СПОСОБ ГАЗОФАЗНОЙ ПОЛИМЕРИЗАЦИИ ОЛЕФИНОВ

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

ТВЕРДОЖИДКОСТНАЯ РЕАКЦИЯ

Изобретение относится к химической промышленности и может быть использовано для получения простых или сложных эфиров или смешанных ангидридов кислот. Способ проведения твердожидкостной реакции включает: а) получение реакционной суспензии, в которой первый реагент находится в суспендированной форме, а второй реагент находится в растворенной форме в суспензионной среде, причем один из продуктов реакции является нерастворимым в суспензионной среде, б) прохождение реакционной суспензии через удлиненную реакционную зону, таким образом, что число Рейнольдса потока составляет меньше чем 20000, в) отделение образовавшегося нерастворимого продукта реакции. Технический результат изобретения заключается в том, что нерастворимый продукт реакции получают в форме, которая легко фильтруется. 13 з.п. ф-лы, 1 ил.

СПОСОБ И УСТРОЙСТВО ДЛЯ ОСУЩЕСТВЛЕНИЯ РЕАКЦИИ В ЖИДКОЙ СРЕДЕ С ВЫДЕЛЕНИЕМ ГАЗА

Изобретение может быть использовано в химической промышленности, в частности, для осуществления реакции с использованием пероксида, такого как пероксид водорода, и, в частности, для восстановления хлора, содержащегося в жидком эфлюенте. Сущность изобретения: устройство содержит, по меньшей мере, статический смеситель, сообщающийся, по меньшей мере, с одним питающим трубопроводом для подачи в него жидкой среды; реактор циклонного типа, соединенный с указанным статическим смесителем и оборудованный вытяжной трубой для удаления образующегося(ихся) газа(ов) и средствами удаления жидкой среды. Настоящее изобретение касается также способа осуществления реакции в жидкой среде, во время которой происходит выделение газа. Изобретение позволяет осуществлять реакцию в условиях абсолютной безопасности, с одной стороны, и повысить кинетику, КПД и производительность, с другой. 2 н. и 24 з.п. ф-лы, 1 ил.

СПОСОБ ПОЛУЧЕНИЯ УКСУСНОЙ КИСЛОТЫ

Изобретение относится к получению уксусной кислоты карбонилированием метанола и/или его реакционноспособного производного. Уксусную кислоту получают введением монооксида углерода через регулирующий клапан при непрерывной подаче сырья предпочтительно при 10-100 атм и 100-300oС. В реакторе содержится жидкая реакционная смесь, включающая по меньшей мере 5 мас.% метилацетата, от 0,1 до 30 мас.% воды, 1-30 мас.% метилиодида, благородный металл группы VIII в качестве катализатора, необязательно по меньшей мере один промотор и уксусную кислоту, составляющую остальную часть смеси. При проведении процесса дозируют поток монооксида углерода посредством регулирующего клапана и выполняют фоновый расчет для получения усредненной по времени объемной скорости потока монооксида углерода с добавлением постоянного значения к усредненной по времени объемной скорости потока монооксида углерода, в результате чего получают максимально допустимые объемные скорости потока моноокисда углерода. Информацию, содержащую ...

СПОСОБ ПОЛУЧЕНИЯ ДИИЗОЦИАНАТОВ В ГАЗОВОЙ ФАЗЕ

Изобретение относится к способу получения диизоцианатов общей формулы R(NCO)n, в которой R означает (цикло)алифатический углеводородный радикал, содержащий до 15 атомов углерода, предпочтительно, от 4 до 13 атомов углерода, при условии, что между двумя изоцианатными группами NCO находится, по меньшей мере, два атома углерода, а n означает число 2, фосгенированием соответствующих аминов общей формулы R(NH2)n, в которой R имеет вышеуказанное значение, в газовой фазе в трубчатом реакторе с подачей в него предварительно нагретых фосгена и аминов. При этом для фосгенирования используют трубчатый реактор, содержащий центрично расширяющуюся в направлении оси вращения трубчатого реактора двухстенную направляющую трубу, причем между внутренней и внешней стенками двухстенной направляющей трубы образован концентрический кольцевой зазор, а отношение площади поперечного сечения трубчатого реактора, ограниченной внутренней стенкой двухстенной направляющей трубы, к площади поперечного сечения трубчатого ...

РЕАКТОР СИНТЕЗА МОЧЕВИНЫ

Изобретение относится к реактору для синтеза мочевины, имеющему вертикальный корпус и по меньшей мере одну внутреннюю перфорированную перегородку (3), расположение которой обеспечивает формирование секций в реакторе. Указанная перегородка содержит решетку отдельных перфорированных плиток (10), из которых каждая плитка (101) имеет боковые стенки (101A-101D) и лицевую поверхность (101F), причем по меньшей мере одна из боковых стенок имеет первые перфорационные отверстия, лицевая поверхность имеет вторые перфорационные отверстия, размер которых меньше размера первых перфорационных отверстий, а плитки распределены по перегородке в виде двухмерной матрицы с зазорами (17) между соседними плитками. Первые перфорационные отверстия образуют в реакторе путь предпочтительного протекания жидкой фазы, а вторые перфорационные отверстия образуют путь предпочтительного протекания паровой фазы. Также предложены способ синтеза мочевины из аммиака и диоксида углерода и способ модернизации вертикального реактора ...

КАТАЛИТИЧЕСКИЙ РЕАКТОР С НИСХОДЯЩИМ ПОТОКОМ

... 1. Каталитический реактор с нисходящим потоком, имеющий множество слоев катализатора, в которые проходит смесь газа и жидкости, причем область между последовательными слоями катализатора снабжена распределительной системой для распределения и смешивания газа и жидкости перед контактом со следующим слоем катализатора, и указанная область содержит (a) линию нагнетания газа, расположенную ниже поддона для поддержания катализатора, (b) собирающий поддон, приспособленный для приема газа и жидкости, (c) коллекторы слива, продолжающиеся выше уровня указанного собирающего поддона и снабженные выходными отверстиями для прохождения газа и жидкости, причем указанные выходные отверстия приспособлены для придания вихревого движения выходящим газу и жидкости, (d) камеру смешения, приспособленную для приема и поддержания вихревого движения газа и жидкости, спускающихся от указанных коллекторов слива, (e) отбойник ниже указанной камеры смешения, приспособленный для направления потока в радиальном направлении ...

СПОСОБ ПОЛУЧЕНИЯ ГОМОПОЛИМЕРОВ ИЛИ СОПОЛИМЕРОВ ЭТИЛЕНА

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

СПОСОБ И УСТАНОВКА ДЛЯ ПОЛУЧЕНИЯ ПОЛИМЕРОВ И СОПОЛИМЕРОВ НА ОСНОВЕ ЭТИЛЕНА

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

СПОСОБ И СИСТЕМА УПРАВЛЕНИЯ УСТАНОВКОЙ ПО НЕПРЕРЫВНОМУ ПРОИЗВОДСТВУ ПОЛИМЕРА

СПОСОБ БЫСТРОГО И РАВНОМЕРНОГО НАНЕСЕНИЯ ПОКРЫТИЯ

СИСТЕМА И СПОСОБ ПОЛУЧЕНИЯ КАТАЛИЗАТОРА

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

ТВЕРДО-ЖИДКОСТНАЯ РЕАКЦИЯ

... 1. Способ проведения твердо-жидкостной реакции, включающий получение реакционной суспензии, в которой первый реагент находится в суспендированной форме, а второй реагент находится в растворенной форме в суспензионной среде, причем один из продуктов реакции является нерастворимым в суспензионной среде, прохождение реакционной суспензии через удлиненную реакционную зону, таким образом, что число Рейнольдса потока составляет меньше чем 20000, и отделение образовавшегося нерастворимого продукта реакции. 2. Способ по п.1, отличающийся тем, что число Рейнольдса потока составляет меньше чем 10000. 3. Способ по п.1 или 2, отличающийся тем, что продольная ось реакционной зоны является вертикальной. 4. Способ по п.1 или 2, отличающийся тем, что реакционную суспензию, получают путем смешивания суспензии первого реагента в суспензионной среде с жидким или растворенным вторым реагентом. 5. Способ по п.4, отличающийся тем, что время нахождения реакционной суспензии в реакционной зоне, по крайней мере ...

Verfahren zur Herstellung von Sulfaminsaeurederivaten

Wasserstoffgenerator mit thermischem Siphonreaktor und thermischer Siphonreaktor

Thermischer Siphonreaktor, umfassend: ein Reaktionsrohr, in dem eine katalytische Reaktion einer Reaktionsquelle stattfindet; und eine Katalysatorschicht, die porös ist, und Gaserzeugung ermöglicht, indem sie mit der Reaktionsquelle in Kontakt steht und in dem Reaktionsrohr platziert ist, wobei in dem Reaktionsrohr ein Konvektionskanal, durch den ein Reaktionsprodukt ausgetragen wird, durch das Reaktionsrohr in Längsrichtung des Reaktionsrohrs durchläuft.

Mass exchange column for counter-current treatment of gases and liquids

The invention relates to a mass exchange column for treating gases, in particular exhaust gases, and liquids, having at least one internal gas distribution plate (10), on which is formed a solids-air jet of defined layer height, having a bottom gas inlet (2) and top gas outlet (3), having lines (8, 9) for the liquid of the solids-air jet, the orifices of which lines are arranged at the level of the solids-air jet. A design is proposed in which the orifices (11a) of the lines (11) removing the liquid from a solids-air jet and having a spacing equivalent to the height of the solids-air jet layer are advantageously arranged to be adjustable in height over the gas distributor plate (10). ...

Reaktionsvorrichtung fuer stetigen Betrieb

Verfahren zur Herstellung von Propylencopolymeren

Polymerisationsverfahren und Vorrichtung zu ihrer Durchfuehrung

Übergang von kontinuierlicher zu diskontinuierlicher Prozeßstufe, Verfahren und Vorrichtung

VERFAHREN ZUR HERSTELLUNG EINES GESCHAEUMTEN POLYAMIDS

Verfahren zur kontinuierlichen Umsetzung von Cyanurfluorid mit Aminen.

HYDROGENIERUNG VON LANGKETTIGEN OLEFINISCHEN OELEN MIT EINEM RANEY-KATALYSATOR.

VERFAHREN UND VORRICHTUNG ZUR BEHANDLUNG EINES WÄSSRIGEN MEDIUMS

VERFAHREN ZUR HERSTELLUNG VON METHYLFORMIAT

Verfahren und Vorrichtung zur Durchführung einer Reaktion zwischen gasförmigen und festen Reaktanten in einer fluidisierten Partikelschicht

In order to allow gaseous and solid reactants to react in a fluidized particle layer a fluidizing gas normally flows through a loose pile of primary particles lifting the pile and thereby creating a fluidized particle layer and reacting with said primary particles. A procedure whereby a solid powder loaded stream (11) is accelerated to supersonic speeds by means of a supersonic nozzle (4) and a carrier gas and is blown in transversally to the main stream direction of flow of the fluidizing gas in the fluidized particle layer is also known in prior art. In order to increase the solid load and the depth of penetration of the carrier gas stream (11), a carrier gas stream (11) which first exits the supersonic nozzle (4) and comprises a solid powder, is blown via a diffuser (2) disposed opposite to said supersonic nozzle (4) into a fluidized particle layer. In this invention a simple and operationally secure reactor is provided in order to perform said method characterized in that it has a supersonic ...

ELEKTROMAGNETISCH ASSISTIERTE CHEMISCHE BEHANDLUNG

VERFAHREN UND GERÄT ZUM VORHERSAGEN VON POLYMER-LATEX EIGENSHAFTEN IN EINEM EMULSIONSPOLYMERISATIONPROZESS ZUR QUALITÄT UND PRODUKTIVITÄTVERBESSERUNG DER POLYMERLATEX

Verfahren zur Durchfuehrung thermischer Zersetzungen

WIRBELBETTGRANULIERVORRICHTUNG

Graphite-based double-walled reaction vessel for - continuous (physical) chemical processes, with high

Heating or cooling media are brought to pressure by passage through circular segments, then passed through a double-wall fitted to a graphite reaction vessel. The reaction column is divided by fixed or loose installations e.g. perforated trays, bubble-plates, etc., of the required size, so that remixing is prevented, and optimum conditions are attained. Photochemical reactns. may be induced by rays of UV light passed through opening in the column wall e.g. of quartz, and when suitable measuring and regulating instruments are switched on the reactn. may proceed continuously. In an example, the apparatus has been used in the preparation of the insecticide "Melipax" by UV-induced reactn. between camphene and Cl2.

Control of gas composition

Improvements relating to the refining of waste oil

Improvements in and relating to the spraying of materials

... 559,594. Spray-producers. SCHORI METALLIZING PROCESS, Ltd. (Dowson and Dobson, Ltd.). Aug. 25, 1942, No. 11943. [Class 69 (iii)] A spraying process consists in spraying the material in a finely divided or atomized condition through an annular heating flame consisting of acetylene and, as a comburent atmospheric air as distinct from oxygen as hithertofore, the annular heating flame being surrounded by an outer annular jet of compressed air to shape and stabilize the flame. The process may be carried-out in apparatus as described in Specification 432,831.

METHOD OF REMOVING HEAT GENERATED IN THE POLYMERIZATION OF MONOMERS IN THE GAS PHASE

... 1354020 Polymerization BADISCHE ANILIN- & SODA-FABRIK AG 7 Oct 1971 [9 Oct 1970] 46671/71 Heading C3P Heat is removed from polymerization reactions of monomers in the gaseous phase by a process in which gaseous or liquid monomer and optionally heat transfer agent is introduced into the polymerization zone and polymer is removed -therefrom and gaseous monomer, optionally together with heat-transfer agent, is removed from the polymerization zone, at least partially liquefied by cooling under the pressure prevailing in the polymerization zone and reintroduced in the liquid state into the polymerization zone, the polymerization temperature being kept constant by regulating the rate of reintroduction of the condensate which is stored as necessary after condensation and before reintroduction. The process may be applied to the polymerization of C 2 -C 6 olefins in the prescence of titanium halide/aluminium alkyl catalysts and vinyl chloride in the presence of peroxides or azo compounds. Apparatus ...

Improvements in or relating to regenerative heat-recovering methods for carrying outgaseous chemical reactions

... Gaseous chemical reactions are carried out by a regenerative heat-recovery method in which the gaseous reactants are compressed to a superatmospheric pressure and passed through a heat regenerative mass, where they are preheated, to a reaction zone, the reaction products being led through a second heat regenerative mass to which they give up heat, and then into a turbine where the pressure energy is utilized; the direction of gas flow through the regenerator masses and reaction zone is periodically reversed. Before passing to the turbine, the product gas may be treated to remove dust, moisture, or a chemical constituent. The heat regenerative masses consist of packing material which provides narrow passages for the gas, and may contain a catalyst. In the apparatus shown, waste oxygen-containing gas to be purified is compressed at C and led through regenerative mass R1 to reaction zone L, while a gaseous fuel, e.g. water gas, is compressed at C1, flows through regenerative ...

MULTISTAGE REACTOR

Method of continuously performing reactions between gases and liquid

... In a continuous process for performing reactions between gases and liquids, liquid is forced by a pump 2 from a container 1 along a vertical flow path formed by reaction tubes 6 and connecting tubes 7. Gas from a container 3 is introduced into the liquid by an injector 4. A valve 8 at the entrance to a collecting chamber 10 controls the pressure in the flow path. The connecting tubes are so dimensioned that the speed of the mixture is greater than that at which gas mixes in the liquid. A modified arrangement comprises three sets of reaction tubes and connecting tubes in series, the first being heated, the third cooled and the second kept at constant temperature, two additional gas injectors being provided in this zone. Every reaction tube may have an injector and additional pumps may be interposed between the tubes.

Improvements in or relating to chemical reactions

In a method for the continuous reaction of at least two fluid reagents, at least one of which is in the gaseous phase and at least one of which is in the liquid phase, at least one of the reaction products being liquid, the liquid reagent entering at 14 flows downwardly over the vertical inner surface of cylinder 2, the temperature of which is controlled by cooling fluids flowing in the space(s) between cylinders 1 and 2, and comes into contact meanwhile with the gaseous reagent which enters cylinder 3 by pipe 8, leaves cylinder 3 by slots 9 and flows downwardly in a helical path into which it is directed by diaphragm 7. A cooling fluid flows in the lower part of cylinder 3. Liquid reaction products leave at 15 and gaseous reaction products at 16. The thickness of the liquid film may be controlled by adjusting the distance between the lower edge of frustoconical device 17 and surface 12, or by varying the height of the free surface of liquid reagent above the lower edge of device 17. Cylinder ...

Contactor

A continuous contactor comprises a rotary tubular rotor (13) through which the two streams to be contacted flow, preferably in countercurrent. The rotor has an inner wall (17) which is substantially cylindrical and an outer wall (16) spaced from the inner wall. The rotor is divided internally into a number of rings of buckets by axial and radial separators. Each bucket (24) has an opening in the cylindrical inner wall at the leading part of the bucket with respect to the direction of rotation of the rotor. The rotor is mounted in a cylindrical stationary drum (12), the ends of which form settlement chambers, in which there is no intermixing of the phases and in which the phases separate. ...

PROCESS AND APPARATUS FOR OBTAINING SILICON FROM FLUOSILICIC ACID

Actively cooled reactor for exothermic reaktions

METHOD AND APPARATUS FOR HYDROLYZING KERATINACEOUS MATERIAL

PROCESS FOR CHLORINATING LINEAR PARAFFINS

... 1284870 Chlorination process SOC ITALIANA RESINE SpA 8 Dec 1970 [23 Dec 1969] 58318/70 Heading C2C Linear alkanes having 9 or more carbon atoms are monochlorinated at 90-170‹ C. in a continuous, liquid-phase, non-catalytic process using a vertically elongated tubular reactor divided by perforated sheets or plates into a plurality of reaction zones, the alkanes being supplied to the base of the reactor, chlorine being supplied to the bottom of each reaction zone at a linear inlet velocity of at least 50 m./sec., the velocity of gas passage from one reaction zone to another being at least 2 m./sec. The temperature is preferably controlled by heat exchangers situated internally in each reaction zone. Examples disclose the chlorination of (1) n-decane and (2) a mixture of n-C 10-14 alkanes.

REACTOR SUITABLE FOR REACTIONS BETWEEN TWO FLUIDS

... 1422246 Reactor; mixing apparatus ETABS GARDINIER SA 13 March 1973 [20 Sept 1972] 11904/73 Headings B1C and B1F [Also in Division Cl] In mixing/reaction apparatus, Fig. 1, comprising coaxial pipes 4, 6 liquefied or gaseous ammonia and aqueous phosphoric acid are admitted through tangential inlets 5 and 7 respectively, and the reaction product leaves at 13. Wheel 6 can be rotated to move a piston 8 axially to control the amount of phosphoric acid entering from 7. The apparatus may be heated and cleaned with steam introduced through pipes 10 and 11. Thus in Ex. 1, mono ammonium phosphate having a strength of 12% N 2 and 52% P 2 O 5 is formed by reacting aqueous phosphoric acid comprising 50% P 2 O 5 at a pressure of 6-7 bars and at # 150‹C. In Ex. 2, ammonium polyphosphates having a N 2 strength of 11 % and a P 2 O 5 strength of 58% is prepared by reacting 56% aqueous phosphoric acid and ammonia at 7 bars, and mono-ammonium phosphate having a strength of 10% N 2 and 52% P 2 O 5 is formed ...

