone and each of the products,{'sub': 3', '3, 'provided that the first Cproduct differs from the second Cproduct.'}2. The system of claim 1 , wherein the epoxide is ethylene oxide (EO) and the ...

System And Method For Producing Neopentyl Glycol

The present invention describes a process for production of neopentyl glycol (NPG) from formaldehyde (FD) and isobutyraldehyde (IBD). FD and IBD first react to form hydroxypivaldehyde (HPD) in an aldol condensation step, then HPD is hydrogenated to form NPG in a hydrogenation step. The aldol condensation step is performed using a solid catalyst such as an ion exchange resin catalyst, which can be easily separated from the reaction product. The feed to the aldol condensation step is made homogeneous by adjusting the ratio of IBD, FD, and water in the feed or by adding a solvent that is miscible with both IBD and water. High purity NPG is recovered from the product of the hydrogenation step by a suitable method such as crystallization. 1. A method for producing neopentyl glycol from isobutyraldehyde , formaldehyde , and hydrogen , comprising the steps of:controlling the composition of feed to a first reaction step such that a homogeneous solution is formed;introducing the homogeneous solution to an aldol condensation reactor in the first reaction step, where at least a portion of the isobutyraldehyde and formaldehyde undergo an aldol condensation reaction to form a reaction mixture comprising hydroxypivaldehyde, in the presence of a suitable solid catalyst;separating excess and unreacted aldehydes from the reaction mixture and recycling the aldehydes to the aldol condensation reactor;contacting hydroxypivaldehyde with hydrogen in a hydrogenation reactor in a second reaction step, where hydroxypivaldehyde is converted to neopentyl glycol in the presence of a suitable hydrogenation catalyst;isolating highly pure neopentyl glycol from the reaction mixture from the hydrogenation reactor; andrecovering solvent from the reaction mixture from the hydrogenation reactor, so that the solvent can be recycled.2. The method according to claim 1 , where the aldol condensation reaction occurs at a temperature of from 40° C. to 100° C. claim 1 , a pressure of from 1 bar to 5 bar ...

PROCESS FOR PREPARATION OF METHACRYLIC ACID AND METHACRYLIC ACID ESTERS

The invention relates to a process for preparation of at least one of methacrylic acid and a methacrylic acid ester, comprising the process stepsgas phase oxidation of at least one Ccompound, quenching of the reaction phase, separation and purification of the obtained methacrylic acid and optionally esterification, wherein the Ccompound is a methacrolein comprising mixture, originating from at least two different methacrolein sources, a first methacrolein source being a feed stream obtained by the heterogeneously catalysed gas phase oxidation of isobutylene or tert-butyl alcohol or isobutylaldehyde or a mixture of two or more thereof, a second methacrolein source being a feed stream obtained by the reaction of propionaldehyde with a Cextending agent, preferably formaldehyde, and where said methacrolein can be obtained either completely from the first methacrolein source, or completely from the second methacrolein source or from any mixture of both. 1: A process for preparing at least one of methacrylic acid and a methacrylic acid ester , the process comprising:{'sub': '4', 'a1) oxidizing a Ccompound in a gas phase to obtain a reaction phase comprising methacrylic acid;'}a2) quenching the reaction phase to obtain a crude aqueous phase comprising methacrylic acid;a3) separating at least a part of the methacrylic acid from the aqueous phase comprising methacrylic acid to obtain at least one crude methacrylic acid-comprising phase;a4) separating and optionally purifying at least a part of the methacrylic acid from the crude methacrylic acid-comprising phase obtained in a3) via a thermal separation process;a5) optionally esterifying at least a part of the methacrylic acid obtained in a4);{'sub': '4', 'wherein the Ccompound oxidised in a1) originates from a mixture of at least two different methacrolein comprising feed streams, and the mixture comprises'}1 to 99 percent by weight of a first methacrolein comprising feed stream obtained by a heterogeneously catalysed gas ...

REACTOR HAVING A VERTICAL CONDENSATION TUBE AND METHOD FOR THE POLYMERIZATION OF POLYAMIDES IN SUCH A REACTOR

The invention relates to a reactor in the form of a VK tube (VK: simplified continuous), for the polymerisation of polyamides, the reactor being subdivided into an upper and lower reactor region, which are controllable independently of each other. Likewise, the invention relates to a method for the production of polyamides in which such a reactor is used. 1. A reactor in the form of a simplified continuous (VK) tube for the polymerisation of polyamides with an upper and a lower reactor region , the upper reactor region havingan inflow region for the addition of the prepolymer melt,a heating unit,a first flow tube part,a heated discharge cone, andover the entire height of the upper reactor region, a wall heating unit, andthe lower reactor region havingan inflow region for the addition of the melt from the upper reactor region and the separation of process vapour,a static cooling unit,a second flow tube part,a heated discharge cone and a discharge pipe connected thereto, andover the entire height of the lower reactor region, a wall heating unit, andthe upper and the lower reactor region being connected via a tube.2. The VK tube according to claim 1 ,wherein the heating unit is a static heating unit, or a dynamic heating unit, and/or the static cooling unit is a tube bundle, an internally heated overflow body, a plate heat exchanger or a heating coil.3. The VK tube according to{'claim-ref': {'@idref': 'CLM-00001', 'claim 1'}, ', wherein, between the discharge cone of the upper reactor region and the inflow region of the lower reactor region, a metering pump or a control valve for the transport of the prepolymer is integrated.'}4. The VK tube according to claim 1 , wherein an agitator is disposed above the heating unit.5. The VK tube according to claim 1 , wherein the VK tube is connected to a prepolymerisation reactor for the prepolymerisation of polyamides claim 1 , havingan inflow region for the addition of the educts,a heating unit,a first flow tube part which has a ...

CARBON DIOXIDE FIXATION APPARATUS

The present invention provides a new carbon dioxide fixation apparatus. The carbon dioxide fixation apparatus () of the present invention includes: a first reaction vessel (); a carbon dioxide fixing agent feeding unit (); and a gas-liquid mixing unit. The first reaction vessel () can contain a carbon dioxide fixing agent, the carbon dioxide fixing agent feeding unit () can feed the carbon dioxide fixing agent into the first reaction vessel (), and the gas-liquid mixing unit can mix a gas containing carbon dioxide into the carbon dioxide fixing agent. 1. A carbon dioxide fixation apparatus , comprising:a first reaction vessel;a carbon dioxide fixing agent feeding unit; anda gas-liquid mixing unit, whereinthe first reaction vessel can contain a carbon dioxide fixing agent,the carbon dioxide fixing agent feeding unit can feed the carbon dioxide fixing agent into the first reaction vessel, andthe gas-liquid mixing unit can mix a gas containing carbon dioxide into the carbon dioxide fixing agent.2. The carbon dioxide fixation apparatus according to claim 1 , whereinthe gas-liquid mixing unit is inserted into the first reaction vessel, a plurality of holes are provided at an insertion end portion, and the gas can be discharged from the plurality of holes into the carbon dioxide fixing agent in the first reaction vessel.3. The carbon dioxide fixation apparatus according to claim 1 , whereinthe gas-liquid mixing unit comprises a liquid circulation flow path and a pump,the liquid circulation flow path comprises a liquid suction end portion and a liquid discharge end portion,the liquid suction end portion and the liquid discharge end portion are inserted into the first reaction vessel, andthe pump can suck the carbon dioxide fixing agent from the liquid suction end portion and can discharge the sucked carbon dioxide fixing agent from the liquid discharge end portion.4. The carbon dioxide fixation apparatus according to claim 3 , whereinthe liquid circulation flow path ...

Apparatus For Mixing Fluids, Including Fluids Containing Solids

An apparatus for mixing fluids, with particular application in the mixing of air and water for facilitating aerobic biological reactions for breaking down organic material. The apparatus includes gas-lift pump effected recirculation through a mixing chamber (in which a toroidal vortex is established) into a reactor vessel having an upper agitation region and a lower separation region. An embodiment for use with compostable materials includes an assembly for handling settleable solids and maintaining suspension of buoyant materials; a foam suppression device and an overflow reservoir. 1. An apparatus for mixing a first fluid and a second fluid , for enabling reactions involving the first fluid and the second fluid , the apparatus comprising: a first chamber cavity with a first cavity inner periphery and a first chamber cavity cross sectional area, being the cross sectional area at the first chamber cavity inner periphery;', 'a first chamber inlet into the first chamber cavity, having a first chamber inlet cross sectional area;', 'a first chamber outlet from the first chamber cavity, having a first chamber outlet cross sectional area; and', 'a first chamber distance being the distance between the first chamber inlet and the first chamber outlet;, 'a mixing body comprising a first mixing chamber having the first chamber inlet cross sectional area is in the range of about 1 to about 2 times the first chamber outlet cross sectional area;', 'the first chamber cavity cross sectional area is in the range of about 10 to 20 times the first chamber outlet cross sectional area; and', 'a square of the first chamber distance is in the range of about 10 to 20 times the first chamber outlet cross sectional area;, 'whereina flow inducing means for causing a flow of the first fluid and the second fluid through the first chamber inlet to and through the first chamber outlet via the first chamber cavity;wherein the flow through the first chamber inlet to and through the first chamber ...

Methods and Systems for the Co-Generation of Gaseous Fuels, Biochar, and Fertilizer From Biomass and Biogenic Wastes

Methods and systems for converting a biomass and biogenic wastes to hydrogen with integrated carbon dioxide capture and storage are disclosed. In some embodiments, the methods include the following: mixing at least one of a dry solid or liquid or liquid hydroxide and catalysts with a biomass to form a biomass mixture; heating the biomass mixture until the hydroxide and the biomass react to produce hydrogen, carbonate, biochar, and potentially fertilizer; calcining the carbonate or performing double replacement reactions of the carbonate to produce sequestration-ready carbon dioxide and a hydroxide; storing the carbon dioxide produced; transferring the hydrogen produced to a fuel cell; and generating electricity with the fuel cell. 1. A method of converting a biomass to hydrogen and carbon dioxide , said method comprising:mixing a dry solid or liquid or liquid hydroxide with a biomass to form a biomass mixture;heating said biomass mixture and water vapor until said hydroxide and said biomass react to produce hydrogen and carbonate; andcalcining said carbonate or performing double replacement reactions of said carbonate to produce carbon dioxide and a hydroxide.2. The method according to claim 1 , further comprising:mixing catalysts with said biomass mixture prior to heating said biomass mixture.3. The method according to claim 2 , wherein said catalysts include nickel and iron.4. The method according to claim 2 , wherein said catalysts include nanoparticle organic hybrid materials (NOHMs).5. The method according to claim 4 , wherein said NOHMs include a nanoparticle core and molecular organic polymeric corona.6. The method according to claim 5 , wherein said nanoparticle core include at least one of nickel and iron.7. The method according to claim 1 , wherein said dry solid or liquid hydroxide is an alkali metal hydroxide or their solutions.8. The method according to claim 7 , wherein said alkali metal hydroxide is one of KOH claim 7 , NaOH claim 7 , LiOH claim 7 , ...

ON-LINE GAS CHROMATOGRAPHY SYSTEM AND THE USE THEREOF FOR ANALYZING CATALYTIC REACTIONS

An on-line gas chromatography system for a fixed-bed continuous flow reactor and a method for on-line gas analysis of a catalytic reaction using the gas chromatography system. A reactor flow loop, a gas chromatogram, and a hydrostatic regulator are present in the gas chromatography system, wherein the reactor flow loop contains a fixed-bed reactor, a purge gas source, a feed gas source, and a by-pass line for reaction calibration. 1. An on-line gas chromatography system for a fixed-bed continuous flow reactor , comprising: a fixed-bed continuous flow reactor having a reactor gas feed line and a reactor gas output line,', 'a purge gas source,', 'a feed gas source, and', 'a by-pass line;, 'a reactor flow loop, comprisingwherein the by-pass line, the reactor gas feed line, the reactor gas output line, the purge gas source, and the feed gas source, are in fluid communication;a gas chromatogram having a gas chromatogram gas inlet line and a gas chromatogram gas outlet line; and a vessel,', 'an exit end of the gas chromatogram gas outlet line, an exit end of the by-pass line, and', 'a liquid;, 'a hydrostatic pressure regulator, comprisingwherein the vessel contains the liquid and the vessel is in fluid communication with the exit end of the gas chromatogram gas outlet line and the exit end of the by-pass line; andwherein the exit end of the by-pass line is submerged in the liquid at a first depth and the exit end of the gas chromatogram gas outlet line is submerged in the liquid at a second depth that is less than the first depth, wherein the gas chromatogram gas outlet line has a first hydrostatic pressure and the by-pass line has a second hydrostatic pressure, and the first hydrostatic pressure is less than the second hydrostatic pressure;wherein the gas chromatogram is downstream of and in fluid communication with the reactor gas output line and the by-pass line through the gas chromatogram gas inlet line, and the gas chromatogram is upstream of and in fluid ...

