СПОСОБ И УСТРОЙСТВО ДЛЯ ОБРАБОТКИ ПОТОКА ИСХОДНОГО ПРОДУКТА ПОДЗЕМНОЙ ГАЗИФИКАЦИИ УГЛЯ

Изобретение относится к способу и устройству для обработки потока исходного продукта (сырого синтез-газа/сингаза), получаемого в процессе подземной газификации угля (ПГУ). Устройство содержит сепаратор для отделения жидкостей и твердых частиц от сырого сингаза, получаемого в процессе ПГУ, содержащий сосуд, содержащий верхнюю секцию и нижнюю секции; входной канал для подачи газа; выходной канал для газа, расположенный над входным каналом для подачи газа; выходной канал для жидкостей, расположенный под входным каналом для подачи газа; и корзиночный фильтр, размещенный в нижней секции сосуда, при этом нижняя секция сосуда вмещает отделяемые жидкости и твердые частицы; и выводную систему для направления сырого сингаза, содержащего высокую концентрацию кислорода, в атмосферу, при этом выводная система содержит вертикально расположенный сосуд; выходной канал для газа в верхней части сосуда; жидкостное уплотнение в нижней части сосуда; и входной канал для газа для подачи поступающего сингаза в ...

КОМБИНИРОВАННЫЙ СПОСОБ ПОЛУЧЕНИЯ ПОРОШКА КАРБОНИЛА ЖЕЛЕЗА И УГЛЕВОДОРОДОВ

Изобретение относится к комбинированному способу, состоящему в том, что на установке A получают чистый порошок карбонила железа путем разложения чистого пентакарбонила железа, а освобождающуюся при разложении пентакарбонила железа моноокись углерода (CO) используют для получения дальнейшего порошка карбонила железа из железа на установке A, или подводят к присоединенной установке B для получения синтез-газа, или подводят к присоединенной установке C для получения углеводородов из синтез-газа. При этом полученный на установке A порошок карбонила железа используют в качестве катализатора или компонента катализатора в присоединенной установке C для получения углеводородов из синтез-газа, полученного на установке B, и собирающийся на установке C отработанный катализатор используют в качестве дополнительного источника железа для получения порошка карбонила железа на установке A. Использование предлагаемого способа позволяет избежать отходов, таких как соли и сточные воды. 10 з.п. ф-лы, 4 ил.

Промоторы гидратообразования углекислого газа на основе амидов аминокислот и этилендиаминтетрауксусной кислоты

Изобретение относится к химии комплексонов, а именно к применению соединений на основе амидов аминокислот и этилендиаминтетрауксусной кислоты общей формулы (I), где R выбран из I-1, I-2, I-3 и I-7, в качестве промоторов гидратообразования углекислого газа. Соединения могут найти применение в улавливании углекислого газа и разделении газов. 2 ил., 1 пр.

Способ получения синтез-газа из биомассы растительного происхождения

Изобретение относится к области получения синтез-газа путем переработки биомассы растительного происхождения и может быть использовано в нефтепереработке, нефтехимии, энергетике. Способ осуществляют путем измельчения исходной биомассы, смешивания ее с мелкодисперсным горючим сланцем с содержанием серы 4,1-16,0 мас.%, имеющим размер частиц 10-100 мкм, и водой, взятых в количестве, мас.%: сланец 3,0-5,0, вода 10,0-30,0, биомасса - остальное, до 100. Затем образованную смесь подвергают диспергированию с получением суспензии, последующей газификацией полученной суспензии при температуре 800-1000°С и направления образовавшегося газового потока на очистку с получением синтез-газа. Технический результат заключается в повышении эффективности способа переработки биомассы с целью получения синтез - газа, а именно в упрощении его технологии, предотвращении явления отложения соединений щелочных металлов на поверхностях оборудования и эффективного предотвращения щелочной коррозии оборудования. 2 табл ...

УДАЛЕНИЕ СЕРОВОДОРОДА В ВИДЕ СУЛЬФАТА АММОНИЯ ИЗ ПАРОВ ПРОДУКТА ГИДРОПИРОЛИЗА

... 1. Способ переработки биомассы на углеводородное топливо, включающий:переработку биомассы в реакторе гидропиролиза, дающую углеводородное топливо, уголь и поток технологического пара;охлаждение потока технологического пара до температуры конденсации;разделение потока технологического пара на первичный поток охлажденного парообразного продукта, поток жидких углеводородов и первичный водный поток:где первичный поток охлажденного парообразного продукта включает неконденсирующиеся технологические пары, H, сероводород, CO и CO, поток жидких углеводородов включает конденсирующиеся углеводороды, и первичный водный поток включает воду, аммиак, сероводород и сульфид аммония;обработку первичного водного потока в колонне для отпарки кислых вод;концентрирование сероводорода и аммиака в поток охлажденной технологической воды и второй поток очищенной воды;направление потока охлажденной технологической воды в каталитический реактор;впрыск воздуха в каталитический реактор с получением концентрированного ...

УДАЛЕНИЕ СЕРОВОДОРОДА В ВИДЕ СУЛЬФАТА АММОНИЯ ИЗ ПАРОВ ПРОДУКТА ГИДРОПИРОЛИЗА

Verfahren zur getrennten Gewinnung des Ammoniaks und der Ammoniakverbindungen aus Gasen

A process for the production of flue gas, having a relatively low no-content

Flue gas (the gas obtained when hydrocarbons are burnt in air) which is to be added to a coal gas stream as diluent, is treated to remove nitric oxide by admixing it with ozone at a pressure of, at most, 6 atmospheres to convert the nitric oxide to nitrogen dioxide. The mixture is added to the coal gas stream prior to the removal of ammonia from the coal gas stream and the nitrogen dioxide is removed in the ammonia washing plants. The amount of ozone introduced may be increased to convert any sulphur dioxide in the flue gas to sulphur trioxide which is removed with the nitrogen dioxide. Alternatively, any sulphur dioxide in the flue gas may be removed before admixture with an ozone by scrubbing the flue gas with aqueous alkali, e.g. sodium carbonate.ALSO:Aprocess for the reduction of the nitric oxide content in flue gas (i.e. that gas obtained by the combustion of hydrocarbons in air) comprises supplying ozone to the flue gas at a pressure of, at most, 6 atmospheres and subsequently scrubbing ...

Removing carbon dioxide from syngas

A method for processing pre-combustion syngas comprises providing an absorber unit having a membrane contactor comprising a plurality of pores, channelling a gas along a first surface of the membrane contactor; channelling a solvent along a second opposing surface of the membrane contactor; and contacting the solvent with the syngas at gas-liquid interface areas, defined by the plurality of pores in the membrane contactor to separate at least carbon dioxide (CO2) from the gas by a chemical absorption of CO2 into the solvent to produce a solvent containing at least CO2. Also disclosed is a pre-combustion syngas (96) processing apparatus comprising an absorber unit (82) including a housing (91), a membrane contactor (90) positioned in the housing, a solvent area within the housing, the solvent area containing a solvent (100), and a syngas area within the housing.

Process for the purification of hot gases obtained by partial combustion and containing soot and carbonyl sulphide

A process for purifying hot gases obtained by the partial combustion of carbonaceous combustible materials and containing soot and carbonyl sulphide comprises contacting the gas with enough water to saturate the gas and cool it to below its dew point, whereby the soot is largely removed in aqueous suspension, contacting the cleaned gas, in the absence of liquid water, with a carbonyl sulphide conversion catalyst (preferably between 120 DEG and 200 DEG C.) and treating the final gas with an agent for removing H2S and, if desired, carbonyl sulphide. The catalyst is one capable of catalyzing the hydrolysis of COS to H2S + CO2. Suitable catalysts, which may be in fixed or moving bed form or fluidized, may be alumina, bauxite, activated clays, aluminium phosphate, thoria, or MgCl2 and preferably contain at least one Group VI and/or Group VIII metal. Cobalt molybdate on alumina is mentioned. The H2S-removing agent may be conventional, e.g. an aqueous solution of an alkanolamine, potassium phosphate ...

A method of operating plant for the conversion of carbon monoxide

A method of purifying a carbon-monoxide-containing containing gas by conversion of the CO as claimed in the parent Specification, is modified in that a volume of oxygen at least sufficient to satisfy the stoichiometric requirements of the reaction H2S+ 1/2 O2 = S + H2O is continuously added, e.g. in the form of air, to the gas to be converted in any case where the oxygen content of the gas is not sufficient to satisfy the reaction. The gas flow circuit and the alkaline solution flow circuit are identical with those described in the parent Specification except that the regenerator for the solution is omitted, solution being intermittently or periodically removed from the base of the saturator and replaced by fresh solution. Alkaline solutions mentioned are those disclosed in the parent Specification, and sodium and potassium vanadate, and the oxidation of H2S in the solution is accelerated by adding a substance, e.g. a redox system, quinone (e.g. 2,7 anthraquinone disulphonic acid) or leuco-compounds ...

REMOVAL OF GASES FROM GAS MIXTURES

Improvements in or relating to methods and apparatus for contacting gases and liquids

... 774,249. Gas-liquid contact apparatus. DIAMOND ALKALI CO. June 20, 1955 [June 21, 1954], No. 17784/55. Class 55 (2). Gas-liquid contact apparatus comprises a tube 2 for the supply of gas, a tube 4 surrounding the same for the supply of liquid and an outer casing 6 having a suction branch 14, the liquid outlet between the tubes 2, 4 being so designed that the liquid issues as a substantially unbroken tubular sheet which encloses the gas, the expansion of which moves the sheet radially outwards towards, and eventually into contact with, the casing 6 where the sheet is disrupted. The gas washed, and deprived of solids by the liquid contact, flows backwards to the exhaust 14. The tube 4 is tapered at the end to form a narrow passageway with the knife-edge 18 formed by flaring the tube 2. , The tube 2 is lined at the end with liquid-repellent material 22. In modifications, the tube 2 is not flared, but projects somewhat from the tube 4 and carries an outwardly flared sleeve which diverts the ...

Method and apparatus for treating a raw UCG product stream

Method and apparatus for treating a raw UCG product stream

VERFAHREN ZUR ERZEUGUNG EINES KOHLENMONOXID UND WASSERSTOFF ENTHALTENDEN GASES UNTER VERWENDUNG EINES PLASMAGENERATORS MIT ANSCHLIESSENDER ENTSCHWEFELUNG

Anlage zum Vergasen von stückigen Brennstoffen

Bei einer Anlage (1) zum Vergasen von stückigen Brennstoffen mit einem Pyrolysereaktor (2) und einem Gasmotor (6), wird vorgeschlagen, dass ein Abgas-Ausgang (65) des Gasmotors (6) mit einem Eingang (71) einer Nachverbrennungsbrennkammer (7) verbunden ist, und dass ein Abgas-Ausgang (75) der Nachverbrennungsbrennkammer (7) mit wenigstens einem Heizgas-Eingang (23) des Pyrolysereaktors (2) verbunden ist.

PROCEDURE FOR THE PRODUCTION A CARBON MONOXIDE AND HYDROGEN OF A CONTAINING GAS USING A PLASMA GENERATOR WITH FOLLOWING DESULPHURISATION

PROCEDURE FOR THE DISTANCE OF MERCURY FROM ORGANIC MEDIA.

PROCEDURE FOR THE COMPLETE MATERIAL ONE, EMISSION LOTS USE BY HIGH TEMPERATURE RECYCLING AND BY FRACTIONATED MATERIAL SPECIFIC CONVERSION OF THE DEVELOPING SYNTHESIS RAW GAS

Methods and systems for the production of hydrocarbon products

Methods and systems for the production of hydrocarbon products, including providing a substrate comprising CO to a bioreactor containing a culture of one or more micro-organisms; and fermenting the culture in the bioreactor to produce one or more hydrocarbon products. The substrate comprising CO is derived from a CO2 reforming process.

Maintaining low carbon monoxide levels in product carbon dioxide

A process for maintaining a low carbon monoxide content in a carbon dioxide product that is made in a synthesis gas purification process is disclosed. More particularly, the invention involves an improved process in which a portion of a loaded solvent is sent through a carbon dioxide absorber instead of to a series of carbon dioxide flash drums.