A converter for continuous acid-saccharification of starch

... 1,128,920. Sugars. NIPPON SHIRYO KOGYO CO. Ltd. 1 Oct., 1965 [22 Oct., 1964; 21 Aug., 1965], No. 41847/65. Heading C2C. [Also in Divisions B1, C3 and F4] A converter for continuous acid - saccharification of starch comprises a vertical multi-tubular heat-exchanger and a plurality of parallel and vertical reaction tubes interconnected with themselves and with the heat - exchanger and provided with rectifying plates or elements having numerous small orifices installed in the reaction tubes so as to rectify the turbulent flow. The heat-exchanger may consist of a central steam pipe, an annular heating or reaction chamber surrounding it, a steam jacket surrounding the heating chamber, and steam tubes located in the heating chamber. The reaction tubes may be interconnected by 3-way cocks so that routing of flow in the tubes may be varied. In one embodiment (Fig. 1) a starch slurry from tank 13 is fed to the lower end of heatexchanger 17, and thence, from the top of the heat-exchanger to reaction ...

Apparatus for the catalytic gas reactions in liquid media

... Apparatus for carrying out gas reactions in the presence of liquid or solid catalysts dissolved or suspended in a liquid medium, through which the gaseous reactants bubble upwardly, comprises a vertical reactor which has a diameter or width not less than 30 centimetres and a length not less than 1.5 metres and which is divided into a number of vertical shafts open at both ends and having a width of at least 5 centimetres and a length of from 10-200 times the width; the lower ends of the shafts are at a distance above the gas inlet which is not substantially less than the width of the reactor, and in use the liquid level is within the shafts. As shown, the cylindrical reactor 21 is divided into shafts 27 of hexagonal cross-section. Gaseous reactants are introduced through nozzle 23 and the tail gas leaves at 26. Baffles 29 prevent the entry of gas into the space between the shafts and the wall of the reactor. A regulator 28 controls the amount of liquid in the reactor ...

Acid catalyst separation in emulsion alkylation of olefins with isoparaffins

In the emulsion alkylation of an isoparaffin with an olefine using a liquid acid catalyst which constitutes more than 50 per cent by volume of the emulsion, emulsion is continuously withdrawn to an agitated emulsion modifying zone where sufficient hydrocarbon is added from an emulsion breaking zone in side-by-side relationship therewith to reduce the acid content to 10-30 per cent by whence the emulsion passes to said non-agitated emulsion breaking zone, acid being recycled to the reaction zone and a portion of the upper hydrocarbon layer being returned to the emulsion modifying zone. In a preferred embodiment emulsion enters the settler by inlet 31 and so enters the stirred modifying zone. Hydrocarbon also passes into the modifying zone from the primary settling zone overflowing the adjustable weirs 42. Modified emulsion passes to the primary settling zone by two holes 39 (Fig. 5) in front of which are two baffles ...

PROCESS AND APPARATUS FOR PRODUCING AROMATIC DICARBOXYLIC ACIDS

Radial-flow reactor apparatus

Chemical reactor

... A vertical reactor for gaseous reactions comprises a casing 10 enclosing at least one venturi mixing device 12 extending upwardly into the casing from its lower end, preferably coaxial with the cylindrical casing, a reactant inlet 11 discharging coaxially upwards into the mixing device, an adjustable inlet for recycled gases 15 with damper 16, and a product outlet 24 near the lower end of the casing. The space in the casing surrounding the mixing device may contain devices to regulate the flow of reaction mixture from the upper end of the mixing device to the lower part of the casing. Exemplified reactions are the chlorination of gaseous hydrocarbons such as methane to form carbon tetrachloride, methylene chloride and perchloroethylene.ALSO: A vertical reactor for gaseous reactions comprises a casing 10 enclosing at least one venturi mixing device 12 extending upwardly into the casing from its lower end, preferably coaxial with the cylindrical ...

PROCESSING BIOMASS

Reactive crystallization method to improve particle size.

This invention provides a method of conducting a simultaneous chemical reaction and controlled crystallization of the product employing impinging fluid jet streams containing reactants capable of producing the product with desired particle size characteristics.

PROCESSING BIOMASS

Reactive cyrstallization method to improve particle size

METHOD FOR THE TREATMENT OF A LIQUID, IN PARTICULAR A MINERAL OIL

A gas reformulation system comprising means to optimize the effectiveness of gas conversion

Fluid shockwave reactor

Method for the treatment of a liquid, in particular a mineral oil

Sophisticated process of maintenance in temperature of engines.

Method of preparation of thio acids.

Reactive crystallization method to improve particle size.

A gas reformulation system comprising means to optimize the effectiveness of gas conversion

Fluid shockwave reactor

Fluid shockwave reactor

PROCESSING BIOMASS

Reactive cyrstallization method to improve particle size

A gas reformulation system comprising means to optimize the effectiveness of gas conversion

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.

PROCEDURE FOR THE PRODUCTION OF DIISOCYANATEN AND/OR TRI ISOCYANATES

HEISGASREAKTOR AND PROCEDURES FOR ITS USE

TWO-STAGE PROX SYSTEM WITH ONLY ONE AIR INJECTION

CONTINUOUS PROCEDURE FOR THE PRODUCTION OF CAPROLACTAM

SYSTEM AND PROCEDURE FOR THE MONITORING OF THE PRODUCTION OF SYNTHETIC FUEL

PROCEDURE FOR THE GASEOUS PHASE POLYMERIZATION OF OLEFINEN

PROCEDURE FOR THE PRODUCTION OF CAPROLACTAM BY BECKMANN RELOCATION

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

DEVICE AND PROCEDURE FOR SUPPLYING A LIQUID CATALYST FOR A BURN PROCESS

KONTINUERLICHES CATALYTIC SOLID/CGAS REACTION PROCEDURE IN NOT KONVENTIONNELLEM ENVIRONMENT, YOUR REACTOR AS WELL AS USE DESSEM

PROCEDURE FOR THE GASEOUS PHASE POLYMERIZATION OF OLEFINEN

PROCEDURE FOR POLYMERIZING OF OLEFINEN ASSISTANCE OF SEVERAL SCHLAUFENREAKTOREN

PEROXOSÄUREHERSTELLUNG

PRODUCTION OF COPPER CONNECTIONS.

PROCEDURE AND DEVICE FOR SEPARATING FROM POLLUTANTS.

INJECTION APPARATUS FOR HYDROCARBON EMPLOYMENTS INTO A CATALYTIC CRACKING REACTOR.

PROCEDURE AND DEVICE FOR THE TREATMENT OF LIQUID MATERIALS

PROCEDURE FOR THE CONTINUOUS PRODUCTION OF AROMATIC DIAZONIUMFLUORID SALTS.

PROCEDURE FOR THE PRODUCTION OF CELEBRATIONS OR PRODUCTS IN THE FORM OF PASTE.

PLATE-TYPE HEAT EXCHANGER WITH REFRIGERANT DISTRIBUTOR

REACTOR WITH CERAMIC CATALYTIC DIAPHRAGM TO THE SEPARATION OF HYDROGEN AND/OR HYDROGEN ISOTOPES FROM A FLUID SUPPLY

Procedure for the continuous production of PP and polyesters and device for the execution of the procedure

DEVICE FOR STEERING MEDIUMSTROMEN IN CHEMICAL OR PHYSICAL APPARATUSES

Thin section evaporator for the polycondensation of until (2-hydroxyäthyl) - terephthalat

PROCEDURE FOR THE PRODUCTION OF POLYPROPYLENE ALLOYS

RECOVERY OF THE PLATINUM METALS OUT PLATINUM METALS ABSTENTION ORGANIC COMPOSITIONS BY REACTION WITH SUPERCRITICAL WATER

PROCEDURE FOR THE PRODUCTION OF A FOOD COMPOSITION

Heater and Related Methods Therefor

The invention relates generally to heaters and methods of using the heaters. In certain embodiments, a heater includes a pressure shell having a cylindrical heating cavity, an annular heat shield disposed within the cylindrical heating cavity, and at least one heating element disposed within an interior volume of the annular heat shield. In another embodiment, a method of preparing a trichlorosilane includes introducing a reactant stream comprising silicon tetrachloride into a heater, passing electrical current through a heating element to heat the reactant stream, and introducing the heated reactant stream into a reactor.

Dispersed Bubble Reactor For Enhanced Gas-Liquid-Solids Contact And Mass Transfer

An apparatus to promote gas-liquid contact and facilitate enhanced mass transfer. The dispersed bubble reactor (DBR) operates in the dispersed bubble flow regime to selectively absorb gas phase constituents into the liquid phase. The dispersion is achieved by shearing the large inlet gas bubbles into fine bubbles with circulating liquid and additional pumped liquid solvent when necessary. The DBR is capable of handling precipitates that may form during absorption or fine catalysts that may be necessary to promote liquid phase reactions. The DBR can be configured with multistage counter current flow sections by inserting concentric cylindrical sections into the riser to facilitate annular flow. While the DBR can absorb CO 2 in liquid solvents that may lead to precipitates at high loadings, it is equally capable of handling many different types of chemical processes involving solids (precipitates/catalysts) along with gas and liquid phases.

Tunable catalytic gasifiers and related methods

The present disclosure provides tunable catalytic gasifier systems suitable for gasifying coal, biomass, and other fuel sources. The gasifier reactors of the disclosed systems may be heated by, e.g., a catalytic tube or other jacket that generates heat by catalytically combusting syngas, which syngas may be syngas produced by the gasifier system.

Method for the Treatment of a Liquid, in Particular a Mineral Oil

A method is disclosed for the treatment of a liquid, in particular a mineral oil, for increasing the portion of low-boiling fractions. The treatment comprises generating pressure waves having a first frequency, subjecting the liquid to said pressure waves in a region of application and feeding the so-treated liquid to a tank. At least one pipe flowed through by the treated liquid and immediately following said region of application is excited to oscillations of a second frequency, which is the resonance frequency of the excited system.

Isothermal reactor for hydrocarbon nitration

Disclosed are a process and an apparatus for synthesizing nitroalkanes by reaction of a hydrocarbon feedstock with aqueous nitric acid. By using an isothermal reactor with multiple input ports for aqueous nitric acid, a hydrocarbon feedstock may be sequentially exposed to a plurality of flows of aqueous nitric acid as it flows through the reactor.

Hydrocarbon Conversion Process

The invention relates to a process for converting hydrocarbons into unsaturated products such as acetylene and/or ethylene. The invention also relates to converting acetylene to olefins such as ethylene and/or propylene, to polymerizing the olefins, and to equipment useful for these processes.

PLANT FOR MANUFACTURING HYDROGEN SULFIDE GAS AND METHOD FOR EXHAUSTING HYDROGEN SULFIDE GAS

An object of the present invention is to reduce costs while maintaining safety in exhausting hydrogen sulfide gas. In exhaust facilities of a plant for manufacturing hydrogen sulfide gas, the concentrations of hydrogen sulfide gas leaking from a reaction facility, a cooling facility, and a sulfur removal facility, respectively, are measured by a measuring apparatus, and when a detected concentration is less than a predetermined concentration, a valve is controlled to exhaust hydrogen sulfide gas from a first exhaust pipe into the air, on the contrary, when a detected concentration is not less than a predetermined concentration, the valve is controlled to exhaust hydrogen sulfide gas from a second exhaust pipe to a gas treatment facility. 1. A plant for manufacturing hydrogen sulfide gas , the plant comprising at least: a reaction facility configured to generate hydrogen sulfide gas from sulfur and hydrogen gas; a cooling facility configured to cool generated hydrogen sulfide gas; a sulfur removal facility configured to remove sulfur contained in the hydrogen sulfide gas; and a gas treatment facility configured to render the hydrogen sulfide gas harmless ,wherein the plant has exhaust facilities which are provided in the reaction facility, the cooling facility, and the sulfur removal facility, respectively, and configured to exhaust hydrogen sulfide gas leaking from the facilities, andwherein each of the exhaust facilities comprises:an exhaust pipe whose one end branches out into a first exhaust pipe configured to exhaust leaking hydrogen sulfide gas to the air and a second exhaust pipe configured to exhaust leaking hydrogen sulfide gas to the gas treatment facility;a concentration measuring apparatus provided between the corresponding facility and a branch point in the exhaust pipe and configured to measure a concentration of the hydrogen sulfide gas; anda valve mechanism configured to perform control in such a manner that, when the concentration measuring apparatus ...

Gas purification device

A gas purification device includes: a converter packed with a catalyst for hydrolyzing both carbonyl sulfide and hydrogen cyanide; an upstream heat exchanger for heat exchange between a gas to be introduced into the converter and a cooling fluid for cooling the gas; a reaction-temperature estimation member for estimating a reaction temperature inside the converter; and a flow-rate adjustment member for adjusting a flow rate of the cooling fluid flowing into the upstream heat exchanger based on an estimated value of the reaction-temperature estimation member to control the reaction temperature.

Process for the Continuous On-Site Production of Percarboxycilic Acid Solutions and Device for Its Implementation

Provided are various methods and systems for producing peroxycarboxylic acid compositions, and in particular, nonequilibrium compositions of peracetic acid. The methods and systems control flow rates and proportions of feedstocks/reactants, perform the required sequence of reaction steps to produce high yield peroxycarboxcylic acid solutions in a continuous manner, and provide optimal reaction time and reactant mixing for continuous and safe on-site production. 1. A method for the continuous production of non-equilibrium peroxycarboxcylic acid , comprising:a. providing at least one source of water on demand at a point of use of the peroxycarboxcylic acid;b. providing at least one source of aqueous peroxide;c. then diluting the aqueous peroxide with the water to generate a diluted aqueous peroxide having a concentration of between 0.1% and 10% and a pH greater than 8;d. next, providing at least one source of aqueous hydroxide;e. then, adjusting the pH of the diluted aqueous peroxide to a pH in a range of 10 to 13.5 by adding the aqueous hydroxide source to the diluted aqueous peroxide;f. providing at least one source of acyl donor; andh. mixing the at least one sources of acyl donor and dilute aqueous peroxide to produce a single-phase composition of non-equilibrium peroxycarboxcylic acid.2. The method of claim 1 , wherein the at least one aqueous peroxide source is hydrogen peroxide.3. The method of claim 1 , wherein the acyl donor is a liquid acetyl donor.4. The method of claim 1 , wherein the acyl donor is selected from the group consisting of asacetin claim 1 , diacetin claim 1 , triacetin claim 1 , acetylsalicylic acid claim 1 , (β)-D-glucose pentaacetate claim 1 , cellulose acetate claim 1 , D-mannitol hexaacetate claim 1 , sucrose octaacetate claim 1 , acetic anhydride claim 1 , N claim 1 ,N claim 1 ,N′N′- tetraacetylethylenediamine (TAED) claim 1 , N-acetyl glycine claim 1 , N-acetyl-5 DL-methionine claim 1 , 6-acetamidohexanoic acid claim 1 , N-acetyl-L- ...

CRYSTALLIZER OR REACTOR AND METHOD FOR CONTINUOUSLY GROWING CRYSTALS OR CONTINUOUSLY MANAGING A REACTION

The invention relates to a processing device in the form of a crystallizer or reactor comprising a tube, at the opposite end regions of which an inlet and an outlet are provided for a crystallization or reaction medium. A helixical web is provided which runs about a longitudinal axis of the tube and which rests against the inner face of the tube casing, and the web is mounted so as to be rotatable about the aforementioned longitudinal axis of the tube. The device also has a drive for rotating the web. 1123452265. An apparatus , in particular a crystallizer () or a reactor , comprising a tube () , at the opposite end regions of which an inflow () and an outflow () are provided for a crystallization or reaction medium , wherein a web () is provided which runs helically about a longitudinal axis of the tube () and which rests against the inner face of the tube jacket , and the web is mounted to be rotatable about the aforementioned longitudinal axis of the tube () and the apparatus has a drive () for rotating the web ().25252562. An apparatus in accordance with claim 1 , wherein the web () is fixedly connected to the inner side of the tube jacket; and/or the tube () is supported such that it can be rotated together with the web () about said longitudinal axis claim 1 , with the rotatable support of the tube () representing the rotatable support of the web () and with the drive () serving the rotation of the tube ().35292. An apparatus in accordance with claim 1 , wherein the web () and the tube () represent separate components; and/or the tube () is supported in a stationary and non-rotatable manner.4278. An apparatus in accordance with claim 1 , wherein the end of the tube () at the outflow side is closed claim 1 , preferably by a cover (); and/or the tube jacket has at least one aperture claim 1 , and preferably a plurality of apertures () claim 1 , distributed over the periphery in the end region at the outflow side.529. An apparatus in accordance with claim 1 , ...

REACTION METHOD WITH HOMOGENEOUS-PHASE SUPERCRITICAL FLUID

A reaction method with a homogeneous-phase supercritical fluid includes introducing a first fluid into a mixing chamber. A mass is less than or equal to that can be absorbed by the molecular sieve component, totally absorbing the first fluid by the molecular sieve component. A second fluid is introduced into the mixing chamber with a mass being greater than that can be absorbed by the molecular sieve component. A temperature and a pressure in the mixing chamber are adjusted to a critical temperature and a critical pressure of the second fluid, respectively, releasing the first fluid in supercritical phase from the molecular sieve component into the mixing chamber, followed by homogeneously mixing with the second fluid in supercritical phase in the mixing chamber to obtain a homogeneous-phase mixing fluid. The homogeneous-phase mixing fluid is then introduced into a reaction chamber connected to the mixing chamber. 1. A reaction method with a homogeneous-phase supercritical fluid , comprising:introducing a first fluid into a mixing chamber, wherein a mass of the first fluid into the mixing chamber is less than or equal to that can be absorbed by the molecular sieve component, totally absorbing the first fluid by the molecular sieve component;introducing a second fluid into the mixing chamber, wherein a mass of the second fluid into the mixing chamber is greater than that can be absorbed by the molecular sieve component;adjusting a temperature and a pressure in the mixing chamber to a critical temperature and a critical pressure of the second fluid, respectively, releasing the first fluid in supercritical phase from the molecular sieve component into the mixing chamber, followed by homogeneously mixing with the second fluid in supercritical phase in the mixing chamber to obtain a homogeneous-phase mixing fluid; andintroducing the homogeneous-phase mixing fluid into a reaction chamber connected to the mixing chamber for conducting a reaction.2. The reaction method with ...

Inherently safe oxygen/hydrocarbon gas mixer

Provided herein is a gas mixer for the safe mixing of a hydrocarbon containing gas with a gaseous oxidant. The gas mixer and method for mixing described includes a closed mixing vessel where bubbles of gas injected at the bottom of the vessel are mixed during their rise to the top of the vessel, forming a homogeneous mixture that can safely be removed. This simple design and method allows for safe mixing of gases and is applicable to catalytic oxidative processes such as oxidative dehydrogenation of paraffins where there is a risk of thermal runaway of reactions.

Linear Alpha Olefin Processes

The present disclosure provides assemblies for producing linear alpha olefins and methods for producing linear alpha olefins. In at least one embodiment, a method for producing a linear alpha olefin includes oligomerizing an olefin in the presence of a catalyst and a process solvent in at least one reactor, quenching the reactor effluent, and subjecting the quenched effluent to separation steps to obtain a stream enriched in one or more linear alpha olefins. 1. A method for forming one or more linear alpha olefins , the method comprising the steps of:(a) providing a feed comprising an olefin, a catalyst, and a process solvent to a reaction zone including at least one reactor under oligomerization conditions to obtain a reactor effluent produced in the at least one reactor;(b) contacting at least a portion of the reactor effluent with a quench agent to obtain a quenched effluent;(c) separating at least a portion of the quenched effluent to obtain a vapor effluent and a liquid effluent;(d) separating at least a portion of the liquid effluent to obtain at least one aqueous phase enriched in catalyst and quench agent and an organic phase depleted in catalyst and quench agent;(e) separating at least a portion of the organic phase to obtain a stream enriched in one or more linear alpha olefins.2. The process of claim 1 , wherein the feed comprises <25 ppb water by weight.3. The method of claim 1 , wherein step (a) comprises:providing the feed to a first tubular reactor under oligomerization conditions to obtain a first effluent; andtransferring the first effluent to a second tubular reactor under oligomerization conditions to obtain the reactor effluent.4. The method of claim 3 , further comprising providing steam to a first steam jacket disposed around the first tubular reactor and providing steam to a second team jacket disposed around the second tubular reactor claim 3 ,optionally further comprising controlling the pressure of steam in the first steam jacket pressure ...