SOLUTION POLYMERIZATION PROCESS

Disclosed herein too is a method comprising charging to a reactor system a feed stream comprising a catalyst, a monomer and a solvent; reacting the monomer to form a polymer; where the polymer is contained in a single phase polymer solution; transporting the polymer solution to a pre-heater to increase the temperature of the polymer solution; charging the polymer solution to a liquid-liquid separator; reducing a pressure of the polymer solution in the liquid-liquid separator and separating a polymer-rich phase from a solvent-rich phase in the liquid-liquid separator; transporting the polymer-rich phase to a plurality of devolatilization vessels located downstream of the liquid-liquid separator, where each devolatilization vessel operates at a lower pressure than the preceding devolatilization vessel; and separating the polymer from volatiles present in the polymer rich phase. 1. A system for solution polymerization comprising:a reactor system that is operative to receive a monomer, a catalyst and a solvent, and to react the monomer to form a polymer;a pre-heater located downstream of the reactor system, where the pre-heater is operative to receive a polymer solution from the reactor system and to heat the polymer solution to a temperature greater than its lower critical solution temperature;a liquid-liquid separator that is operative to receive a polymer solution from the pre-heater and to facilitate a separation between the polymer and volatiles by reducing the pressure and/or the temperature of the polymer solution to below the lower critical solution temperature of the polymer solution; where the monomer content in the polymer solution entering the liquid-liquid separator is greater than 5 wt % of a total weight of the polymer solution; and where the polymer is present in a polymer-rich phase and the volatiles are present in a solvent-rich phase; anda plurality of devolatilization vessels located downstream of the reactor system, where each devolatilization ...

PROCESS AND PLANT FOR PRODUCING HYDROCARBONS WITH REDUCED CO2-FOOTPRINT AND IMPROVED HYDROGEN INTEGRATION

Process and plant for producing hydrocarbon products from a feedstock originating from a renewable source, where a hydrogen-rich stream and on off-gas stream comprising hydrocarbons is formed. A portion of the hydrogen-rich stream is used as a recycle gas stream in a hydroprocessing stage for the production of said hydrocarbon products, and another portion may be used for hydrogen production, while the off-gas stream is treated to remove its HS content and used as a recycle gas stream in the hydrogen producing unit, from which the hydrogen produced i.e. make-up hydrogen, is used in the hydroprocessing stage. The invention enables minimizing natural gas consumption in the hydrogen producing unit as well as steam reformer size. 1. A process for producing a hydrocarbon product , said process comprising the steps of:i) passing a feedstock originating from a renewable source through a hydroprocessing stage for producing a main hydrotrotreated stream;{'claim-text': ['an aqueous stream,', 'a hydrogen-rich stream as a first recycle gas stream,', 'an off-gas stream comprising hydrocarbons,', 'and said hydrocarbon product, boiling at above 50° C.;'], '#text': 'ii) passing the main hydrotreated stream to a separation stage for producing:'}iii) passing the first recycle gas stream to the hydroprocessing stage;iv) passing the off-gas stream as a second recycle gas stream to a hydrogen producing unit for producing a hydrogen stream as a make-up hydrogen stream; andv) passing the make-up hydrogen stream to the hydroprocessing stage;{'sub': '2', '#text': 'wherein prior to conducting step iv), said off-gas stream passes to a separation stage for removing HS and thereby producing said second recycle gas stream.'}2. Process according to claim 1 , wherein the process further comprises: vi) splitting said hydrogen-rich stream into said first recycle gas stream and a third recycle gas stream claim 1 , and passing said third recycle gas stream to said hydrogen producing unit.3. Process ...

PROCESS COMPRISING EXOTHERMAL CATALYTIC REACTION OF A SYNTHESIS GAS AND RELATED PLANT

A synthesis process comprising steam reforming a gaseous hydrocarbon feedstock (); exothermically reacting the resulting synthesis gas; removing heat from said exothermal reaction by producing steam (); using said steam as heat input to the steam reforming, wherein the steam reforming comprises: a) forming a mixture () containing steam and hydrocarbons by at least the step of adding a first stream of water () to the hydrocarbon feedstock (); b) heating said mixture () by indirect heat exchange with synthesis gas; c) reforming said mixture after said heating step b). 115-. (canceled)16. A synthesis process , comprising:steam reforming a gaseous hydrocarbon feedstock, thereby obtaining a synthesis gas;exothermically reacting said synthesis gas in the presence of a catalyst, thereby obtaining a synthesis product;removing heat from said exothermal reaction by producing steam, wherein at least part of said steam provides a heat input to the reforming of said hydrocarbon feedstock; a) forming a mixture containing steam and hydrocarbons by at least a step of adding a first stream of water to the hydrocarbon feedstock in a saturating tower, said stream of water being pre-heated by indirect heat exchange, prior to admission into said tower, with at least a portion of the steam produced by removing heat from the exothermal synthesis reaction;', 'b) heating said mixture by indirect heat exchange with at least part of said synthesis gas; and', 'c) reforming said mixture after said heating step b)., 'wherein the steam reforming of the hydrocarbon feedstock includes17. The synthesis process of claim 16 , wherein the formation of said mixture further includes mixing an effluent of said tower with a second stream of water claim 16 , and said second stream is pre-heated by indirect heat exchange with said synthesis gas.18. The synthesis process of claim 17 , wherein a stream of synthesis gas transfers heat to said mixture during the heating step b) claim 17 , and the synthesis gas ...

Multiple Reactor and Multiple Zone Polyolefin Polymerization

Apparatuses and processes that produce multimodal polyolefins, and in particular, polyethylene resins, are disclosed herein. This is accomplished by using two reactors in series, where one of the reactors is a multi-zone circulating reactor that can circulate polyolefin particles through two polymerization zones optionally having two different flow regimes so that the final multimodal polyolefin has improved product properties and improved product homogeneity. 1. A trimodal polyethylene resin having a low molecular weight (LMW) component , an intermediate molecular weight (IMW) component , and a high molecular weight (HMW) component; wherein the LMW component is present in an amount of from about 20 wt. % to about 75 wt. %; wherein the IMW component is present in an amount of from about 5 wt. % to about 40 wt. %; wherein the LMW component has a weight average molecular weight of from about 20 kg/mol to about 150 kg/mol; wherein the IMW component has a weight average molecular weight of from about 85 kg/mol to about 350 kg/mol; wherein the weight average molecular weight of the IMW component is greater than the weight average molecular weight of the LMW component; wherein the weight average molecular weight of the HMW component is greater than the weight average molecular weight of the IMW component; wherein the trimodal polyethylene resin has a Young's modulus (E) of equal to or greater than about 900 MPa , when tested in accordance with ASTM D638; and wherein the trimodal polyethylene resin has a density of equal to or greater than about 0.952 g/cc , when tested in accordance with ASTM D1505.2. The trimodal polyethylene resin of claim 1 , wherein the trimodal polyethylene resin has a melt index of less than about 1 g/10 min claim 1 , when tested in accordance with ASTM D1238 under a force of 2.16 kg.3. The trimodal polyethylene resin of claim 1 , wherein the trimodal polyethylene resin has a density of equal to or greater than about 0.955 g/cc claim 1 , when tested ...

Conversion of C2 Hydrocarbons in the Presence of Methane

A catalyst and corresponding methods of using a catalyst are provided that can be beneficial for conversion of paraffins into a product stream enriched in aromatics and/or methane while reducing or minimizing the content of ethane in the product stream. Such catalysts and methods can be useful, for example, for processing a raw gas, associated gas, tail gas, natural gas, or other type of methane-containing feed stream to convert Chydrocarbons in the stream to heavier hydrocarbons and methane while reducing or minimizing content of ethane in the products from the conversion reaction. Such conversion can be useful for upgrading a methane-containing feed stream to have an energy content that is suitable for pipeline transport under one or more specifications for transport of natural gas. The catalyst and corresponding method can also be beneficial when used as a second stage catalyst in a configuration involving multiple conversion stages. 1. A method for converting a feed stream , comprising:exposing a feed stream comprising methane and ethane, under effective conversion conditions, to a conversion catalyst comprising a medium pore zeolitic framework structure material and 0.1 wt. % to 10 wt. % of Zn and an additional element comprising one or more of Mo, Pt, and Fe, to form a converted product stream,{'sub': 2', '2, 'wherein a molar ratio of Chydrocarbons in the converted product stream to Chydrocarbons in the feed stream is 0.8 or less.'}2. The method of claim 1 , wherein the molar ratio of Chydrocarbons in the converted product stream to Chydrocarbons in the feed stream is 0.7 or less claim 1 , and wherein the conversion exhibits a greater selectivity for methane than for aromatics.3. The method of claim 1 , wherein a molar ratio of methane in the converted product stream to the methane in the feed stream is 1.4 or more.4. The method of claim 1 , wherein the feed stream further comprises Chydrocarbons claim 1 , a molar ratio of Chydrocarbons in the converted ...

DIRECT COMBUSTION HEATING

An electrode includes a network of compressed interconnected nanostructured carbon particles such as carbon nanotubes. Some nanostructured carbon particles of the network are in electrical contact with adjacent nanostructured carbon particles. Electrodes may be used in various devices, such as capacitors, electric arc furnaces, batteries, etc. A method of producing an electrode includes confining a mass of nanostructured carbon particles and densifying the confined mass of nanostructured carbon particles to form a cohesive body with sufficient contacts between adjacent nanostructured carbon particles to provide an electrical path between at least two remote points of the cohesive body. The electrodes may be sintered to induce covalent bonding between the nanostructured carbon particles at contact points to further enhance the mechanical and electrical properties of the electrodes. 1. A method , comprising:mixing oxygen with a reducing gas in a vessel having an interior temperature above a reaction temperature of the reducing gas with oxygen;reacting at least a portion of the oxygen with at least a portion of the reducing gas to form at least one carbon oxide in a heated reaction gas mixture; andreacting the heated reaction gas mixture in the presence of a catalyst to form a tail gas and at least one of a solid carbon product and a hydrocarbon.2. The method of claim 1 , wherein mixing oxygen with a reducing gas comprises mixing the oxygen with the reducing gas in a vessel having an interior temperature above about 400° C.3. The method of claim 1 , wherein reacting at least a portion of the oxygen with at least a portion of the reducing gas comprises reacting at least a portion of the oxygen with at least a portion of the reducing gas in the presence of a catalyst selected to promote the exothermic reaction of the at least a portion of the oxygen with at least a portion of the reducing gas to form at least one carbon oxide in a heated reaction gas mixture.4. The ...

Portable fuel synthesizer

A portable fuel synthesizer, comprising multiple shipping containers, the various modules within one of the multiple shipping containers, a boiler utilizing a hydrocarbon gas as fuel, a cooling system module connected to the boiler, the cooling system adjusts a temperature of the boiler, a syngas reformer, a reactor connected to the syngas reformer and the boiler, the reactor converts the syngas to a hydrocarbon liquid, a hot separator connected to the reactor, a cold separator connected to the hot separator separates liquid hydrocarbons and gaseous hydrocarbons at a lower temperature and pressure than the hot separator, a distillation unit connected to the cold separator performs fractional distillation and separation of hydrocarbon products received from the cold separator, a recycle module connected to the cold separator and distillation unit recycles unreacted gases to the reactor, and a fuel testing and blending unit to receive separated hydrocarbons from the distillation unit.

PROCESS TO FORM ETHYLENE/ALPHA-OLEFIN INTERPOLYMERS

The invention provides a process to form a “first composition comprising a first ethylene/α-olefin interpolymer and a second ethylene/α-olefin interpolymer,” said process comprising polymerizing a first mixture comprising ethylene, an α-olefin, and optionally a polyene, in a stirred tank reactor to form a first ethylene/α-olefin interpolymer, and transferring at least some of the first ethylene/α-olefin interpolymer to a loop reactor, and polymerizing, therein, a second mixture comprising ethylene, an alpha-olefin, and optionally a polyene, in the presence of the first ethylene/α-olefin interpolymer, to form the “first composition comprising the first ethylene/α-olefin interpolymer and the second ethylene/α-olefin interpolymer.” The invention also provides a polymerization reactor configuration comprising at least the following: a stirred tank reactor followed by a loop reactor. 1. A process to form a “first composition comprising a first ethylene/α-olefin interpolymer and a second ethylene/α-olefin interpolymer ,”said process comprising polymerizing a first mixture comprising ethylene, an α-olefin, and optionally a polyene, in a stirred tank reactor to form a first ethylene/α-olefin interpolymer, andtransferring at least some of the first ethylene/α-olefin interpolymer to a loop reactor, and polymerizing, therein, a second mixture comprising ethylene, an alpha-olefin, and optionally a polyene, in the presence of the first ethylene/α-olefin interpolymer, to form the “first composition comprising the first ethylene/α-olefin interpolymer and the second ethylene/α-olefin interpolymer.”2. The process of claim 1 , wherein the stirred tank reactor is a continuous stirred tank reactor (CSTR).3. The process of claim 1 , wherein the polymerization of the first mixture is a solution polymerization.4. The process of claim 1 , wherein the polymerization of the second mixture is a solution polymerization.5. The process of claim 4 , wherein the ratio of “the solution viscosity of ...

Catalysts, related methods and reaction products

The present invention generally relates to improved catalysts that provide for reduced product contaminants, related methods and improved reaction products. It more specifically relates to improved direct fuel production and redox catalysts that provide for reduced levels of certain oxygenated contaminants, methods related to the use of those catalysts, and hydrocarbon fuel or fuel-related products that have improved characteristics. In one aspect, the present invention is directed to a method of converting one or more carbon-containing feedstocks into one or more hydrocarbon liquid fuels. The method includes the steps of: converting the one or more carbon-containing feedstocks into syngas; and, converting the syngas to one or more hydrocarbons (including liquid fuels) and a water fraction. The water fraction comprises less than 500 ppm of one or more carboxylic acids. 1. A method of converting one or more carbon-containing feedstocks into one or more hydrocarbons comprising:a) converting the one or more carbon-containing feedstocks into syngas;b) converting the syngas to one or more hydrocarbons and a water fraction wherein the water fraction comprises less than 500 ppm of one or more carboxylic acids.2. The method according to claim 1 , wherein the one or more carbon-containing feedstocks are selected from a group consisting of: gas-phase feedstocks; liquid-phase feedstocks; and claim 1 , solid-phase feedstocks.3. The method according to claim 1 , wherein the one or more carboxylic acids are selected from a group consisting of: methanoic acid; ethanoic acid;propanoic acid; butanoic acid; pentanoic acid; hexanoic acid; and octanoic acid.4. The method according to claim 1 , wherein a conversion catalyst is used to convert the syngas to one or more hydrocarbons and a water fraction claim 1 , and wherein the conversion catalyst comprises a substrate claim 1 , and wherein the substrate comprises a surface having a pH ranging from about 6.0 to about 8.0.5. The method ...