Method for total material, emission-free utilisation by high-temperature recycling and by fractional material- specific' conversion of the resultant synthesis raw gas

PROCESS AND EQUIPMENT FOR THE SIMULTANEOUS PRODUCTION OF HYDROGEN AND CARBON MONOXIDE

METHOD OF TREATING AN OFF-GAS STREAM AND AN APPARATUS THEREFOR

The present invention provides a method of treating an off-gas stream (80) comprising NH3 and H2S to provide a sulphate stream (910), the method comprising the steps of : (i) providing a first off-gas stream (80) comprising NH3, H2S, CO2 and optionally one or more of HCN, COS and CS2; (ii) passing the first off-gas stream (80) to an incinerator (300) to oxidise NH3, H2S, and optionally one or more of HCN, COS and CS2 to provide a second off-gas stream (310) comprising N2, H2O, SO2 and CO2; (iii) scrubbing the second off-gas stream (310) with a first aqueous alkaline stream (380, 876a) in a caustic scrubber (350) to separate SO2 and a part of the CO2 from the second off-gas stream to provide a spent caustic stream (360) comprising carbonate and one or both of sulphite and bisulphite and a caustic scrubber off-gas stream (370) comprising N2 and CO2; and (iv) passing the spent caustic stream (360) to an aerator (900) comprising sulphur-oxidising bacteria in the presence of oxygen to biologically ...

PROCESS FOR REMOVING HYDROGEN CYANIDE FROM GASEOUS STREAMS

... 12,299 PROCESS FOR REMOVING HYDROGEN CYANIDE FROM GASEOUS STREAMS This invention relates to a process for reducing the hydrogen cyanide content of a gaseous stream which comprises providing an adsorbent bed wherein the adsorbent comprises zinc oxide and contains no more than 5%, by weight, of an oxide of an alkali or alkaline earth metal, and contacting said process stream with said adsorbent bed at a temperature of from about ambient to about 350.degree.C for a period of time sufficient to reduce the concentration of hydrogen cyanide in said gaseous stream to the desired value.

PRODUCTION OF CLEAN FUEL GAS

PROCESS FOR PRODUCING A HYDROCARBON PRODUCT FLOW FROM A GASEOUS HYDROCARBONACEOUS FEED FLOW AND RELATED INSTALLATION

The process comprises : - introducing the feed flow (14) in a synthesis gas generation unit (16) to form a synthesis gas flow (32) and introducing the synthesis gas flow (32) in a Fischer-Tropsch synthesis unit (18); - at least partially removing carbon dioxide from a first flow (44) formed from a Fischer-Tropsch tail gas flow (38) to form a carbon dioxide depleted flow (50); - forming a tail gas recycle flow (36) from the carbon dioxide depleted flow (50); - introducing the tail gas recycle flow (36) in the synthesis gas generation unit (16) and/or in the synthesis gas flow (32). The process comprises adjusting the carbon dioxide content in the tail gas recycle flow (36) to control the hydrogen to carbon monoxide molar ratio in the synthesis gas flow (32) to a target hydrogen to carbon monoxide molar ratio.

CATALYST AND PROCESS FOR THE PRODUCTION OF DIESEL FUEL FROM NATURAL GAS, NATURAL GAS LIQUIDS, OR OTHER GASEOUS FEEDSTOCKS

A process is described that operates efficiently to produce diesel fuel blend from hydrogen and carbon monoxide. The process uses a reduced catalyst on a metal oxide catalyst support which are configured to selectively convert the hydrogen and carbon monoxide into a hydrocarbon product stream, wherein the hydrocarbon product stream comprises light gases, diesel fuel and a wax. These are then condensed, and the diesel fuel blended with a petroleum derived fuel, to produce a diesel fuel blend.

COKE MANUFACTURING METHOD

This method for producing coke includes the following: a preparation step in which a blended coal is prepared by blending two or more types of coal; a stirring and mixing step in which at least some pseudo-particles present in the blended coal, which are formed by coal particles aggregating, are crushed by stirring and mixing the blended coal; and a carbonization step for producing coke by charging the stirred and mixed blended coal into a coke oven and carbonizing the same.

Teervorlage für Gaserzeugungsöfen mit einer Scheidewand zwischen Fallrohr und Gasabzugsrohr.

Reiniger für Generatorgase, insbesondere auf Fahrzeugen angeordneter Reiniger.

Verfahren zur Abscheidung von feinen, festen oder flüssigen Beimengungen aus einem Gas- oder Dampfstrom und Vorrichtung zur Ausübung des Verfahrens.

Einrichtung zum Kühlen und Reinigen von Holzgas.

Einrichtung zum Reinigen und Trocknen von Holz- und Holzkohlengas.

Generatorgasanlage, insbesondere zum Betrieb von Fahrzeugmotoren.

Filter für Gase.

Procédé d'épuration des gaz de gazogène et appareil pour la mise en oeuvre de ce procédé.

Vorrichtung zum Abschrecken und Entfernen von Teer und Russ aus Pyrolysegasen

Verfahren zum Betrieb von Anlagen zur Kohlenoxydkonvertierung

Mechanism for thermal refuse disposal.

СПОСОБ И ОБОРУДОВАНИЕ ДЛЯ ОСВОБОЖДЕНИЯ ГАЗА ОРОШЕНИЯ, ЦИРКУЛИРУЮЩЕГО В ТЕЧЕНИИ ПРЯМОГО ВОССТАНОВЛЕНИЯ ЖЕЛЕЗНОЙ РУДЫ, ОТ ВОДЯНОГО ПАРА И УГЛЕКИСЛОГО ГАЗА, СОДЕРЖАЩЕГО ГАЗ ОРОШЕНИЯ

Способ и оборудование для освобождения газа орошения, циркулирующего в течении прямого восстановления железной руды, от водяного пара и CO2, содержащего газ орошения, причем газ орошения насыщен водяным паром и CO2, имеющим температуру от 50 °C до 250 °C при давлении от 2 до 8 bar[а], отводят от циркуляции газа орошения прямого восстановления железной руды, охлаждают до температуры от 15 °C до 45 °C, сжимают до давления от 25 до 75 bar[а] и добавляют оксигенаты, имеющие температуру от +10 до -80 °C для физического адсорбционного удаления CO2.

REMOVAL OF HYDROGEN SULFIDE AS AMMONIUM SULFATE FROM HYDROPYROLYSIS PRODUCT VAPORS

Process of gas cleaning of the distillation of coals

METHOD OF PRODUCING A COLD GAS CONTAINING CARBON MONOXIDE AND HYDROGEN

Procédé et installation de récupération d'hydrogène et de monoxyde de carbone

L'hydrogène excédentaire est séparé par perméation (en 4) en amont du traitement cryogénique 5. Application au traitement des gaz de réformage d'hydrocarbures.

Purifying apparatus for gas generator

Gas generator with wood for the engine supply to explosions

Process of purification of gas products, more particularly of gas, of gas generators, device by allowing its application and implementation

METHOD OF PREPARATION OF GAS Of INDUSTRIAL APPLICATION

PROCESS AND DEVICE OF TREATMENT Of a GAS OF SYNTHESIS

Improvements with the processes and devices of recovery of the coal by-products of the vegetable matters

A METHOD FOR REMOVING FROM GASES OF VAPORS AND AEROSOLS AND INSTALLATION FOR the REALIZATION OF the PROCESS

Method of preparation of the by-products of gas, with simultaneous purification

METHOD AND APPARATUS FOR TREATING AN OFF-GAS STREAM

PROCESS FOR RECOVERY OF SALTS WITH MINIMIZING FORMATION OF SCALE DURING GASIFICATION

PURPOSE: A process for minimizing formation of scale during the recovery of liquids and solids from the aqueous effluent discharged during a partial oxidation gasification from a gasifier is provided, wherein the aqueous effluent contains ammonium chloride and no effluent discharges to the environment. CONSTITUTION: A method comprises the steps of: washing a synthetic gas with the water of more than about pH 6.0 whose pH is controlled by using ammonia; separating the synthetic gas from the water; separating some of the water to form the aqueous effluent which is introduced into the evaporation system; evaporating the aqueous effluent in an evaporator(106) to produce brine(112) with a brine concentration of about 10-60 wt% and steam; separating the steam from the brine; condensing the steam to produce a distilled water; recycling the distilled water to a partial oxidation gasification; and recovering ammonium chloride crystals from the brine. COPYRIGHT 2000 KIPO ...

CRYOGENIC AND MEMBRANE SYNTHESIS GAS PRODUCTION

A system and process for the production of synthesis gas with a specific H2CO ratio, for example, 0.7 to 1.2 and a low residual methane content, for example, less than 5 percent (5 %). Excess hydrogen from the syngas feed steam is removed by a membrane (11) as a permeate (23) and the retentate gas (26) cryogenically (13) separated.

Process for removing mercury from a non-polar organic medium

Treatment of artificial gas

Apparatus for the recovery of dry distillation material

PROCESSES FOR CONVERTING LIGNOCELLULOSICS TO REDUCED ACID PYROLYSIS OIL

Processes for producing reduced acid lignocellulosic-derived pyrolysis oil are provided. In a process, lignocellulosic material is fed to a heating zone. A basic solid catalyst is delivered to the heating zone. The lignocellulosic material is pyrolyzed in the presence of the basic solid catalyst in the heating zone to create pyrolysis gases. The oxygen in the pyrolysis gases is catalytically converted to separable species in the heating zone. The pyrolysis gases are removed from the heating zone and are liquefied to form the reduced acid lignocellulosic-derived pyrolysis oil.

СПОСОБ И ОБОРУДОВАНИЕ ДЛЯ ОБРАБОТКИ ГАЗА, ПОЛУЧАЕМОГО ГАЗИФИКАЦИЕЙ ТВЕРДОГО ТОПЛИВА ПОД ДАВЛЕНИЕМ

Изобретение относится к области химии. По трубопроводу 1 через газопромывную колонну 2 первой стадии пропускают входящий газ после удаления HCN и NH. Первая стадия предназначена для удаления HS, COS и любых других серосодержащих соединений с получением обессеренного газа. Через теплообменник 15 проходит газообразная флегма, отводимая с прямого восстановления железной руды. Турбина 9 на валу содержит ступень дросселирования 8 и ступень компрессии 10. Ступень компрессии 10 предназначена для приема и сжатия газообразной флегмы, которая может быть пропущена через теплообменник 15, расположенный на трубопроводе 14. Обессеренный газ с первой стадии и сжатую газообразную флегму со ступени компрессии 10 турбины 9 на валу подают в газопромывную колонну 5 второй стадии для отделения СО. Давление смеси чистого газа может быть затем снижено на ступени 8 дросселирования турбины 9 на валу. Газовую смесь с пониженным давлением затем пропускают через теплообменник 12 до ее возврата на стадию прямого восстановления ...

Verfahren und Vorrichtung zum Abscheiden von Teer, insbesondere aus Generatorgas

Process for removing nitric oxide from gases containing the same

In a process for removing nitric oxide from gases containing nitric oxide and oxygen, e.g. coal distillation gases, by irradiation with ultra-violet rays, vapours of such organic compounds as produce peroxides when so irradiated in the presence of oxygen are added in quantities of from 0.01 to 0.1% by volume to the gases before irradiation. The irradiation is performed at gas temperatures below 40 DEG C. Organic compounds mentioned are olefins, especially diolefins, and non-olefinic hydrocarbons, e.g. isobutane, isooctane, methyl cyclohexane, cyclopentadiene, cumene and turpentine, and oxygen-containing compounds, e.g. ethers, aldehydes and alcohols. The cracking products of propane-butane mixture may be used.ALSO:Nitric oxide is oxidized to nitrogen dioxide in a gas mixture containing oxygen, e.g. coal distillation gases, by adding to the mixture in an amount of 0.01% to 0.1% by volume of the mixture, the vapour of at least one organic compound of the group comprising olefins, especially ...