APPARATUS AND METHOD FOR INVESTIGATING NAPHTHA REFORMING PROCESSES

An apparatus and a method are used for investigating the naphtha reforming process in catalyst test devices with reactors arranged in parallel. The apparatus has a plurality of reactors arranged in parallel with reaction chambers (R, R, . . . ), a product fluid supply, a process control, and at least one analysis unit. Each individual reactor has an outlet line for the product fluid stream, wherein the analysis unit is operatively connected to each outlet line for the product fluid stream and the apparatus is functionally connected to the control of the apparatus. In carrying out the method, naphtha-containing reactant fluid streams are brought into contact with catalysts in the individual reactors and the product fluid streams are subsequently supplied to the online analysis unit from the respective outlet lines of the individual reactors and analyzed. Using the evaluation of the online analytical characterization data, the process parameters of the respective reactor unit are adapted. The process steps of analytical characterization, evaluation, and adaptation of process parameters are repeated for the duration of the investigation. 1. An apparatus for investigating naphtha reforming , wherein the apparatus comprises:{'b': 1', '2, 'a plurality of reactors arranged in parallel with reaction chambers (R, R, . . . ),'}a product fluid supply common to one or a plurality of these reactors,a process control, andan analysis unit,wherein each individual reactor has an outlet line for the product fluid stream,wherein the analysis unit is operatively connected to each outlet line for the product flow unit, and the analysis unit is functionally connected to the control of the apparatus,and wherein the analysis unit is suitable for analysis of a gaseous product fluid stream, and the analysis unit, together with the process control, allows the determination and optimization of an octane number in the reactors arranged in parallel.2. The apparatus as claimed in claim 1 , ...

Decomposition mediation in chlorine dioxide generation systems through sound detection and control

A method of controlling a chemical reaction is disclosed. The method may include feeding a solution at a first flow rate into a reactor and detecting a sound in the reactor using a sound sensor that is adjacent to the reactor. The sound sensor may convert the sound into a sound signal. After the sound signal is acquired, it is compared to a stored sound signal or a stored sound threshold to detect a reaction event. The method may include adjusting the flow rate of solutions into the reactor in response to the reaction event.

RING-OPENING POLYMERIZATIONS USING A FLOW REACTOR

Techniques regarding the synthesis of polyesters and/or polycarbonates through one or more ring-opening polymerizations conducted within a flow reactor and facilitated by a urea anion catalyst and/or a thiourea catalyst are provided. For example, one or more embodiments can comprise a method, which can comprise polymerizing, via a ring-opening polymerization within a flow reactor, a cyclic monomer in the presence an organocatalyst comprising a urea anion. 1. A method , comprising:polymerizing, via a ring-opening polymerization within a flow reactor, a cyclic monomer in the presence of an organocatalyst comprising a urea anion.2. The method of claim 1 , wherein the cyclic monomer is selected from a group consisting of a lactone monomer claim 1 , a cyclic carbonate monomer claim 1 , a substituted cyclic carbonate monomer claim 1 , a cyclic phospholane monomer claim 1 , a morpholinone monomer claim 1 , tetrahydro-2H-pyran-2-thione claim 1 , oxepane-2-thione claim 1 , tetrahydrothiopyranone claim 1 , and 2-thiepanone.3. The method of claim 2 , wherein the organocatalyst is derived from a chemical compound selected from a second group consisting of 1 claim 2 ,3-bis[3 claim 2 ,5-bis(trifluoromethyl)phenyl]urea claim 2 , 1-[3 claim 2 ,5-bis(trifluoromethyl)phenyl]-3-[2-(trifluoromethyl)phenyl]urea claim 2 , 1-[3 claim 2 ,5-bis(trifluoromethyl)phenyl]-3-phenylurea claim 2 , 1-[3 claim 2 ,5-bis(trifluoromethyl)phenyl]-3-cyclohexylurea claim 2 , 1-phenyl-3-[3-(trifluoromethyl)phenyl]urea claim 2 , 1 claim 2 ,3-diphenylurea claim 2 , and 1-cyclohexyl-3-phenylurea.4. The method of claim 3 , wherein the urea anion is derived from a chemical reaction between the chemical compound and a chemical base claim 3 , wherein the chemical base is selected from a third group consisting of 1 claim 3 ,8-diazabicyclo[5.4.0[undec-7-ene claim 3 , 7-methyl-] claim 3 ,5 claim 3 ,7-triazabicyclo[4.4.0]dec-5-ene claim 3 , phosphazene bases claim 3 , ] claim 3 ,3 claim 3 ,2-diazaphosphorin-2-amin ...

SYSTEMS AND METHODS FOR PREDICTING AND CONTROLLING THE PROPERTIES OF A CHEMICAL SPECIES DURING A TIME-DEPENDENT PROCESS

Devices and methods for controlling the properties of chemical species during time-dependent processes. A device includes a reactor for containing one or more chemical species of a time-dependent process, an extraction pump for automatically and continuously extracting an amount of the one or more chemical species from the reactor, one or more detectors for measuring property changes of the one or more extracted chemical species and generating a continuous stream of data related to the one or more property changes to the one or more chemical species during a time interval, and a process controller configured to fit the continuous stream of data to a mathematical function to predict one or more properties of the one or more chemical species at a future time point and make one or more process decisions based on the prediction of one or more properties at the future time point. 131-. (canceled)32. A method comprising:introducing, in a reactor, one or more chemical species to be monitored during a time-dependent process;detecting, using one or more detectors, one or more property changes to the one or more chemical species over a time interval;receiving, from the one or more detectors, a continuous stream of data related to the one or more property changes to the one or more chemical species during the time interval;fitting, using a process controller, the continuous stream of data to a mathematical function to predict one or more properties of the one or more chemical species at a future time point; andmaking, by the process controller, one or more process decisions based on the prediction of one or more properties at the future time point.33. The method of claim 32 , wherein the one or more process decisions comprise any one of terminating of the time-dependent process claim 32 , recovering the reactor contents claim 32 , proceeding to a subsequent reaction or processing stage in the same or a different reactor.34. The method of claim 32 , further comprising fitting ...

APPARATUS AND PROCESS FOR SYNTHESIZING NATURAL GAS USING CARBON DIOXIDE AND WATER IN AIR

An apparatus for producing a natural gas using carbon dioxide and water in air that includes an air-compressing member, a water collecting member, a water storing member, a carbon dioxide collecting member, a water electrolysis member, and a methanation reaction member. The water electrolysis member electrolyzes water separated from compressed air. The methanation reaction member generates a natural gas by reacting hydrogen from the electrolysis and carbon dioxide from the carbon dioxide collecting member. A method of producing a natural gas using carbon dioxide and water in air includes supplying hydrogen electrolyzed from water separated from air and carbon dioxide collected from the dry air to a methanation reaction member to generate a natural gas. A natural gas-synthesizing equipment system includes an apparatus for producing a natural gas using carbon dioxide and water in air. 1. An apparatus for producing a natural gas using carbon dioxide and water in air , comprising:an air-compressing member;a water collecting member for collecting and separating water from the compressed air supplied from the air-compressing member;a water storing member connected to the water collecting member and for storing the collected water;a carbon dioxide collecting member connected to the water collecting member and for collecting carbon dioxide from dry air supplied after the water collecting member collects water;a water electrolysis member for electrolyzing water supplied from the water storing member to generate oxygen and hydrogen;a methanation reaction member for generating a natural gas by methanation reaction of hydrogen supplied from a hydrogen storing member connected to the water electrolysis member and carbon dioxide supplied from a carbon dioxide storing member connected to the carbon dioxide collecting member;a separation member having a means for separating the natural gas, carbon dioxide and water contained in a methanation reaction product supplied from the ...

Process of Removing Heat

The present invention provides an improved process for removing heat from an exothermic reaction. In particular, the present invention provides a process wherein heat can be removed from multiple reaction trains using a common coolant system.

A PROCESS FOR MAKING BROMINATING AGENTS IN FLOW

A process for making a brominating agent includes the step of continuously feeding a bromide source and an oxidizing agent into a continuous flow reactor. 110-. (canceled)11. A process for making a brominating agent comprising:continuously feeding a bromide source and an oxidizing agent into a continuous flow reactor; whereinthe oxidizing agent is selected from the group consisting of a hypochlorite anion, nitric acid, oxygen, osmium tetroxide, chlorine, fluorine, ozone, peracids, potassium permanganate, and potassium peroxymonosulfate.12. The process according to claim 11 , wherein the bromide source is selected from the group consisting of hydrogen bromide and an organic or inorganic bromide salt.13. The process according to claim 11 , wherein the bromide source is selected from the group consisting of an alkali metal bromide salt claim 11 , an earth alkali metal bromide salt claim 11 , and an ammonium bromide salt.14. The process according to claim 11 , wherein the bromide source is an alkali metal bromide salt.15. The process according to claim 12 , wherein the bromide source is an alkali metal bromide salt.16. The process according to claim 11 , wherein the oxidizing agent has a standard reduction potential claim 11 , with respect to a potential of a standard hydrogen electrode claim 11 , greater than 0.5 V.17. The process according to claim 12 , wherein the oxidizing agent has a standard reduction potential claim 12 , with respect to a potential of a standard hydrogen electrode claim 12 , greater than 0.5 V.18. The process according to claim 14 , wherein the oxidizing agent has a standard reduction potential claim 14 , with respect to a potential of a standard hydrogen electrode claim 14 , greater than 0.5 V.19. The process according to claim 11 , wherein the oxidizing agent is a hypochlorite anion.20. The process according to claim 12 , wherein the oxidizing agent is a hypochlorite anion.21. The process according to claim 14 , wherein the oxidizing agent is a ...

OZONE-GENERATING SYSTEM AND OZONE GENERATION METHOD

A system including: an ozone generating device including discharge electrodes forming a discharge space; a gas supplying device; a power source device that supplies power to the discharge electrodes; a temperature adjustment device that adjusts temperature of the discharge electrodes; a control unit that controls the ozone generating device; and a detection unit that detects an ozone generation parameter in the ozone generating device. The control unit increases temperature of the discharge electrodes up to a vaporizing temperature of dinitrogen pentoxide by controlling the temperature adjustment device and the gas supplying device or the temperature adjustment device and the power source device, based on the output ozone generation parameter, to thereby switch operation from a normal operation mode to a cleaning operation mode in which surfaces of the discharge electrodes and the discharge space are cleaned up while continuing generation of ozone in the discharge space. 110-. (canceled)11. An ozone generating system , comprising:an ozone generating device including discharge electrodes that are arranged opposite to each other to thereby form a discharge space;a gas supplying device that supplies an oxygen-containing gas as a source gas for generating ozone to the discharge space;a power source device that supplies power for discharging to the discharge electrodes;a temperature adjustment device that adjusts a temperature of the discharge electrodes;a control unit that controls the gas supplying device, the power source device and the temperature adjustment device, to thereby control an operation of the ozone generating device; anda detection unit that detects an ozone generation parameter in the ozone generating device;wherein, the control unit causes the temperature of the discharge electrodes to increase up to a vaporizing temperature of dinitrogen pentoxide by controlling the temperature adjustment device and the gas supplying device or the temperature ...

Method And Apparatus For Monitoring And Controlling Exothermic And Endothermic Chemical Reactions

A method of controlling an exothermic or endothermic chemical reaction is provided. The method involves measuring a temperature of a first reactant flowing at a first flow rate, contacting the first reactant with a second reactant flowing at a second flow rate to form a reaction product, measuring the temperature of the reaction product, and determining the temperature difference between the temperature of the first reactant and the temperature of the reaction product. The method can further involve adjusting the flow rate of at least one of the first reactant and the second reactant, or shutting down flow, based on the temperature difference. An apparatus to carry out the method is also provided. The method and apparatus can be useful in controlling many different reactions, including the reaction of sodium hypochlorite and ammonia to form monochloramine.

Hydrocarbon Pyrolysis Process

Disclosed is a pyrolysis process that is capable of being with reduced coke and/or tar formation. The process can pyrolyze hydrocarbon feed that contains low- to mid-range levels of non-volatiles. Pyrolysis is carried out with a predetermined amount of the feed being in the liquid phase so as to minimize coke and/or tar formation in the pyrolysis reactor. The pyrolysis feed may also include a diluent, such as molecular hydrogen, that further acts to minimize coke and/or tar formation in the pyrolysis reactor. The amount of diluent in the pyrolysis feed can be adjusted to adjust or control dry point of the hydrocarbon in the pyrolysis feed. 1. A regenerative reactor system comprising: a housing enclosing an interior region;', 'one or more process flow components configured to manage the flow of a pyrolysis stream through the interior region, wherein the one or more process flow components comprise one or more reactor beds;, 'a reverse flow regenerative reactor comprisinga pyrolysis inlet conduit having an internal surface and in fluid communication with the reverse flow regenerative reactor, whereby the pyrolysis inlet conduit is configured to manage the flow of the pyrolysis stream to the reverse flow regenerative reactor; anda liquid distribution device disposed along the flow path of the pyrolysis stream and in fluid communication with the pyrolysis inlet conduit, whereby the liquid distribution device is configured to disperse a liquid portion of the pyrolysis stream along the internal surface of the pyrolysis inlet conduit.2. The regenerative reactor system of claim 1 , wherein the reverse flow regenerative reactor further comprises one or more structural members disposed within the internal region and near the pyrolysis inlet conduit to lessen fouling near the pyrolysis inlet conduit within the internal region.3. The regenerative reactor system of claim 1 , further comprising a non-combustible non-volatile removal unit upstream of the pyrolysis inlet conduit ...

Continuous reaction apparatus and method of continuous polymerization using the same

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

Methods for Determining Transition Metal Compound Concentrations in Multicomponent Liquid Systems

Methods for determining the concentration of transition metal compounds in a solution containing more than one transition metal compound are described. Polymerization reactor systems providing real-time monitoring and control of the concentrations of the transition metal components of a multicomponent catalyst system are disclosed, as well as methods for operating such polymerization reactor systems. 121-. (canceled)22. A process for operating a polymerization reactor system , the process comprising:(I) contacting a catalyst system comprising a first transition metal compound, a second transition metal compound, an activator, and an optional co-catalyst, with an olefin monomer and an optional olefin comonomer in a reactor within the polymerization reactor system under polymerization reaction conditions to produce an olefin polymer;wherein the polymerization reactor system comprises a solution reactor, a gas-phase reactor, a slurry reactor, or a combination thereof; (i) submitting a sample of the solution to a sample chamber;', '(ii) irradiating the sample in the chamber with a light beam at a wavelength in the UV-visible spectrum; and', '(iii) generating a sample absorbance profile of the sample, subtracting a reference absorbance profile of the second transition metal compound in a reference solution from the sample absorbance profile to result in a first transition metal compound absorbance profile, and correlating the first transition metal compound absorbance profile to a standard to determine the concentration of the first transition metal compound in the solution; and, '(II) determining a concentration of the first transition metal compound in a solution comprising the first transition metal compound and the second transition metal compound, the concentration determined via the steps of(III) adjusting a flow rate of the first transition metal compound into the reactor when the concentration of the first transition metal compound in the solution has reached a ...

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 ...

METHOD FOR THE EPOXIDATION OF AN OLEFIN WITH HYDROGEN PEROXIDE

Epoxidation of an olefin is carried out by continuously reacting the olefin with hydrogen peroxide in the presence of a homogeneous epoxidation catalyst in a reaction mixture comprising an aqueous liquid phase and an organic liquid phase, using a loop reactor with mixing of the liquid phases. The loop reactor comprises a measuring section in which the liquid phases are temporarily separated, at least one pH electrode is arranged in the measuring section in contact with the separated aqueous phase, a pH of the separated aqueous phase is determined with the pH electrode and the pH is maintained in a predetermined range by adding acid or base to the loop reactor. 111-. (canceled)12. A method for the epoxidation of an olefin , comprising continuously reacting the olefin with hydrogen peroxide in the presence of a homogeneous epoxidation catalyst , wherein: i) a measuring section in which the liquid phases are temporarily separated into a separated aqueous phase and a separated organic phase;', 'ii) at least one pH electrode in said measuring section in contact with the separated aqueous phase;, 'a) the reaction is carried out in a reaction mixture comprising an aqueous liquid phase and an organic liquid phase using a loop reactor with mixing of the liquid phases, wherein the loop reactor comprisesb) a pH of the separated aqueous phase is determined with said pH electrode and said pH is maintained in a predetermined range by adding acid or base to the loop reactor.13. The method of claim 12 , wherein the liquid phases are temporarily separated by lowering the flow rate.14. The method of claim 13 , wherein the flow rate is lowered in the measuring section by enlarging the flow cross section.15. The method of claim 12 , wherein the measuring section is located in a side stream to the loop reactor.16. The method of claim 15 , wherein a valve is used for lowering the flow rate or temporarily stopping the flow in the measuring section.17. The method of claim 12 , wherein at ...

Method for producing butadiene from ethanol with optimised 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 4 or a multiple thereof, comprising a catalyst, said regeneration step comprising four successive regeneration phases, said step b) also implementing three regeneration loops.

HIGH VOLUME LOW PRESSURE FEEDER SYSTEM

Embodiments described herein relate to an apparatus for a feeder system. The apparatus includes a reactant source, a reactant reservoir, a frame, and a valve. The reactant source contains a first reactant. The reactant reservoir receives the first reactant from the reactant source and applies a second reactant to the first reactant to facilitate a chemical reaction. The frame is coupled to the reactant source to maintain the reactant source gravitationally directly above the reactant reservoir. The valve is disposed between the reactant source and the reactant reservoir to control flow of the first reactant into the reactant reservoir. 1. An apparatus for a feeder system , the apparatus comprising:a reactant source to contain a first reactant;a reactant reservoir to receive the first reactant from the reactant source and apply a second reactant to the first reactant to facilitate a chemical reaction;a frame coupled to the reactant source to maintain the reactant source gravitationally directly above the reactant reservoir; anda valve disposed between the reactant source and the reactant reservoir to control flow of the first reactant into the reactant reservoir.2. The apparatus of claim 1 , wherein the frame comprises a first portion associated with the reactant source and a second portion associated with the reactant reservoir claim 1 , the first portion and the second portion separated by one or more load cells.3. The apparatus of claim 2 , wherein the first portion of the frame is sized to accept a 2200 lb. container of the first reactant.4. The apparatus of claim 1 , further comprising a controller to receive information from one or more sensors and adjust an operating parameter of the apparatus.5. The apparatus of claim 4 , wherein the operating parameter comprises a flow rate of one or more of the first reactant and the second reactant.6. The apparatus of claim 4 , wherein the one or more sensors comprise an ultraviolet spectrometer positioned to monitor ...

WATER-ABSORBENT RESIN PRODUCTION APPARATUS

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

Systems and Methods for the Continuous On-Site Production of Peroxycarboxcylic Acid Solutions

Methods and systems for on-site production of peroxycarboxcylic acid compositions, and in particular, nonequilibrium compositions of peracetic acid (PAA) enable the economical and safe production of PAA on-demand at the point of use. The methods and systems control flow rates and proportions of feedstocks/reactants, perform the required sequence of reaction steps to produce high yield peroxycarboxcylic acid solutions in a continuous manner, and provide optimal reaction time and reactant mixing for continuous and safe on-site production. 1. A method for the continuous production of non-equilibrium peracetic acid solutions containing biocidal concentrations of peroxycarboxylic acids , the method comprising:providing a source of hydrogen peroxide having an initial pH of less than 7.0;diluting the hydrogen peroxide with water to create a diluted solution having a concentration which is less than 10% weight/volume;adding an alkali metal hydroxide to the diluted solution to adjust the pH to a pH in a range of approximately 10.0 to approximately 13.5;reacting the diluted solution with an O-acetyl or N-acetyl donor;vigorously mixing the solution.2. The method of further including the step of controlling the stoichiometry of the peroxide component with respect to the acetyl donor to bias the reaction in favor of either producing peracetic acid or producing a solution having a specified remaining concentration of peroxide.3. The method of wherein the alkali metal hydroxide is sodium hydroxide.4. The method of wherein the alkali metal hydroxide is potassium hydroxide.5. The method of wherein the O-acetyl donor is triacetin.6. The method of wherein the step of mixing the solution includes producing a turbulent flow having high shear within the solution and having a Reynolds number of 500 or greater.7. The method of including the step of vigorously mixing the solution following the diluting step.8. The method of further including the step of vigorously mixing the solution ...