METHOD FOR LIQUEFACTION OF INDUSTRIAL GAS BY INTEGRATION OF METHANOL PLANT AND AIR SEPARATION UNIT

A method for the liquefaction of an industrial gas by integration of a methanol plant and an air separation unit (ASU) is provided. The method can include the steps of: (a) providing a pressurized natural gas stream, a pressurized purge gas stream originating from a methanol plant, and a pressurized air gas stream comprising an air gas originating from the ASU; (b) expanding three different pressurized gases to produce three cooled streams, wherein the three different pressurized gases are the pressurized natural gas stream, the pressurized purge gas stream, and the pressurized air gas stream; and (c) liquefying the industrial gas in a liquefaction unit against the three cooled streams to produce a liquefied industrial gas stream. The industrial gas to be liquefied is selected from the group consisting of a first portion of the pressurized natural gas stream, a nitrogen gas stream, hydrogen and combinations thereof. 1. A method for the liquefaction of an industrial gas selected from the group consisting of natural gas , nitrogen , hydrogen and combinations thereof , the method comprising the steps of:a) withdrawing a pressurized natural gas stream from a natural gas pipeline;b) removing carbon dioxide and water from the pressurized natural gas stream;c) expanding the pressurized natural gas stream to form an expanded natural gas stream and warming the expanded natural gas stream in a first portion of a heat exchanger against the industrial gas to form a warmed natural gas stream;d) sending the warmed natural gas stream to a methanol production facility under conditions effective for producing a methanol stream, a purified hydrogen stream, and a purge gas rich in hydrogen;e) expanding the purge gas rich in hydrogen to form an expanded purge gas and warming the expanded purge gas in a second portion of the heat exchanger against the industrial gas to form a warmed purge gas stream;f) sending the warmed purge gas stream to the methanol production facility for use as ...

PROCESS FOR PRODUCING BUTADIENE FROM ETHANOL WITH IN SITU REGENERATION OF THE CATALYST OF THE SECOND REACTION STEP

The present invention relates to a process for producing butadiene from ethanol, in two reaction steps, comprising a step a) of converting ethanol into acetaldehyde and a step b) of conversion into butadiene, said step b) simultaneously implementing a reaction step and a regeneration step in (n+n/2) fixed-bed reactors, n being equal to 2 or a multiple thereof, comprising a catalyst, said regeneration step comprising four successive regeneration phases, said step b) also implementing a regeneration loop for the inert gas and at least one regeneration loop for the gas streams comprising oxygen. 1. A process for producing butadiene from ethanol , comprising at least the following steps:a) a step of converting ethanol into acetaldehyde, to produce an ethanol/acetaldehyde effluent, comprising at least one reaction section (A) fed with a stream comprising ethanol and operated in the presence of a catalyst (Ca);b) a butadiene conversion step comprising at least one reaction-regenerative section in which are simultaneously performed a reaction step and a regeneration step in (n+n/2) fixed-bed reactors, n being an integer equal to 2 or a multiple thereof, said (n+n/2) fixed-bed reactors each comprising at least one fixed bed of a catalyst (Cb), said (n+n/2) fixed-bed reactors functioning in parallel and in sequence so that said reaction step starts in each of said reactors with a time shift equal to half of the catalytic cycle time of said catalyst (Cb), said reaction-regenerative section comprising a regeneration loop for inert gas and at least one regeneration loop for a gas stream comprising oxygen, and so that, at each instant:b1) said reaction step is operated in n of said fixed-bed reactors, n being an integer equal to 2 or a multiple thereof, fed at least with a fraction of said ethanol/acetaldehyde effluent obtained from step a), at a temperature of between 300 and 400° C., at a pressure of between 0.1 and 1.0 MPa, for a time equal to the catalytic cycle time of said ...

ETHYLENE HOMOPOLYMER HAVING GOOD BARRIER PROPERTIES

A polyethylene homopolymer composition comprises: a first ethylene homopolymer having a density, dof from 0.930 to 0.975 g/cm, a melt index, Iof from 0.01 to 10 g/10 min, and a molecular weight distribution, Mw/Mn of less than 2.5; and a second ethylene homopolymer having a density, dof from 0.945 to 0.980 g/cm, a melt index, Iof at least 1.0 g/10 min, and a molecular weight distribution, M/Mof less than 2.5; wherein melt index, Iof the second ethylene homopolymer is greater than the melt index, Iof the first ethylene homopolymer. The polyethylene homopolymer compositions which may be nucleated have a weight average molecular weight, Mof 75,000, a molecular weight distribution, M/Mof less than 4.0 and may be usefully employed in molding applications, such as, for example, in compression molded closures. 1. A polyethylene homopolymer composition , the polyethylene homopolymer composition comprising:{'sup': 1', '3', '1, 'sub': '2', '(1) 10 to 90 weight % of a first ethylene homopolymer having a density, dof from 0.930 to 0.975 g/cm, a melt index, Iof from 0.01 to 10 g/10 min, and a molecular weight distribution, Mw/Mn of less than 2.5; and'}{'sup': 2', '3', '2, 'sub': 2', 'w', 'n, '(2) 90 to 10 weight % of a second ethylene homopolymer having a density, dof from 0.945 to 0.980 g/cm, a melt index, Iof at least 1.0 g/10 min, and a molecular weight distribution, M/Mof less than 2.5;'}{'sub': 2', '2', 'w', 'w', 'n, 'sup': 2', '1, 'wherein melt index, Iof the second ethylene homopolymer is greater than the melt index, Iof the first ethylene homopolymer, and wherein the polyethylene homopolymer composition has a weight average molecular weight, Mof ≤75,000 and a molecular weight distribution, M/Mof less than 4.0.'}2. The polyethylene homopolymer composition of wherein the first ethylene homopolymer has a melt index claim 1 , Iof from 0.1 to 10 g/10 min.3. The polyethylene homopolymer composition of wherein the second ethylene homopolymer has a melt index claim 1 , Iof from ...

APPARATUS AND PROCESS FOR HEATING HYDROISOMERIZATION FEED

The process and apparatus of the disclosure utilize a heater between a hydroprocessing reactor and a hydroisomerization reactor. A hydroprocessing feed exchanger cools hydroprocessed effluent to effect turndown of heated hydroprocessed effluent so as to not feed the hydroprocessed effluent to the hydroisomerization reactor at a higher temperature than necessary. 1. A process for hydroprocessing and hydroisomerizing a hydrocarbon feed stream comprising:heating said hydrocarbon feed stream by heat exchange with a heated hydroprocessed effluent stream;hydroprocessing said hydrocarbon feed stream in the presence of hydrogen over a hydroprocessing catalyst to produce a hydroprocessed effluent stream;heating said hydroprocessed effluent stream to provide said heated hydroprocessed effluent stream;hydroisomerizing said heated hydroprocessed effluent stream in the presence of hydrogen over a hydroisomerization catalyst to produce a hydroisomerized effluent stream.2. The process of further comprising preheating said hydrocarbon feed stream by heat exchanging said hydrocarbon feed stream with said hydroisomerized effluent stream prior to heating said hydrocarbon feed stream.3. The process of further comprising adding a hydrogen stream to said hydrocarbon feed stream prior to preheating said hydrocarbon feed stream.4. The process of further comprising adding a quench stream to said hydroprocessed effluent stream after heat exchanging said hydrocarbon feed stream with said heated hydroprocessed effluent stream.5. The process of further comprising heating said hydroprocessed effluent stream in a fired heater.6. The process of wherein said hydroprocessed effluent stream is periodically hotter at discharge from a hydroprocessing reactor than when fed to a hydroisomerization reactor.7. The process of further comprising cooling said heated hydroprocessed effluent stream by heat exchange with said hydrocarbon feed stream.8. The process of further comprising hydrotreating said ...

CONFIGURATION FOR OLEFINS PRODUCTION

Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize an ebullated bed reactor. Products from the upgrading operations may be used as feed to a steam cracker. 1. A process for converting whole crudes , the process comprising:separating a whole crude into at least a medium boiling fraction and a high boiling residue fraction;separating the high boiling fraction in a solvent deasphalting unit to produce a deasphalted oil fraction and a pitch fraction;converting the medium boiling fraction and the deasphalted oil fraction into one or more stream crackable products to produce a hydrotreated effluent;feeding the hydrotreated effluent to a steam cracker to convert hydrocarbons therein into one or more light olefins.2. The process of claim 1 , wherein the medium boiling fraction has two or more of the following properties:a 5% boiling point temperature in the range from about 130° C. to about 200° C.;a 95% boiling point temperature in the range from about 400° C. to about 600° C.;a hydrogen content in the range from about 12 wt % to about 14 wt %;a BMCI in the range from about 5 to less than 50;an API gravity of in the range from about 10° to about 40°;a sulfur content in the range from about 1000 ppm to about 10000 ppm;a nitrogen content in the range from about 1 ppm to about 100 ppm;a viscosity, measured at 40° C., of greater than 1 cSt;less than 5 wt % MCRT; andless than 50 ppm total metals.3. The process of claim 1 , wherein the high boiling residue fraction has two or more of the following ...

CONFIGURATION FOR OLEFINS PRODUCTION

Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize an ebullated bed reactor. Products from the upgrading operations may be used as feed to a steam cracker. 1. (canceled)2. (canceled)3. (canceled)4. (canceled)5. (canceled)6. (canceled)7. (canceled)8. (canceled)9. (canceled)10. (canceled)11. (canceled)12. (canceled)13. A system for converting whole crudes and other heavy hydrocarbon streams to produce olefins , the system comprising:a separation unit for separating a whole crude into at least a light boiling fraction, a medium boiling fraction, and a high boiling residue fraction;a solvent deasphalting unit for deasphalting the high boiling residue fraction and producing a deasphalted oil fraction and a pitch fraction;a conditioning system for destructively hydrogenating the medium boiling fraction and the deasphalted fraction to produce a hydrotreated effluent;a steam cracker unit for converting the hydrotreated effluent and the light boiling fraction into one or more light olefins and a pyrolysis oil.14. (canceled)15. (canceled)16. (canceled)17. The system of claim 13 , wherein the conditioning system for hydrotreating the medium boiling fraction and the deasphalted oil fraction comprises:a first hydroprocessing unit for hydroprocessing the medium boiling fraction; anda second hydroprocessing unit for hydroprocessing the deasphalted oil fraction.18. The system of claim 13 , further comprising a flow line for diverting the deasphalted oil fraction to the first hydroproces sing unit.19. The ...

METHOD FOR PRODUCING BROMINE

To provide a method that enables production of bromine in good yield. 1. A method for producing bromine , comprisinga step of supplying a gas containing a bromine compound and a gas containing oxygen to a reactor that includes a catalyst packed bed, and oxidizing the bromine compound to obtain a gas containing bromine, [{'br': None, 'i': '≤a≤', '0.300.55\u2003\u2003Inequality (1)'}, {'br': None, 'i': '≤L', '0.401≤6.0\u2003\u2003Inequality (2)'}], 'wherein the step satisfies the following Inequality (1) and Inequality (2) {'br': None, 'i': L', 'L', 'V', 'P', 'aV+b', 'T+, '1=2/(())×(273.14)/273.14\u2003\u2003Formula (3)'}, 'where “a” represents porosity [-] of the catalyst packed bed, and “L1” is defined by the following Formula (3)L2: Superficial velocity of reaction gas [m/s]P: Reaction pressure [atm]T: Reaction temperature [° C.]V: Reactor volume corresponding to catalyst packed bed [L]a: Porosity of catalyst packed bed [-]b: Pore volume of catalyst packed bed [L].2. The method for producing bromine according to claim 1 , wherein the bromine compound is hydrogen bromide.3. The method for producing bromine according to claim 1 , wherein the bromine compound in an outlet of the reactor has a conversion of 90% or more.4. The method for producing bromine according to claim 1 , wherein a temperature at an outlet of the reactor is 250° C. to 400° C.5. The method for producing bromine according to claim 1 , wherein the catalyst is at least one type of metal or metal compound selected from the group consisting of ruthenium claim 1 , a compound of ruthenium claim 1 , copper claim 1 , a compound of copper claim 1 , titanium claim 1 , and a compound of titanium.6. The method for producing bromine according to claim 1 , wherein the reactor is an adiabatic reactor.7. The method for producing bromine according to claim 1 , wherein the reactor includes two or more catalyst packed beds connected in series.8. The method for producing bromine according to claim 7 , wherein a ...