Improvements in or connected with gas producers

... 186,262. Climie, W. June 15, 1921. Cleaning internally, rotary appliances for; cleaning externally.-Gas from a producer is freed from dust, &c. by passage through tubes, casings or passages, from the walls of which the dust is removed by brushes. Apertures 14 are formed in the headers, rotary shafts 15 which carry brushes 20 passing through these apertures and casings 10 to brush tubes 9. Brushes 22 are secured to the casings 10, or may be mounted on shafts beyond the tubes. Brushes 29, 37, 30 mounted on shafts 31, 32 connected by crossheads 36 sweep the casing surfaces, the shaft 32 being rotated by gearing 55 and the shafts 31 being carried by a plate 33 rotating on bearings 35, water seals 34, 38 are provided. Air passing through a partitioned jacket 40 is heated for supply to the generator. The soot &c. is discharged from the shoots 18, 43 by a rotary valve-plate 46 having pockets 47 which register alternately with the shoots and with discharge openings in a stationary plate 48. Scrapers ...

Electrostatic separation of gases at low temperature

... 1,045,707. Electrostatic separation. CONCH INTERNATIONAL METHANE Ltd. Sept. 27, 1965 [Oct. 15, 1964], No. 41026/65. Addition to 1, 017. 660 Heading B2J. The process described with reference to Fig. 1 of the parent Specification is modified in that, prior to reducing the pressure of the mixture of liquified gases, the mixture is subjected to an ionization step in order to produce an increased concentration of charged solid particles during the pressure reducing step. The process may be applied to the separation of mixtures including two or more different gases, e.g. the separation of CO 2 and/or H 2 S from natural methane gas, CO 2 from air or CO 2 from a nitrogen/CO 2 mixture. One form of apparatus for separating CO 2 from methane gas, Figs. 1 and 2 (not shown) is as described in Figs. 1, 3 and 4 of the parent Specification except that a section of the pipeline leading from the liquefaction plant to the throttling valve is protected by lead shielding and contains a source of gamma radiation ...

Plasma-assisted method and system for treating raw syngas comprising tars

Process and apparatus for decomposing coke-oven gas by cooling to low temperatures

... 289,817. Ges. fur Linde's Eismaschinen Akt.-Ges- May 2, 1927, [Convention date]. Separating gases by liquefaction. - Acetylene hydrocarbons are removed by absorption or chemical reaction, from coke oven &c. gas which is to be separated by liquefaction, before entering the heart exchangers preceding the separation apparatus proper, and only so far as to prevent solid deposits therein. This separation may be effected by passage over heated catalysts, with hydrogenation or decomposition, by polymerization over heated copper, or by solution in water or ketones. Other constituents favourable to explosion or resinification such as ammonia or nitric oxide, may be removed, e.g. by concentrated sulphuric acid. Parts of the apparatus made of copper may be coated with tin, lead, or their alloys. Specification 288,216, [Class 55 (ii), Gas manufacture &c.], is referred to.

Producing clean gas containing hydrogen and carbon monoxide

In a method of producing a gas containing carbon monoxide and hydrogen, in which method the gas does not need to be subjected to energy-consuming and costly scrubbing steps before being used as reduction gas, combustion gas or synthesis gas, the gas is produced from material containing carbon and/or hydrocarbon and oxidant and is supplied to a reaction chamber (2) simultaneously with a gas heated by plasma generator (at 3), in order to crack the hydrocarbon in the gas. The gas may be passed through a limestone or dolomite filling to the remove sulphur therefrom. ...

Method for preventing resin formation in gas piping

... 483,428. Gas - purifying processes. MEZGER, R., and PAYER, T. May 19, 1937, No. 13958. Convention date, May, 19, 1936. [Class 55 (ii)] Oxide of nitrogen is removed from illuminating gas before drying the gas, such as by calcium chloride, so as to inhibit resin formation in the distributing piping.

Improvements in means for treating fuel gases

... 476,332. Treating gases with electrical discharges. KOPPERS CO. April 4, 1936, No. 10050. Convention date, Oct. 9, 1935. [Class 39 (i)] Apparatus for stabilizing coal distillation, &c. fuel gases against the formation of resinous compounds caused by the presence therein of oxides of nitrogen as described in Speci. fication 473,009, [Group XII], comprises a treating chamber 13, Fig. 5, provided with fixed parallel electrode plates 7, 12 arranged in two series with the plates of one series alternating with those of the other, at least one of the series being insulated. As shown, one set of plates 12 is grounded through the casing 13 and are plane, while the plates of the other set 7 are mounted on insulators 9 disposed in housings 20 heated by steam coils 21, and provided with rows of discharge points 3 equally spaced apart from each other and separated from the plates 12 by an air gap through which the gas passes. The plates are connected in a high potential circuit such as to produce a ...

Method of treating gases produced by gasification under pressure

In a method of producing long-distance supply gas, town gas or synthesis gas which has a low CO content, a carbonaceous fuel is gasified under pressure, e.g. 23 atmospheres, with oxygen or oxygen-containing gases, and with steam and/or CO2, and the resulting gas at the same pressure is contacted with a catalyst to convert CO in the gas to CO2 and hydrogen by reaction with steam in the gas, which is thereafter washed if necessary to reduce its CO2 content, and, after the gasification and before the conversion, the gas is subjected to a partial condensation with the addition of tar and/or oil, in addition to water to remove from it solid, liquid or polymerizable constituents which would adversely affect the catalyst employed for the conversion, while allowing appreciable quantities of oil and tar vapours to remain in the gas, mists and/or drops of liquid contained in the gas being removed therefrom before the gas is subjected to the conversion reaction. After the condensation the gas may ...

Process

PROCEDURE FOR THE PARTIAL OXIDATION OF HYDROCARBONS

Anlage zum Vergasen von stückigen Brennstoffen

Bei einer Anlage (1) zum ·Vergasen von stückigen Brennstoffen mit einem Pyrolysereaktor (2) und einem Gasmotor (6), wird vorgeschlagen, dass ein Abgas­ Ausgang (65) des Gasmotors (6) mit einem Eingang (71) einer Nachverbrennungsbrennkammer (7) verbunden ist, und dass ein Abgas-Ausgang (75) der Nachverbrennungsbrennkammer (7) mit wenigstens einem Heizgas-Eingang (23) des Pyrolysereaktors (2) verbunden ist.

PURIFICATION OF AQUEOUS EFFLUENTS FORM SYNTHESIS GAS

COOLING AND CLEANING PRODUCER AND BLAST FURNACE GAS

A gas conditioning system

A gas conditioning system

Fuel processing

A system for processing carbonaceous in-feed material has a pyrolyzer kiln for pyrolysis the carbonaceous in-feed material, the kiln operating in a slow pyrolysis process in which the in-feed material is pyrolysed in the kiln for a period of minutes in order to produce primarily a gaseous output fraction; a steam reformer positioned downstream of the kiln to which combustion gasses from the pyrolyzer kiln are fed; a water scrubber positioned gas flow-wise downstream of the steam reformer; a methanation stage; a C02 scrubbing stage. The system includes means for splitting the gas and directing a portion of the split gas back to the pyrolyzer kiln.

PRODUCTION OF INDUSTRIALLY USABLE GAS

MULTI-STAGE CRYOGENIC ACID GAS REMOVAL

A relatively simple and energy efficient multiple stage cryogenic process for the purification of a hydrogen-rich stream by the removal of acid gases, mainly CO2 and H2S, by method of autorefrigeration and delivering or producing those acid gases, mainly CO2, at pressure sufficiently high for disposal by containment, commonly known as sequestration. Autorefrigeration is comprised of (a) condensing acid gases from the syngas stream by cooling the syngas, (b) separating the liquefied acid gases from the syngas, and (c) evaporating the liquefied acid gases at a pressure lower than that of the syngas to provide cooling. The process is composed of multiple autorefrigeration stages to generate multiple acid gas product streams with a pressure as high as practical in each stream so as to lessen the power needed to pressurize the acid gas streams for sequestration. The final autorefrigeration stage utilizes an antifreeze liquid that allows the final stage to operate below the freezing point of ...

PROCESS AND APPARATUS FOR PURIFYING AND COOLING A HOT GAS

PROCESS AND APPARATUS FOR PURIFYING AND COOLING A HOT GAS Process for cooling and cleaning hot fly ash containing synthesis gas in which the gas is first passed through a cooler, the bulk of the fly ash being separated from the cooled gas in a cyclone, whereupon the gas is further cleaned in a water scrubber. A fly ash/water slurry obtained in the scrubber is at least in part injected into the crude synthesis gas. In order to avoid fouling of the cooler the fly ash particles in the hot crude gas and/or in the slurry are agglomerated preferably by adding a binder, e.g. water glass.

HIGH RECOVERY CARBON MONOXIDE PRODUCTION PROCESS

The present invention provides for a monolith reactor process for the production of syngas from hydrocarbon and oxygen feeds. The syngas is cooled and separated to produce carbon monoxide and hydrogen, and the purification equipment utilized in this separation process recycles tail gas and fuel gas to the syngas feed gas line and recycles methane from the carbon monoxide separation system for feed back to the monolith reactor. This process results in almost complete carbon to carbon monoxide conversion and very high carbon monoxide and hydrogen recoveries.

METHODS AND SYSTEMS FOR THE PRODUCTION OF HYDROCARBON PRODUCTS

Methods and systems for the production of hydrocarbon products, including providing a substrate comprising CO to a bioreactor containing a culture of one or more micro-organisms; and fermenting the culture in the bioreactor to produce one or more hydrocarbon products. The substrate comprising CO is derived from a CO2 reforming process.

CATALYST AND PROCESS FOR THE PRODUCTION OF DIESEL FUEL FROM NATURAL GAS, NATURAL GAS LIQUIDS, OR OTHER GASEOUS FEEDSTOCKS

A unique process and catalyst is described that operates efficiently for the direct production of a high cetane diesel type fuel or diesel type blending stock from stochiometric mixtures of hydrogen and carbon monoxide. This invention allows for, but is not limited to, the economical and efficient production high quality diesel type fuels from small or distributed fuel production plants that have an annual production capacity of less than 10,000 barrels of product per day, by eliminating traditional wax upgrading processes. This catalytic process is ideal for distributed diesel fuel production plants such as gas to liquids production and other applications that require optimized economics based on supporting distributed feedstock resources.

METHODS, SYSTEMS, AND APPARATUSES FOR UTILIZING A FISCHER-TROPSCH PURGE STREAM

Systems, apparatuses and methods of utilizing a Fischer-Tropsch ("FT") tail gas purge stream for recycling are disclosed. One or more methods include removing an FT tail gas purge stream from an FT tail gas produced by an FT reactor, treating the FT tail gas purge stream with steam in a water gas shift ("WGS") reactor, having a WGS catalyst, to produce a shifted FT purge stream including carbon dioxide and hydrogen, and removing at least a portion of the carbon dioxide from the shifted FT purge stream, producing a carbon dioxide stream and a treated purge stream. Other embodiments are also disclosed.

PROCESS FOR OBTAINING CARBON MONOXIDE AND HYDROGEN

The present invention is directed to a process for simultaneously obtaining pure carbon monoxide and pure hydrogen in a steam reformer plant for hydrogen or ammonia generation, having a primary reformer, a secondary reformer and downstream thereof, a CO conversion stage. A part gas stream of the synthesis gas stream, which is discharged from the secondary reformer having a CO content of between 2 and 20 mol.% and is at a temperature of from 200 to 500.degree.C and a pressure between 15 and 50 bar, is removed between the secondary reformer and the CO conversion stage. The part gas stream is then is cooled to a temperature below 100.degree.C, thereby condensing out the major part of the steam contained in the gas stream. The remaining raw synthesis gas stream is then guided by way of a multistage gas separation plant in which the gas components H2, residual steam, CH4, CO2 and optionally N2 are separated, either individually or together, from the CO. The separated gas components are then ...