METHOD FOR PRODUCING PEROXYMONOSULFURIC ACID AND APPARATUS FOR CONTINUOUSLY PRODUCING PEROXYMONOSULFURIC ACID

The invention provides a method for producing a peroxymonosulfuric acid solution with high stability, including the steps of mixing 35 mass % or more of hydrogen peroxide and 70 mass % or more of sulfuric acid to react them, cooling the reaction solution to 80° C. or lower within five minutes after initiation of the mixing step, and diluting the reaction solution with water four times or more as much as the reaction solution by mass. 1. An apparatus for continuously producing peroxymonosulfuric acid , comprising:a first static mixer for mixing hydrogen peroxide with sulfuric acid to react them, thereby obtaining a reaction solution;a second static mixer for mixing the reaction solution obtained in the first static mixer with a dilution water; anda reaction solution transporting pipe for transporting the reaction solution from the first static mixer to the second static mixer, with the first static mixer and the reaction solution transporting pipe being disposed underwater in a vessel.2. The apparatus of claim 1 , further comprising a hydrogen peroxide feed pipe and a sulfuric acid feed pipe which are located upstream from the first static mixer claim 1 , each of the hydrogen peroxide feed pipe and the sulfuric acid feed pipe being equipped with a back pressure control valve.3. The apparatus of claim 1 , wherein the reaction solution transporting pipe and a dilution water feed pipe are located upstream from the second static mixer claim 1 , each of the reaction solution transporting pipe and the dilution water feed pipe being equipped with a back pressure control valve.4. The apparatus of claim 1 , wherein the second static mixer is disposed underwater.5. The apparatus of claim 1 , further comprising a pump for feeding claim 1 , as the dilution water claim 1 , water held in the vessel into the second static mixer.6. The apparatus of claim 1 , further comprising means for detecting the amount of water held in the vessel and means for controlling the amount of water to ...

METHOD AND APPARATUS FOR THE PREPARATION OF SILANES

The invention relates to a process for preparing dimeric and/or trimeric silanes by conversion of monosilane in a plasma and to a plant for performance of the process. 2. The process according to claim 1 , wherein the pressure in process step iii) is elevated relative to the pressure in process stage ii).3. The process according to claim 1 ,{'sub': ab', 'abs, 'wherein the resulting phase in process step iii) has a pressure of 1 barto 100 bar.'}4. The process according to{'sub': abs', 'abs, 'wherein the monosilane in process step ii) is subjected to the gas discharge in the presence of hydrogen at a pressure between 0.05 mbarand 15,000 mbar.'}5. The process according to claim 1 ,{'sub': abs', 'abs, 'wherein the gas discharge in process step ii) is effected at a pressure between 0.1 mbarand 1,000 mbar.'}6. The process according towherein the gas discharge in process step ii) is effected at a temperature between −60° C. and 10° C.7. The process according to wherein the reactant stream has a defined ratio of hydrogen and monosilane in percent by volume (% by vol.) of 15:1 to 1:5.8. The process according to claim 1 , wherein the reactant stream in step ii) is exposed to a nonthermal plasma.9. The process according to claim 1 , wherein the defined ratio in process step iii) of the partial hydrogen pressure to the partial pressure of the gaseous silanes is set by means of a hydrogen-permeable membrane.10. The process according to claim 9 , wherein the membrane is permeable to hydrogen and essentially impermeable to silanes.11. The process according to claim 9 , wherein said membrane comprises at least one of the following materials: quartz claim 9 , metal claim 9 , metallic alloy claim 9 , ceramic claim 9 , zeolite claim 9 , organic polymer and/or a composite membrane having an at least two-layer structure comprising one or more of the aforementioned materials.12. A plant for performance of the process according to comprising:a reactor for generation of a gas discharge, ...

METHOD FOR TREATING WATER WITH CHLORINE DIOXIDE

A method for treating water with chlorine dioxide wherein the reactor is contained inside of the water supply line being treated and an eductor is used to draw in the chemical precursors. The method offers facilitated chlorine dioxide (ClO ) generation and safer operation over wider ClOmass flow capacity, thus offering a more adaptable system for CLOtreatments. Noise reduction and ease-of-use versus traditional eductor-based ClOgenerators are additional benefits from using this method. 1. A method for ClOtreatment that uses an eductor-based reactor assembly to expand the ClOflow capacity comprising:{'sub': '2', 'an eductor to provide flows of precursor chemicals to generate the ClO'}{'sub': 2', '2, 'a mixing zone to ensure the ClOis generated at safe operating pressures below explosive limits of the ClO;'}{'sub': '2', 'a pipe to which the reactor assembly is mounted that allows for containment of the eductor inside the process stream and direct treatment of the process stream with the ClO;'}a means to provide motive water supply for the eductor;{'sub': '2', 'a control system that monitors precursor chemical flow rates and process flow rates to ensure that proper dilution and safe ClOdosage is being applied to the process stream being treated.'}2. The method according to whereby the precursors are acid and sodium chlorite.3. The method according to whereby the precursors are acid claim 1 , sodium hypochlorite claim 1 , and sodium chlorite.4. The method according to whereby the precursors are chlorine and sodium chlorite.5. The method according to wherein a flushing zone is an additional component of the reactor assembly that prevents ClOfrom accumulating within the process line and reactor assembly volume by continuously flushing volume outside of the eductor.6. The method according to wherein the reactor assembly is of modular design to accommodate interchangeable reactor assemblies for variable chlorine dioxide production capacity and turn down ratio.7. The method ...

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.

PROCESSING BIOMASS

Biomass (e.g., plant biomass, animal biomass, and municipal waste biomass) is processed to produce useful intermediates and products, such as amino-alpha, omega-dicarboxylic acid and amino-alpha, omega-dicarboxylic acid derivatives. These products include polymers and copolymers of alpha-amino, omega-dicarboxylic acids. 1. A method comprising:treating a reduced recalcitrance lignocellulosic and/or cellulosic material with one or more enzymes and/or microorganisms to produce an amino-alpha, omega-dicarboxylic acid.2. The method of further comprising converting the amino-alpha claim 1 , omega-dicarboxylic acid to product.3. The method of further comprising pretreating a feedstock with at least one of irradiation claim 1 , sonication claim 1 , oxidation claim 1 , mechanical size reduction claim 1 , pyrolysis and steam explosion to produce the reduced recalcitrance lignocellulosic and/or cellulosic material.4. The method of wherein irradiation is performed with an electron beam.5. The method of wherein converting the amino-alpha claim 2 , omega-dicarboxylic acid to the product comprises chemically converting.6. The method of wherein converting the amino-alpha claim 2 , omega-dicarboxylic acids to the product comprises biochemically converting.7. The method of wherein chemically converting is selected from the group consisting of polymerization claim 5 , isomerization claim 5 , esterification claim 5 , amidation claim 5 , cyclization claim 5 , oxidation claim 5 , reduction claim 5 , disproportionation claim 5 , phosgenation claim 5 , and combinations thereof.8. The method of wherein treating is performed with one or more enzymes to release one or more sugars from the lignocellulosic and/or cellulosic material prior to producing the amino-alpha claim 1 , omega-dicarboxylic acid.9. The method of wherein producing the amino-alpha claim 1 , omega-dicarboxylic acid comprises treating initially to release one or more sugars from the lignocellulosic and/or cellulosic material ...

MANUFACTURING PROCESS FOR CYCLODEXTRIN DERIVATIVES

A process and equipment assembly for reacting a substituent precursor with a cyclodextrin starting material to provide a raw product comprising a cyclodextrin derivative and 1% or less of an initial amount of the substituent precursor is provided. The process of the present invention provides cyclodextrin derivatives in substantially shorter time and with fewer side products than previous processes that utilize substantially the same starting materials. 1. A process for preparing a derivatized cyclodextrin , the process comprising: reacting a cyclodextrin starting material , a substituent precursor , and an optional catalyst to provide a raw product comprising a derivatized cyclodextrin , wherein:the raw product comprises 1% or less of an initial amount of the substituent precursor andthe reacting is performed in a continuous or semi-continuous manner comprising:providing a feedstock comprising a liquid or gas medium, the cyclodextrin starting material, the substituent precursor, and the optional catalyst andcontinuously or semi-continuously flowing the feedstock into a reactor and flowing out of the reactor the raw product comprising a derivatized cyclodextrin.2. The process of claim 1 , wherein the process does not include after the reacting claim 1 , adding a reagent to the raw product in order to degrade the substituent precursor.3. The process of claim 1 , wherein the cyclodextrin starting material comprises an unsubstituted cyclodextrin selected from the group consisting of: an α-cyclodextrin claim 1 , a β cyclodextrin claim 1 , a γcyclodextrin claim 1 , and combinations thereof.4. The process of claim 1 , wherein the substituent precursor and the cyclodextrin starting material are present in a molar ratio of 1:1 to 50:1.5. The process of claim 1 , wherein the substituent precursor is selected from the group consisting of: a sulfoalkylating agent claim 1 , an alkylating agent claim 1 , and combinations thereof.6. The process of claim 5 , wherein the ...

METHOD AND APPARATUS FOR THE RAPID DISCOVERY AND DESIGN OF POLYMERIZATIONS

A reactor system includes at least one reactant provided to perform a reaction. The system includes one or more sensors configured to detect sensor data regarding the reaction. The system includes processing circuitry configured to receive the sensor data from the one or more sensors, apply one or more machine learning models to the sensor data to generate a measurement regarding at least one of the reaction or an activity of at least one catalyst used to perform the reaction, and control at least one of a temperature of the reactor, a flow rate of the at least one reactant, or a concentration of the at least one reactant responsive to the measurement. 1. A system , comprising: 'at least one reactant provided to perform a reaction;', 'a reactor, comprisingone or more sensors configured to detect sensor data regarding the reaction; and receive the sensor data from the one or more sensors;', 'apply one or more machine learning models to the sensor data to generate a measurement regarding at least one of the reaction or an activity of at least one catalyst used to perform the reaction; and', 'control at least one of a temperature of the reactor, a flow rate of the at least one reactant, or a concentration of the at least one reactant responsive to the measurement., 'processing circuitry configured to2. The system of claim 1 , wherein the processing circuitry is configured to control the at least one of the temperature of the reactor claim 1 , the flow rate of the at least one reactant claim 1 , or the concentration of the at least one reactant to increase the measurement to be greater than a threshold measurement.3. The system of claim 1 , wherein the sensor data comprises at least one of molecular weight claim 1 , polydispersity claim 1 , cross-linking claim 1 , temperature of the reaction claim 1 , or flow rate of the reaction.4. The system of claim 1 , wherein the sensor data comprises at least one of dynamic light scattering data detected by a dynamic light ...

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

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

METHOD AND APPARATUS FOR CARBONYLATING METHANOL WITH ACETIC ACID ENRICHED FLASH STREAM

A carbonylation process for producing acetic acid including: (a) carbonylating methanol or its reactive derivatives in the presence of a Group VIII metal catalyst and methyl iodide promoter to produce a liquid reaction mixture including acetic acid, water, methyl acetate and methyl iodide; (b) feeding the liquid reaction mixture at a feed temperature to a flash vessel which is maintained at a reduced pressure; (c) heating the flash vessel while concurrently flashing the reaction mixture to produce a crude product vapor stream, wherein the reaction mixture is selected and the flow rate of the reaction mixture fed to the flash vessel as well as the amount of heat supplied to the flash vessel is controlled such that the temperature of the crude product vapor stream is maintained at a temperature less than 90° F. cooler than the feed temperature of the liquid reaction mixture to the flasher and the concentration of acetic acid in the crude product vapor stream is greater than 70% by weight of the crude product vapor stream. 125.-. (canceled)26. A carbonylation process for producing acetic acid comprising:(a) carbonylating methanol or its reactive derivatives in a reactor in the presence of a rhodium metal catalyst and methyl iodide promoter to produce a liquid reaction mixture including acetic acid, water, methyl acetate and methyl iodide;(b) feeding the liquid reaction mixture to a flash vessel and heating the liquid reaction mixture in the flash vessel to separate the liquid reaction mixture into a crude product vapor stream and a catalyst solution;(c) recycling the catalyst solution to the reactor;(d) separating the crude product vapor stream in a first distillation column into an overhead stream comprising methyl iodide, methyl acetate and water and process stream comprising acetic acid; and(e) condensing the overhead stream and separating the condensed overhead stream into an aqueous stream and an organic stream,wherein the ratio of the crude product vapor stream ...

METHOD FOR PRODUCING POLYOLEFIN AND POLYOLEFIN PRODUCTION SYSTEM

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

FLOW REACTOR SYNTHESIS OF POLYMERS

A flow reactor system and methods having tubing useful as polymerization chamber. The flow reactor has at least one inlet and at least one mixing chamber, and an outlet. The method includes providing two phases, an aqueous phase and a non-aqueous phase and forming an emulsion for introduction into the flow reactor. 120-. (canceled)21. A system for polymerizing one or more monomers for producing a polymer salt , comprising: at least one inlet port configured for receiving an emulsified reactant composition comprising an aqueous monomer solution and a non-aqueous solution; and', 'at least one outlet port configured for discharging a polymer salt;, 'an amount of tubing havinga temperature controller sized to receive at least a portion of the amount of tubing;a mixing chamber, the mixing chamber having an inlet and an outlet, the outlet fluidically coupled to the inlet port of the tubing, the mixing chamber configured to emulsify a reactant composition; andat least one fluid flow control device fluidically coupled to the inlet of the mixing chamber.22. The system of ; wherein the at least one fluid flow control device comprises an aqueous monomer fluid flow control device and a non-aqueous fluid flow control device.23. The system of claim 21 , further comprising a second mixing chamber fluidically coupled to the inlet of the tubing.24. The system of claim 23 , further comprising a catalyst fluid flow control device fluidically coupled to the second mixing chamber or to the amount of tubing claim 23 , the catalyst fluid flow control device configured to introduce a catalyst to the reactant composition.25. The system of claim 21 , further configured to introduce organic solvent to the amount of tubing for recovering the polymer salt.26. A system for continuous flow synthesis of polyaniline (PANI) salt claim 21 , comprising: at least one inlet port configured for receiving an emulsified reactant composition comprising an aqueous aniline solution and a non-aqueous acid ...

Aerosol Generator, In Particular Soot Generator

An aerosol generator, in particular a soot generator. The aerosol generator includes a combustion chamber, in which fuel can be burned with an oxidizing agent in at least one soot-particle-creating flame, and a fluid feeding device for feeding fuel and an oxidizing agent into the combustion chamber. The fluid feeding device has at least three feed lines, the outlet-side end portions of which run parallel, so that at least three fluids of different types, in particular gases, can be introduced into the combustion chamber unmixed and in a parallel inflow direction. 1. An aerosol generator , configured as a soot generator , comprisinga combustion chamber, in which fuel can be burned with an oxidizing agent in at least one soot-particle-creating flame;a fluid feeding device for feeding the fuel and the oxidizing agent into the combustion chamber;wherein the fluid feeding device has at least three feed lines each feed line having a respective end portion, the respective end portions of each feed line are arranged parallel to each other so that at least three fluids of different types can be introduced into the combustion chamber unmixed and in a parallel inflow direction.2. The aerosol generator according to claim 1 , wherein the respective end portions of the at least three feed lines are arranged coaxially in one another.3. The aerosol generator according to claim 1 , wherein at least one ofthe respective end portions are arranged lying parallel next to one another; andthe respective end portions are arranged parallel next to one another to form an arrangement of lines with a packing density that is as great as possible.4. The aerosol generator according to claim 1 , wherein the fluid feeding device has one of:at least four feed lines;four feed lines; andseven feed lines.5. The aerosol generator according to claim 1 , wherein respective outlets of the feed lines are located at a same height with respect to an inflow direction.6. The aerosol generator according to claim ...

Automated purification and formulation device for radiopharmaceutical compounds

A device for purifying and formulating a radiopharmaceutical compound includes an automated purification subsystem that automates the loading of a sample into a sample loop for downstream purification via HPLC. A column selector valve is provided to select from one of a plurality of columns. Fractions can be collected as well as the desired product. The device includes an automated formulation subsystem that first sends the product to a dilution reservoir prior to being pneumatically pushed onto a solid phase extraction (SPE) cartridge. Automated rinse, elution, and reconstitution are also performed with the automated formulation subsystem. The device may be directly coupled to the output of an automated radiosynthesizer.

METHOD AND APPARATUS FOR CARBONYLATING METHANOL WITH ACETIC ACID ENRICHED FLASH STREAM

A carbonylation process for producing acetic acid including: (a) carbonylating methanol or its reactive derivatives in the presence of a Group VIII metal catalyst and methyl iodide promoter to produce a liquid reaction mixture including acetic acid, water, methyl acetate and methyl iodide; (b) feeding the liquid reaction mixture at a feed temperature to a flash vessel which is maintained at a reduced pressure; (c) heating the flash vessel while concurrently flashing the reaction mixture to produce a crude product vapor stream, wherein the reaction mixture is selected and the flow rate of the reaction mixture fed to the flash vessel as well as the amount of heat supplied to the flash vessel is controlled such that the temperature of the crude product vapor stream is maintained at a temperature less than 90° F. cooler than the feed temperature of the liquid reaction mixture to the flasher and the concentration of acetic acid in the crude product vapor stream is greater than 70% by weight of the crude product vapor stream. 125-. (canceled)26. A carbonylation process for producing acetic acid comprising:carbonylating methanol or its reactive derivatives in the presence of a rhodium catalyst in a reactor to produce a liquid reaction mixture comprising acetic acid, the rhodium metal catalyst, water, iodide catalyst stabilizer, methyl acetate and methyl iodide;flashing the liquid reaction mixture in a flash vessel to form a crude product vapor stream comprising acetic acid, methyl iodide, and methyl acetate, and a catalyst solution comprising the rhodium metal catalyst, iodide catalyst stabilizer, methyl acetate, and water; and distilling the crude product vapor stream to form a first overhead, and a side stream comprising acetic acid; and', 'distilling the side stream into a second overhead, and a purified acetic acid stream,, 'an acetic acid collection step comprisingwherein the catalyst solution comprises methyl acetate in an amount less than or equal to 1.9% by weight ...

Process of Removing Heat

The present invention provides an improved process for removing heat from an exothermic reaction. In particular, the present invention provides a process wherein heat can be removed from multiple reaction trains using a common coolant system. 120-. (canceled)21. A method of starting up an exothermic reaction comprising:(a) providing at least two separate reaction trains each comprising at least one reactor;(b) providing a common coolant circulation system which comprises a single common reservoir comprising a coolant which is fed into each reaction train;(c) starting circulation of the coolant to each reaction train;(d) increasing the pressure the reactors to a desired reaction pressure;(e) feeding a reactant feedstream into each reaction train;(f) increasing the temperature of the single common reservoir while adjusting the GHSV of the reactant feedstreams through each reaction train to obtain the desired extent of exothermic reaction.2226-. (canceled)27. A method of starting up an exothermic reaction in a start-up reactor comprised in a reaction train , said method comprisinga) providing multiple reaction trains each comprising at least one reactor;b) providing a common coolant circulation system which comprises a single common reservoir comprising a first coolant which is fed into each reaction train except the reaction train comprising the start-up reactor in which the exothermic reaction is to be started up;c) providing a second coolant circulation system associated with a second coolant reservoir comprising a second coolant which is fed into the reaction train comprising the start-up reactor;d) increasing the pressure in the start-up reactor to a desired reaction pressure;e) feeding a reactant feedstream into the reaction train comprising the start-up reactor;f) running the process until the operating conditions of the start-up reactor are such that the coolant exiting the start-up reactor may be reintroduced to the common coolant circulation system; andg) ...