Process for Treating Gasoline

The present application relates to a process for treating gasoline, comprising the steps of: splitting a gasoline feedstock into a light gasoline fraction and a heavy gasoline fraction; optionally, subjecting the resulting light gasoline fraction to etherification to obtain an etherified oil; contacting the heavy gasoline fraction with a mixed catalyst and subjecting it to desulfurization and aromatization in the presence of hydrogen to obtain a heavy gasoline product; wherein the mixed catalyst comprises an adsorption desulfurization catalyst and an aromatization catalyst. The process of the present application is capable of reducing the sulfur and olefin content of gasoline and at the same time increasing the octane number of the gasoline while maintaining a high yield of gasoline. 1. A process for treating gasoline , comprising:1) splitting a gasoline feedstock into a light gasoline fraction and a heavy gasoline fraction;2) optionally, subjecting at least a portion of the resulting light gasoline fraction to etherification to obtain an etherified oil; and3) contacting the resulting heavy gasoline fraction with a mixed catalyst and subjecting it to desulfurization and aromatization in the presence of hydrogen to obtain a heavy gasoline product;wherein the mixed catalyst comprises an adsorption desulfurization catalyst and an aromatization catalyst, and at least about 50 wt %, preferably at least about 80 wt %, more preferably at least about 90 wt %, particularly preferably at least about 95 wt %, and most preferably about 100 wt % of the aromatization catalyst has undergone a passivation and/or aging treatment.2. A process for treating gasoline , comprising:1) splitting a gasoline feedstock into a light gasoline fraction and a heavy gasoline fraction;2) subjecting at least a portion of the resulting light gasoline fraction to etherification to obtain an etherified oil; and3) contacting the resulting heavy gasoline fraction with a mixed catalyst and subjecting it ...

Reactive Scrubbing for Upgrading Product Value, Simplifying Process Operation and Product Handling

A method for removing formaldehyde from a blend of partially oxygenated hydrocarbons is provided. The method including a step of reacting a hydrocarbon-containing gas with an oxygen-containing gas in a reaction vessel to form first product blend. The first product blend includes a blend of partially oxygenated compounds that include formaldehyde. The blend of partially oxygenated compounds is provided to a reactive scrubbing station where it is contacted with a reactive scrubbing liquid to form a reactive liquid-formaldehyde compound. The reactive liquid-formaldehyde compound is then removed from the first blend of partially reactive compounds.

Process and Apparatus for Making Phenol and/or Cyclohexanone

A process for producing phenol and/or cyclohexanone by cleaving cyclohexylbenzene hydroperoxide in a loop cleavage reactor comprising multiple reaction zones connected in series. In desirable embodiments, fresh cyclohexylbenzene hydroperoxide feed(s) are supplied to reaction zones the final reaction zone, and fresh acid catalyst is supplied only to the final reaction zone. In desirable embodiments, a portion of the effluent exiting the final reaction zone is recycled to the first reaction zone. Each reaction zone is equipped with a heat exchanger downstream of the feed port to extract heat generated from the cleavage reaction. 1. A process for making phenol and/or cyclohexanone , the process comprising:(A) providing a cleavage reactor having a plurality of reaction zones connected in series, the reaction zones comprising a first reaction zone, a final reaction zone and optionally one or more intermediate reaction zone(s) between the first reaction zone and the final reaction zone; wherein:each of the reaction zones comprises a processed feed port, a fresh feed port, a heat exchanger at least partly downstream of the processed feed port and the fresh feed port in the same reaction zone, and an effluent port, except that the heat exchanger for the final reaction zone is optional;the effluent port of any given reaction zone other than the final reaction zone is in fluid communication with the processed feed port of the immediately following reaction zone in the series; andthe effluent port of the final reaction zone is in fluid communication with the processed feed port of the first reaction zone;(B) supplying a fresh reaction feed comprising cyclohexylbenzene hydroperoxide to each reaction zone other than the final reaction zone via the fresh feed port of the reaction zone and producing an effluent at the effluent port of the reaction zone;(C) supplying at least a portion of the effluent exiting the effluent port of each of the reaction zones other than the final ...

PROCESS FOR THE PRE-TREATMENT OF FEEDS FOR THE PRODUCTION OF BIOFUELS BY HYDROLYSIS OF FATS AT HIGH TEMPERATURE AND PRESSURE

A hydrotreating and isomerization pre-treatment process in a biofuel production plant, which is characterized in that it occurs from a raw supply consisting of an organic feed comprising secondary materials such as frying oils, category 1 animal fats, residual oils or by-products consisting of monoglycerides, diglycerides, triglycerides and free fatty acids, which is added to a recycling stream consisting of a mixture of mono-, di- and triglycerides free of impurities and exiting an esterification unit, said process occurring by means of hydrolysis with excess water, under controlled pressure and temperature conditions, thus obtaining the partial or total conversion of the supply into glycerol and fatty acids, the excess water introduced into the hydrolysis process acting as a solvent for impurities of various nature present in ionic form, thus removing most of the heavy metals, as well as of the chlorides present in said supply. 1. A hydrotreating and isomerization pre-treatment process in a biofuel production plant , characterized in that it is fulfilled from a raw stream consisting of an organic feed comprising secondary materials such as frying oils , category animal fats , residual oils or by-products consisting of monoglycerides , diglycerides , triglycerides and free fatty acids , which is added to a recycling stream consisting of a mixture of mono- , di- and triglycerides free of impurities and exiting an esterification unit , said process taking place by means of hydrolysis with excess water , under controlled pressure and temperature conditions , thus obtaining the partial or total conversion of the incoming feed into glycerol and fatty acids , the excess water introduced into the hydrolysis process acting as a solvent for impurities of various nature present in ionic form , thus removing most of the heavy metals , as well as of the chlorides contained in said incoming feed.2. A process according to claim 1 , wherein the water sent to the pre-treatment is ...

GENERATING METHANOL USING ULTRAPURE, HIGH PRESSURE HYDROGEN

In various implementations, methanol is produced using a (CO+H) containing synthesis gas produced from a combined PDX plus EHTR or a combined ATR plus EHTR at a pressure of 70 bar to 100 bar at the correct stoichiometric composition for methanol synthesis so that no feed gas compressor is required for the feed to the methanol synthesis reactor loop. 1. A method for producing methanol , comprising;producing oxygen in an air separation plant with air compressors driven by a gas turbine;heating a hydrocarbon feed stream using exhaust from the gas turbine;exothermically reacting a first portion of the heated hydrocarbon feed stream with at least one of steam or an oxidant gas comprising molecular oxygen to produce an exothermically generated syngas product;endothermically reforming a second portion of the hydrocarbon feed stream with steam over a catalyst in a heat exchange reformer to produce an endothermically-reformed syngas product, wherein at least a portion of heat used in generation of the endothermically-reformed syngas product is obtained by recovering heat from the exothermically-generated syngas product and the endothermically reformed syngas product;combining the exothermically generated syngas product and the endothermically-reformed syngas product to produce a combined syngas stream;producing steam in a waste heat boiler by cooling the combined syngas stream;separating water from the cooled combined syngas to produce a methanol plant feed at substantially reaction loop pressure;after separating water, passing the cooled combined syngas to a methanol plant; andcombining methanol plant combustible effluent with methane fuel to the gas turbine.2. The method of claim 1 , wherein the exothermically-generated syngas product is generated using a partial oxidation burner followed by a catalytic reforming section in a convectively heated steam plus hydrocarbon reformer.3. The method of claim 1 , wherein the hydrocarbon feed stream includes methane.4. The method of ...

METHOD FOR TREATING OFF GAS AND PRODUCING HYDROGEN

The present invention relates to a method for obtaining a hydrogen rich gas from an off gas. Further, the invention relates to a system for operating said method. 1. A method for treating an off gas , said off gas being a tail gas of a Fischer-Tropsch reaction , said method comprising the following steps:(1) feeding said off gas and an appropriate amount of steam to a reforming unit comprising a steam methane reforming reactor, obtaining a first effluent;(2) feeding said first effluent and optionally an appropriate amount of steam through a high, medium or low temperature shift reactor(s) or a combination thereof to convert at least part of the carbon monoxide and water into hydrogen and carbon dioxide, to obtain a second effluent;(3) optionally, removing bulk water from the second effluent obtained in steps (1) or (2);(4) feeding the second effluent of step (2)and/or (3) through a pressure swing adsorption (PSA) unit operated such that a hydrogen rich gas stream is obtained;wherein natural gas is added to the off gas and/or the first effluent obtained in step (1).2. The method according to wherein step 4 comprises the following steps:(A) feeding the second effluent obtained in step (2) and/or (3) through one or more columns in the PSA unit, said one or more columns comprising an adsorbent bed, wherein the adsorbent bed comprises alumina, a carbon molecular sieve, silicalite, activated carbon, a zeolite, or mixtures thereof,with upon commencement of said feeding, the bed and column being pre-saturated and pre-pressurized to a pressure in the range of 20 to 80 bar absolute (bar a), or comprising 80 to 99.9 volume % hydrogen, anddischarging a third effluent from the other end of said bed, andcontinuing said feeding and said discharging until a nitrogen and/or argon comprising gas has reached at least 45% of the length of the bed and has reached at most 80% of the length of the bed, calculated from the end of the bed at which the second effluent is being fed;(B) ...

METHODS AND SYSTEMS FOR PRODUCING ISOSORBIDE FROM BIOMASS

Methods and systems for producing isosorbide from biomass are disclosed. In one embodiment, a method of producing isosorbide from biomass may include contacting biomass, a catalyst mixture of a noble metal and a first solid acid, and hydrogen to form a first reaction mixture, and heating the first reaction mixture to form at least one intermediate compound. Further, the intermediate compound is contacted with a second solid acid to form a second reaction mixture, and heating the second reaction mixture to form isosorbide. 1. A method of producing isosorbide from a biomass , the method comprising:contacting biomass, a catalyst mixture of a noble metal and a first solid acid, and hydrogen to form a first reaction mixture;heating the first reaction mixture to form at least one intermediate compound;contacting the at least one intermediate compound with a second solid acid to form a second reaction mixture;heating the second reaction mixture to form isosorbide; andisolating the isosorbide.2. The method of claim 1 , wherein contacting the biomass comprises contacting a carbohydrate claim 1 , polysaccharide claim 1 , monosaccharide claim 1 , disaccharide claim 1 , cellulose claim 1 , lignin claim 1 , starch claim 1 , pentose claim 1 , or any combination thereof.3. The method of claim 1 , wherein heating the first reaction mixture comprises heating to form a depolymerization product of biomass selected from a monosaccharide claim 1 , a disaccharide claim 1 , sorbitol claim 1 , sorbitan claim 1 , or any combination thereof4. The method of claim 1 , further comprising removing the catalyst mixture from the at least one intermediate compound prior to contacting the at least one intermediate compound with the second solid acid.5. The method of claim 1 , wherein contacting the catalyst mixture comprises contacting the catalyst mixture comprising a noble metal including Au claim 1 , Pt claim 1 , Pd claim 1 , Ir claim 1 , Os claim 1 , Ag claim 1 , Rh claim 1 , Ru claim 1 , or any ...

SYSTEM AND METHOD FOR THE PRODUCTION OF ALKENES BY THE DEHYDROGENATION OF ALKANES

Disclosed is a method and plant for the catalytic dehydrogenation of alkanes, such as propane. The plant is a plant of hybrid architecture wherein one or more membrane-assisted reactor configurations according to open architecture are combined with one or more membrane-containing reactors of closed architecture. Hydrogen remaining in the reaction mixture after separation in the membrane separation unit of a first open architecture configuration, is fed to a first membrane-reactor of the closed architecture type. Also disclosed are methods of modifying plants so as to create the hybrid architecture plant. 1. A method for the production of an alkene by the dehydrogenation of a corresponding alkane , comprising the steps of:(i) providing a hydrocarbon source comprising at least one alkane;(ii) subjecting, in a first reactor system, the hydrocarbon source to a first dehydrogenation reaction in the presence of a dehydrogenation catalyst, so as to form a first reaction mixture comprising hydrogen, unreacted alkane, and an initial yield of the alkene corresponding to said at least one alkane;(iii) in a first separation step, subjecting the reaction mixture to membrane separation so as to obtain a permeate comprising hydrogen and a retentate comprising an alkene-enriched reaction mixture;(iv) feeding said alkene enriched reaction mixture to a second reactor system, wherein unreacted alkane comprised in said reaction mixture is subjected to a second dehydrogenation reaction in the presence of a dehydrogenation catalyst so as to form a second reaction mixture comprising hydrogen and a further yield of the alkene corresponding to said at least one alkane;(v) in a second separation step subjecting the second reaction mixture to membrane separation so as to remove hydrogen, thereby producing a further alkene-enriched reaction mixture;wherein the first dehydrogenation reaction and the first separation step are conducted in separate reaction and separation units, and the second ...

SYSTEM AND METHOD FOR PREPARING VANADIUM BATTERY HIGH-PURITY ELECTROLYTE

A system and method for preparing a vanadium battery high-purity electrolyte, comprising preparing a low-valence vanadium oxide with a valence of 3.5 with liquid phase hydrolysis and fluidization reduction with vanadium oxytrichioride, adding clean water and sulfuric acid for dissolution, and further performing ultraviolet activation to obtain the vanadium electrolyte, for use in an all-vanadium redox flow battery stack. The high-temperature tail gas in the reduction fluidized bed is combusted for preheating the vanadium powder material, to recover the sensible heat and latent heat of the high-temperature tail gas, and the sensible heat of the reduction product is recovered through heat transfer between the reduction product and the fluidized nitrogen gas. An internal member is arranged in the reduction fluidized bed to realize the precise regulation of the valence state of the reduction product, and ultraviolet is used to activate the vanadium ions, improving the activity of the electrolyte. 14. A system for preparing a vanadium battery high-purity electrolyte , comprising a vanadium oxytrichloride storage tank , a liquid phase hydrolysis device , a vanadium pentoxide feeding device , a preheating system () , a reduction fluidized bed , a combustion chamber , a cooling system , a secondary cooling system , a low-valence vanadium oxide feeding device , a dissolution reactor and an activation device;wherein the liquid phase hydrolysis device comprises a liquid phase hydrolysis reaction tank and a washing filter;the vanadium pentoxide feeding device comprises a vanadium pentoxide hopper and a vanadium pentoxide screw feeder;the preheating system comprises a venturi preheater, a primary cyclone preheater, a secondary cyclone preheater and a bag-type dust collector;the reduction fluidized bed comprises a feeder, a bed body, a discharger, a gas heater, a gas purifier and a first cyclone separator;the cooling system comprises a venturi cooler, a cyclone cooler and a ...