MINIMIZING EVAPORATOR SCALING AND RECOVERY OF SALTS DURING GASIFICATION

The invention relates to a process for minimizing evaporator scaling during the recovery of liquids and solids from the aqueous effluent discharged duri ng a partial oxidation gasification from a gasifier (16), wherein the aqueous effluent contains ammonium chloride. The aqueous effluent is evaporated in a n evaporator (106) to produce a distillate water line (110) and a line containing brine (112) with a brine concentration of about 10 to 60 weight percent. The brine can be further concentrated and ammonium chloride crystal s are recovered. The distillate is recycled to the gasification reaction. No effluent discharges to the environment.

purifier for gas generator

PROCESS AND INSTALLATION OF TREATMENT OF GASES RESULTING FROM the DECOMPOSITION BY EFFETTHERMIQUE Of a SOLID LOAD

Process and device for employment, in installations of gas generators which comprise only one circulation of low or zero cooling air, of cooling systems and purification planned for the gas generator vehicles

Improvement with the apparatuses of purification and filtering of the portable gas generators

Gas generator automatically destroying the tar as of the their formation and obtaining by his devices of relaxation and fitration a very purified gas

Improvements brought to the devices of gas purification, in particular for gas generators assembled on cars

Improvements brought to the purifying devices of lean fuels, in particular to those assembled on board motor vehicles

PROCEDE POUR RECUPERER DES GAZ DANS UN MELANGE GAZEUX

On prépare des mélanges gazeux 1 constitués d'éthylène, d'acétylène, de monoxyde de carbone, de dioxyde de carbone, d'eau, d'alcools, d'acide sulfhydrique, de propylène et d'hydrocarbures plus lourds, de sulfure de carbone, etc., par élimination de l'eau, des alcools, du sulfure de carbone, de l'acide sulfhydrique, du propylène et des hydrocarbures plus lourds, dans des systèmes separés d'absorption par solvant (C, E, G) puis on effectue un contact K avec un halogénure d'aluminium et de cuivre cuivreux pour éliminer par complexation l'éthylène, l'acétylène et/ou le monoxyde de carbone et on utilise le gaz de dégagement provenant de la zone d'élimination de l'éthylène, de l'acétylène et/ou du monoxyde de carbone pour effectuer le préstrippage H et/ou la régénération I du solvant du système d'absorption. L'invention s'applique en particulier au traitement de mélanges gazeux dérivant des gaz de four à coke.

A METHOD FOR RECOVERING GASES IN A GAS MIXTURE

purifier by wet process for lean fuel or others

PROCESS AND INSTALLATION OF TREATMENT OF GASES RESULTING FROM the DECOMPOSITION BY HEATING EFFECT Of a SOLID LOAD

La présente invention concerne un procédé de traitement de gaz issus de la décomposition par effet thermique d'une charge solide dans un four notamment par pyrolyse ou gazéification, cette décomposition générant à la sortie du four des gaz bruts contenant des polluants solides et gazeux. Selon l'invention, on procède, de manière simultanée et à la sortie dudit four, à une opération mécanique de dépoussiérage des gaz et à un traitement chimique desdits gaz. Application notamment aux traitements de déchets urbains et/ ou industriels, de boues de station d'épuration, de biomasse ou de sols pollués.

Method and System for Synthesizing Liquid Hydrocarbon Compounds

Provided is a method for synthesizing liquid hydrocarbon compounds wherein synthesizing liquid hydrocarbon compounds from a synthesis gas by a Fisher-Tropsch synthesis reaction. The method includes a first absorption step of absorbing a carbon dioxide gas, which is contained in gaseous by-products generated in the Fisher-Tropsch synthesis reaction, with an absorbent, and a second absorption step of absorbing a carbon dioxide gas, which is contained in the synthesis gas, with the absorbent which is passed through the first absorption step.

Method of treating an off-gas stream and an apparatus therefor

The present invention provides a method of treating an off-gas stream ( 80 ) comprising NH 3 and H 2 S to provide a sulphate stream ( 910 ), the method comprising the steps of: (i) providing a first off-gas stream ( 80 ) comprising NH 3 , H 2 S, CO 2 and optionally one or more of HCN, COS and CS 2 ; (ii) passing the first off-gas stream ( 80 ) to an incinerator ( 300 ) to oxidise NH 3 , H 2 S, and optionally one or more of HCN, COS and CS 2 to provide a second off-gas stream ( 310 ) comprising N 2 , H 2 O, SO 2 and CO 2 ; (iii) scrubbing the second off-gas stream ( 310 ) with a first aqueous alkaline stream ( 380, 876 a ) in a caustic scrubber ( 350 ) to separate SO 2 and a part of the CO 2 from the second off-gas stream to provide a spent caustic stream ( 360 ) comprising carbonate and one or both of sulphite and bisulphite and a caustic scrubber off-gas stream ( 370 ) comprising N 2 and CO 2 ; and (iv) passing the spent caustic stream ( 360 ) to an aerator ( 900 ) comprising sulphur-oxidising bacteria in the presence of oxygen to biologically disc sulphite and bisulphite to sulphate to provide a sulphate stream ( 910 ).

Catalytic gasification of organic matter in supercritical water

A catalyst system including at least one metal and an oxide support, said oxide support including at least one of Al 2 O 3 , Mn x O y , MgO, ZrO 2 , and La 2 O 3 , or any mixtures thereof; said catalyst being suitable for catalyzing at least one reaction under supercritical water conditions is disclosed. Additionally, a system for producing a high-pressure product gas under super-critical water conditions is provided. The system includes a pressure reactor accommodating a feed mixture of water and organic matter; a solar radiation concentrating system heating the pressure reactor and elevating the temperature and the pressure of the mixture to about the water critical temperature point and pressure point or higher. The reactor is configured and operable to enable a supercritical water process of the mixture to occur therein for conversion of the organic matter and producing a high-pressure product fuel gas.

Integrated gasification combined cycle plant with char preparation system

Provided herein are systems, methods and equipment that include Integrated Gasification Combined-Cycle technology to retrofit existing plants, that include, e.g., subsystems for separating char fines from syngas after it emerges from an internally-circulating fluidized bed carbonizer and injecting the char into the carbonizer draft tube as a fuel source. Efficiency and power generation are thus increased to the extent that inclusion of carbon capture systems are now possible for existing coal plants in order to significantly reduce carbon dioxide emissions.

System and method for dry mixing a gasification feed

Present embodiments include systems and methods for reducing variations in a solid feed provided to a gasifier. For example, in an embodiment, a gasification feed vessel includes a solid fuel inlet configured to receive a solid fuel into the gasification feed vessel, a dry mixer configured to dry mix the solid fuel within the feed vessel, a solid fuel outlet configured to deliver a feed of the solid fuel to a gasification system, and a metering device coupled to the solid fuel outlet. The metering device is configured to control an amount of the feed of the solid fuel delivered to the gasification system. The gasification feed vessel is configured to provide the feed of the solid fuel to the gasification system within a desired energy concentration range over time.

SYSTEM AND METHOD FOR GASIFICATION

A system includes a gasifier having a first enclosure having a first inlet, a first outlet, and a first interior volume. The first inlet is configured to receive a first fuel feedstock into the first interior volume, and the first outlet is configured to output a first syngas away from the first interior volume. The system also includes a plasma gasifier disposed downstream from the first outlet and coupled to a waste stream produced by the gasifier from the first fuel feedstock. 1. A system , comprising:a gasifier comprising a first enclosure having a first inlet, a first outlet, and a first interior volume, wherein the first inlet is configured to receive a first fuel feedstock into the first interior volume, and the first outlet is configured to output a first syngas away from the first interior volume; anda plasma gasifier disposed downstream from the first outlet and coupled to a waste stream produced by the gasifier from the first fuel feedstock.2. The system of claim 1 , wherein the plasma gasifier comprises a second enclosure having a second inlet claim 1 , a second outlet claim 1 , and a second interior volume claim 1 , wherein a plurality of plasma torches are coupled to the second enclosure.3. The system of claim 2 , wherein the second interior volume is at least less than approximately 5 percent of the first interior volume.4. The system of claim 2 , wherein the plurality of plasma torches are directed toward one another to generally converge plasma streams.5. The system of claim 1 , wherein the waste stream comprises a filter cake produced from a black water source filtered through a fines filter unit in fluid communication with the plasma gasifier.6. The system of claim 5 , wherein the plasma gasifier comprises a second inlet configured to receive the filter cake from the fines filter.7. The system of claim 5 , wherein the filter cake is treated in the plasma gasifier to produce a second syngas.8. The system of claim 7 , wherein plasma gasifier is ...

Supplemental fuel to combustor of dual fluidized bed gasifier

A method of gasification by introducing a feed material to be subjected to gasification into a dual fluidized bed gasifier comprising a pyrolyzer fluidly connected with a combustor such that a circulation stream comprising a heat transfer material can be continuously circulated between the pyrolyzer, in which the temperature of the circulation stream is reduced, and the combustor, in which the temperature of the circulation stream is increased, wherein the pyrolyzer is operable to convert at least a portion of the feed material into a gasifier product gas comprising hydrogen and carbon monoxide, and wherein the combustor is operable to increase the temperature of the circulation stream via combustion of char introduced thereto with the circulation stream and at least one supplemental fuel. A system for carrying out the method is also provided.

System and method for production of fischer-tropsch synthesis products and power

A method for generation of power and Fischer-Tropsch synthesis products by producing synthesis gas comprising hydrogen and carbon monoxide, producing Fischer-Tropsch synthesis products and Fischer-Tropsch tailgas from a first portion of the synthesis gas, and generating power from a second portion of the synthesis gas, from at least a portion of the Fischer-Tropsch tailgas, or from both. The method may also comprise conditioning at least a portion of the synthesis gas and/or upgrading at least a portion of the Fischer-Tropsch synthesis products. A system for carrying out the method is also provided.

PROCESS FOR SELECTIVE OXIDATION OF HYDROGEN SULPHIDE

The present invention provides a process for the selective oxidation of hydrogen sulphide in a hydrogen sulphide-containing hydrocarbon and/or hydrogen feed gas to elemental sulphur in a reaction zone containing a Claus catalyst, comprising the steps of: i) reacting in the reaction zone the hydrogen sulphide in the hydrogen sulphide-containing hydrocarbon and/or hydrogen feed gas with sulphur dioxide at a pressure in the range of from 4 to 200 bar (absolute) and a temperature in the range of from 120 and 160° C., such that the elemental sulphur formed is essentially in liquid form; ii) contacting the catalyst with a reducing atmosphere at elevated temperatures. 1. A process for the selective oxidation of hydrogen sulphide in a hydrogen sulphide-containing hydrocarbon and/or hydrogen feed gas to elemental sulphur in a reaction zone containing a Claus catalyst , comprising the steps of:i) reacting in the reaction zone the hydrogen sulphide in the hydrogen sulphide-containing hydrocarbon and/or hydrogen feed gas with sulphur dioxide at a pressure in the range of from 4 to 200 bar (absolute) and a temperature in the range of from 120 and 160° C., such that the elemental sulphur formed is essentially in liquid form;ii) contacting the Claus catalyst with a reducing atmosphere at elevated temperatures.2. A process according to claim 1 , wherein a sequence comprising step (i) and subsequently step (ii) is repeated one or more times.3. A process according to claim 1 , wherein the Claus catalyst is a TiO-comprising catalyst.4. A process according to claim 1 , wherein the reducing atmosphere comprises at least one of hydrogen sulphide claim 1 , hydrogen or carbon monoxide.5. A process according to claim 1 , wherein the reducing atmosphere comprises a hydrogen sulphide-containing hydrocarbon gas.6. A process according to claim 1 , wherein the reducing atmosphere comprises a hydrogen-comprising gas.7. A process according to claim 1 , wherein step (ii) includes contacting the ...

System and Method for Processing Alternate Fuel Sources

An energy conserving wastewater treatment system capable of being fueled by alternate fuel sources comprises a synthesis gas generator that produces synthesis gas from a fuel and an organic waste digester that produces biogas. A combined synthesis gas and biogas storage reservoir that is in communication with both the synthesis gas generator and the organic waste digester. At least one boiler is in communication with the combined synthesis gas and biogas storage reservoir.

Method and apparatus for producing liquid hydrocarbon fuels from coal

A method of converting coal into a liquid hydrocarbon fuel utilizes a high pressure, high temperature reactor which operates upon a blend of micronized coal, a catalyst, and steam. Microwave power is directed into the reactor. The catalyst, preferably magnetite, will act as a heating media for the microwave power and the temperature of the reactor will rise to a level to efficiently convert the coal and steam into hydrogen and carbon monoxide.