METHOD AND SYSTEM FOR CONTROLLING A HYDROCRACKER AND FRACTIONATOR

A method and system for controlling a hydrocracker and fractionator reaction loop is disclosed. The method and system utilizes a sidedraw tray within the fractionator distillation zone upon which liquid is collected. This liquid is withdrawn as a sidedraw stream. The withdrawal of the liquid from the sidedraw tray is controlled based on the level of liquid on the sidedraw tray rather than at a set or determined flow rate. The sidedraw stream is separated into a first stream and a product stream. Unlike other processes where the flow rate of the product stream is set and the internal reflux flow rate varies, the method involves fixing the flow rate of the first stream that is returned to the distillation zone of the fractionators with the flow rate of the product stream being set so as to control the liquid level on the sidedraw tray. 1. A method of controlling the operation of a fractionator and hydrocracker reaction loop , wherein said method comprises:providing a fractionator for receiving a hydrocracker effluent yielded from a hydrocracker reactor as a fractionator feed, wherein said fractionator defines a distillation zone that includes a bottom zone, an upper zone, and an intermediate zone between said bottom zone and said upper zone, wherein said intermediate zone has a sidedraw tray;introducing said fractionator feed into said bottom zone of said fractionator;collecting on said sidedraw tray a liquid level of hydrocarbons having a desired boiling range;withdrawing a sidedraw stream of said hydrocarbon from said sidedraw tray;separating said sidedraw stream into a first stream and a product stream;introducing said first stream to said distillation zone;responsive to a difference between a measured flow of said first stream and a desired flow of said first stream, controlling the flow of said first stream;responsive to a difference between a measured liquid level on said sidedraw tray and a desired liquid level on said sidedraw tray, controlling the flow of ...

GRAPHENE WOOL AND MANUFACTURE THEREOF

The invention provides a system for manufacturing graphene wool which includes a receptacle, a graphene growth substrate locatable inside the receptacle, a heating device for increasing the temperature inside the receptacle, an inlet gas flow communication with the receptacle for controlling the introduction of gaseous substances into the receptacle, and a cooling device for rapidly decreasing the temperature inside the receptacle. The invention extends to a method for manufacturing graphene wool and to an air pollutant trap which includes: a sorbent, and a housing for housing the sorbent, wherein the sorbent includes graphene. 1. A system for manufacturing graphene wool which includes:a receptacle;a graphene growth substrate beatable inside the receptacle;a heating device for increasing the temperature inside the receptacle;an inlet gas flow communication with the receptacle for controlling the introduction of gaseous substances into the receptacle; anda cooling device for rapidly decreasing the temperature inside the receptacle, wherein the graphene growth substrate includes quartz wool.2. A system as claimed in wherein the receptacle includes one or more of a furnace and a deposition chamber.3. A system as claimed in claim 1 , wherein the receptacle is a quartz vessel.4. A system as claimed in claim 3 , wherein the receptacle is a quartz tube.5. (canceled)6. A system as claimed in claim 1 , wherein the graphene growth substrate includes coarse quartz wool having a fibre thickness ranging between 9 and 30 μm.7. A system as claimed in claim 1 , wherein the heating device increases the temperature inside the receptacle to the desired temperature so as to allow annealing of the graphene growth substrate and subsequent graphene growth at a rate of about 10 degrees Celsius per minute up to about 1200 degrees Celsius with the conditions for annealing the graphene growth substrate kept at a constant for a period of from 5 to 60 minutes.8. A system as claimed in claim 7 , ...

PROCESS OF REMOVING HEAT

The present invention provides an improved process for removing heat from an exothermic reaction. In particular, the present invention provides a process wherein heat can be removed from multiple reaction trains using a common coolant system. 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. (canceled)14. (canceled)15. (canceled)16. (canceled)17. (canceled)18. (canceled)19. (canceled)20. (canceled)21. (canceled)22. A method of isolating a reaction train from an exothermic reaction process circuit which comprises multiple reaction trains to which a first coolant is fed from a common first coolant reservoir and wherein each reaction train comprises a reactor to which a reactant substream is fed , comprising:performing the exothermic reaction in the reactor to produce reaction products and first coolant to which heat has been transferred;providing a second coolant circulation system associated with a second coolant reservoir;redirecting the first coolant to which heat has been transferred from the reaction train to be isolated to the second coolant reservoir; and thenstopping the feed of the first coolant to the reaction train to be isolated while simultaneously initiating the feed of the second coolant from the second coolant reservoir to the reaction train to be isolated.23. The method according to claim 22 , wherein the first coolant and the second coolant are the same.24. The method according to claim 22 , wherein the first coolant and the second coolant are different.25. A method of reintroducing a reaction train which has been isolated from an exothermic reaction process circuit which comprises multiple reaction trains to which a first coolant is fed from a common coolant reservoir claim 22 , wherein each reaction train comprises a reactor to which a reactant substream is fed and wherein:an exothermic reaction is performed in the reactor of each ...

Nylon salt solution preparation processes with trim diamine

Disclosed are nylon salt solution preparation processes including a trim diamine feed. The nylon salt solution is prepared by feeding a dicarboxylic acid monomer and a diamine monomer to a single continuous stirred tank reactor. The dicarboxylic acid is metered, based on weight, from a loss-in-weight feeder to the reactor. The nylon salt solution is formed continuously and has low variability from a target pH and/or a target salt solution concentration. The nylon salt solution is transferred directly to a storage tank, without further monomer addition, pH adjustment, or salt solution adjustment after exiting the continuous stirred tank reactor.

VANADIUM OXIDE FOR INFRARED COATINGS AND METHODS THEREOF

The present invention relates to vanadium oxide and methods of controlling reaction processes for making such materials (e.g., powders). In particular embodiments, the method includes control of oxygen partial pressure in order to kinetically control the oxidation species of the crystalline vanadium oxide material. Other methods, uses, systems, protocols, and coatings are also described. 1. A method of preparing crystalline vanadium oxide , the method comprising:(i) providing a vanadium oxide precursor;{'sub': '2', '(ii) annealing the precursor at a reduced Opartial pressure, thereby preparing the crystalline vanadium oxide in tetragonal form; and'}{'sub': 1', '2', '2, '(iii) determining a first temperature Tat which a metastable VOform and/or a tetragonal VOform is present.'}2. The method of claim 1 , further comprising (iv) adjusting to a further reduced Opartial pressure claim 1 , thereby further isolating the crystalline vanadium oxide in tetragonal form.3. The method of claim 1 , wherein the crystalline vanadium oxide is VO.4. The method of claim 1 , wherein the vanadium oxide precursor comprises vanadium oxide particles.5. The method of claim 4 , wherein the crystalline vanadium oxide has substantially the same morphology as the vanadium oxide particles.6. The method of claim 5 , wherein the vanadium oxide particles comprise vanadium pentoxide VO.7. A method of preparing crystalline vanadium oxide claim 5 , the method comprising:(i) providing a vanadium oxide precursor;{'sub': 2', '1, '(ii) annealing the precursor at a first Opartial pressure P, thereby forming one or more vanadium oxide form(s);'}(iii) obtaining one or more spectroscopy measurements of the vanadium oxide form(s);{'sub': 1', '2', '2, '(iv) determining a first temperature Tat which a metastable VOform and/or a tetragonal VOform is present; and'}{'sub': 2', '2', '1, '(v) adjusting to a second Opartial pressure Pwhile maintaining T, thereby preparing the crystalline vanadium oxide.'}8. The method ...

Aerosol Generator, In Particular Soot Generator

An aerosol generator, in particular a soot generator. The aerosol generator includes a combustion chamber, in which fuel can be burned with an oxidizing agent in at least one soot-particle-creating flame, and a fluid feeding device for feeding fuel and an oxidizing agent into the combustion chamber. The fluid feeding device has at least three feed lines, the outlet-side end portions of which run parallel, so that at least three fluids of different types, in particular gases, can be introduced into the combustion chamber unmixed and in a parallel inflow direction. 1. An aerosol generator , configured as a soot generator , comprisinga combustion chamber, in which fuel can be burned with an oxidizing agent in at least one soot-particle-creating flame;a fluid feeding device for feeding the fuel and the oxidizing agent into the combustion chamber;wherein the fluid feeding device has at least three feed lines each feed line having a respective end portion, the respective end portions of each feed line are arranged parallel to each other so that at least three fluids of different types can be introduced into the combustion chamber unmixed and in a parallel inflow direction.2. The aerosol generator according to claim 1 , wherein the respective end portions of the at least three feed lines are arranged coaxially in one another.3. The aerosol generator according to claim 1 , wherein at least one ofthe respective end portions are arranged lying parallel next to one another; andthe respective end portions are arranged parallel next to one another to form an arrangement of lines with a packing density that is as great as possible.4. The aerosol generator according to claim 1 , wherein the fluid feeding device has one of:at least four feed lines;four feed lines; andseven feed lines.5. The aerosol generator according to claim 1 , wherein respective outlets of the feed lines are located at a same height with respect to an inflow direction.6. The aerosol generator according to claim ...

System and Method for Hydrothermal Upgrading of Fatty Acid Feedstock

A system and method is provided for upgrading a continuously flowing process stream including heavy crude oil (HCO). A reactor receives the process stream in combination with water, at an inlet temperature within a range of about 60° C. to about 200° C. The reactor includes one or more process flow tubes having a combined length of about 30 times their aggregated transverse cross-sectional dimension, and progressively heats the process stream to an outlet temperature T(max)1 within a range of between about 260° C. to about 400° C. The reactor maintains the process stream at a pressure sufficient to ensure that it remains a single phase at T(max)1. A controller selectively adjusts the rate of flow of the process stream through the reactor to maintain a total residence time of greater than about 1 minute and less than about 25 minutes. 1. A system for upgrading a continuously flowing process stream including hydrocarbons , comprising:a fluid flow path configured to convey the process stream continuously therethrough in a downstream direction, the flow path including a reactor;the reactor configured to receive the process stream in combination with water, at an inlet temperature within a range of about 60° C. to about 200° C.;the reactor including one or more process flow tubes defining an aggregated interior cross-sectional dimension in a plane extending transversely to the downstream direction therethrough, the one or more flow tubes having a combined length of at least about 4 times the aggregated interior cross-sectional dimension;the reactor configured to apply heat to the process stream flowing therethrough, to progressively heat the process stream from the inlet temperature at an upstream portion of the reactor, to an outlet temperature T(max)1 within a range of between about 260° C. to about 425° C. at a downstream portion of the reactor;the reactor configured to maintain the process stream at a pressure sufficient to ensure that the process stream remains a ...

Vent Gas Purge Optimizer for Slurry Loop Polyethylene Reactors

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

APPARATUS TO SIMULATE BIOCIDE PERFORMANCE IN CRUDE PIPELINE CONDITIONS

An apparatus to simulate biocide performance in crude oil pipeline conditions is disclosed. The apparatus includes: a reactor to simulate a two-phase crude oil pipeline which includes a crude oil phase above a water phase. The reactor has an agitator to control a flow of the water phase in the reactor in response to a motor that drives an agitation rate of the agitator. A crude oil inlet supplies crude oil to the reactor for the crude oil phase. A water inlet supplies water to the reactor for the water phase. A control circuit is configured by code to control a proportion of the water to the crude oil supplied to the reactor and to control the motor to drive a desired agitation rate of the agitator. A biocide inlet supplies biocide to the reactor. A water sample outlet enables sampling of the water phase of the reactor. 1. An apparatus to simulate biocide performance in crude oil pipeline conditions , the apparatus comprising:a reactor to simulate a two-phase crude oil pipeline and including a crude oil phase above a water phase, the reactor comprising an agitator to control a flow of the water phase in the reactor in response to a motor that drives an agitation rate of the agitator;a crude oil inlet to supply crude oil to the reactor for the crude oil phase;a water inlet to supply water to the reactor for the water phase; control a proportion of the water to the crude oil supplied to the reactor by the crude oil inlet and the water inlet, and', 'control the motor to drive a desired agitation rate of the agitator;, 'a control circuit configured by logic or code toa biocide inlet to supply biocide to the reactor; anda water sample outlet to sample the water phase of the reactor.2. The apparatus of claim 1 , whereinthe reactor further comprises a plurality of reactors each having a dedicated biocide inlet and a dedicated water sample outlet, andthe control circuit is further configured by logic or code to independently control the proportion of the water to the crude ...

CONTROL SYSTEM FOR A COMPRESSOR WITH PRESURE-BASED SUBSYSTEM, SYNTHESIS PLANT AND CONTROL METHOD

Control system arranged for a rotary compressor driven by a rotary engine, and includes: a first control subsystem, a second control subsystem and a selector; the first control subsystem is arranged to provide a first control signal as a function of the performance and the speed of the compressor; the second control subsystem is arranged to provide a second control signal as a function of the performance of the compressor; the selector is arranged to select the first control signal or the second control signal as a third control signal to be provided to a power control input of the engine. 1. A control system for a rotary compressor driven by a rotary engine , comprising:a first control subsystem comprising:a performance input arranged to receive a first measure signal indicating performance of the rotary compressor,a speed input arranged to receive a second measure signal indicating rotation speed of the rotary compressor or the rotary engine, anda first control output arranged to provide a first control signal as a function of the first measure signal and the second measure signal;a second control subsystem comprising:a performance input arranged to receive a third measure signal indicating performance of the rotary compressor, anda second control output arranged to provide a second control signal as a function of the third measure signal; a first input electrically connected to the first control output,', 'a second input electrically connected to the second control output, and', 'a third control output arranged to provide a third control signal to a power control input of the rotary engine,, 'a selector comprisingwherein the selector is arranged to select the first control signal or the second control signal as the third control signal to be provided at the third control output.2. The control system of claim 1 , wherein the selector is arranged to select the second control signal based on one or more of at least the following criteria:an absolute value of a ...

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.

APPARATUS AND METHOD FOR SYNTHESIZING F-18 LABELED RADIOACTIVE PHARMACEUTICALS

The present invention relates to an apparatus for synthesizing F-18 labeled radioactive pharmaceutical. The apparatus for synthesizing F-18 labeled radioactive pharmaceutical includes an F-18 radioactive isotope supplier, a reagent supplier, a polymer precursor cartridge, a first heating unit, a polymer compound cartridge, a synthesizing container, a second heating unit, a water liquid container, a transmitting gas supplier, a cleansing liquid supplier, a connection tube, a plurality of control valves, and a controller. 1. An apparatus for synthesizing F-18 labeled radioactive pharmaceutical comprising:an F-18 radioactive isotope supplier which supplies F-18 radioactive isotope;a reagent supplier which supplies reagent reacting with the F-18 radioactive isotope;a polymer precursor cartridge which is filled with polymer precursor and collects the F-18 radioactive isotope and causes a labeling reaction;a first heating unit which selectively heats the polymer precursor cartridge;a polymer compound cartridge which is filled with polymer compound and separates polar compound and nonpolar compound from each other;a synthesizing container which causes hydrolysis reaction of produced intermediate compound;a second heating unit which selectively heats the synthesizing container;a waste liquid container which contains fluid which is discarded after having been used for synthesis;a collecting container which collects a final synthesized product;a transmitting gas supplier which supplies transmitting gas;a cleansing liquid supplier which supplies a cleansing liquid;a connection tube which connects the F-18 radioactive isotope supplier, the reagent supplier, the polymer precursor cartridge, the polymer compound cartridge, the synthesizing container, the waste liquid container, the collection container, the transmitting gas supplier, and the cleansing liquid supplier together;a plurality of control valves which are disposed at predetermined positions of the connection tube to ...

PROCESS FOR ACID-CATALYZED DECOMPOSITION OF ARYL a- HYDROPEROXIDE WITH CONTINUOUS FLOW TUBULAR REACTOR

The present disclosure relates to a process for acid-catalyzed decomposition of aryl α-hydroperoxide with a continuous flow tubular reactor. The process is a novel process performed in a tubular reactor, taking the aryl α-hydroperoxide such as cumene hydroperoxide (CHP) as a raw material and taking acids as a catalyst, performing acid-catalyzed decomposition of the aryl α-hydroperoxide solution in a short reaction time ranging from tens of seconds to several minutes, thereby obtaining the phenols; wherein an inert component may be filled in the reactor, so that the effects of heat transmission and mass transfer can be enhanced. The aryl α-hydroperoxide and acid are respectively introduced by a metering pump into a mixing module to be mixed, and then enter the tubular reactor to be reacted so as to produce the products such as phenols. 3. The process for acid-catalyzed decomposition of aryl α-hydroperoxide with a continuous flow tubular reactor according to claim 1 , wherein the aryl α-hydroperoxide is cumyl hydroperoxide (CHP).4. The process for acid-catalyzed decomposition of aryl α-hydroperoxide with a continuous flow tubular reactor according to claim 1 , wherein the process further comprises the following step (2):(2) the concentration of each substance in the reaction products is analyzed by a liquid chromatography external standard method, and the aryl α-hydroperoxide is titrated by an iodometric method.5. The process for acid-catalyzed decomposition of aryl α-hydroperoxide with a continuous flow tubular reactor according to claim 3 , wherein the CHP in step (1) is a concentrated oxidation liquid of cumene claim 3 , the solvent is one of acetone and cumene or a mixture thereof; or the oxidation liquid of cumene is used as a source of the CHP.6. The process for acid-catalyzed decomposition of aryl α-hydroperoxide with a continuous flow tubular reactor according to claim 1 , wherein the acid in step (1) is one or more selected from a group consisting of sulfuric ...

Catalyst and Process for the Production of Hydrogen from Ammonia Boranes

The present invention relates to a process for the production of hydrogen comprising contacting at least one complex of formula (I), (I) wherein: Xis an anion; M is a metal selected from Ru, Os, Fe, Co and Ni; D is optionally present and is one or more monodentate or multidentate donor ligands; Yis selected from CR, B and N; Zand Zare each independently selected from ═N, ═P, NR, PR, O, S and Se; or Zis a direct bond between carbocyclic ring B and substituent R; each of A and B is independently a saturated, unsaturated or partially unsaturated carbocyclic hydrocarbon ring; Rand Rare each independently selected from H, C-alkyl, aryl and C-haloalkyl, and a linker group optionally attached to a solid support; or Rand Rtogether form the following moiety: (AB) Yis a direct single bond or double bond, or is CR; R, R, Rand Rare each independently selected from H, C-alkyl, C-alkenyl, C-alkynyl, aryl, C-haloalkyl, NRRand a linker group optionally attached to a solid support; or two or more of said Rand Rgroups are linked, together with the carbons to which they are attached, to form a saturated or unsaturated hydrocarbon group; R, R, Rand Rare each independently selected from H, C-alkyl, C-alkenyl, C-alkynyl, aryl, C-haloalkyl, and a linker group optionally attached to a solid support; with at least one substrate of formula (II), RRNH—BHRR, wherein Rto Rare each independently selected from H, C-alkyl, fluoro-substituted C-alkyl, C-aryl and C-aralkyl, or any two of R, R, Rand Rare linked to form a C-alkylene group or C-alkenylene group, which together with the nitrogen and/or boron atoms to which they are attached, forms a cyclic group; or a substrate comprising two, three or four substrates of formula (II) linked via one or more bridging groups so as to form a dimeric, trimeric or tetrameric species, and wherein the bridging group is selected from straight or branched C-alkylene optionally substituted by one or more fluoro groups, boron, C-aryl and C-aralkyl; or a substrate ...