A SYSTEM AND METHOD FOR PRODUCING HIGH-PURITY AND HIGH-ACTIVITY VANADIUM ELECTROLYTE

A system and method for producing a high-purity and high-activity vanadium electrolyte, comprising converting high-purity vanadium oxytrichloride into an ammonium salt in a fluidized bed by gas phase ammoniation, then in another fluidized bed, reducing the ammonium salt into a low-valence vanadium oxide having an average vanadium valence of 3.5, adding clean water and sulfuric acid for dissolution, and further performing activation by ultrasound to obtain a 3.5-valence vanadium electrolyte which can be directly used in a new all-vanadium redox flow battery stack. The method of producing an ammonium salt containing vanadium in the fluidized bed by gas phase ammoniation is of short process and high efficiency. Precise regulation of the valence state of the reduction product is implemented by arranging an internal member in the reduction fluidized bed, and ultrasonication is used to activate the vanadium ion, thereby greatly improving the activity of the electrolyte. 1. A system for producing a high-purity and high-activity vanadium electrolyte , comprising a vanadium oxytrichloride storage tank , a gas phase ammoniation fluidized bed , a reduction fluidized bed , a pre-cooling device , a secondary cooling device , a low-valence vanadium oxide feeding device , a dissolution reactor , and an activation device;wherein the gas phase ammoniation fluidized bed comprises a vanadium oxytrichloride vaporizer, a purified ammonia liquor vaporizer, a chloride spray gun, a gas phase ammoniation fluidized bed body, a first cyclone separator, and an ammonium chloride settling tower;the reduction fluidized bed comprises a material valve, a bed body, a discharger, a gas heater, a gas purifier, and a second cyclone separator;the pre-cooling device comprises a cyclone cooler and a third cyclone separator;the low-valence vanadium oxide feeding device comprises a low-valence vanadium oxide hopper and a low-valence vanadium oxide screw feeder;wherein a feed outlet at the bottom of the ...

Methods and apparatuses for detection of properties of fluid conveyance systems

A system and method for monitoring and/or detecting the flow of one or more fluids in a fluid system including leak detection system integral to the fluid system (e.g., at any point along a conduit, at a connection between conduits such as at a fitting assembly, etc.) configured to detect incipient, early stage levels of the leak. Based on one or more factors related to the fluid and/or the leak, the methods, devices, and systems disclosed herein can provide an indication of a suitable action or process in response to the fluid or the leak including performing preventative maintenance or providing an indication of the need of maintenance in response to the leak.

SELECTIVE HYDROXYL GROUP REMOVAL FROM ALKYLPHENOLS

A process for selective removal of hydroxyl groups from phenolic compounds is disclosed. The process uses a combination of catalytic hydrodeoxygenation and catalytic direct deoxygenation to convert alkylphenols into alkylbenzenes. 1. A process for removing hydroxyl groups from phenolic compounds , the process comprising:providing in a first reactor at least one hydrodeoxygenation catalyst containing sulphided NiMo, CoMo or NiW;providing a feedstock containing phenolic compounds;carrying out hydrodeoxygenation by contacting the feedstock with the hydrodeoxygenation catalyst to obtain a phenolic hydrocarbon feedstock;providing in a second reactor at least one direct deoxygenation catalyst containing Pt/Nb2O5;forming a mixture by feeding into the second reactor the phenolic hydrocarbon feedstock and hydrogen gas; andcarrying out direct deoxygenation to the phenolic hydrocarbon feedstock to obtain hydrocarbons, wherein at least 50 mol-% of the hydroxyl groups originally bonded to phenolic compounds are removed while the aromaticity of the hydrocarbon is preserved.2. The process of claim 1 , wherein the hydrodeoxygenation is carried out at a temperature in a range 270-380° C. claim 1 , at a hydrogen pressure in a range 30-100 bar and WHSV of 2-0.5 1/h.3. The process of claim 1 , wherein the direct deoxygenation is carried out at a temperature in a range of 340-450° C. claim 1 , at a hydrogen pressure in a range 15-50 bar.4. The process of claim 1 , wherein the phenolic hydrocarbon feedstock contains alkylphenols.5. The process of claim 4 , wherein alkylphenols are converted to alkylbenzenes during direct deoxygenation.6. The process of claim 1 , wherein the phenolic hydrocarbon feedstock is contacted with the catalyst in liquid phase.7. The process of claim 1 , comprising:obtaining the feedstock from lignocellulosic biomass.8. The process of claim 1 , wherein no water or hydrogen sulfide is added in the first and second reactors during the performance of the process.9. A ...

POLYETHYLENE HOMOPOLYMER COMPOSITIONS HAVING GOOD BARRIER PROPERTIES

A polyethylene homopolymer composition comprises: a first ethylene homopolymer having a density, dof from 0.943 to 0.975 g/cm, a melt index, Iof from 0.01 to 10 g/10 min, and a molecular weight distribution, Mw/Mn of less than 3.0; and a second ethylene homopolymer having a density, dof from 0.950 to 0.985 g/cm, a melt index, Iof at least 500 g/10 min, and a molecular weight distribution, M/Mof less than 3.0; wherein the ratio of the melt index, Iof the second ethylene homopolymer to the melt index, Iof the first ethylene homopolymer is at least 50. The polyethylene homopolymer compositions which may be nucleated have a weight average molecular weight, Mof ≤75,000, a high load melt index, Iof at least 200 g/10 min, a molecular weight distribution, M/Mof from 4.0 to 12.0 and may be usefully employed in molding applications, such as, for example, in compression molded closures.

SYSTEM AND METHOD FOR PRODUCTION OF HYDROCARBONS FROM CARBON DIOXIDE

A system and method for producing liquid hydrocarbons is disclosed. In one embodiment, the system includes at least one renewable power system configured to generate a DC electric power output; at least one water electrolysis system in electrical communication with the renewable power system and configured to utilize the DC electric power to produce a hydrogen output; and a liquid hydrocarbon synthesis system in fluid communication with the water electrolysis system and configured to utilize the hydrogen output and a carbon dioxide feed to produce a liquid hydrocarbon product.

Process and system for producing light olefins from inferior oils

A process for producing light olefins from inferior oils includes the steps of: subjecting an inferior oil to a thermal conversion reaction in the presence of hydrogen to obtain a conversion product; separating the conversion product to obtain a first separated product; separating the first separated product to obtain an upgraded oil and a pitch; subjecting the upgraded oil to hydro-upgrading to obtain a hydro-upgraded oil; separating the hydro-upgraded oil to obtain a hydro-upgraded heavy oil; and subjecting the hydro-upgraded heavy oil to catalytic cracking to obtain a catalytic cracking product comprising a light olefin.

PROCESS AND PLANT FOR PRODUCING METHANOL

The invention relates to a process for producing methanol and to a plant for producing methanol. A first fresh gas suitable for production of methanol is precompressed by a first compressor stage to obtain a second fresh gas. The second fresh gas is merged with a recycle gas stream and further compressed to synthesis pressure in a second compressor stage. Catalytic conversion of the thus obtained synthesis gas stream in a plurality of serially arranged reactor stages with intermediate condensation and separation of the crude methanol reduces the recycle gas amount in the synthesis circuit to such an extent that recycle gas may be directly recycled to the second fresh gas stream, thus ensuring that no recycle gas compressor stage is required and that the total compressor power may be reduced. 1. A process for producing methanol , comprising:a) providing an input gas comprising carbon oxides and hydrogen;b) introducing the input gas as a first fresh gas stream into a first compressor stage for precompression of the first fresh gas stream to obtain a second fresh gas stream;c) introducing a recycle gas stream and the second fresh gas stream into a second compressor stage for compression of the recycle gas stream and the second fresh gas stream to synthesis pressure to obtain a synthesis gas stream;d) catalytically converting the synthesis gas of the synthesis gas stream in a plurality of serially arranged reactor stages at synthesis pressure to obtain a product stream comprising methanol and unreacted synthesis gas per reactor stage;e) cooling the product stream obtained per reactor stage for condensation and separation of methanol from unreacted synthesis gas and introducing unreacted synthesis gas into a respective subsequent stage of the serially arranged reactor stages; andf) withdrawing unreacted synthesis gas from at least one of the reactor stages as a recycle gas stream for introduction of the recycle gas stream into the second compressor stage according to ...

PROCESS AND PLANT FOR PRODUCING METHANOL FROM SYNTHESIS GASES HAVING A HIGH PROPORTION OF CARBON DIOXIDE

The invention relates to a process for producing methanol and to a plant for producing methanol. A first fresh gas suitable for production of methanol and having a high carbon dioxide content is pre-compressed by a first compressor stage to obtain a second fresh gas. The second fresh gas is merged with a recycle gas stream and further compressed to synthesis pressure in a second compressor stage. Catalytic conversion of the thus obtained synthesis gas stream in a plurality of serially arranged reactor stages with intermediate condensation and separation of the crude methanol reduces the recycle gas amount in the synthesis circuit to such an extent that recycle gas may be directly recycled to the second fresh gas stream, thus ensuring that no recycle gas compressor stage is required and that the total compressor power may be reduced. 1. A process for producing methanol , comprising:a) providing an input gas comprising carbon oxides and hydrogen, wherein the proportion of carbon dioxide in the input gas, based on the total amount of the carbon oxides, is at least 80% by volume;b) introducing the input gas as a first fresh gas stream into a first compressor stage for precompression of the first fresh gas stream to obtain a second fresh gas stream;c) introducing a recycle gas stream and the second fresh gas stream into a second compressor stage for compression of the recycle gas stream and the second fresh gas stream to synthesis pressure to obtain a synthesis gas stream;d) catalytically converting the synthesis gas of the synthesis gas stream in a plurality of serially arranged reactor stages at synthesis pressure to obtain a product stream comprising methanol and unreacted synthesis gas per reactor stage;e) cooling the product stream obtained per reactor stage for condensation and separation of methanol from unreacted synthesis gas and introducing unreacted synthesis gas into a respective subsequent stage of the serially arranged reactor stages;f) withdrawing ...

STAGGERED FIRED HEATER MANIFOLDS

A hydrocarbon conversion process is described. The process includes passing a hydrocarbon stream through a plurality of reaction zones and a plurality of fired heaters, the effluent from a first reaction zone passing through one of the plurality of fired heaters before entering a second reaction zone. The plurality of fired heaters include a radiant section, an inlet manifold, an outlet manifold, at least one heater tube having an inlet and an outlet, the inlet being in fluid communication with the inlet manifold and the outlet being in fluid communication with the outlet manifold, and at least one burner, the inlet manifold of one of the plurality of fired heaters being at a vertical height different from a vertical height of at least one of the other inlet manifolds or at least one of the outlet manifolds. 1. A hydrocarbon conversion process comprising: 'a radiant section, an inlet manifold, an outlet manifold, at least one heater tube having an inlet and an outlet, the inlet being in fluid communication with the inlet manifold and the outlet being in fluid communication with the outlet manifold, and at least one burner, the inlet manifold of one of the plurality of fired heaters being at a vertical height different from a vertical height of at least one of the other inlet manifolds or at least one of the outlet manifolds.', 'passing a hydrocarbon stream through a plurality of reaction zones and a plurality of fired heaters, an effluent from a first reaction zone passing through one of the plurality of fired heaters before entering a second reaction zone, the plurality of fired heaters comprising2. The process of wherein the inlet and outlet manifolds of one of the fired heaters are at the vertical height different from the vertical height of the inlet and outlet manifolds of at least one other fired heater.3. The process of wherein the inlet and outlet manifolds of two of the fired heaters are at the vertical height different from the vertical height of the inlet ...

METHOD TO OBTAIN METHYLENE MALONATE VIA BIS(HYDROXYMETHYL) MALONATE PATHWAY

Method to obtain methylene malonate and related monomers following a bis(hydroxymethyl) malonate pathway. A bis(hydroxymethyl) malonate intermediary is subsequently reacted (i.e., subjected to thermolysis) to provide a methylene malonate monomer species. A source of formaldehyde (e.g., formalin) is provided in the presence of a basic catalyst (e.g., calcium hydroxide), to which a malonate (e.g., diethyl malonate) is added under suitable reaction conditions to obtain the desired intermediary (e.g., dialkyl bis(hydroxymethyl) malonate). The intermediary is reacted (i.e., subjected to thermolysis) under suitable conditions in the presence of a suitable catalyst (e.g., a zeolite) to obtain a methylene malonate monomer. In an exemplary embodiment, the thermolysis reaction includes the addition of the bis(hydroxymethyl) malonate intermediary onto a heated catalyst. The reaction product is collected and purified. The disclosed methods may be performed in a continuous operation. Discrete steps may be performed by using modular units within a plant. 162-. (canceled)63. A plant for producing a methylene malonate monomer comprising:at least one diol production unit comprising a diol reactor apparatus capable of reacting a dialkyl malonate ester and a source of formaldehyde in the presence of a catalyst,at least one diol purification unit,at least one monomer production unit comprising a plurality of catalyst columns and at least one heating apparatus for maintaining the temperature of the plurality of catalyst columns, andat least one monomer purification unit comprising a condensation apparatus, a fractional distillation apparatus, or both;wherein the at least one diol production unit is in communication with the at least one diol purification unit, and the at least one diol purification unit is in communication with the at least one monomer production unit, and the at least one monomer production unit is in communication with the at least one monomer purification unit.6473-. ...