Method and Apparatus for Adjustably Treating a Sour Gas

A feed gas comprising CO, HS and His treated to produce an H-enriched product and an HS-lean, COproduct. The feed gas is separated to provide the H-enriched product and a stream of sour gas. The stream of sour gas is divided into two parts, one of which is processed in an HS removal system to form one or more streams of sweetened gas, and the other of which bypasses the HS removal system, the stream(s) of sweetened gas and the sour gas bypassing the HS removal system then being recombined to form the HS-lean, COproduct gas. The division of the sour gas between being sent to and bypassing the HS removal system is adjusted responsive to changes in the HS content of the sour gas, so as to dampen or cancel the effects of said changes on the HS content of the HS-lean, COproduct gas. 1. Apparatus for treating a feed gas , comprising CO , HS and H , to produce an H-enriched product gas and an HS-lean , COproduct gas , the apparatus comprising:{'sub': 2', '2', '2', '2', '2', '2', '2, 'a pressure swing adsorption (PSA) system for separating the feed gas to form a stream of H-enriched product gas and a stream of sour gas, the sour gas comprising CO, HS and Hbut being depleted in Hand enriched in HS and COrelative to the feed gas;'}{'sub': 2', '2', '2, 'an HS removal system for processing a part of the sour gas to form one or more streams of sweetened gas, depleted in HS and enriched in COrelative to the feed gas;'}{'sub': 2', '2, 'conduit means for transferring a part of said sour gas into the HS removal system and bypassing the HS removal system with another part of said sour gas;'}{'sub': '2', 'a valve system for adjustably controlling the division of said sour gas between being sent to the HS removal system and bypassing said system; and'}{'sub': 2', '2', '2', '2, 'conduit means for withdrawing one or more streams of sweetened gas from the HS removal system, and combining said stream(s) with the sour gas bypassing the HS removal system to form HS-lean, COproduct gas.'}2. ...

SYSTEM AND METHOD FOR DUAL FLUIDIZED BED GASIFICATION

A method of producing a high quality synthesis gas comprising less than a desired percentage of non-synthesis gas components and a desired mole ratio of hydrogen to carbon monoxide by providing a low quality synthesis gas comprising greater than the desired percentage; introducing the low quality synthesis gas into a conditioner; introducing a flue gas into a combustor; extracting a first catalytic heat transfer stream from the conditioner, and introducing at least a portion of the first catalytic heat transfer stream into the combustor; extracting a second catalytic heat transfer stream from the combustor, and introducing at least a portion of the second catalytic heat transfer stream into the conditioner; extracting a spent flue gas from the combustor; and extracting from the conditioner the high quality synthesis gas comprising the desired percentage and the desired mole ratio. 1. A method of producing a high quality synthesis gas comprising less than a desired percentage of non-synthesis gas components , which are components other than hydrogen and carbon monoxide , and a desired mole ratio of hydrogen to carbon monoxide , the method comprising:providing a low quality synthesis gas comprising greater than the desired percentage of non-synthesis gas components;introducing the low quality synthesis gas into a fluid bed conditioner, the fluid bed conditioner one fluidized bed reactor of a dual fluidized bed loop;introducing a flue gas into a fluid bed combustor, wherein the fluid bed combustor is the second fluidized bed reactor of the dual fluidized bed loop;extracting a first catalytic heat transfer stream comprising a catalytic heat transfer material and having a first temperature from the fluid bed conditioner, and introducing at least a portion of the first catalytic heat transfer stream into the fluid bed combustor;extracting a second catalytic heat transfer stream comprising catalytic heat transfer material and having a second temperature greater than the ...

CONFIGURATIONS AND METHODS FOR GASIFICATION PLANTS

A syngas treatment plant has a decarbonization section and a desulfurization section that use the same solvent to remove various acid gases. Contemplated methods and plants are highly effective in removal of CO2, recycle sulfurous contaminants to extinction. Minimal loss of H2 while maximizing H2S concentration in a Claus plant feed during regeneration of the solvent is achieved by stripping the solvent with both treated syngas and a flash vapor of the desulfurization section. 1. A method of operating a syngas treatment plant , comprising:providing a syngas and a CO2-loaded lean solvent from a CO2 absorber to an H2S absorber to so produce in the H2S absorber a CO2-loaded rich solvent and a desulfurized syngas;stripping CO2 and H2 from the CO2-loaded rich solvent in a first stripper using a treated syngas as a first stripping gas and using a flash vapor as a second stripping gas to thereby produce a stripped rich solvent and a CO2/H2-rich recycle gas;flashing the stripped rich solvent to thereby produce the flash vapor;further stripping the stripped rich solvent in a second stripper to thereby regenerate a lean solvent for use in the CO2 absorber and to thereby produce a concentrated acid gas; andfeeding the desulfurized syngas into the CO2 absorber to thereby produce the treated syngas and the CO2-loaded rich solvent.2. The method of further comprising a step regenerating a portion of the CO2-loaded lean solvent in a plurality of flash steps claim 1 , and using refrigeration content from the flash steps for refrigeration in the CO2 absorber.3. The method of wherein at least one of the plurality of flash steps produces a flash gas claim 2 , further comprising a step of recycling the flash gas to the CO2 absorber.4. The method of further comprising a step of feeding the concentrated acid gas into a Claus plant and combining a Claus plant tail gas after hydrogenation with the syngas.5. The method of further comprising a step of separating water from the CO2/H2-rich ...

Process for regulating joule value of offgases from plants for pig iron production or of synthesis gas

In a plant having integrated CO 2 removal, for pig iron production or synthesizing gas, at least part of the offgas or synthesis gas is discharged as export gas from the plant, optionally collected in an export gas container and subsequently thermally utilized in a gas turbine. The offgas from the gas turbine is fed to a waste heat boiler for generation of steam. To reduce the addition of high-grade fuel gases, at least part of the tailgas from the CO 2 removal plant is mixed into the export gas upstream of the gas turbine as a function of the joule value of the export gas after addition of the tailgas. The proportion of tailgas is increased when the joule value of the export gas goes above a predefined maximum joule value and the proportion of tailgas is reduced when the joule value of the export gas drops below a predefined minimum joule value.

METHOD OF SUPPRESSING METAL CONTAMINATION OF SYNTHESIS GAS PRODUCTION APPARATUS

A synthesis gas production apparatus (reformer) to be used for a synthesis gas production step in a GTL (gas-to-liquid) process is prevented from being contaminated by metal components. A method of suppressing metal contamination of a synthesis gas production apparatus operating for a GTL process that includes a synthesis gas production step of producing synthesis gas by causing natural gas and gas containing steam and/or carbon dioxide to react with each other for reforming in a synthesis gas production apparatus in which, at the time of separating and collecting a carbon dioxide contained in the synthesis gas produced in the synthesis gas production step and recycling the separated and collected carbon dioxide as source gas for the reforming reaction in the synthesis gas production step, a nickel concentration in the recycled carbon dioxide is not higher than 0.05 ppmv. 1. A method of suppressing metal contamination of a synthesis gas production apparatus operating for a GTL (gas-to-liquid) process , comprising:a synthesis gas production step of producing synthesis gas by causing natural gas and gas containing steam and/or carbon dioxide to react with each other for reforming in a synthesis gas production apparatus;a Fischer-Tropsch oil manufacturing step of manufacturing Fischer-Tropsch oil by subjecting the synthesis gas produced in the synthesis gas production step to a Fischer-Tropsch reaction and subsequently isolating a gaseous product from the Fischer-Tropsch reaction products; andan upgrading step of manufacturing various hydrocarbon oils by subjecting the Fischer-Tropsch oil manufactured in the Fischer-Tropsch oil manufacturing step to hydrotreatment and distillation, whereinat the time of separating and collecting a carbon dioxide contained in the synthesis gas produced in the synthesis gas production step and recycling the separated and collected carbon dioxide as source gas for the reforming reaction in the synthesis gas production step, a nickel ...

Process for the purification of crude gas from solids gasification

A process and device is provided for the generation and purification of a crude gas for synthesis gas generation from a solid carbon-containing fuel by a coal gasification reaction. The fuel is mixed with a quenching medium directly after generation to dissipate the internal energy and is then brought into contact with a compound or a sorbent in the mixing chamber or downstream of the mixing chamber such that the acidic or basic or sulphur-containing or halogen-containing constituents contained in the crude gas and originating from the gasification reaction are absorbed. A solids-separating device removes the solid or solidified constituents from the system. The sorbent can be regenerated and returned to the process such that an energy-intensive cooling of the crude gas is not required for its purification and the synthesis gas thus purified can be used in a subsequent process without any further heating.

COLD BED ADSORPTION SULFUR RECOVERY PROCESS

A process for removing sulfur from a gas stream is provided in which a plurality of reactor units, each comprising a condenser and reactor, are selectively operable under Claus reaction and cold bed adsorption conditions. The arrangement of reactor units within the plant is periodically changed following a front-middle-back sequencing scheme. This ensures that the final reactor unit in the series utilizes fully cooled catalyst which is most efficient for operation under cold bed adsorption conditions. In addition, the condenser of the final reactor unit in the series operates at or below the freezing point of sulfur thereby permitting even greater sulfur recovery. 1. A process for recovering sulfur from a gas stream comprising:{'sub': 2', '2', '2', '2, 'passing a process gas comprising HS and SOthrough a primary Claus reactor operable to convert at least a portion of the HS and SOpresent in the process gas into elemental sulfur;'}sequentially passing the gas exiting the primary Claus reactor through at least first, second, and third reactor units, each reactor unit comprising a catalytic reactor and a sulfur condenser, each of the catalytic reactors being capable of selective operation under both Claus reaction conditions and cold bed adsorption conditions, during a first period of operation the reactor of the third reactor unit operates under cold bed adsorption conditions; andafter the first period of operation of the reactor units, rearranging the sequence of the reactor units such that during a second period of operation the gas exiting the primary Claus reactor first passes through the third reactor unit, followed by the first and second reactor units with the reactor of the second reactor unit operating under cold bed adsorption conditions.2. The process according to claim 1 , wherein during the first period of operation the first reactor unit undergoes regeneration in which elemental sulfur deposited on the catalyst present in the catalytic reactor is ...

Cement clinker manufacturing plant

A cement clinker manufacturing plant that includes a plant for producing purified syngas, obtained from solid waste, and process for transferring ash recovered from the ash pan of the gasifier to at least one inlet of the feedstock conversion device, which the plant includes, and/or of the furnace for the purpose of incorporating said ash into the feedstock; and a process for conveying the purified syngas to the main tuyere of the furnace and/or to at least one inlet of the feedstock conversion device.

HYDROGEN SULFIDE AND CARBONYL SULFIDE REMOVAL APPARATUS USING MICROWAVE PLASMA, AND METHOD THEREOF

Disclosed are a hydrogen sulfide and carbonyl sulfide removal apparatus using microwave plasma and a method thereof. More particularly, in the apparatus and the method, poisonous gases, such as hydrogen sulfide (HS) and carbonyl sulfide (COS), contained in natural gas, refined crude oil refinery gas, gasified synthetic gas, etc. are removed by using microwave plasma, and elemental sulfur and hydrogen are generated from the gases. 13-. (canceled)41. A hydrogen sulfide and carbonyl sulfide removal method using microwave plasma by using the apparatus as claimed in claim ,the apparatus comprising a hydrogen sulfide and carbonyl sulfide supply chamber, a plasma decomposition chamber, and a rebinding chamber which are vertically piped as upper/middle/lower pipes, wherein to the hydrogen sulfide and carbonyl sulfide supply chamber, a vertical pipe, a synthetic gas comprising hydrogen sulfide and carbonyl sulfide and a plasma generating gas are supplied, in the plasma decomposition chamber, as a vertical pipe, the supplied hydrogen sulfide and the carbonyl sulfide are decomposed by plasma flame, in the rebinding chamber, as a vertical pipe, from among elements of the hydrogen sulfide and the carbonyl sulfide decomposed by the plasma flame, hydrogen and carbon monoxide are rebound and are separated from sulfur, and between the hydrogen sulfide and carbonyl sulfide supply chamber and the plasma decomposition chamber, a waveguide of a plasma generating device is communicated so as to generate plasma,the method comprising:a hydrogen sulfide and carbonyl sulfide containing mixed-gas supplying step, in which a mixed-gas comprising the plasma generating gas with the synthetic gas comprising the hydrogen sulfide and the carbonyl sulfide is swirlingly supplied into the hydrogen sulfide and carbonyl sulfide supply chamber;a microwave supplying step, in which microwaves generated from the plasma generating device are supplied to the supplied mixed-gas;a plasma flame forming step, in ...