BIOMASS CONVERSION REACTORS AND ASSOCIATED SYSTEMS AND METHODS

Systems and methods associated with biomass decomposition are generally described. Certain embodiments are related to adjusting a flow rate of a fluid comprising oxygen into a reactor in which biomass is decomposed. The adjustment may be made, at least in part, based upon a measurement of a characteristic of the reactor and/or a characteristic of the biomass. Certain embodiments are related to cooling at least partially decomposed biomass. The biomass may be cooled by flowing a gas over an outlet conduit in which the biomass is cooled, and then directing the gas to a reactor after it has flowed over the outlet conduit. Certain embodiments are related to systems comprising a reactor and an outlet conduit configured such that greater than or equal to 75% of its axially projected cross-sectional area is occupied by a conveyor. Certain embodiments are related to systems comprising a reactor comprising an elongated compartment having a longitudinal axis arranged substantially vertically and an outlet conduit comprising a conveyor. 1. A method of decomposing biomass within a reactor to form a primarily solid product , comprising:adjusting a flow rate of a fluid comprising oxygen into the reactor in which the biomass is decomposed, wherein the adjustment is made, at least in part, based upon a measurement of a characteristic of the reactor and/or a characteristic of the biomass.2. The method of claim 1 , wherein the reactor comprises an inlet fluidically connected to a source of fluid comprising oxygen.3. The method of claim 1 , further comprising measuring a characteristic of the reactor claim 1 , wherein the characteristic comprises:a flow rate of the biomass into the reactor;a temperature at a point inside the reactor, outside the reactor, or of a surface of the reactor and/or a measurement of a variation in a temperature at a point inside the reactor, outside the reactor, or of a surface of the reactor;a pressure within the reactor; and/ora flow rate of decomposed ...

Method For Preparing Modified Polymerization Initiator And Apparatus For Preparing Modified Polymerization Initiator

The present invention relates to a method for producing a modified polymerization initiator, and more particularly, to a method for preparing a modified polymerization initiator, wherein the method includes the steps of: (S) introducing a first fluid and a second fluid into a reactor, and reacting the compounds included in the fluids, and (S) obtaining the modified polymerization initiator prepared by the reaction of the step (S) through an outlet of the reactor, wherein the step (S) and step (S) are continuously performed, wherein in the step (S), the flow amount of the first fluid and the second fluid is maintained constant at the time when the first fluid and the second fluid are mixed, and the flow rate of the first fluid is increased. Also, the present invention provides an apparatus for producing a modified polymerization initiator for performing the same. 1. A method for preparing a modified polymerization initiator , the method comprising the steps of:{'b': '1', '(S) introducing a first fluid through a first fluid inlet and a second fluid through a second fluid inlet into a reactor having the first fluid inlet including a first functional group-containing compound and the second fluid inlet including a second functional group-containing compound, and reacting the first functional group-containing compound with the second functional group-containing compound; and'}{'b': 2', '1, '(S) obtaining a third fluid including the modified polymerization initiator prepared by the reaction of the step (S) through an outlet provided in the reactor,'}{'b': 1', '2, 'wherein the step (S) and step (S) are continuously performed,'}{'b': '1', 'wherein in the step (S), the flow amounts of the first fluid and the second fluid are maintained constant at the time when the first fluid and the second fluid are mixed, and the flow rate of the first fluid is increased at the time when the first fluid and the second fluid are mixed.'}2. The method of claim 1 , wherein the first ...

Halogen Selective Detection Gas Chromatography for the On-Line Analysis and Control of Selective Oxidation Chemical Production Processes

A method for process monitoring and control of a chemical reactor in which a chemical reaction utilizing a halogenated selectivity modifier is performed includes: measuring a level of halogenated components in an inlet stream of a reactor inlet; measuring a level of halogenated components in an outlet stream of a reactor outlet; based on the level of halogenated components at the inlet stream and the outlet stream, determining a process performance indicator associated with a halogenated component; and adjusting an amount of halogenated selectivity modifier added to the reactor based on the process performance indicator. 1. A method for process monitoring and control of a chemical reactor in which a chemical reaction utilizing a halogenated selectivity modifier is performed comprising:measuring a level of halogenated components in an inlet stream of a reactor inlet;measuring a level of halogenated components in an outlet stream of a reactor outlet;based on the level of halogenated components at the inlet stream and the outlet stream, determining a process performance indicator associated with a halogenated component; andadjusting an amount of halogenated selectivity modifier added to the reactor, an amount of reactor feedstock, a flow rate, and/or a reactor temperature, based on the process performance indicator.2. The method of claim 1 , wherein the level of halogenated components in the inlet stream and the outlet stream includes all halogenated components contained in the inlet stream and outlet stream.3. The method of claim 1 , wherein the level of halogenated components in the inlet stream and outlet stream is measured with a halogen-selective detector using gas chromatography.4. The method of claim 1 , wherein the level of halogenated components in the inlet stream and outlet stream is measured without significant chemical interference.5. The method of claim 1 , further comprising separating halogenated components from the inlet stream and/or the outlet stream ...

APPARATUS AND PROCESS FOR CONVERSION OF AMMONIA INTO OXIDES OF NITROGEN

Disclosed is an apparatus for conversion of ammonia into oxides of nitrogen which may comprise an adiabatic burner (), a set of platinum/rhodium alloy catalytic gauzes (A), (B), and (C), a waste heat recovery boiler (WHRB) (), an absorption tower (A), (B), (C), (D) and (E), a NaOH tank () and a surge tank (). Further, the adiabatic burner may be configured to carry out catalytic oxidation of air and ammonia, using catalytic gauzes (A), (B), and (C) of platinum/rhodium alloy. Further, the mixture of air and ammonia may be selectively oxidized to oxides of nitrogen, which may be absorbed in an alkali medium in the absorption tower (A), (B), (C), (D) and (E), to yield sodium nitrites and nitrates.

CONTINUOUS DESULFURIZATION PROCESS BASED ON METAL OXIDE-BASED REGENERABLE SORBENTS

A continuous desulfurization process and process system are described for removal of reduced sulfur species at gas stream concentrations in a range of from about 5 to about 5000 ppmv, using fixed beds containing regenerable sorbents, and for regeneration of such regenerable sorbents. The desulfurization removes the reduced sulfur species of hydrogen sulfide, carbonyl sulfide, carbon disulfide, and/or thiols and disulfides with four or less carbon atoms, to ppbv concentrations. In specific disclosed implementations, regenerable metal oxide-based sorbents are integrated along with a functional and effective process to control the regeneration reaction and process while maintaining a stable dynamic sulfur capacity. A membrane-based process and system is described for producing regeneration and purge gas for the desulfurization.

LIQUID LEVEL METER, VAPORIZER EQUIPPED WITH THE SAME, AND LIQUID LEVEL DETECTION METHOD

The liquid level meter according to the present invention includes a resistive temperature detector, a temperature measuring body located above it, a temperature detecting unit detecting temperatures of the resistive temperature detector and the temperature measuring body, a current controlling unit determining a current value to be flowed through the resistive temperature detector so that the resistive temperature detector and the temperature measuring body become a predetermined temperature difference, a power supply unit supplying the current of the determined current value to the resistive temperature detector, and a liquid level detecting unit detecting a position of a liquid level. The liquid level detecting unit detects the change in the relative position of the liquid level relative to the resistive temperature detector by determining whether a change width of the current value flowing through the resistive temperature detector during a predetermined period of time is positive or negative, and whether the change width is not less than a predetermined value. As a result, the position of the liquid level can be accurately detected without being affected by the variation in the characteristics of the resistive temperature detector. 1. A liquid level meter comprising:a first resistive temperature detector;a temperature measuring body disposed at a position higher than a position of the first resistive temperature detector disposed; anda control unit detecting a position of a liquid level using the temperature measuring body and the first resistive temperature detector; whereinwhen a current value flowing through the first resistive temperature detector has changed by a predetermined constant value or more within a predetermined period of time, the control unit detects that the position of the liquid level has changed from a position higher than the position of the first resistive temperature detector disposed to a position lower than the position of the first ...

Para-Orthohydrogen Conversion Using a Vortex Tube

A para-orthohydrogen conversion device comprises a vortex tube. The vortex tube may include an inlet disposed at a first end of the vortex tube, a catalyst disposed on the interior wall of the vortex tube, a first outlet comprising an opening on the perimeter of a second end of the vortex tube, a stopper disposed at the center of the second end of the vortex tube, and a second outlet disposed on the first end of the vortex tube. A method includes converting parahydrogen to orthohydrogen via the catalyst and rotational force as hydrogen gas moves through the vortex tube such that cooled parahydrogen-rich gas or liquid hydrogen accumulates near the center of the vortex tube. 1. A method comprising:transferring hydrogen gas into a proximal end of a vortex tube, at least a portion of an interior wall of the vortex tube comprising a catalyst, wherein the hydrogen gas comprises orthohydrogen and parahydrogen;flowing the hydrogen gas toward a distal end of the vortex tube, the hydrogen gas rotating within the vortex tube as the hydrogen gas flows toward the distal end;reacting the hydrogen gas with the catalyst such that at least a portion of the parahydrogen is converted to orthohydrogen;expelling orthohydrogen-rich hydrogen gas from the distal end of the vortex tube; andflowing parahydrogen-rich hydrogen gas out the proximal end of the vortex tube.2. The method of claim 1 , wherein the hydrogen gas transferred into the proximal end of the vortex tube comprises approximately 50% orthohydrogen and approximately 50% parahydrogen.3. The method of claim 1 , wherein the orthohydrogen-rich hydrogen gas comprises more orthohydrogen than parahydrogen.4. The method of claim 1 , wherein the orthohydrogen-rich hydrogen gas comprises approximately 75% orthohydrogen and approximately 25% parahydrogen.5. The method of claim 1 , wherein the parahydrogen-rich hydrogen gas comprises more parahydrogen than orthohydrogen.61. The method of clam claim 1 , wherein the parahydrogen-rich ...

PROCESS FOR OPERATING A GAS PHASE PHOSGENATION PLANT

This invention relates to a process for operating a gas phase phosgenation plant () to form an isocyanate () by reacting an amine () with phosgene (), in which the gas phase phosgenation plant is shut down by first stopping the amine stream and still maintaining the phosgene stream. After a period of time which corresponds to at least 10 times the residence time of phosgene () in the main parts of the gas phase phosgenation plant () in regular operation, calculated from the time at which the amine inflow has been completely stopped, the feed of phosgene is also stopped. An inert gas stream () is maintained through the amine and phosgene feeding devices and through all the other essential parts of the gas phase phosgenation plant () during the shutdown. 110042124100. A method of operating a gas phase phosgenation plant () for producing an isocyanate () comprising reacting an amine () with phosgene () in a stoichiometric excess in relation to the primary amino groups of the amine () to give the corresponding isocyanate () , in which said gas phase phosgenation plant () comprises at least{'b': 1000', '10', '1', '3, '(i) an apparatus for providing a gaseous phosgene stream (), optionally comprising, as well as phosgene (), an inert substance (),'}{'b': 2000', '20', '2', '3, '(ii) an apparatus for providing a gaseous amine stream (), optionally comprising, as well as amine (), an inert substance (),'}{'b': 3100', '10', '20', '1100', '2100', '1000', '2000, '(iii) a mixing zone () for mixing the streams () and (), the mixing zone being connected by connecting devices (, ) to the apparatus and the apparatus ,'}{'b': 3200', '3100', '10', '20, '(iv) a reaction zone () arranged downstream of the mixing zone () or further conversion of the previously mixed streams () and (),'}{'b': 4000', '3200, '(v) a reaction stopping zone () arranged downstream of the reaction zone () to end the reaction,'}and optionally{'b': 5000', '1', '5100', '5200, '(vi) a workup section () which ...

Flow reactor synthesis of polymers

A flow reactor system and methods having tubing useful as polymerization chamber. The flow reactor has at least one inlet and at least one mixing chamber, and an outlet. The method includes providing two phases, an aqueous phase and a non-aqueous phase and forming an emulsion for introduction into the flow reactor.

AUTOMATIC AMMONIA HYDROXIDE DEPLOYMENT SYSTEM

An automatic ammonia hydroxide deployment system comprises an ammonia hydroxide deployment device and an automatic ammonia hydroxide deployment controlling device. The ammonia hydroxide deployment device includes a chamber for storing ammonia hydroxide, an ammonia pipe and a water pipe. The automatic ammonia hydroxide deployment controlling device includes an electrical conductivity meter, a liquid level sensor and an operating controller. The electrical conductivity meter is for detecting an electrical conductivity of the ammonia hydroxide in the chamber. The operating controller is configured to obtain an ammonia concentration of the ammonia hydroxide according to the electrical conductivity of the ammonia hydroxide. The operating controller adjusts ammonia gas flowing into the chamber according to whether the ammonia concentration is less than a predetermined threshold or not, and adjusts water flowing into the chamber according to whether the liquid level is lower than a predetermined lower threshold or not. 1. An automatic ammonia hydroxide deployment system , comprising:an ammonia hydroxide deployment device including a chamber for storing ammonia hydroxide which comprises ammonia gas and water, an ammonia pipe for supplying ammonia gas and a water pipe for supplying water, wherein the chamber is connected to the ammonia pipe and the water pipe, and the ammonia pipe is provided with an ammonia valve for regulating the flow of the ammonia gas flowing into the chamber, and the water pipe is provided with a water valve for regulating the flow of the water flowing into the chamber; andan automatic ammonia hydroxide deployment controlling device including an electrical conductivity meter, a liquid level sensor, and an operating controller, wherein the electrical conductivity meter is disposed to detect an electrical conductivity of the ammonia hydroxide of the chamber, the liquid level sensor is disposed to detect a liquid level of the chamber, and the operating ...

Reactor and method for production of silicon

Reactor for production of silicon, comprising a reactor volume, distinctive in that the reactor comprises or is operatively arranged to at least one means for setting a silicon-containing reaction gas for chemical vapor deposition (CVD) into rotation inside the reactor volume. Method for production of silicon.

REACTOR VESSELS WITH PRESSURE AND HEAT TRANSFER FEATURES FOR PRODUCING HYDROGEN-BASED FUELS AND STRUCTURAL ELEMENTS, AND ASSOCIATED SYSTEMS AND METHODS

Reactor vessels with pressure and heat transfer features for producing hydrogen-based fuels and structural elements, and associated systems and methods. A representative reactor system includes a first reaction zone and a heat path, a reactant source coupled to the first reaction zone, and a first actuator coupled to cyclically pressurize the first reaction zone. A second reaction zone is in fluid communication with the first, a valve is coupled between the first and second reaction zones to control a flow rate therebetween, and a second actuator is coupled in fluid communication with the second reaction zone to cyclically pressurize the second reaction zone. First and second heat exchangers direct heat from products to reactants in the reaction zones. A controller controls the first and second actuators in a coordinated manner based at least in part on a flow rate of the second product from the second reaction zone. 1. A method for processing a hydrogenous compound , comprising:directing reactants, including a hydrogenous compound, to a first reaction zone;cyclically varying a pressure at the first reaction zone in accordance with a first cycle;directing heat into the first reaction zone to heat the reactants;disassociating the hydrogenous compound to produce a first produce in an endothermic reaction;transferring the first produce to a second reaction zone;cyclically varying a pressure at the second reaction zone in accordance with a second cycle;at the second reaction zone, producing a second product including at least one of a hydrogen-based fuel and a structural building block in an exothermic reaction;controlling a flow rate between the first and second reaction zones with a mechanism coupled between the first and second reaction zones; andcontrolling the pressure in the second reaction zone based at least in part on a flow rate of the first product from the first reaction zone to the second reaction zone.2. The method of wherein cyclically varying the ...

SYSTEM FOR TREATING SOLUTION FOR USE IN ELECTROPLATING APPLICATION AND METHOD FOR TREATING SOLUTION FOR USE IN ELECTROPLATING APPLICATION

Electroplating techniques including a system for treating a solution for use in an electroplating application and a method for using the system are provided. The system can have: a gas dispersing portion configured to treat the solution by dispersing a gas into the solution to control a concentration of a predetermined cation of a metal to be electroplated in the electroplating application; a filter portion configured to treat the solution by filtering the solution to remove a quantity of metal residue; and a circulation mechanism configured to divert the solution to one of a plating tool and a combination of the gas dispersing portion and the filter portion based on a result of an analysis of the solution. 1. A system for treating a solution for use in an electroplating application , the system comprising:a gas dispersing portion configured to treat the solution by dispersing a gas into the solution to control a concentration of a predetermined cation of a metal to be electroplated in the electroplating application;a filter portion configured to treat the solution by filtering the solution to remove a quantity of a metal residue; anda circulation mechanism configured to divert the solution to one of a plating tool and a combination of the gas dispersing portion and the filter portion based on a result of an analysis of the solution.2. The system according to claim 1 ,wherein the metal to be electroplated in the electroplating application is copper (Cu), andwherein the gas dispersing portion is configured to treat the solution by dispersing oxygen into the solution to oxidize Cu(I) to Cu(II) to control a concentration of Cu(I) in the solution.3. The system according to claim 2 ,wherein the circulation mechanism is configured to divert the solution to the plating tool based on a first result of the analysis of the solution, the first result indicating that the concentration of Cu(I) is at or below a predetermined concentration, andwherein the circulation mechanism is ...

Drive System for Static Batch Reactor

A device for driving a plurality of rotatable agitators for use in a static batch reactor system, a reactor bottle cap for use with the rotatable agitator driving device and a static batch reactor system which includes the rotatable agitator driving device and bottles fitted with the reactor bottle cap are disclosed. The rotatable agitator driving device includes a planar case having first and second opposite faces, a plurality of drive heads projecting from the case through the second face and a gear train protectively housed in the case. The gear train includes a driver gear having a coupling for receiving drive from a motor, a set of idler gears and a set of driven gears. Each driven gear attached to a respective drive head for driving a rotatable agitator. The gear train is configured to cause the drive heads to rotate at the same rate. 1. A device for driving a plurality of rotatable agitators for use in a static batch reactor system , the device comprising:a planar case having first and second opposite faces;a plurality of drive heads projecting from the case through the second face; anda gear train protectively housed in the case, the gear train comprising a driver gear having a coupling for receiving drive from a motor, a set of idler gears and a set of driven gears, each driven gear attached to a respective drive head for driving a rotatable agitator, the gear train configured to cause the drive heads to rotate at the same rate.2. The device according to claim 1 , wherein the gear train is configured to cause the drive heads to rotate in the same angular direction.3. The device according to claim 1 , wherein the drive heads are arranged in an array.4. The device according to claim 3 , wherein the array is a rectangular array.5. The device according to claim 3 , wherein the drive heads comprise at least 3 drive heads arranged spaced along a first direction and at least 3 drive heads spaced along a second direction orthogonal to the first direction.6. The ...

BIOMASS TREATMENT SYSTEM

In an outlet flow control arrangement () arrangeable to control a flow of material through an outlet () with a predetermined diameter arranged at an end of a pressurized processing container (), the outlet flow control arrangement () comprises an adaptor unit () configured so that a cross-section of a flow into the adaptor unit () is reduced as compared to a cross-section of the outlet (), to enable the adaptor unit () to control and center a flow of processed material out of the processing container () and through the outlet () into a discharge pipe (). 1123. An outlet flow control arrangement () arrangeable to control a flow of material through an outlet () with a predetermined diameter arranged at an end of a pressurized processing container () , wherein{'b': 1', '4', '4', '2', '4', '3', '2', '5, 'said outlet flow control arrangement () comprises an adaptor unit () configured so that a cross section of a flow into the adaptor unit () is reduced compared to a cross section of the outlet (), to enable the adaptor unit () to control and center a flow of processed material out of said processing container () and through said outlet () into a discharge pipe ().'}246. The arrangement according to claim 1 , wherein said adaptor unit () comprises a cylindrical body with a central bore () claim 1 , and a flange arranged at an end of said cylindrical body.3661426245. The arrangement according to claim 2 , wherein said bore () is tapered from a first end () of the adaptor unit () arranged at said outlet () and with an increased diameter towards a second end () of said adaptor unit () arranged at said discharge pipe ().466126625. The arrangement according to claim 3 , wherein a diameter of said bore () in said first end () is smaller than a diameter of said outlet () claim 3 , and wherein a diameter of said bore () in said second end () corresponds to an internal diameter of said discharge pipe ().544362. The arrangement according to claim 1 , wherein said adaptor unit () ...