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

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

Process for Reducing Unsaturated Hydrocarbons in Aromatic Fraction Through Selective Hydrogenation

Disclosed are a process and system that are capable of performing selective hydrogenation on aromatic fractions by configuring a catalyst bed through staged loading of a plurality of hydrogenation catalysts with different catalytic properties, or configuring a catalyst system in which a plurality of hydrogenation catalysts are arranged using a plurality of reactors in such a way as to be equivalent with the staged loading, and as a result, are capable of suppressing aromatic loss while improving the selective removal of unsaturated hydrocarbons in the aromatic fraction and durability compared to the case of using a single catalyst. 1. A method of removing unsaturated hydrocarbons in an aromatic fraction , which comprises:a) providing an aromatic hydrocarbon-containing feedstock having a bromine index of at least 30, andb) bringing the feedstock into contact with a multi-stage catalyst bed comprising at least one first catalyst bed and a second catalyst bed disposed downstream of the first catalyst bed in a reactor and performing hydrogenation under supply of hydrogen to form an aromatic hydrocarbon-containing product having a reduced bromine index,wherein,the first catalyst bed comprises a support containing inorganic oxide, and at least one active metal selected from the group consisting of Ni, Pd, Pt, Ru, Re, Co, Mo, Co—Mo, Ni—Mo, and Ni—W, in which, among the active metals, each of Re, Co, Mo, and Co—Mo is a reduced or sulfide form, and each of Ni, Pd, Pt, Ru, Ni—Mo and Ni—W is a sulfide form, andthe second catalyst bed comprises a support containing inorganic oxide, and Ni—Mo and/or Ni—W in a reduced form as an active metal.2. A method of removing unsaturated hydrocarbons in an aromatic fraction , which comprises:a) providing an aromatic hydrocarbon-containing feedstock having a bromine index of at least 30, andb) transferring the feedstock to a multi-stage hydrogenation unit comprising a first reaction unit containing at least one first catalyst and a second ...

METHOD AND SYSTEM FOR PRODUCING A SYNTHESIS GAS USING AN OXYGEN TRANSPORT MEMBRANE BASED REFORMING SYSTEM WITH SECONDARY REFORMING AND AUXILIARY HEAT SOURCE

A method and system for producing a synthesis gas in an oxygen transport membrane based reforming system is disclosed that carries out a primary reforming process within a reforming reactor, and a secondary reforming process within an oxygen transport membrane reactor and in the presence of heat generated from a oxygen transport membrane reactor and an auxiliary source of heat. The auxiliary source of heat is disposed within the reactor housing proximate the reforming reactors and may include an auxiliary reactively driven oxygen transport membrane reactor or a ceramic burner. 112-. (canceled)13. An oxygen transport membrane based reforming system comprising:a reactor housing;a reforming reactor disposed in the reactor housing and configured to reform a hydrocarbon containing feed stream in the presence of a reforming catalyst disposed in the reforming reactor and heat to produce a reformed synthesis gas stream;a reactively driven oxygen transport membrane reactor disposed in the reactor housing proximate the reforming reactor and configured to receive the reformed synthesis gas stream and react a portion of the reformed synthesis gas stream with permeated oxygen and generate a reaction product and heat, including a first portion of the heat required by the reforming reactor;wherein the reactively driven, catalyst containing oxygen transport membrane reactor is further configured to reform any unreformed hydrocarbon gas in the reformed synthesis gas stream in the presence of some of the heat and the reaction product generated by the reaction of the reformed synthesis gas stream and permeated oxygen to produce a synthesis gas product stream; andan auxiliary heat source disposed in the reactor housing proximate the reforming reactor and configured to supply a second portion of the heat required by the reforming reactor through the radiation mode of heat transfer to produce the reformed synthesis gas stream, wherein the auxiliary heat source provides between about 15% ...

System for Making a Composition of Matter

A system for making a composition of matter that may include a neutralization reactor; an oil phase mixer or preparation vessel; an aqueous phase mixer or preparation vessel; an emulsifier; a homogenizer or comparable; a polymerization reactor, which may be a tube reactor; and an inversion vessel or comparable. The system may be suitable to make or otherwise produce the composition that includes by weight percent about: 15-25% oil phase; 35-50% water; 20-35% polymer; 0-10% surfactant; and 0-3% other trace materials. 1. A system for making a composition of matter , the system comprising;a neutralization reactor configured to produce an at least 99% ammonium acrylate neutralization product, wherein the neutralization reactor is operated under pressure, controlled to a neutralization reaction temperature in the range of about 65° F. to about 70° F., and has a bulk reaction residence time of about 0.1 minutes to about 5 minutes;an oil phase mixer configured to mix an oil-based material, and a blend of sorbitan monooleate and a non-ionic, oil soluble primary surfactant;an aqueous phase mixer configured to receive the at least 99% ammonium acrylate neutralization product, and mix with a monomer solution to form an aqueous phase product, wherein the aqueous phase mixer is controlled to produce the aqueous phase product having a pH of about 6.9 to about 7.1;an emulsifier operated under batch conditions, the emulsifier configured to receive the oil phase product first, and then the aqueous phase product second, and to form a water-in-oil emulsification characterized by having oil as a continuous phase and water as a dispersed phase;a homogenizer configured to receive the water-in-oil emulsification, and form an emulsification product comprising micelles having a bulk average diameter of about 0.1 microns to about 1 micron;a polymerization reactor configured to receive the emulsification product and an initiator, and upon reaction to produce a polymerization reaction product, ...

PLANT FOR THE SYNTHESIS OF MELAMINE WITH OFFGAS RECOVERY IN A TIED-IN UREA PLANT

Plant for the synthesis of melamine starting from urea, wherein the stream of offgas containing NHand CO2 produced by the synthesis of melamine is converted into urea in a dedicated urea plant. 1) A melamine-urea plant comprising:a melamine plant (MEL) for the production of melamine starting from urea, obtaining a product stream containing melamine and a stream of offgas containing NH3 and CO2 in gaseous form;a offgas-fed urea plant (UR) dedicated to the synthesis of urea starting from said stream of offgas, said offgas-fed urea plant being apt to produce urea starting from ammonia and CO2, and comprising at least a high-pressure synthesis section running at a synthesis pressure and a recovery section running at a recovery pressure lower than said synthesis pressure,wherein said stream of offgas provides at least 90% of ammonia and CO2 supply of said offgas-fed urea plant.2) The plant according to claim 1 , wherein said stream of offgas provides the sole supply of ammonia and CO2 of said offgas-fed urea plant.3) The plant according to claim 1 , wherein all or part of the urea produced by said offgas-fed urea plant supplies said melamine plant.4) The plant according to claim 1 , wherein the offgas-fed urea plant further includes a concentration section arranged to receive a urea solution effluent from the recovery section and to produce a concentrated solution or a urea melt containing at least 95% urea.5) The plant according to claim 4 , wherein the offgas-fed urea plant further includes a finishing section to produce solid urea.6) The plant according to claim 1 , comprising:a first urea plant, which is a main urea plant and comprises at least a high-pressure synthesis section running at a synthesis pressure and a recovery section running at a recovery pressure lower than said synthesis pressure,a second urea plant, which is said offgas-fed urea plant,wherein the urea supply of said melamine plant is produced at least in part by said main urea plant.7) The plant ...

METHODS AND APPARATUSES FOR PROCESSING BIORENEWABLE FEEDSTOCKS WITH REDUCED EXTERNAL SULFIDING AGENT INPUT

Methods and apparatuses for processing biorenewable feedstocks are disclosed. In accordance with one exemplary embodiment, a method for processing a biorenewable feedstock includes the steps of combining an untreated, diesel boiling range petroleum distillate feedstock comprising sulfur with the biorenewable feedstock to form a combined feedstock and contacting the combined feedstock with a deoxygenation catalyst in the presence of hydrogen gas to form a deoxygenated, biorenewable product. 1. A method for processing a biorenewable feedstock comprising the steps of:combining an untreated, diesel boiling range petroleum distillate feedstock comprising sulfur with the biorenewable feedstock to form a combined feedstock; andcontacting the combined feedstock with a deoxygenation catalyst in the presence of hydrogen gas to form a deoxygenated, biorenewable product.2. The method of claim 1 , wherein the step of combining comprises combining sufficient untreated claim 1 , diesel boiling range petroleum distillate feedstock with the biorenewable feedstock to form a combined feedstock comprising at least about 150 wt. ppm sulfur.3. The method of claim 2 , wherein the step of combining comprises combining sufficient untreated claim 2 , diesel boiling range petroleum distillate feedstock with the biorenewable feedstock to form a combined feedstock comprising at least about 500 wt. ppm sulfur.4. The method of claim 1 , further comprising the step of passing the combined feedstock through a guard bed prior to the step of contacting.5. The method of claim 1 , wherein the step of contacting is performed in a single-pass or once-through manner.6. The method of claim 1 , further comprising the step of contacting the deoxygenated claim 1 , biorenewable product with an isomerization catalyst in the presence of hydrogen gas to form an isomerized claim 1 , biorenewable product.7. The method of claim 6 , wherein the step of contacting the deoxygenated claim 6 , biorenewable product with ...

Methods and apparatuses for hydroprocessing hydrocarbons

Methods and apparatuses for hydroprocessing a hydrocarbon stream are provided herein. In an embodiment, a method of hydroprocessing the hydrocarbon stream includes hydrocracking the hydrocarbon stream in a first hydrocracking stage in the presence of a first hydrocracking catalyst to produce a first conversion stream. Components from the first conversion stream are treated in a downstream processing stage in the presence of a downstream resid hydrotreating catalyst to produce a second conversion stream.

REVERSE ACID AND HYDROCARBON CASCADING IN ALKYLATION

A cascade reactor scheme with acid and hydrocarbon flowing in reverse directions. The systems and processes for alkylation of olefins herein may include providing a first olefin to a first alkylation zone, and a second olefin to a second alkylation zone. Isoparaffin may be provided to the first alkylation zone. The isoparaffin and first olefin may be contacted with a partially spent sulfuric acid in the first alkylation zone to form a spent acid phase and a first hydrocarbon phase including alkylate and unreacted isoparaffin. The first hydrocarbon phase and second olefin may be contacted with a sulfuric acid feed in the second alkylation zone to form a second hydrocarbon phase, also including alkylate and unreacted isoparaffin, and the partially spent sulfuric acid that is fed to the first alkylation zone. Further, the second hydrocarbon phase may be separated, recovering an isoparaffin fraction and an alkylate product fraction. 1. A system for the alkylation of olefins , the system comprising:a first flow line for providing a first olefin to a first alkylation zone;a second flow line for providing a second olefin to a second alkylation zone, wherein the second olefin may be the same or different than the first olefin;a third flow line for providing an isoparaffin to the first alkylation zone;the first alkylation zone, for contacting the isoparaffin and the first olefin with a partially spent sulfuric acid under alkylation conditions to form a spent acid phase and a first hydrocarbon phase comprising alkylate and unreacted isoparaffin;the second alkylation zone for contacting the first hydrocarbon phase and the second olefin with a fresh sulfuric acid feed under alkylation conditions to form a second hydrocarbon phase, comprising alkylate and unreacted isoparaffin, and the partially spent sulfuric acid fed to the first alkylation zone; anda separator for separating the second hydrocarbon phase to recover an isoparaffin fraction and an alkylate product fraction.2. ...

Process for Preparing Fluorobenzene Derivatives and Benzoic Acid Hypofluorite Derivatives

The invention relates to a use of a fluorination gas, and the elemental fluorine (F) is preferably present in a high concentration, for example, in a concentration of elemental fluorine (F), especially of equal to much higher than 15% or even 20% by volume, and to a process for the manufacture of a fluorinated benzene derivative starting from benzoic acid derivative by direct fluorination employing a fluorination gas, wherein the elemental fluorine (F) is preferably present in a high concentration, and subsequent decarboxylation of the benzoic acid hypofluorite derivative obtained by direct fluorination. The process of the invention is also directed to the manufacture of a benzoic acid hypofluorite derivative by direct fluorination of benzoic acid derivative. Especially the invention is of interest in the preparation of fluorinated benzene derivative, final products and as well intermediates, for usage in agro-, pharma-, electronics-, catalyst, solvent and other functional chemical applications. 1. A process for the manufacture of a fluorinated benzene derivative , preferably monofluorobenzene derivative , wherein the process comprises the steps of:a) provision of a liquid medium comprising benzoic acid derivative as starting compound;{'sub': '2', 'b) provision of a fluorination gas comprising or consisting of elemental fluorine (F), preferably wherein the fluorine is present in the fluorination gas in a high concentration of at least substantially more than, in particular very much more than 15% by volume (vol.-%), preferably equal to or more than 20% by volume (vol.-%);'}{'sub': '2', 'c) provision of a first reactor or reactor system, resistant to elemental fluorine (F) and hydrogen fluoride (HF);'}{'sub': '2', 'd) in a step of direct fluorination, passing the fluorination gas of b), in a reactor or reactor system of c), through the liquid medium of a) comprising the benzoic acid derivative as starting compound, and thereby reacting the benzoic acid derivative ...

Catalytic Alkane Conversion and Olefin Separation

Disclosed is a hydrocarbon conversion process that is less energy intensive than comparable processes. The hydrocarbon conversion process is particularly desirable for converting alkanes, such as methane into C 2+ olefins, such as ethylene and propylene, particularly with increasing selectivity to ethylene production. It is also desirable for effectively removing a C 2 composition (i.e., ethane, ethylene and/or acetylene) produced from the catalytic conversion of hydrocarbon comprised of C 2+ olefins. In addition, the hydrocarbon process is desirable for providing a substantially non-cryogenic separation of the desired C 2 compositions from the hydrocarbons (e.g., methane) present in the reaction mixture.