METHODS, SYSTEMS, AND DEVICES FOR SYNTHESIS GAS RECAPTURE

Methods, systems, and/or devices for synthesis gas recapture are provided, which may include methods, systems, and/or devices for filtering a synthesis gas stream. In some cases, tars, particulates, water, and/or heat may be removed from the synthesis gas stream through the filtering of the synthesis gas stream. The filtered synthesis gas stream may then be captured and/or utilized in a variety of different ways. Some embodiments utilizing a C—O—H compound to filter a synthesis gas stream. In some embodiments, the C—O—H compound utilized to filter the synthesis gas stream may be utilized to produce additional synthesis gas. The additional synthesis gas may be filtered by additional C—O—H compound. 1. A method of recapture for a synthesis gas stream , the method comprising:generating the synthesis gas stream; andfiltering the synthesis gas stream through a compound comprising carbon, hydrogen, and oxygen.2. The method of claim 1 , wherein filtering the synthesis gas stream comprises:removing at least tars, particulates, water, or heat from the synthesis gas stream.3. The method of claim 1 , further comprising:utilizing the compound comprising carbon, hydrogen, and oxygen to produce an additional synthesis gas stream after the compound filters the synthesis gas stream.4. The method of claim 3 , further comprising:filtering the additional synthesis gas stream produced through an additional compound comprising carbon, hydrogen, and oxygen.5. The method of claim 1 , further comprising:capturing hydrogen gas from the filtered synthesis gas stream.6. The method of claim 1 , further comprising:capturing the filtered synthesis gas.7. The method of claim 1 , further comprising:directing the filtered synthesis gas to subsystem for utilization.8. The method of claim 3 , wherein producing the additional synthesis gas comprising:combining water with the compound comprising carbon, hydrogen, and oxygen to form a wet compound;transferring the wet compound to a reaction chamber; ...

PRODUCTION OF HYDROCARBON LIQUIDS

A process to efficiently convert organic feedstock material into liquid non-oxygenated hydrocarbons in the Cto Ccarbon skeleton range is disclosed. The process can utilize gaseous, liquid or solid organic feedstocks containing carbon, hydrogen and, optionally, oxygen. The feedstock may require preparation of the organic feedstock for the process and is converted first into a synthesis gas containing carbon monoxide and hydrogen. The synthesis gas is then cleaned and conditioned and extraneous components removed, leaving substantially only the carbon monoxide and hydrogen. It is then converted via a series of chemical reactions into the desired liquid hydrocarbons. The hydrocarbons are suitable for combustion in a vehicle engine and may be regarded a replacement for petrol made from fossil fuels in the Cto Ccarbon backbone range. The process also recycles gaseous by-products back through the various reactors of the process to maximize the liquid hydrocarbon in the Cto Ccarbon skeleton range yield. 1. A process for producing a Cto Chydrocarbon fuel from organic material , comprising:a) applying a heat source to heat an organic feedstock and oxygen at substoichiometric conditions to a temperature sufficient for partial combustion of said organic feedstock to occur and then ceasing application of said heat source once partial combustion has commenced;b) partially combusting said organic feedstock so as to produce a synthesis gas stream, said synthesis gas stream containing at least carbon monoxide, carbon dioxide and hydrogen;{'sub': '10', 'c) substantially removing unwanted solid and liquid matter comprising oxides, ash and hydrocarbons having a carbon skeleton of greater than Cfrom said synthesis gas stream to produce a first cleaned synthesis gas stream containing at least carbon monoxide, carbon dioxide and hydrogen;'}d) compressing said first cleaned synthesis gas stream and substantially removing water;e) conditioning and further cleaning the first cleaned ...

GASIFIER FLUIDIZATION

A system for the production of synthesis gas, including a gasification apparatus configured to convert at least a portion of a gasifier feed material introduced thereto into a gasification product gas comprising synthesis gas having a molar ratio of hydrogen to carbon monoxide; at least one additional apparatus selected from the group consisting of feed preparation apparatus located upstream of the gasification apparatus, synthesis gas conditioning apparatus, and synthesis gas utilization apparatus; and at least one line fluidly connecting the at least one additional apparatus or an outlet of the gasification apparatus with the at least one vessel of the gasification apparatus, whereby a gas from the at least one additional apparatus or exiting the gasification apparatus may provide at least one non-steam component of a fluidization gas. A method of utilizing the system is also provided. 1. A system for the production of synthesis gas , the system comprising:a gasification apparatus configured to convert at least a portion of a gasifier feed material introduced thereto into a gasification product gas comprising synthesis gas having a molar ratio of hydrogen to carbon monoxide, wherein the gasification apparatus comprises at least one vessel configured for fluidization of the contents thereof via introduction thereto of a fluidization gas comprising at least one non-steam component;at least one additional apparatus selected from the group consisting of feed preparation apparatus located upstream of the gasification apparatus and configured to prepare a carbonaceous material for introduction into the gasification apparatus; synthesis gas conditioning apparatus configured to produce a conditioned synthesis gas having a molar ratio of hydrogen to carbon monoxide that is different from the molar ratio of hydrogen to carbon monoxide in the gasification product gas, to provide a conditioned synthesis gas having a reduced amount of at least one component relative to the ...

Plasma-assisted method and system for treating raw syngas comprising tars

The invention provides a system and method for conversion of raw syngas and tars into refined syngas, while optionally minimizing the parasitic losses of the process and maximizing the usable energy density of the product syngas. The system includes a reactor including a refining chamber for refining syngas comprising one or more inlets configured to promote at least two flow zones: a central zone where syngas and air/process additives flow in a swirling pattern for mixing and combustion in the high temperature central zone; at least one peripheral zone within the reactor which forms a boundary layer of a buffering flow along the reactor walls, (b) plasma torches that inject plasma into the central zone, and (c) air injection patterns that create a recirculation zone to promotes mixing between the high temperature products at the core reaction zone of the vessel and the buffering layer, wherein in the central zone, syngas and air/process additives mixture are ignited in close proximity to the plasma arc, coming into contact with each other, concurrently, at the entrance to the reaction chamber and method of using the system.

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.

ACID GAS MANAGEMENT IN LIQUID FUEL PRODUCTION PROCESS

A process and method for producing liquid fuel product from hydrogen and carbon monoxide containing streams produced by gasifying solid carbonaceous feedstock and steam reforming of light fossil fuels. The gasifier syngas is treated to preferentially remove at least 99% of sulfur containing impurities and less than 50% of the COto produce a treated gasifier syngas and a COenriched gas. The treated gasifier syngas and the light fossil fuel conversion unit product gas are combined to form a mixed syngas that is converted into a liquid fuel product. The COenriched gas is used in the gasification unit. 1. A method for liquid production , comprising:a) converting a solid carbonaceous material in a gasification unit to form a gasifier syngas;b) passing the gasifier syngas to a gas conditioning unit, and treating the gasifier syngas therein;{'sub': 2', '2, 'c) forming at least a treated gasifier syngas stream containing at least 50% of COin the gasifier syngas, a CO-enriched gas stream, and a sulfur-enriched stream;'}{'sub': 2', '2, 'd) utilizing at least a portion of the CO-enriched gas stream containing at least 90% of COremoved from the gasifier syngas in the formation of the gasifier syngas;'}{'sub': 2', '2', '2, 'e) converting a light fossil fuel in a light fossil fuel conversion unit to form a H-rich syngas comprising Hand CO at a H/CO mole ratio of at least 2:1;'}{'sub': 2', '2, 'f) combining treated gasifier syngas and H-rich syngas to form a mixed syngas having a H/CO ratio greater than that of treated gasifier syngas stream;'}g) converting the mixed syngas to form a liquid fuel product and a byproduct stream comprising one or more of hydrogen, CO, water vapor, methane, and hydrocarbons containing 2 to 8 carbon atoms and 0 to 2 oxygen atoms; andh) reacting up to 100% of the byproduct stream in the light fossil fuel conversion unit to facilitate formation of the H2-rich syngas.2. The method according to claim 1 , further comprises reacting 100% of the byproduct ...

SYSTEM FOR GASIFICATION OF SOLID WASTE AND METHOD OF OPERATION

A system and method of producing syngas is provided. The system includes a low tar gasification generator that receives at least a first and second feedstock stream, such as a solid waste stream. The first and second feedstock streams are mixed and gasified to produce a first gas stream. An operating parameter is measured and a ratio of the first and second feedstock streams is changed in response to the measurement. 1. A system for converting solid waste material to a syngas comprising:a feedstock module configured to receive at least a first feedstock stream and a second feedstock stream, the second feedstock stream being different than the first feedstock stream, the feedstock module being further configured to mix the first feedstock stream and the second feedstock stream at a first ratio to produce a first refuse derived feedstock;an input module having a low tar gasification generator configured to produce a first gas stream in response to receiving the refuse derived feedstock, the first gas stream including hydrogen;a process module fluidly coupled to receive the first gas stream, the process module including at least one clean-up process module configured to remove at least one contaminant from the first gas stream and produce a second gas stream containing hydrogen;a first sensor arranged to measure a first operating parameter; anda control system coupled for communication to the feedstock module and the sensor, the control system having a processor responsive to executable computer instructions for changing the ratio of the first mixture of the first feedstock stream to the second feedstock stream to a second ratio in response to receiving the first parameter.2. The system of claim 1 , wherein the first operating parameter is a temperature of the syngas entering the process module.3. The system of claim 2 , wherein the second feedstock stream has a higher energy content than the first feedstock stream.4. The system of claim 3 , wherein the temperature is ...

PROCESS FOR HYDROGEN SULFIDE SCRUBBING AND METHOD FOR FERRIC ION REGENERATION

A process and method for removing hydrogen sulfide from a gas and regenerating ferric ions consumed in the hydrogen sulfide scrubbing process at low pH. A two-scrubber regenerative chemical scrubbing system for removing hydrogen sulfide from a gas that provides an economical system for removing hydrogen sulfide from a gas at low pH without the need for chelating agents. An oxide of manganese is used as a catalyst to enhance the regeneration of ferric ions in an aqueous solution under acidic conditions in the presence of oxygen. The process may further include contacting the aqueous solution with a second gas comprising air to replenish the dissolved oxygen in the aqueous solution. The regenerated solution comprising ferric ions can be reused to treat additional hydrogen sulfide containing gases. 1. A process for treating a hydrogen sulfide containing gas , comprising:contacting an aqueous solution containing ferric ions with the hydrogen sulfide containing gas, wherein the aqueous solution has a pH of about 6.0 or less,extracting and dissolving hydrogen sulfide from the hydrogen sulfide containing gas into the aqueous solution,reacting the dissolved hydrogen sulfide with the ferric ions in the aqueous solution to produce ferrous ions and sulfur, wherein the sulfur is insoluble in solution; andregenerating ferric ions in the aqueous solution using a catalyst.2. The process of claim 1 , further comprising contacting the aqueous solution with a second gas.3. The process of claim 2 , wherein the second gas is air.4. The process of claim 1 , wherein the aqueous solution has a pH of 4.5 or less.5. The process of claim 4 , wherein the aqueous solution has a pH of 2.0 or less.6. The process of claim 1 , wherein the catalyst is an oxide of manganese.7. The process of claim 6 , wherein the oxide of manganese is at least one of MnO claim 6 , MnO claim 6 , MnO claim 6 , MnO claim 6 , MnO claim 6 , and MnO.8. The process of claim 6 , wherein the oxide of manganese is MnO.9. The ...