STEAM REFORMER BYPASS LINE AND FLOW CONTROLLER

A reformer unit and high temperature, pressure, or both variable orifice flow controller is provided. The reformer unit may have a reforming section, a heat exchanging section, and a bypass section. The bypass section provides a flow path for the hydrocarbon-containing fuel around the reforming section and has a variable orifice flow controller positioned in the bypassing flow path. 1. A reformer unit for a fuel cell system comprising:a reforming section for reforming a hydrocarbon-containing fuel, said reforming section having an inlet adapted for fluid communication with a source of hydrocarbon-containing fuel, and an outlet adapted for fluid communication with an anode inlet of a fuel cell stack;a heat exchanging section for heating a fluid flowing in the reforming section, said heat exchanging section having an inlet adapted for fluid communication with an exhaust of a cathode of a fuel cell stack, and an outlet adapted for fluid communication with an inlet of a cathode of the fuel cell stack, said heat exchanging section being in thermal communication with said reforming section to effect heat transfer between a fluid flowing through said heat exchanger section and a fluid flowing through said reforming section; anda bypass section for providing a bypassing flowpath for a hydrocarbon-containing fuel around said reforming section, said bypass section having an inlet in fluid communication with said reforming section inlet, an outlet in fluid communication with said reforming section outlet, and a variable orifice flow controller positioned in the bypassing flowpath.2. The reformer unit of wherein said heat exchanging section is in thermal communication with said bypass section to effect heat transfer between a fluid flowing through said heat exchanger section and a fluid flowing through said bypass section.3. The reformer unit of wherein said variable orifice flow controller comprises:an upstream connector having a cylindrical tubular portion defining a conduit ...

Reformer With Bypass For Internal Fuel Cell Reforming

A fuel cell system having a fuel cell stack, comprising an anode portion and a cathode portion, a source of hydrocarbon fuel, and a reformer unit having one or more cold-side, reforming passages, a fuel supply conduit, a reformate exhaust conduit, one or more hot-side channels, a cathode exhaust conduit, a cathode inlet conduit, one or more bypass channels having non-reforming passages for fuel to bypass the cold-side channels, and a flow controller for controlling the flowrate in the bypass channels, and methods for operating the same, is provided.

Hydrogen Generation Apparatus

The apparatus includes: a hydrogen generation container provided with a magnesium-based hydride accommodation part accommodating magnesium-based hydride; a reaction water tank storing water or an aqueous solution; the pipes connected to the reaction water tank and the hydrogen generation container; a pump operating such as to suction water or the aqueous solution from the reaction water tank and then exhaust it through the pipes to the hydrogen generation container; a pressure gauge measuring the pressure in the inside of the hydrogen generation container; and a control unit, on the basis of the pressure value of the pressure gauge, controlling the amount of water caused to flow through the pipes by the pump. 18-. (canceled)9. A hydrogen generation apparatus , comprising:a hydrogen generation container including an inner container whose upper side is opened for accommodating magnesium-based hydride and an outer container covering the inner container, the outer container being provided with a liquid injection hole which is arranged above the inner container;a liquid tank for storing liquid that is water or an aqueous solution containing any one of an acidic and alkaline substance;a pipe connected to the liquid tank and the liquid injection hole;a pump for operating to suction the liquid from the liquid tank and then pour the liquid through the pipe into the liquid injection hole so as to generate hydrogen by supplying the magnesium-based hydride with the liquid;a pressure gauge for measuring a pressure inside of the outer container; anda control unit for controlling the pump, whereinthe outer container is provided with an exhaust hole for exhausting generated hydrogen,the control unit controls the amount of the liquid to flow through the pipe by the pump on the basis of the pressure value of the pressure gauge.10. The hydrogen generation apparatus according to claim 9 , further comprisinga temperature adjustment part for adjusting a temperature of the hydrogen ...

DEVICE AND METHOD FOR PRODUCING AQUEOUS CHLORINE DIOXIDE SOLUTIONS, AND STORAGE UNITS AND KITS FOR CORRESPONDING USAGE

An apparatus for preparing aqueous chlorine dioxide solutions is described, comprising (a) a reactor (), (b) a first reservoir unit () comprising a first reactant for preparation of chlorine dioxide, the first reactant being in solid form, having an inlet () for water and a separate outlet (), the first reservoir unit () being exchangeable, (c) a second reservoir unit () for storing a second reactant for preparation of chlorine dioxide. Additionally described are an exchangeable reservoir unit for such an apparatus, a kit comprising or consisting of one or more exchangeable reservoir units and a process for preparing a chlorine dioxide-containing solution usable directly for water treatment. 1. An apparatus for preparing aqueous chlorine dioxide solutions , comprising{'b': '1', '(a) a reactor (),'}{'b': '8', 'claim-text': comprising a first reactant for preparation of chlorine dioxide, the first reactant being in solid form,', {'b': 15', '21, 'having an inlet () for water and a separate outlet (),'}, {'b': '8', 'the first reservoir unit () being exchangeable,'}], '(b) a first reservoir unit (),'}{'b': '4', '(c) a second reservoir unit () for storing a second reactant for preparation of chlorine dioxide.'}28. The apparatus as claimed in claim 1 , wherein the first reactant in the first reservoir unit ()is selected from the group consisting of peroxodisulfate and chlorite.3. The apparatus as claimed in for preparation of aqueous chlorine dioxide solutions usable directly for water treatment.4. The apparatus as claimed in further comprising{'b': 9', '15', '8, '(d) a feed () connected liquid-tight to the inlet () for water, for connection of the first reservoir unit () to a water reservoir,'}and optionally{'b': 14', '14', '9, 'claim-text': {'b': 14', '9', '8, 'water heated or cooled by the device () is fed via the feed () to the first reservoir unit ()'}, '(e) a device () for heating and/or cooling water, the relationship of the device () to the feed () being such that ...

Ozone converter bypass

An ozone converter includes an outer housing having an inlet and an outlet and a core disposed within the outer housing, the core including a central passageway formed therein and passing thorough the core. The converter also includes an ozone control assembly that allows air to pass through the central passageway in an closed mode and prevents flow thorough the central passageway in an open mode, the assembly including cover flaps that cover a portion of the core in the closed mode and that do not cover the core in the open mode.

METHOD FOR PRODUCING A PRODUCT GAS HAVING COMPONENT GAS RATIO RELATIONSHIPS

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. 1. A method of producing a third reactor product gas , the method comprising:(a) providing a source of carbonaceous material including one or more materials selected from the group consisting of agricultural residues, agro-industrial residues, animal waste, biomass, cardboard, coal, coke, energy crops, farm slurries, fishery waste, food waste, fruit processing waste, lignite, municipal solid waste, paper, paper mill residues, paper mill sludge, paper mill spent liquors, plastic, refuse derived fuel, sewage sludge, tires, urban waste, wood products, wood wastes, and combinations thereof;{'sub': 2', '2, '(b) after step (a), reacting the carbonaceous material with steam to produce a first reactor product gas having a first Hto CO ratio and a first CO to COratio;'}{'sub': 2', '2, '(c) after step (b), substoichiometrically oxidizing at least a portion of the first reactor product gas to form a second reactor product gas having a second Hto CO ratio and a second CO to COratio;'}(d) after step (c), mixing the first reactor product gas and second reactor product gas to form a combined product gas; and{'sub': 2', '2, '(e) after step (d), reacting the combined product gas with an oxygen-containing gas to produce a third reactor product gas having a third Hto CO ratio and a third CO to COratio;'} [{'sub': 2', '2, '(I) the first Hto CO ratio is greater than the second Hto CO ratio;'}, {' ...

New Process to make non nucleosidal reverse transcriptase inhibitors (NNRTI) for the treatment of HIV

A chemical process that can form pharmaceutically acceptable medicaments NNRTI's for the treatment of HIV starting from thiotriazole compounds. The chemical process can form thiotetrazoles such as 2-((1-(naphthalen-1-yl)-1H-tetrazol-5-yl) thio)-N-(2-nitrophenyl)actetamide that is, a potent NNRTI with nanomolar activity. 1. A chemical process that uses a solvent , thiotriazole , a base and a suitable electrophile to form thiotetrazole pharmaceutical compounds for the treatment of infection caused by the human immunodeficiency virus (HIV) and for the treatment of hyperuricaemia.2. The process in can form thiotetrazole pharmaceutical compounds that are non-nucleosidal reverse transcriptase inhibitors (NNRTI).3. The process in can form thiotetrazole pharmaceutical compounds that can treat hyperuricaemia.4. The process in uses an electrocyclization reaction that forms a thiolate that is trapped by the electrophile in situ.5. The process in can be carried out in 1 step starting with the corresponding thiotriazole.6. The process in can be carried out in 2 steps starting with the corresponding thiotriazole.7. The solvent in can be benzene.8. The thiotetrazole in can be a naphthalene derived thiotetrazole or other C1 functionalized thiotetrazole that is suitable.9. The base in can be triethyl amine.10. The process in is heated to at least 50° C.11. The process in can form pharmaceutical compounds that are non-nucleosidal reverse transcriptase inhibitors (NNRTI) that have inhibitory concentrations in the range of gram (g) to femtomolar (fm).12. The process in forms pharmaceutical compounds that are non-nucleosidal reverse transcriptase inhibitors (NNRTI) in chemical yields that range from 0.0001%-99.99%.13. The process in can be performed in a batch vessel that can be sealed.14. The batch vessel in can hold an inert atmosphere.15. The inert atmosphere in can be any noble gas.16. The reaction vessel in can be a microreactor and/or flow apparatus bearing a design engineering ...

SYSTEM AND METHOD FOR POLYMERIZATION

Techniques are provided for polymerization. A polymerization method may include polymerizing a monomer in a polymerization reactor to produce a slurry comprising polyolefin particles and a diluent, flowing the slurry out of the polymerization reactor through an outlet of the polymerization reactor, receiving the slurry from the outlet into a slurry handling system, conveying a first mixture from the slurry handling system to a diluent and monomer recovery system, and injecting steam into the first mixture downstream of the slurry handling system using a steam injection system. 1. A method , comprising:polymerizing a monomer in a polymerization reactor to produce a slurry comprising polyolefin particles and a diluent;flowing the slurry out of the polymerization reactor through an outlet of the polymerization reactor;receiving the slurry from the outlet into a slurry handling system;conveying a first mixture from the slurry handling system to a diluent and monomer recovery system; andinjecting steam into the first mixture downstream of the slurry handling system using a steam injection system.2. The method of claim 1 , comprising receiving the slurry from the outlet into a continuous take-off of the slurry handling system.3. The method of claim 1 , comprising indicating a flow rate of the steam based on a measurement provided by a steam flow meter of the steam injection system.4. The method of claim 1 , comprising at least one of adjusting a flow rate of the steam using a flow control valve of the steam injection system claim 1 , adjusting a pressure of the steam using a pressure control valve of the steam injection system claim 1 , or any combination thereof claim 1 , based on a value of a polymerization characteristic.5. The method of claim 4 , wherein the polymerization characteristic comprises at least one of a catalyst productivity claim 4 , a catalyst flow rate claim 4 , a catalyst concentration claim 4 , a catalyst component concentration claim 4 , a ...

Cyclonic Injector And Method For Reagent Gasification And Decomposition In A Hot Gas Stream

A system for vaporizing and optionally decomposing a reagent, such as aqueous ammonia or urea, which is useful for NOx reduction, includes a cyclonic decomposition duct, wherein the duct at its inlet end is connected to an air inlet port and a reagent injection lance. The air inlet port is in a tangential orientation to the central axis of the duct. The system further includes a metering valve for controlling the reagent injection rate. A method for vaporizing and optionally decomposing a reagent includes providing a cyclonic decomposition duct which is connected to an air inlet port and an injection lance, introducing hot gas through the air inlet port in a tangential orientation to the central axis of the duct, injecting the reagent axially through the injection lance into the duct; and adjusting the reagent injection rate through a metering valve.

CONVERSION OF GREENHOUSE GASES BY DRY REFORMING

A method for conversion of greenhouse gases comprises: introducing a flow of a dehumidified gaseous source of carbon dioxide into a reaction vessel; introducing a flow of a dehumidified gaseous source of methane into the reaction vessel; and irradiating catalytic material in the reaction vessel with microwave energy. The irradiated catalytic material is heated and catalyzes an endothermic reaction of carbon dioxide and methane that produces hydrogen and carbon monoxide. At least a portion of heat required to maintain a temperature within the reaction vessel is supplied by the microwave energy. A mixture that includes carbon monoxide and hydrogen can undergo catalyzed reactions producing multiple-carbon reaction products in a lower-temperature portion of the reaction vessel. 1. A method for simultaneously consuming carbon dioxide and generating one or more multiple-carbon reaction products in a single reaction vessel , the method comprising:(a) introducing a flow of a dehumidified gaseous source of carbon dioxide into a higher-temperature portion of a reaction vessel;(b) introducing a flow of a dehumidified gaseous source of methane into the higher-temperature portion of the reaction vessel;(c) irradiating first catalytic material in the higher-temperature portion of the reaction vessel with microwave energy so as to heat the first catalytic material and drive an endothermic reaction of the carbon dioxide and the methane, catalyzed by the first catalytic material, that produces hydrogen and carbon monoxide;(d) cooling a lower-temperature portion of the reaction vessel, thereby establishing a temperature gradient within the reaction vessel wherein the irradiated, higher-temperature portion of the reaction vessel exhibits a higher temperature than the cooled, lower-temperature portion of the reaction vessel, wherein at least a portion of heat required to maintain the temperature gradient is supplied by the microwave energy irradiating the first catalytic material in ...

CONVERSION OF GREENHOUSE GASES TO SYNTHESIS GAS BY DRY REFORMING

A method for conversion of greenhouse gases comprises: introducing a flow of a dehumidified gaseous source of carbon dioxide into a reaction vessel; introducing a flow of a dehumidified gaseous source of methane into the reaction vessel; and irradiating catalytic material in the reaction vessel with microwave energy. The irradiated catalytic material is heated and catalyzes an endothermic reaction of carbon dioxide and methane that produces hydrogen and carbon monoxide. At least a portion of heat required to maintain a temperature within the reaction vessel is supplied by the microwave energy. If desired, a mixture that includes carbon monoxide and hydrogen can flow out of the reaction vessel and be introduced into a second reaction vessel to undergo catalyzed reactions producing multiple-carbon reaction products. 1. A method for generating a mixture of carbon monoxide and hydrogen , the method comprising:(a) introducing a flow of a dehumidified gaseous source of carbon dioxide into a reaction vessel;(b) introducing a flow of a dehumidified gaseous source of methane into the reaction vessel;(c) irradiating catalytic material in the reaction vessel with microwave energy so as to heat the catalytic material and drive an endothermic reaction of the carbon dioxide and the methane, catalyzed by the catalytic material, that produces hydrogen and carbon monoxide, wherein at least a portion of heat required to maintain a temperature within the reaction vessel is supplied by the microwave energy irradiating the catalytic material in the reaction vessel; and(d) allowing a mixture that includes the carbon monoxide and the hydrogen to flow out of the reaction vessel.2. The method of further comprising separating at least a portion of the carbon monoxide and the hydrogen from the mixture that leaves the reaction vessel.3. The method of further comprising dehumidifying the gaseous source of carbon dioxide or the gaseous source of methane before introduction into the reaction ...

RECONFIGURABLE MULTI-STEP CHEMICAL SYNTHESIS SYSTEM AND RELATED COMPONENTS AND METHODS

The instant disclosure is related to fluidic distributors, fluidic systems, and associated methods and articles. Certain embodiments are related to fluidic distributors that comprise bays including fluidic connections with relative positions that substantially correspond to each other. In some embodiments, a fluidic distributor may comprise bays with electrical interfaces with relative positions that substantially correspond to each other. 1. A fluidic distributor , comprising:a first bay comprising first and second fluidic connections; anda second bay comprising first and second fluidic connections;wherein the relative positions of the first and second fluidic connections of the first bay substantially correspond to the relative positions of the first and second fluidic connections of the second bay.2. A fluidic distributor , comprising:a first bay comprising first and second fluidic connections and an electrical interface;a second bay comprising first and second fluidic connections and an electrical interface; and a processor is electronically coupled to the electrical interfaces of the first and second bays; and', 'the relative positions of the first fluidic connection of the first bay and the electrical interface of the first bay substantially correspond to the relative positions of the first fluidic connection of the second bay and the electrical interface of the second bay., 'wherein3. The fluidic distributor of claim 2 , wherein the degree of overlap of the first fluidic connector of the first bay and the first fluidic connector of the second bay is at least 50% claim 2 , and wherein the degree of overlap of the electrical interface of the first bay and the electrical interface of the second bay is at least 50%.4. The fluidic distributor of claim 2 , wherein the degree of overlap of the first fluidic connector of the first bay and the first fluidic connector of the second bay is at least 95% claim 2 , and wherein the degree of overlap of the electrical ...

METHOD FOR PRODUCING POLYCRYSTALLINE SILICON

A process for producing polycrystalline silicon and a gas phase deposition chamber for the same. The process includes introducing a reaction gas containing an amount of silane and/or an amount of at least one halosilane as well as an amount of hydrogen into a reaction space of a gas phase deposition reactor. The reaction space includes at least one heated support body upon which by deposition silicon is deposited to form the polycrystalline silicon. For the detection of dust depositions, at least one measuring apparatus is used to determine the amount of haze inside the reaction space during deposition. 115-. (canceled)16. A process for producing polycrystalline silicon , comprising:introducing a reaction gas comprising silane and/or at least one halosilane as well as hydrogen into a reaction space of a gas phase deposition reactor, wherein the reaction space comprises at least one heated support body upon which by deposition silicon is deposited to form the polycrystalline silicon, and wherein for detection of dust depositions at least one measuring apparatus is used to determine the haze inside the reaction space during the deposition.17. The process of claim 16 , wherein the measuring apparatus comprises a scattered radiation detector and/or extinction detector.18. The process of claim 17 , wherein the measuring apparatus further comprises an external source of electromagnetic radiation.19. The process of claim 16 , wherein the measuring apparatus comprises an optical camera; andwherein the haze is determined as a change in the quality of the images produced with the camera.20. The process of claim 16 , wherein the measuring apparatus comprises a temperature sensor; andwherein the haze is determined as a change in temperature.21. The process of claim 20 , wherein the temperature sensor is selected from the group comprising pyrometer claim 20 , thermal imaging camera claim 20 , thermocouple and combinations thereof.22. The process of claim 16 , wherein the ...