Catalytic Alkane Conversion

Disclosed is a hydrocarbon conversion process in which an alkane component is catalytically converted in the presence of an oxygen or oxidizing component (i.e., oxidant). The hydrocarbon conversion process can be an oxidative coupling reaction, which refers to the catalytic conversion of alkane in the presence of oxidant to produce an olefin product, i.e., a composition containing Colefin. Reverse-flow reactors can be used to carry out the oxidative coupling reaction. 1. An alkane conversion process , comprising:(a) providing a first flow, the first flow comprising alkane and oxidant and having an alkane : oxidant molar ratio ≧2.0;(b) providing a catalytic flow-through reactor configured to accept the first flow, the catalytic flow-through reactor comprising at least one hydrocarbon conversion catalyst and at least one thermal mass, wherein (i) the hydrocarbon conversion catalyst has an initial average temperature in the range of 550° C. to 1100° C., (ii) at least a first portion of the thermal mass is located downstream of the hydroconversion catalyst with respect to the first flow's flow direction, and (iii) the first portion of the thermal mass has an initial average temperature such that the hydroconversion catalyst's initial average temperature minus the first portion of the thermal mass's initial average temperature is ≧50° C.; the catalytic conversion includes catalytically transferring hydrogen from the alkane to the oxidant and', 'the reaction mixture comprises (i) olefin produced by the catalytic transfer and (ii) any unreacted alkane and/or any unreacted oxidant;, '(c) catalytically converting at least a portion of the alkane in the presence of the hydrocarbon conversion catalyst to produce a reaction mixture, wherein'}(d) quenching the reaction mixture in the flow-through reactor by transferring heat from the reaction mixture to the thermal mass at a location downstream of the hydroconversion catalyst, downstream being with respect to the first flow's ...

SYSTEMS AND METHODS FOR PROCESSING GASES

The invention includes a gas processing system for transforming a hydrocarbon-containing inflow gas into outflow gas products, where the system includes a gas delivery subsystem, a plasma reaction chamber, and a microwave subsystem, with the gas delivery subsystem in fluid communication with the plasma reaction chamber, so that the gas delivery subsystem directs the hydrocarbon-containing inflow gas into the plasma reaction chamber, and the microwave subsystem directs microwave energy into the plasma reaction chamber to energize the hydrocarbon-containing inflow gas, thereby forming a plasma in the plasma reaction chamber, which plasma effects the transformation of a hydrocarbon in the hydrocarbon-containing inflow gas into the outflow gas products, which comprise acetylene and hydrogen. The invention also includes methods for the use of this gas processing system. 1. A method for processing a methane-containing inflow gas to produce outflow gas products , comprising directing the methane-containing inflow gas into a system comprising: a gas delivery subsystem , a plasma reaction chamber , a microwave subsystem , a vacuum subsystem , and an effluent separation and disposal subsystem; wherein the gas injector comprises an injector body comprising two or more separate gas feeds, a first gas feed conveying the methane-containing inflow gas into the plasma reaction chamber through a first set of one or more nozzles, and a second gas feed conveying a hydrogen-rich reactant gas into the plasma reaction chamber through a second set of one or more nozzles,', 'wherein the delivery conduit is in fluid communication with the gas injector, wherein the delivery conduit comprises a feed gas conveying circuit that delivers the methane-containing inflow gas into the gas injector, and', 'wherein the delivery conduit further comprises an auxiliary gas conveying circuit that delivers the hydrogen-rich reactant gas into the gas injector, and', 'wherein the methane-containing inflow gas ...

PROCESS AND PLANT FOR PRODUCING OLEFINS FROM OXYGENATES

A process for producing olefins from oxygenates can include the following steps: (i) heterogeneously catalyzed conversion of at least one oxygenate to a product stream containing Colefins, Colefins, Colefins, Chydrocarbon compounds, and C hydrocarbon compounds; and (ii) separation of a propylene stream consisting of Colefins for at least 95 wt-%, wherein at least 10 wt-% of the propylene stream are recirculated into process step (i). 2. The process according to claim 1 , wherein more than 90 wt-% of the propylene stream are recirculated into process step (i).3. The process according to claim 1 , wherein at least a part of the Chydrocarbon compounds and/or of the C hydrocarbon compounds are recirculated into process step (i) claim 1 , wherein the amount of aromatic compounds in the recirculated Cand/or C hydrocarbon compounds is ≦5 wt-%.4. The process according to claim 1 , wherein a Cstream is separated from the product stream and that up to 90 wt-% of this Cstream are recirculated into process step (i).5. The process according to claim 1 , wherein the ratio of the molar sum of the recirculated olefins to the molar sum of the oxygenates lies between 0.1 and 3.6. The process according to claim 1 , wherein the heterogeneously catalyzed conversion is effected in two stages claim 1 , wherein in the first stage methanol is converted into dimethyl ether and in the second stage dimethyl ether is converted to the product stream containing Colefins claim 1 , Colefins claim 1 , Colefins claim 1 , Chydrocarbon compounds and C hydrocarbon compounds.7. The process according to claim 6 , wherein that methanol and water are separated from the product stream and that methanol is recirculated to before the first stage and/or water in the form of steam is recirculated to before the second stage of the heterogeneously catalyzed conversion.8. The process according to claim 6 , wherein the second stage of the heterogeneously catalyzed conversion is operated at a temperature of 390° C. ...

REGENERATOR FOR CATALYSTS

The present invention concerns a moving bed catalyst regenerator () comprising a vessel () extending in a vertical direction, said vessel being divided into at least two regeneration zones extending along the vertical height of said vessel, in which particles of catalyst move under gravity, the regenerator being configured such that each regeneration zone is capable of separately regenerating a different composition of catalyst and in which each regeneration zone comprises, in succession and in the order in which the catalysts move: 112. A moving bed catalyst regenerator () comprising a vessel () extending in a vertical direction , said vessel being divided into at least two regeneration zones extending along the vertical height of said vessel , in which particles of catalyst move under gravity , the regenerator being configured such that each regeneration zone is capable of separately regenerating a different composition of catalyst and in which each regeneration zone comprises , in succession and in the order in which the catalysts move:a) a combustion section (CO);b) an oxychlorination section (O) disposed below the combustion section and comprising means for bringing catalyst from the combustion section (CO) to the oxychlorination section (O);c) a calcining section (CA) disposed below the oxychlorination section.2. The regenerator according to claim 1 , in which each of the combustion sections comprises an annular space defined by two sieves which are permeable to gas and impermeable to catalysts in which the catalyst moves under gravity.330309934. The regenerator according to claim 1 , in which each of the combustion sections is formed by a portion of an annular space () claim 1 , the annular space () being defined by two sieves ( claim 1 , ′) which are permeable to gas and impermeable to catalysts and divided into portions by separation means () which are impermeable to catalysts claim 1 , said portions each being capable of containing a catalyst with a ...

A Process for Producing Hydrogen and Graphitic Carbon from Hydrocarbons

In accordance with the present invention, there is provided a process for producing hydrogen and graphitic carbon from a hydrocarbon gas comprising: contacting at a temperature between 600° C. and 1000° C. the catalyst with the hydrocarbon gas to catalytically convert at least a portion of the hydrocarbon gas to hydrogen and graphitic carbon, wherein the catalyst is a low grade iron oxide. 1. A process for producing hydrogen and graphitic carbon from a hydrocarbon gas comprising:contacting at a temperature between 600° C. and 1000° C. the catalyst with the hydrocarbon gas to catalytically convert at least a portion of the hydrocarbon gas to hydrogen and graphitic carbon, wherein the catalyst is a low grade iron oxide.2. A process for producing hydrogen and graphitic carbon according to claim 1 , wherein the pressure is greater than atmospheric pressure.3. A process for producing hydrogen and graphitic carbon according to claim 1 , wherein the pressure is 0 bar to 100 bar.4. A process for producing hydrogen and graphitic carbon according to claim 1 , wherein the temperature is between 700° C. and 950° C.5. A process for producing hydrogen and graphitic carbon according to claim 1 , wherein the temperature is between 800° C. and 900° C.6. A process for producing hydrogen and graphitic carbon according to claim 1 , wherein the temperature is between 650° C. and 750° C.7. A process for producing hydrogen and graphitic carbon according to claim 1 , wherein the hydrocarbon gas is methane.8. A process for producing hydrogen and graphitic carbon according to claim 1 , wherein the hydrocarbon gas is natural gas.9. A process for producing hydrogen and graphitic carbon according to claim 1 , wherein claim 1 , the contacting the catalyst with the hydrocarbon gas is performed in a plurality of pressurized reactors arranged in series.10. A process for producing hydrogen and graphitic carbon according to claim 1 , wherein the arrangement of the reactors in series allows gas to ...

MANUFACTURING HYDROCARBONS

Systems and a method for manufacturing a base stock from a hydrocarbon stream are provided. An example method includes cracking the hydrocarbon stream to form a raw product stream, separating an ethylene stream from the raw product stream, and oligomerizing the ethylene stream to form a raw oligomer stream. A Light olefinic stream is distilled from the raw oligomer stream and oligomerized the light olefinic stream with the ethylene stream. A heavy olefinic stream is distilled from the raw oligomer stream. The heavy olefinic stream is to form a hydro-processed and distilled to form the base stock. 1. A system for manufacturing a base stock from a hydrocarbon stream , comprising:a steam cracker configured to form a raw product stream from the hydrocarbon stream;a purification system configured to separate an ethylene stream from the raw product stream;an oligomerization reactor configured to oligomerize the ethylene stream to form a raw oligomer stream;a distillation column configured to separate the raw oligomer stream into:a light olefinic stream, wherein the distillation column is configured to blend the light olefinic stream with the ethylene stream provided to the oligomerization reactor;an intermediate olefinic stream; anda heavy olefinic stream;a hydro-processing reactor configured to hydro-process the heavy olefinic stream to form a hydro-processed stream; anda product distillation column configured to separate the hydro-processed stream to form the base stock.2. The system of claim 1 , comprising a dimerization reactor configured to dimerize the intermediate olefinic stream and return a dimerized stream to the distillation column.3. The system of claim 1 , comprising an alkylation reactor configured to alkylate the intermediate olefinic stream and provide an alkylated stream to an alkylation distillation column.4. The system of claim 3 , wherein the alkylation distillation column is configured to separate an unreacted olefin stream from the alkylated stream ...

System And Process For The Production Of Renewable Fuels And Chemicals

A renewable fuel production system includes a carbon dioxide capture unit for extracting carbon dioxide from atmospheric air, a carbon dioxide electrolyzer for converting carbon dioxide to carbon monoxide, a water electrolyzer for converting water to hydrogen, a synfuels generator for converting carbon monoxide produced by the carbon dioxide electrolyzer and hydrogen produced by the water electrolyzer to a fuel. The fuel produced can be synthetic gasoline and/or synthetic diesel. A renewable fuel production process includes the steps of extracting carbon dioxide from atmospheric air via a carbon dioxide capture unit, converting carbon dioxide to carbon monoxide via a carbon dioxide electrolyzer, converting water to hydrogen via a water electrolyzer, and converting carbon monoxide produced via the carbon dioxide electrolyzer and Hproduced via the water electrolyzer to a fuel. The system is also capable of simultaneously or alternatively producing a separate industrial chemical. 1. A system for the manufacture of renewable fuels and/or renewable chemicals comprising:{'sub': 2', '2', '2', '2, '(a) a COelectrolyzer for converting COto CO and O, wherein said COelectrolyzer has a CO selectivity of at least 40%;'}{'sub': 2', '2', '2, '(b) a separate water electrolyzer for converting HO to Hand O;'}{'sub': '2', '(c) a control unit for directing signals to each of said electrolyzers to vary the ratio of CO to Hproduced by said electrolyzers; and'}{'sub': '2', '(d) a series of reactors to convert the CO/Hmixture to fuels and/or chemicals,'}{'sub': '2', 'wherein said COelectrolyzer operates in the temperature range of 40° C. to 120° C.'}2. The system of wherein the selectivity is at least 50%.3. The system of wherein the selectivity is at least 60%.4. The system of wherein the selectivity is at least 70%.5. The system of wherein the selectivity is at least 80%.6. The system in claim 1 , wherein the system is capable of producing at least one fuel and at least one chemical.7. ...

Low sulfur biodiesel composition and method of making

The invention provides fatty acid methyl ester fuel compositions and methods of making same.

Transalkylation System

The invention relates to a transalkylation system to convert feedstreams containing benzene and/or toluene (C7− aromatic hydrocarbons) and feedstreams containing C9+ aromatic hydrocarbons into a product stream comprising xylenes.

APPARATUS AND METHOD FOR PRODUCING CARBON NANOFIBERS FROM LIGHT HYDROCARBONS

A process and apparatus for producing carbon nanofibers. The process comprises two stages. The first stage involves oxidizing light hydrocarbon with carbon dioxide or water, or oxygen, or a combination thereof to a mixture of hydrogen and carbon monoxide. The second stage involves converting the produced hydrogen and the carbon monoxide to carbon nanofibers and steam. In this way, greenhouse gases may be reduced by using carbon dioxide and methane (and/or other light hydrocarbons) as reactants; and useful products may be produced, such as Carbon NanoFibers (CNF). 137.-. (canceled)38. A process for producing carbon nanofibers , the process comprising:in a first reactor, reacting a light hydrocarbon stream with an oxidizing agent to perform reforming reaction to produce an intermediate gas stream comprising hydrogen and carbon monoxide; andin a subsequent second reactor, converting the produced hydrogen and the carbon monoxide selectively to carbon nanofibers that build up inside the second reactor, and steam which exits the second reactor.39. The process of claim 38 , further comprising: separating claim 38 , using a separator claim 38 , the unreacted portions of COand the light hydrocarbon from the intermediate gas stream; and recycling the separated unreacted portions of COand the light hydrocarbon into the first reactor.40. The process of claim 39 , wherein the step of separating the unreacted portions of COand the hydrocarbon from the converted gas stream from the first reactor is carried out using a membrane separator.41. The process according to claim 38 , wherein the first reactor is configured to enable dry catalytic reforming of the hydrocarbon.42. The process according to claim 38 , wherein the process of conversion in the first reactor is carried out at a temperature between about 480° C. and about 850° C. claim 38 , and at a pressure up to about 5 MPa.43. The process according to claim 38 , wherein the hydrocarbon is methane.44. The process according to ...