METHOD AND APPARATUS FOR RECOVERING ABSORBING AGENTS IN ACID GAS TREATMENT

A method and apparatus for continuously treating acid gases including recovering absorbent chemicals by introducing streams leaving a regenerator and/or leaving an absorber into a static mixing zone wherein supplemental washing water is added to recover absorbent chemicals. Improvements to the prior art methods are provided where one or more absorbent chemical recovery units are included to increase the amount of recovered absorbent chemicals exiting the regenerator and/or exiting the absorber are increased and/or maximized. Absorbent chemical recovery units can include mixing units where liquid is added to the stream of sour gas and absorbent chemical to mix with and absorb the absorbent chemical from the stream. 1. A continuous process for acid gas removal comprising the following steps:(a) introducing into an absorption zone [ a hydrocarbon,', 'a mixture of hydrocarbons,', 'synthesis gas, and', 'a mixture of nitrogen and hydrogen, and, 'a process gas selected from the group consisting of, 'about 1 to about 99 percent by volume', carbon dioxide,', 'hydrogen sulfide,', 'other sulfur containing gases, and', 'mixtures of the acid gases,, 'of an acid gas selected from the group consisting of], 'a mixture of process gas and acid gas comprising'} the mixture of process gas and acid gas', 'introduced into the absorption zone;, 'wherein percent by volume is based on the total volume of'} 'the mixture of process gas and acid gas referred to in step “a”', '(b) counter-currently contacting in the absorption zone'} [ 'and', 'absorbent chemical,'}, 'water,, 'with an'} 'are in solution prior to contact and', 'the absorbent chemical and water'} 'from the absorption zone;', '(c) removing the process gas overhead'} with the acid gas absorbed therein', 'from the bottom of the absorption zone;, '(d) removing the absorbent chemical and water solution'} 'into a regeneration zone;', '(e) introducing the solution from step “d”'} 'acid gas, absorbent chemical, and water from the solution ...

AQUEOUS ABSORBENT COMPOSITION FOR ENHANCED REMOVAL OF HYDROGEN SULFIDE FROM GASEOUS MIXTURES AND METHOD FOR USING THE SAME

The present invention relates to an aqueous alkanolamine solution for the removal of hydrogen sulfide from gaseous mixtures containing hydrogen sulfide. The aqueous alkanolamine solution comprises (i) an amino compound with the formula: 18-. (canceled)9. A process for removing hydrogen sulfide from a gaseous mixture comprising hydrogen sulfide comprising the step of: (i) 3-(dimethylamino)-1,2-propanediol,', '(ii) piperazine,', 'and', '(iii) optionally a physical solvent', 'wherein said aqueous alkanolamine solution does not contain an acid having a pKa of 8 or less or an acid-forming material capable of forming in aqueous medium an acid having a pKa of 8 or less., 'A) contacting the gaseous mixture with an aqueous alkanolamine solution wherein the aqueous alkanolamine solution consists of101. The process of claim wherein(i) the 3-(dimethylamino)-1,2-propanediol is present in an amount from 0.1 to 75 weight percent,and(ii) the piperazine is present in an amount from 0.1 to 15 weight percent,wherein weight percent is based on the total weight of the aqueous alkanolamine solution.111. The process of claim wherein the physical solvent is present in an amount from 1 to 75 weight percent based on the total weight of the aqueous alkanolamine solution.123. The process of claim wherein the physical solvent (iii) is selected from cyclotetramethylenesulfone , dimethyl ethers of polyethylene glycol , 1 ,3-dimethyl-3 ,4 ,5 ,6-tetrahydro-2(1H)-pyrimidinone , N-formylmorpholine , N-acetylmorpholine , triethylene glycol monomethyl ether , or mixtures thereof.131. The process of claim further comprising the step ofB) steam stripping the aqueous alkanolamine solution such that an acid gas-lean aqueous alkanolamine solution is formed which may be used in said contacting step.141. The process of claim wherein the temperature of the aqueous alkanolamine solution is equal to or greater than 140° F. The present invention relates to a composition comprising an aqueous solution of ...

METHOD AND APPARATUS FOR PRODUCING LIQUID HYDROCARBON FUELS

A method of converting carbon containing compounds such as coal, methane or other hydrocarbons into a liquid hydrocarbon fuel utilizes a high pressure, high temperature reactor which operates upon a blend of a carbon compound including COand a carbon source, a catalyst, and steam. Microwave power is directed into the reactor. The catalyst, preferably magnetite, will act as a heating media for the microwave power and the temperature of the reactor will rise to a level to efficiently convert the carbon and steam into hydrogen and carbon monoxide. 115-. (canceled)16. A method for simultaneously consuming carbon dioxide and generating petroleum products , the method comprising:(a) introducing particles of a catalytic material, absorbent of microwave energy, into a higher-temperature portion of a reaction vessel;(b) introducing coal particles into the higher-temperature portion of the reaction vessel;(c) introducing steam into the higher-temperature portion of the reaction vessel;(d) introducing carbon dioxide into the higher-temperature portion of the reaction vessel;(e) irradiating the higher-temperature portion of the reaction vessel with microwave energy absorbed by the catalytic material in the reactor so as to heat the catalytic material and drive an endothermic reaction of the coal and the steam, catalyzed by the catalytic material, that produces hydrogen and carbon monoxide, wherein (i) at least a portion of the hydrogen reacts with the carbon dioxide to produce water and carbon monoxide and (ii) at least a portion of the hydrogen undergoes exothermic reactions with the carbon monoxide, catalyzed by the catalytic material, to produce multiple petroleum products;(f) 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, ...

HIGH RECOVERY PROCESS FOR PURIFICATION OF MULTICOMPONENT GASES

The process of the present invention provides high recovery and low capital cost giving it an economic advantage over previously known purification processes. The present process has particular applicability to the purification of synthesis gases comprising at least hydrogen (H), carbon monoxide (CO), methane (CH), CO, and HO to obtain a gas stream including at least H, CO, and CH, that is substantially free of HO and CO. The process also has applicability to the purification of natural gases inclusive of at least CH, N, CO, and HO to produce a gas stream including at least CHand N, but which is substantially free of HO and CO. 1. A cyclic pressure swing adsorption (PSA) process for the substantial removal of HO and COcomprising: contacting a multicomponent feed gas at elevated pressure with an adsorbent bed to obtain a multicomponent product gas substantially free of HO and COwith high recovery of the product gas components , the process wherein a plurality of adsorbent beds in a PSA system are subjected to a series of process steps which include an adsorption step , three or more pressure equalization steps at decreasing pressure , a blowdown step , a purge step in which the purge gas comprises a portion of the product gas or a gas originating externally from the process that is substantially free of HO and COand comprises at least one of the major components of the product gas , three or more pressure equalization steps at increasing pressure , and a final repressurization step , wherein each of the adsorbent beds contains at least one adsorbent layer for the substantial removal of COcharacterized by:{'sub': 2', '2', '2, 'i. a COloading capacity of greater than or equal to 0.1 mol COper kg of adsorbent at a COpartial pressure of 1000 Pa at 300 K, and'}ii. a differential capacity of the product gas components of less than or equal to 0.1 mol per kg of adsorbent, where the differential capacity is defined as the difference between the loading capacity at partial ...

Gas recycle loops in process for converting municipal solid waste into ethanol

Facilities and processes for generating ethanol from municipal solid waste (MSW) in an economical way via generating a syngas, passing the syngas through a catalytic synthesis reactor, separating fuel grade ethanol, extracting energy at particular strategic points, and recycling undesired byproducts.

CATALYTICALLY ACTIVE FILTER FOR USE IN HOT GAS FILTRATION, A PROCESS FOR PREPARING THE FILTER AND A METHOD FOR SIMULTANEOUS REMOVAL OF SOLID PARTICLES AND UNDESIRED CHEMICAL COMPOUNDS FROM GAS STREAMS

A catalytically active filter for use in hot gas filtration to simultaneously remove solid particles and one or more undesirable compounds from a hot gas stream is partly or fully impregnated with a suitable catalyst. The compounds are selected from HCN, arsenic, organic sulfur compounds and carbonyls. The filter is prepared by making an impregnation liquid, which comprises a catalytically effective amount of at least one active metal and an oxide support, impregnating the filter substrate with the impregnation liquid by dipping it in the liquid or spraying it with the liquid to control the amount of liquid and drying and optionally calcining the impregnated filter. 1. A catalytically active filter for use in hot gas filtration to simultaneously remove solid particles and one or more compounds selected from hydrogen cyanide (HCN) , arsenic , organic sulfur compounds and carbonyls from a hot gas stream , said filter , which is partly or fully impregnated with a suitable catalyst , consists of two layers or zones , whereinthe outer layer or zone, facing the gas first, is inert and serves to remove the solid particles from the gas, andthe underlying layer or zone is impregnated with a catalyst-containing liquid and serves to remove one or more of said compounds from the gas.2. Catalytically active filter according to claim 1 , wherein the catalyst comprises cobalt claim 1 , molybdenum claim 1 , nickel and active alumina.3. A process for preparing a catalytically active filter for use in hot gas filtration according to claim 1 , said method comprising the steps ofproviding an appropriately shaped filter substrate having a gas inlet surface and a gas outlet surface,preparing an impregnation liquid, which comprises an effective amount of one or more catalyst metal precursors which, inherently or upon activation, are capable of catalytically removing one or more compounds selected from hydrogen cyanide (HCN), arsenic, organic sulfur compounds and carbonyls,impregnating the ...

CATALYSTS FOR OXIDATIVE SULFUR REMOVAL AND METHODS OF MAKING AND USING THEREOF

Catalysts for oxidative sulfur removal and methods of making and using thereof are described herein. The catalysts contain one or more reactive metal salts dispersed on one or more substrates. Suitable reactive metal salts include those salts containing multivariable metals having variable valence or oxidation states and having catalytic activity with sulfur compounds present in gaseous fuel streams. In some embodiments, the catalyst contains one or more compounds that function as an oxygen sponge under the reaction conditions for oxidative sulfur removal. The catalysts can be used to oxidatively remove sulfur-containing compounds from fuel streams, particularly gaseous fuel streams having high sulfur content. Due to the reduced catalyst cost, anticipated long catalyst life and reduced adsorbent consumption, the catalysts described herein are expected to provide a 20-60% reduction in annual desulfurization cost for biogas with sulfur contents ranges from 1000-5000 ppmv compared with the best adsorbent approach. 128-. (canceled)29. A method for removing sulfur-containing compounds from fluid fuel streams , the method comprising contacting the gaseous fuel stream with one or more catalysts comprising one or more substrates and one or more reactive metal salts to convert the sulfur-containing compounds to elemental sulfur , wherein the one or more reactive metal salts are selected from chlorides of transition metals having multiple oxidation states , sulfates of transition metals have multiple oxidation states , and combinations thereof , wherein the metal is in the lowest possible oxidation state.30. The method of claim 29 , wherein the method further comprises contacting the gaseous fuel stream with the one or more catalysts in the presence of an oxygen containing gas.31. The method of claim 30 , wherein the oxygen-containing gas is selected from the group consisting of oxygen claim 30 , sulfur dioxide claim 30 , air claim 30 , ozone claim 30 , hydrogen peroxide ...

GAS PURIFICATION APPARATUS AND GAS PURIFICATION METHOD

The present invention is intended to provide a gas purification apparatus and a gas purification method with an excellent thermal efficiency and capable of degrading COS at a high degradation rate. A gas purification apparatus configured to purify gas at least including COS, HO, CO, and HS includes a COS treatment device which is provided with a COS conversion catalyst and configured to treat and degrade COS in the gas by hydrolysis, and HO adjustment means configured to adjust the concentration of HO in the gas to be introduced into the COS treatment device. 110-. (canceled)11. A gas purification apparatus configured to purify gas at least including COS , HO , CO , and HS , the apparatus at least comprising:a COS treatment device comprising a COS conversion catalyst and configured to degrade COS in the gas by hydrolyzing;{'sub': 2', '2, 'HO adjustment means configured to adjust a concentration of HO in the gas to be introduced into the COS treatment device;'}a coal drying device configured to dry coal by removing moisture from the coal; anda gasification furnace configured to gasify the dried coal,{'sub': '2', 'wherein the HO adjustment means is configured to adjust the moisture content in the coal by using the coal drying device.'}13. The gas purification apparatus according to claim 11 , further comprising:at least one water washing device configured to wash the gas discharged from the COS treatment device with water; andat least one waste water treatment device configured to treat the waste water discharged from the water washing device,{'sub': '2', 'wherein the HO adjustment means is configured to mix water from the waste water treatment device with the gas to be introduced into the COS treatment device.'}14. The gas purification apparatus according to claim 11 , wherein the HO adjustment means is configured to mix steam with the gas to be introduced into the COS treatment device.15. A gas purification method for purifying gas at least including COS claim 11 , ...