FLOW REACTION SUPPORT APPARATUS, FLOW REACTION SUPPORT METHOD, FLOW REACTION FACILITY, AND FLOW REACTION METHOD

A flow reaction support apparatus includes a computing section and a determination section. The computing section generates a prediction data set by calculating a prediction result for each reaction condition whose reaction result is unknown, using measurement data. The computing section extracts the reaction condition of the prediction result closest to a target result as an extracted reaction condition. The determination section determines whether or not a difference between the reaction result under the extracted reaction condition and the prediction result is within an allowable range, and adds, in a case where the difference is not within the allowable range, reaction information in which the extracted reaction condition and the reaction result are associated with each other to the measurement data. 1. A flow reaction support apparatus that supports a flow reaction process of causing a reaction of a raw material during flow , the flow reaction support apparatus comprising: calculates a prediction result for each reaction condition of a condition data set having a plurality of reaction conditions whose reaction results are unknown using measurement data including a plurality of pieces of reaction information in which a reaction condition whose reaction result is known and the reaction result are associated with each other to generate a prediction data set in which the reaction condition and the prediction result are associated with each other,', 'specifies the prediction result closest to a preset target result among the obtained plurality of prediction results, and', 'extracts a reaction condition associated with the specified prediction result as an extracted reaction condition; and, 'a computing section that'} determines whether or not a difference between the reaction result in a case where the reaction is performed under the extracted reaction condition and the prediction result associated with the extracted reaction condition is within a preset allowable ...

MODIFIED SULFUR, METHOD FOR PREPARING SAME, APPARATUS FOR PREPARING SAME, AND USE THEREOF

Disclosure relates to modified sulfur, preparation method thereof, preparation equipment thereof. The modified sulfur has spinnability or includes micro-structures such as fiber-, film- and network-like structure. The modified sulfur can be prepared by inducing polymerization with ultrasonic or ageing. The modified sulfur has various excellent features such as anticorrosiveness, waterproofing, strength, and fast drying and can control the features depending on its viscosity or polymerization degree. In addition due to the above features, the modified sulfur can be applied to anticorrosive or waterproofing material and can prepare anticorrosive or waterproofing material which has good workability, hardening, salt spray resistance, and weldability exceeding a certain level, and specially improved adhesiveness. Furthermore, when applying the modified sulfur to asphalt composition, gelation and depression are reduced, properties such as bending strength and tensile strength are improved, and it is possible to obtain asphalt composition with good working stability at RT. 1. Modified sulfur comprising 100 parts by weight of sulfur and 1˜300 parts by weight of dicyclopentadiene-based modifier and having 3 ,000˜2 ,000 ,000 cP of viscosity at 135° C. , which comprises micro-structures such as fiber , film , or network structure , or has spinnability.2. The modified sulfur of which comprises 1˜200 parts by weight of initiator claim 1 , based on 100 parts by weight of the sulfur.3. The modified sulfur of claim 2 , wherein the initiator comprises at least one selected from the group consisting of sulfur claim 2 , modified sulfur claim 2 , asphalt claim 2 , sulfide claim 2 , polysulfide claim 2 , hydrocarbon compound claim 2 , and their combinations.4. The modified sulfur of claim 2 , wherein the initiator comprises at least one selected from the group consisting of trans cinnamaldehyde claim 2 , dimethylaniline claim 2 , dibuthylphthalate claim 2 , diiodomethane claim 2 , ...

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

A gas-phase polyolefin reactor system for rapidly transitioning from one polyolefin product to another is disclosed. The reactor system comprises a control valve, a high-flow valve, a polyolefin reactor, a flow meter, a totalizer and an empirical model. During a transition, the empirical model predicts a required amount based upon an initial concentration and a selected ending concentration, the flow meter measures a flow rate, the totalizer determines a totalized amount when the flow rate of the first stream reaches the required amount based upon the measured flow rate and outputs the totalized amount to the empirical model, and the empirical model compares the required amount to the totalized amount and determines a transition endpoint. A method of rapidly transitioning the reactor system from one polyolefin product to another is also disclosed. 125-. (canceled)26) A gas-phase polyolefin reactor system , comprising:a) a control valve, wherein a first stream is connected to an input end of the control valve and to an input end of a high-flow valve and a second stream is connected to an output end of the control valve and the high-flow valve, wherein the second stream is connected to a third stream, wherein the third stream is connected to an input of a gas-phase polyolefin reactor;b) wherein the first, second and third streams comprise a reaction component, wherein an empirical model predicts a required amount of a reaction component based upon an initial concentration and a selected ending concentration, and wherein a flow meter measures a flow rate of the first stream near the input end of the high-flow valve and outputs the measured flow rate to a totalizer.27) The system of claim 26 , wherein an on-line analyzer measures the initial concentration of the reaction component in the third stream upstream from the gas-phase polyolefin reactor.28) The system of claim 26 , wherein the totalizer determines a totalized amount when the flow rate of the first stream ...

FLUID CAPTURE OF NANOPARTICLES

A system for preparing nanoparticles is described. The system can include a reactor for producing a nanoparticle aerosol comprising nanoparticles in a gas. The system also includes a diffusion pump that has a chamber with an inlet and an outlet. The inlet of the chamber is in fluid communication with an outlet of the reactor. The diffusion pump also includes a reservoir in fluid communication with the chamber for supporting a diffusion pump fluid and a heater for vaporizing the diffusion pump fluid in the reservoir to a vapor. In addition, the diffusion pump has a jet assembly in fluid communication with the reservoir having a nozzle for discharging the vaporized diffusion pump fluid into the chamber. The system can further include a vacuum pump in fluid communication with the outlet of the chamber. A method of preparing nanoparticles is also provided. 1. A system comprising:a reactor for producing a nanoparticle aerosol comprising nanoparticles in a gas, wherein the reactor comprises a precursor gas inlet and an outlet; a chamber having an inlet and an outlet, wherein the inlet of the chamber is in fluid communication with the outlet of the reactor;', 'a reservoir in fluid communication with the chamber for supporting a diffusion pump fluid;', 'a heater for vaporizing the diffusion pump fluid in the reservoir to a vapor; and', 'a jet assembly in fluid communication with the reservoir comprising a nozzle for discharging the vaporized diffusion pump fluid into the chamber; and, 'a diffusion pump comprisinga vacuum pump in fluid communication with the outlet of the chamber.2. The system according to claim 1 , wherein the reactor further comprises at least one flow rate controller for controlling a rate of introducing at least one precursor gas into the reactor.3. The system according to claim 2 , wherein the at least one precursor gas comprises a gas comprising a Group IV element.4. The system according to claim 1 , further comprising a power source for powering the ...

Production of Cyclic Imides Suitable for Oxidation Catalysis

Disclosed are novel processes for the production of cyclic imide compounds such as N-hydroxyphthalimide (NHPI). The processes may be particularly well-suited for commercial-scale production of cyclic imides such as NHPI. Such cyclic imide compounds are suitable for use as oxidation catalysts, and specifically may be used to oxidize cyclohexylbenzene to cyclohexyl-1-phenyl-1-hydroperoxide. Such an oxidation may be particularly useful in a process for the production of phenol and/or cyclohexanone from benzene via a process comprising hydroalkylation of benzene to cyclohexylbenzene, oxidation of the cyclohexylbenzene to cyclohexyl-1-phenyl-1-hydroperoxide, and cleavage of the cyclohexyl-1-phenyl-1-hydroperoxide to phenol and cyclohexanone. The cyclic imide production process may advantageously include water washing and reactant recovery steps to maximize purity and yield. 2. The process of claim 1 , wherein each of R claim 1 , R claim 1 , R claim 1 , and Ris independently selected from one of: (i) H and (ii) linear or branched alkyl groups having 1 to 5 carbon atoms.3. The process of claim 2 , wherein the carboxylic acid anhydride is phthalic anhydride claim 2 , the intermediate hydroxamic acid is N-hydroxyphthalamic acid (NHPA) claim 2 , and the cyclic imide is N-hydroxyphthalimide (NHPI).4. The process of claim 1 , wherein (b) raising the reaction medium temperature to the transition temperature Tfurther comprises agitating the reaction medium.5. The process of claim 1 , wherein the temperature of the reaction medium is raised from the initial temperature Tto the transition temperature Tat a rate within the range from 100 to 500° C./min.6. The process of claim 1 , wherein (b) raising the reaction medium temperature to the transition temperature Tt comprises adding steam and/or water to the reaction medium.7. The process of claim 6 , wherein (c) further heating the reaction medium comprises adding additional steam and/or additional water to the reaction medium.8. The ...

MEMBRANE-LESS REACTOR DESIGN AND PROCESS FOR BIOTRANSFORMATION OF CARBON DIOXIDE

The present invention discloses a membrane-less reactor design for microbial electrosynthesis of alcohols from carbon dioxide (CO). The membrane-less reactor design thus facilitates higher and efficient COtransformation to alcohols via single pot microbial electrosynthesis. The reactor design operates efficiently avoiding oxygen contact at working electrode without using membrane, in turn there is an increase in COsolubility and its bioavailability for subsequent COconversion to alcohols at faster rate. The present invention further provides a process of operation of the reactor for biotransformation of the carbon dioxide. 1. A membrane-less reactor for conversion of carbon dioxide to alcohols by microbial electrosynthesis , wherein the membrane-less reactor comprises:a) a tubular gas diffusion electrode with an active layer modified with an electroactive material as a working electrode;b) a circular counter electrode;c) a porous bio-electroactive filter;d) an electrolyte; and 'wherein the reactor is single chambered and can be operated in batch or continuous or semi-continuous mode in a continuous stirred tank reactor or in a sequential batch reactor.', 'e) samplings ports;'}2. The membrane-less reactor as claimed in claim 1 , wherein the working electrode comprises a gas compartment either towards inner core or towards outside claim 1 , and a) an activated carbon powder with graphite in 60:40 proportion; and', {'sup': '2', 'b) the electroactive materials present in a concentration range of 0.4-0.6 mg/cm.'}], 'wherein the active layer of the working electrode comprises3. The membrane-less reactor as claimed in claim 1 , wherein the working electrode is treated with polymerized redox mediators dissolved in the electrolyte at a concentration of 0.4-0.6 mM;wherein the electrolyte comprises trace metal solution along carbon dioxide as carbon source.4. The membrane-less reactor as claimed in claim 1 , wherein the counter electrode is a circular disc in shaped with ...

APPARATUS FOR PYROLYSIS USING MOLTEN METAL

An embodiment of the present invention is directed to a pyrolysis device including a reactor in which an injected raw material and a melted liquid metal are present together, a circulating pump connected to the reactor, a buffer tank disposed on an upper portion of the reactor and receiving the liquid metal from the circulating pump, a nozzle coupled with the buffer tank and jetting the liquid metal within the buffer tank into the reactor, a separating apparatus separating pyrolyzed char and slag, and a combustion furnace connected to the reactor to combust the fuel supplied from the reactor and supply heat to the reactor, thereby reacting the liquid metal sprays jetted from the nozzle with gases generated in the reactor to purify the gases. 1. A pyrolysis device using a liquid metal , comprising:a reactor in which the liquid metal is received;a circulating pump connected to the reactor;a buffer tank disposed on an upper portion of the reactor and receiving the liquid metal from the circulating pump;a nozzle coupled with the buffer tank and jetting the liquid metal within the buffer tank into the reactor; anda combustion furnace combusting char generated in the reactor to supply heat to the reactor,wherein liquid metal sprays jetted from the nozzle react with gases generated in the reactor to purify the gases.2. The pyrolysis device of claim 1 , further comprising:a slag outlet connected to the reactor, wherein the slag melted in the liquid metal within the reactor is discharged to the outside of the reactor through the slag outlet.3. The pyrolysis device of claim 1 , wherein the liquid metal is selected from a group consisting of Sn claim 1 , Bi claim 1 , and a mixture of Sn and Bi.4. The pyrolysis device of claim 2 , further comprising:a control unit connected to the circulating pump, the combustion furnace, and the slag outlet connected to the reactor, wherein the control unit controls at least one of the pumping speed of the circulating pump, the combustion ...

HYDROGEN GENERATOR AND FUEL CELL SYSTEM

A hydrogen generator has: a reformer that produces hydrogen-containing gas from raw material gas through reforming; a temperature detector that detects the temperature of the reformer; a hydro-desulfurizer that removes sulfur from the raw material gas through hydrodesulfurization; a recycle flow passage through which recycle gas as a portion of the hydrogen-containing gas is supplied to the hydro-desulfurizer; a raw material gas flow detector that detects the flow rate of the raw material gas, the raw material gas flow detector located somewhere in a flow passage for the raw material gas upstream of a junction of the recycle gas and the raw material gas; and a controller that controls the flow rate of the recycle gas in accordance with the temperature of the reformer, the flow rate of the raw material gas, and the flow rate of the recycle gas. 1. A hydrogen generator comprising:a reformer that produces hydrogen-containing gas from raw material gas through reforming;a temperature detector that detects a temperature of the reformer;a hydro-desulfurizer that removes sulfur from the raw material gas through hydrodesulfurization;a recycle flow passage through which recycle gas as a portion of the hydrogen-containing gas is supplied to the hydro-desulfurizer;a raw material gas flow detector that detects a flow rate of the raw material gas, the raw material gas flow detector located somewhere in a flow passage for the raw material gas upstream of a junction of the recycle gas and the raw material gas; anda controller that controls a flow rate of the recycle gas in accordance with the temperature of the reformer, the flow rate of the raw material gas, and the flow rate of the recycle gas.2. The hydrogen generator according to claim 1 , wherein the controller controls the flow rate of the recycle gas to keep a hydrogen content of a raw material after return constant.3. The hydrogen generator according to claim 2 , wherein the controller controls the flow rate of the recycle ...

APPARATUS AND PROCESS FOR CONTINUOUS SACCHARIFICATION OF MARINE ALGAE AND CELLULOSIC BIOMASS

The present disclosure relates to an apparatus and process for continuous saccharification of marine algae and cellulosic biomass. 1. A apparatus for continuous saccharification of marine algae and cellulosic biomass , the apparatus comprising:a source input unit;a reactor;a reaction unit including a downward reactor and an upward reactor;a reactant liquid discharge unit; anda deposit removal unit.2. The apparatus of claim 1 ,wherein the source includes marine algae including micro-algae, terrestrial cellulosic biomass, or the combination thereof.3. The apparatus of claim 1 ,wherein the marine algae include marine algae containing water or marine algae from which water is removed by a dehydration process.4. The apparatus of claim 1 ,wherein the source input unit further includes an agitator.5. The apparatus of claim 1 ,wherein the reactor comprises a spraying device, a driving unit, and a pressure control device.6. The apparatus of claim 5 ,wherein the spraying device is configured to directly inject high-pressure steam into the reactor.7. The apparatus of claim 1 ,wherein a plurality of the reaction unit is included.8. The apparatus of claim 1 ,wherein the downward reactor and the upward reactor further include a impeller.9. The apparatus of claim 8 ,wherein a slope of the impeller is adjusted depending on a reaction direction of the downward reactor and the upward reactor.10. The apparatus of claim 1 ,wherein the source is mixed with a reaction catalyst in the reactor.11. The apparatus of claim 10 ,wherein the reaction catalyst includes one selected from the group consisting of water, an acid, a base, an enzyme, and the combinations thereof.12. The apparatus of claim 10 ,wherein the reaction catalyst is recycled by collecting through the deposit removal unit.13. The apparatus of claim 1 ,wherein the temperature of the downward reactor and the upward reactor is about from about 50° C. to about 300° C.14. The apparatus of claim 1 ,wherein the reactor, the downward ...

HYDROGEN GENERATOR

A hydrogen generator includes: a reformer configured to generate a hydrogen-containing gas by a reforming reaction of a material gas; a combustor configured to heat the reformer by diffusion combustion of the material gas and combustion air; a supplementary air flow rate adjuster configured to adjust the flow rate of supplementary air added to the material gas; and a controller configured to control the supplementary air flow rate adjuster such that the flow rate of a mixture gas of the material gas and the supplementary air becomes a predetermined value. 1. A hydrogen generator comprising:a reformer configured to generate a hydrogen-containing gas by a reforming reaction of a material gas;a combustor configured to heat the reformer by diffusion combustion of the material gas and combustion air;a supplementary air flow rate adjuster configured to adjust a flow rate of supplementary air added to the material gas; anda controller configured to control the supplementary air flow rate adjuster such that the flow rate of a mixture gas of the material gas and the supplementary air becomes a predetermined value.2. The hydrogen generator according to claim 1 , further comprising a first detector used to detect composition of the material gas claim 1 , whereinthe controller controls the supplementary air flow rate adjuster based on the composition of the material gas.3. The hydrogen generator according to claim 1 , wherein in a case where the combustor did not ignite at the time of start-up claim 1 , the controller controls the supplementary air flow rate adjuster so as to stepwisely increase the flow rate of the supplementary air.4. The hydrogen generator according to claim 1 , further comprising:a first detector used to detect composition of the material gas; anda second detector configured to detect a temperature inside the combustor, whereinthe controller obtains an ignition determination temperature based on the composition of the material gas and then determines ...

System and Method for Catalyst Preparation

Techniques are provided for catalyst preparation. A system for catalyst preparation may include an agitator disposed inside a polymerization catalyst tank and configured to mix a polymerization catalyst and a solvent to generate a polymerization catalyst solution. The system may also include a heating system coupled to the polymerization catalyst tank and configured to maintain a temperature of the polymerization catalyst solution above a threshold. The system may also include a precontactor configured to receive feed streams comprising an activator and the polymerization catalyst solution from the polymerization catalyst tank to generate a catalyst complex. The system may also include a transfer line configured to transfer the catalyst complex from an outlet of the precontactor to a reactor. 120-. (canceled)21. A polymer manufacturing system comprising:(A) a catalyst solution tank configured to contain a metallocene catalyst solution and to supply a precontactor with at least a portion of the metallocene catalyst solution;(B) a precontactor configured to contact the metallocene catalyst solution, an activator, and a co-catalyst to form a catalyst complex;(C) a polymerization reactor system configured to contact the catalyst complex with an olefin monomer and an optional olefin comonomer to produce a polyolefin;(D) an ultraviolet-visible analyzer configured to determine a first concentration of a metallocene catalyst in the metallocene catalyst solution; and(E) a control system configured to control the first concentration of the metallocene catalyst in the metallocene catalyst solution.22. The polymer manufacturing system of claim 21 , wherein the catalyst solution tank contains an agitator configured to mix the metallocene catalyst and a solvent to form the metallocene catalyst solution.23. The polymer manufacturing system of claim 21 , further comprising a heating system coupled to the catalyst solution tank and configured to maintain a temperature of the ...

PROCESS FOR A CONTINUOUS SYNTHESIS OF ZEOLITIC MATERIALS

The present invention relates to a continuous process for preparing a zeolitic material comprising (i) preparing a mixture comprising a source of YO, optionally a source of XO, and a liquid solvent system; (ii) continuously feeding the mixture prepared in (i) into a continuous flow reactor at a liquid hourly space velocity in the range of from 0.3 to 20 hfor a duration of at least 1 h; and (iii) crystallizing the zeolitic material from the mixture in the continuous flow reactor, wherein the mixture is heated to a temperature in the range of from 100 to 300° C.; wherein the volume of the continuous flow reactor is in the range of from 150 cmto 75 m, as well as to zeolitic materials which may be obtained according to the inventive process and to their use. 1. A continuous process for preparing a zeolitic material , comprising:{'sub': 2', '2', '3, 'preparing a mixture comprising a source of YO, optionally a source of XO, and a liquid solvent system;'}{'sup': '−1', '(ii) continuously feeding the mixture prepared in (i) into a continuous flow reactor at a liquid hourly space velocity in the range of from 0.3 to 20 hfor a duration of at least 1 h; and'}(iii) crystallizing the zeolitic material from the mixture in the continuous flow reactor,wherein the mixture is heated to a temperature in the range of from 100 to 300° C.;{'sup': 3', '3, 'wherein the volume of the continuous flow reactor is in the range of from 150 cmto 75 m.'}2. The process of claim 1 , wherein the continuous flow reactor is selected from the group consisting of a tubular reactor claim 1 , a ring reactor claim 1 , and a continuously oscillating reactor.3. The process of claim 1 , wherein the wall of the continuous flow reactor comprises a metallic material.4. The process of claim 1 , wherein the surface of the inner wall of the continuous flow reactor is lined with an organic polymer material.5. The process of claim 1 , wherein in (iii) the mixture is heated under autogenous pressure.6. The process of ...