PROCESSES AND APPARATUSES FOR TOLUENE METHYLATION IN AN AROMATICS COMPLEX

This present disclosure relates to processes and apparatuses for toluene methylation in an aromatics complex for producing paraxylene. More specifically, the present disclosure relates to processes and apparatuses wherein a toluene methylation zone is integrated within an aromatics complex for producing paraxylene thus allowing no benzene byproduct to be produced. This may be accomplished by incorporating a toluene methylation process into the aromatics complex and recycling the benzene to the transalkylation unit the aromatics complex. 1. A process for producing paraxylene with no benzene byproduct , comprising:{'sub': 9', '10, 'passing a lighter aromatic stream containing benzene and a heavier aromatic stream containing C-Caromatic compounds to a transalkylation zone;'}{'sub': '8', 'subjecting the lighter aromatic stream and the heavier aromatic stream in the transalkylation zone to transalkylation conditions including the presence of a first catalyst to provide a transalkylation product stream having a greater concentration of toluene to Caromatics;'}{'sub': 8', '9+, 'separating by fractionation from the transalkylation product stream a first boiling fraction comprising benzene, a second boiling fraction comprising toluene, a third boiling fraction comprising Caromatics and a fourth boiling fraction comprising C aromatics;'}recycling at least a portion of the benzene from the transalkylation product stream back to the transalkylation zone;passing at least a portion of the second boiling fraction from steps c, g and i and a methanol stream to a toluene methylation zone operating under toluene methylation conditions to produce a toluene methylation product stream;separating by fractionation from the toluene methylation product stream the same fractions described in step c{'sub': 8', '8, 'subjecting at least a portion of the third boiling fraction comprising Caromatics of steps c, g and i to a separation zone to selectively remove a para-xylene product and provide a ...

System and Method for Monitoring and Controlling a Polymerization System

The present disclosure relates generally to a system having a reactor system with a polymerization reactor and a feed system fluidly coupled to a feed inlet of the reactor. The feed system supplies components to the reactor via the feed inlet, and the reactor has a flow path that continuously conveys the components through the reactor and subjects the components to polymerization conditions to produce a polymer. The system also has an analysis system coupled to the reactor for online monitoring of a particle size of the polymer. Further, the system includes a control system, coupled to the analysis and feed systems, that receives a signal from the analysis system indicative of the monitored particle size of the polymer and adjusts an operating parameter of the feed system to control a flow rate of at least one of the components to the reactor based at least on the signal. 1. A polymerization system , comprising:a reactor system comprising a polymerization reactor and a feed system fluidly coupled to a feed inlet of the polymerization reactor, wherein the feed system is configured to supply polymerization components to the polymerization reactor via the feed inlet, and the polymerization reactor comprises a flow path configured to continuously convey the polymerization components through an interior of the polymerization reactor and configured to subject the polymerization components to polymerization conditions to produce a polymer slurry comprising polymer particles;an analysis system coupled to the polymerization reactor along the flow path, wherein the analysis system is configured to monitor a particle size of the polymer; anda control system coupled to the analysis system and the feed system, wherein the control system is configured to receive a signal from the analysis system indicative of the monitored particle size of the polymer particles, and is configured to adjust an operating parameter of the feed system to control a flow rate of at least one of the ...

Slurry Loop Reactor Bad Catalyst Range Control

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

Slurry Loop Reactor Polymerization Rate and Quality Controller

A process and system for maintaining optimum polymerization production in a loop polymerization reactor by continuously and periodically obtaining polymerization results, such as melt index (MI), production rate and ash content of the polymer produced, determining whether each of the results is within desired ranges, storing and averaging recently obtained results in a database within a reaction rate controller program, and when one of the results is out of the desired range modifying at least one reaction parameter set-point such as monomer concentration, catalyst feed rate and reactor temperature to drive any out-of-range polymerization result(s) toward the desired range for that result. 1. A process for optimizing polymerization of a monomer in a loop polymerization reactor controlled by a reaction rate controller program , comprising:continuously and periodically obtaining polymerization results comprising at least melt index (MI), production rate and ash content on the polymerized monomer;the reaction rate controller program (RRC):determining whether each of the polymerization results is within predetermined target ranges for those results;storing recently obtained polymerization results in a computer readable database stored within the RRC, and averaging the recently obtained results with previously stored results; andwhen at least one of the polymerization results is out-of-range with respect to its predetermined target range, modifying at least one reaction parameter set-point comprising monomer concentration, catalyst feed rate and reactor temperature, and controlling associated hardware for modifying reaction parameter set-point(s) to drive any out-of-range polymerization result(s) toward the predetermined target range for that result.2. The process of claim 1 , further comprising the RRC assessing the reasonableness of the MI result when the MI result is out-of-range claim 1 , and if the result is unreasonable claim 1 , retaining it for comparison to ...

USE OF DUPLEX STAINLESS STEEL IN AN AMMONIA-STRIPPING OF UREA PLANTS

In an ammonia stripping or self-stripping plant for the synthesis of urea, it is disclosed that a shell-and-tube stripper has a bundle of tubes made of a duplex stainless steel 29Cr-6.5Ni-2Mo—N according to UNS S32906 or 27Cr-7.6Ni-1 Mo-2.3W—N according to UNS S32808. A revamping of urea plants is also disclosed, including the revamping of ammonia stripping plants, self-stripping plants and conventional total recycle plants, wherein said duplex stainless steel is used for the tubes of the stripper. 1. A shell-and-tube stripper , for use in an ammonia stripping plant or self-stripping plant for the synthesis of urea , said stripper comprising a shell and a bundle of tubes , and being arranged to provide the stripping of a carbamate solution fed to said tubes by means of heat and optionally by means of ammonia as a stripping medium , said stripper being characterized in that the tubes are made of a duplex stainless steel which is one of the following: 'or:', 'A) the Safurex® steel 29Cr-6.5Ni-2Mo—N, which is also designated by ASME Code 2295-3 and by UNS 532906,'}B) the DP28W™ steel 27Cr-7.6Ni-1Mo-2.3W—N, which is also designated by ASME Code Case 2496-1 and by UNS 532808.2. The stripper according to claim 1 , for operation at a temperature of around 205° C. and a pressure of 140 to 160 bar.3. The stripper according to claim 1 , said stripper being of falling-film type.4. A plant for the synthesis of urea according to the ammonia stripping or thermal stripping process claim 1 , comprising a high-pressure synthesis loop which includes a synthesis reactor claim 1 , a shell-and-tube stripper claim 1 , and a condenser claim 1 , wherein said stripper is in accordance with .5. The plant according to claim 4 , comprising a feed line arranged to feed a stream containing oxygen at the bottom of the stripper.6. The plant according to claim 5 , said feed line of a stream containing oxygen being a dedicated air feed line directed to the bottom of the stripper.7. The plant ...

INTEGRATED PROPANE DEHYDROGENATION PROCESS

Processes and systems for the integrated production of propylene and an alkylate, such as cumene, may include feeding a hydrocarbon feedstock containing propane to a propane dehydrogenation reaction zone to convert a portion of the propane to propylene. The propylene is separated in a separation system to form a polymer-grade propylene stream, a low purity propylene stream, and a propane stream. The low purity propylene stream is then fed to an alkylation reaction zone where the propylene is reacted to produce an alkylated product and generate a low pressure steam. The low pressure steam may then be fed to the separation system as a heat source, integrating the dehydrogenation system and the alkylation system. 1. A process for the production of cumene comprising:feeding a hydrocarbon feedstock comprising propane to a propane dehydrogenation reaction zone, converting a portion of the propane to propylene, forming a dehydrogenated effluent;separating the dehydrogenated effluent in a separation system, forming a polymer-grade propylene stream, a low purity propylene stream, and a propane stream;feeding the low purity propylene stream to an alkylation reaction zone, wherein propylene is reacted with benzene to concurrently produce an alkylated product and generate a low pressure steam stream; andfeeding the low pressure steam stream to the separating step as a heat source.2. The process of claim 1 , further comprising recycling the propane stream to the propane dehydrogenation reaction zone.3. The process of claim 1 , further comprising separating the alkylated product into one or more of a benzene stream claim 1 , a C3 stream claim 1 , a cumene product stream claim 1 , and a heavies effluent claim 1 , wherein the C3 stream comprises one or more of propane and propylene.4. The process of claim 3 , wherein the separating comprises recovering the C3 stream at a higher pressure than an operating pressure of the propane dehydrogenation reaction zone.5. The process of claim ...

THERMAL CONVERSION VESSEL USED IN A PROCESS FOR AMIDIFICATION OF ACETONE CYANOHYDRIN

The invention relates to a thermal conversion vessel () used during amidification step of acetone cyanohydrin (ACH), in the industrial process for production of a methyl methacrylate (MMA) or methacrylic acid (MAA). The thermal conversion vessel () is used for converting an hydrolysis mixture of α-hydroxyisobutyramide (HIBAM), α-sulfatoisobutyramide (SIBAM), 2-methacrylamide (MACRYDE) and methacrylique acid (MAA), into a mixture of 2-methacrylamide (MACRYDE). It comprises: 1200. A thermal conversion vessel () for converting an hydrolysis mixture of α-hydroxyisobutyramide (HIBAM) , α-sulfatoisobutyramide (SIBAM) , 2-methacrylamide (MACRYDE) and methacrylic acid (MAA) , into a mixture comprising 2-methacrylamide (MACRYDE) , wherein said vessel comprises:{'b': 1', '2', '3', '206', '206', '206', '1', '1', '1, 'i': a', 'b', 'i', 'a', 'b', 'c, 'at least three compartments (C, C, C, . . . Ci) comprising an inner wall (, , . . . ) separating said compartments into at least three communicating parts (C, C, C, . . . Ci) by a passage provided between the bottom of the vessel and said inner wall,'}said compartments having a space above said inner wall, for separating a gas phase from a liquid phase during thermal conversion,{'b': 204', '204', '204, 'i': a', 'b', 'i, 'said compartments being connected to an outlet valve (, , . . . ).'}2123205205205204204204abiabi. The thermal conversion vessel according to wherein said vessel comprises at least three compartments (C claim 1 , C claim 1 , C claim 1 , . . . Ci) separated from each other by an overflow wall ( claim 1 , claim 1 , . . . claim 1 , ) claim 1 , over which the hydrolysis mixture to be converted flows to pass from one compartment to the other claim 1 , each compartment being connected to an outlet valve ( claim 1 , claim 1 , . . . ).3205205205206206206abiabi. The thermal conversion vessel of claim 2 , wherein the height (h) of either overflow walls ( claim 2 , claim 2 , . . . claim 2 , ) or inner walls ( claim 2 , claim 2 ...

PLANT FOR THE PRODUCTION OF METHANOL FROM SYNTHESIS GAS RICH IN INERTS

During the production of methanol from inert-rich syngas, a catalytic pre-reactor is installed upstream of the single- or multi-stage synthesis loop, a first part of the syngas being converted to methanol in the catalytic pre-reactor. An inert gas separation stage, for example a pressure swing adsorption system or a membrane system, can be connected downstream of the synthesis loop, whereby a hydrogen-enriched syngas stream can be returned to the synthesis loop. In the processing of methane-rich syngas, the inert gas separation stage may also have an autothermal reformer in which methane is converted to carbon oxides and hydrogen, which are also returned into the synthesis loop. 1. A plant for the production of methanol from a synthesis gas containing hydrogen , one or more carbon oxides , and one or more inert components , the plant comprising:a methanol pre-reactor in which a first part of the carbon oxides is catalytically converted to methanol;a methanol main reactor in which a second part of the carbon oxides is catalytically converted to methanol;a first separator, downstream of the methanol pre-reactor, configured to separate the methanol from the synthesis gas;a second separator, downstream of the methanol main reactor, configured to separate further methanol from the synthesis gas;a conduit configured to recirculate a synthesis gas cycle stream to the methanol main reactor;an inert gas separation stage;a conduit configured to supply synthesis gas from the methanol main reactor to the inert gas separation stage;a conduit configured to discharge a purge stream from the inert gas separation stage; anda conduit configured to recirculate a recirculation stream, depleted of one or more inert components, to the methanol main reactor.2. The plant of claim 1 , comprising a first and a second methanol pre-reactor.3. The plant of claim 1 , comprising a first and a second methanol main reactor.4. The plant of claim 3 , wherein the first methanol main reactor in flow ...

Cavitation Generation Ring, Apparatus for Producing Carbon-Based Fuel, and Method for Producing Carbon-Based Fuel

A cavitation generation ring configured to be housed in a part of a liquid communicating pipe, an apparatus for producing carbon-based fuel using the cavitation generation ring, and a production method of carbon-based fuel are disclosed. The production method comprises a petroleum decomposing step for decomposing a molecule of petroleum by cavitation, a water decomposing step for decomposing a molecule of water by cavitation, and a different-molecules composing step for composing the decomposed molecule of petroleum and the decomposed molecule of water by cavitation.