CO SHIFT CATALYST, CO SHIFT REACTION APPARATUS, AND METHOD FOR PURIFYING GASIFIED GAS

A CO shift catalyst according to the present invention reforms carbon monoxide (CO) in gas. The CO shift catalyst has one of molybdenum (Mo) or iron (Fe) as a main component and has an active ingredient having one of nickel (Ni) or ruthenium (Ru) as an accessory component and one or two or more kinds of oxides from among titanium (Ti), zirconium (Zr), and cerium (Ce) for supporting the active ingredient as a support. The temperature at the time of manufacturing and firing the catalyst is equal to or higher than 550° C. 1. A CO shift catalyst which reforms carbon monoxide (CO) in gas ,has molybdenum (Mo) or iron (Fe) as a main component,has an active ingredient having nickel (Ni) or ruthenium (Ru) as an accessory component and a complex oxide including two or more kinds from among titanium (Ti), and silica (Si), for supporting the active ingredient as a support, and formed by firing them at a temperature from 550° C. to 800° C.2. The CO shift catalyst according to claim 1 ,wherein a support amount of the main component of the active ingredient is 0.1 to 25 percent by weight, and a support amount of the accessory component is 0.01 to 10 percent by weight.3. A CO shift reaction apparatus comprising the CO shift catalyst according to .4. A method for purifying gasified gas claim 1 , comprising:a step of removing smoke and dust in gasified gas obtained by a gasification furnace by a filter;a step of clarifying the gasified gas after removal of smoke and dust by a wet scrubber apparatus;a step of removing carbon dioxide and hydrogen sulfide in the gasified gas after clarification; and{'sub': '2', 'claim-ref': {'@idref': 'CLM-00001', 'claim 1'}, 'a step of obtaining purified gas by performing the CO shift reaction for converting CO in the gasified gas after removal of carbon dioxide and hydrogen sulfide into COby using the CO shift catalyst according to .'} The present invention relates to a CO shift catalyst for converting CO in gasified gas into CO, a CO shift reaction ...

Systems And Methods For Producing Substitute Natural Gas

Systems and methods for producing synthetic gas are provided. The method can include gasifying a carbonaceous feedstock in the presence of an oxidant within a gasifier to provide a raw syngas. The raw syngas can be cooled within a cooler to provide a cooled syngas. The cooled syngas can be processed within a purification system to provide a treated syngas. The purification system can include a saturator adapted to increase a moisture content of the cooled syngas. The treated syngas and a first heat transfer medium can be introduced to a methanator to provide a synthetic gas, a second heat transfer medium, and a methanation condensate. At least a portion of the methanation condensate can be recycled from the methanator to the saturator.

Coke Processing Energy Production

A method is disclosed, for producing coke in which at least a first and second source of carbonaceous materials are introduced as feedstock into a mixer. The materials are mixed into a single feedstock, and the single feedstock is analyzed to determine its coking feasibility. The single feedstock is pyrolyzed in a pyrolyzer to produce at least a coke material and a gaseous by-product. At least a portion of the gaseous by-product is used outside of the pyrolyzer. Other embodiments are also disclosed. 1. A method for producing coke comprising:introducing a first source of carbonaceous material as a first feedstock into a mixer;introducing a second source of carbonaceous material as a second feedstock into the mixer;mixing at least the first and second source carbonaceous materials into a single feedstock of carbonaceous materials;pyrolyzing said single feedstock in a pyrolyzer to produce coke material;harnessing a gas by-product from said pyrolyzing; andtreating said gas before supplying at least a portion of it to an energy provider.2. The method of wherein the first source of carbonaceous material is coal fines.3. The method of wherein the second source of carbonaceous material is coke waste fines.4. The method of wherein a third source of material is added to the mixture.5. The method of wherein said pyrolyzing the single feedstock of materials comprise the act of producing a high-grade coking material.6. The method of wherein said single feedstock is selected from the group consisting ofa particular composition;a particular reactivity;a particular shape;a particular by-product generation;a particular size;a particular strength; anda particular heating value.7. A method for producing coke comprising:mixing at least a first and a second carbonaceous material into a single feedstock of carbonaceous materials;determining coking feasibility said single feedstock of carbonaceous materials;modifying said single feedstock into a predetermined material composition; ...

METHOD FOR TREATMENT OF A HOT PYROLYSIS GAS

The present invention relates to a method for treatment of a hot gas generated by a pyrolysis or a gasification process, wherein the hot gas is passed to a first unit for particle removal and cooling, whereby subsequently, a gaseous stream is removed from a first condensed stream thus obtained and passed to a second unit for particle removal and cooling, wherein a second condensed stream is obtained, said first condensed stream and second condensed stream being recycled to said first unit and said second unit, respectively. 1. A method for treatment of a hot gas generated by a pyrolysis or a gasification process , whereinthe hot gas is passed to a first unit for particle removal and cooling, whereby subsequently, a gaseous stream is removed from a first condensed stream thus obtained and passed to a second unit for particle removal and cooling, wherein a second condensed stream is obtained, said first condensed stream and second condensed stream being recycled to said first unit and said second unit, respectively.2. The method of claim 1 , wherein said step of recycling comprises injecting in said first unit of said first condensed stream as small droplets in the stream of hot gas.3. The method of claim 1 , wherein said step of recycling comprises injecting in said second unit of said second condensed stream as small droplets in the gaseous stream originating from said first condensed stream.4. The method of claim 2 , wherein a liquid-to-gas ratio (L/G ratio) in said first unit is in a range of 10-40 claim 2 , preferably 15-30 claim 2 , even more preferably 20-25 claim 2 , said L/G ratio being expressed on mass basis (i.e. kg liquid per kg gas).5. The method of claim 3 , wherein the liquid-to-gas ratio (L/G ratio) in said second unit is in a range of 20-60 claim 3 , preferably 30-50 claim 3 , even more preferably 35-45 claim 3 , said L/G ratio being expressed on mass basis (i.e. kg liquid per kg gas).6. The method of claim 1 , wherein the effluent from said first ...

Method for Operating Fuel Gas Manufacturing Device

Provided is a method for operating a fuel gas manufacturing device for stopping the operation in such a manner that the operation can be immediately resumed, while keeping facilities from becoming complex. When stopping the operation while supply of source gas to a desulfurizing unit is stopped, after supply of source gas to the desulfurizing unit and discharge of fuel gas to the outside are stopped, a standby operation process is performed in which fuel gas is circulated by a circulation driving unit in such a manner that the whole amount of fuel gas passed through a moisture removing unit is circulated through a circulation gas path to return to the desulfurizing unit and the circulated fuel gas is heated by a heating unit to a set standby temperature to heat a reforming unit to a temperature that is equivalent to an operation temperature at which reforming is performed, and supply of water vapor is continued in a state where a supply amount of water vapor is at least an amount with which carbon deposition due to thermal decomposition of fuel gas can be prevented and is smaller than an amount that is supplied when reforming is performed.

PROCESS FOR DESULPHURIZING A GAS MIXTURE

The invention relates to a process and a device for generating a fuel gas for a gas turbine by separating off sulphur components from a gas mixture containing hydrogen, carbon monoxide, carbon dioxide and also carbonyl sulphide and/or hydrogen sulphide, which gas mixture is in this case scrubbed in a physical gas scrubber with a methanol scrubbing medium at a pressure between 30 and 80 bar(a) in order to obtain a first sulphur-free gas mixture and also a methanol scrubbing medium loaded with sulphur components and carbon dioxide, which methanol scrubbing is then regenerated, wherein a carbon dioxide-rich gas phase that contains sulphur components and is formed by pressure reduction is treated in a further gas scrubber with a methanol scrubbing medium in order to back-wash sulphur components and to generate a second sulphur-free gas mixture. 1. A process for generating a fuel gas for a gas turbine by separating off sulphur components from a gas mixture comprising hydrogen , carbon monoxide , carbon dioxide and also carbonyl sulphide and/or hydrogen sulphide , which gas mixture is in this case scrubbed in a physical gas scrubber with a methanol scrubbing medium at a pressure between 30 and 80 bar(a) in order to obtain a first sulphur-free gas mixture and also a methanol scrubbing medium loaded with sulphur components and carbon dioxide , which methanol scrubbing medium is then regenerated , wherein a carbon dioxide-rich gas phase that contains sulphur components and is formed by pressure reduction is treated in a further gas scrubber with a methanol scrubbing medium in order to back-wash sulphur components and to generate a second sulphur-free gas mixture , characterized in that the pressure of the loaded methanol scrubbing medium is reduced to a value between 2.5 and 9 bar(a) and at least a part of the second sulphur-free gas mixture is compressed and combined with the first sulphur-free gas mixture to form the fuel gas for the gas turbine.2. The process according to ...

SYSTEM AND METHOD FOR DUAL FLUIDIZED BED GASIFICATION

A method for deep desulfurization of synthesis gas comprising introducing carbonaceous material and optionally steam into a gasifier comprising a heat transfer media, extracting a first heat transfer stream comprising heat transfer media and optionally unconverted carbonaceous material from the gasifier, and introducing at least a portion of the first heat transfer stream into a combustor, introducing oxidant and optionally a fuel into the combustor, extracting a second heat transfer stream comprising heat transfer media from the combustor, and introducing at least a portion of the second heat transfer stream into the gasifier, introducing a compound capable of reacting with sulfur to produce sulfate, sulfide or both, extracting a purge stream comprising ash, sulfate, halide, or a combination thereof from the second heat transfer stream, extracting a flue gas from the combustor, and extracting a gasifier product synthesis gas stream comprising less than 1000 ppm sulfur from the gasifier. 1. A method for deep desulfurization of synthesis gas , the method comprising: introducing a carbonaceous material and optionally steam into a fluid bed gasifier comprising a heat transfer media;', 'extracting a first heat transfer stream comprising heat transfer media and optionally unconverted carbonaceous material from the fluid bed gasifier, and introducing at least a portion of the first heat transfer stream into a fluid bed combustor, wherein the first heat transfer stream has a first temperature;', 'introducing oxidant and optionally a fuel into the fluid bed combustor, whereby unconverted carbonaceous material in the first heat transfer stream, fuel, or both is combusted and the temperature of the heat transfer media is raised;', 'extracting a second heat transfer stream comprising heat transfer media and having a second temperature from the fluid bed combustor, and introducing at least a portion of the second heat transfer stream into the fluid bed gasifier, wherein the ...

Two-stage syngas production with separate char and product gas inputs into the second stage

A two-stage syngas production method to produce a final product gas from a carbonaceous material includes producing a first product gas in a first reactor, separating char from the first product gas to produce separated char and char-depleted product gas, and separately reacting the separated char and the char-depleted product gas with an oxygen-containing gas in a second reactor to produce a final product gas. The separated char is introduced into the second reactor above the char-depleted product gas. The solids separation device may include serially connected cyclones, and the separated char may be entrained in a motive fluid in an eductor to produce a char and motive fluid mixture prior to being transferred to the second reactor. A biorefinery method produces a purified product from the final product gas.

Catalyst for hydrolysis of carbonyl sulfide and method of producing same

A catalyst for COS hydrolysis includes titanium dioxide and a barium compound supported on the titanium dioxide. The catalyst, when expressing Ba and S in the catalyst in terms of BaO and SO 3 , respectively, has a molar ratio of SO 3 to BaO of at least 1. The catalyst converts COS and H 2 O in a raw material gas to CO 2 and H 2 S.

REFORMED GAS AS FUEL FOR PRIMARY REFORMER DURING STARTUP

The present invention provides a method and apparatus for recovery of reformed gas produced in a methanol plant during startup. In one aspect, the method for recovery of a reformed gas produced in a methanol plant during startup comprising: a) decreasing the temperature of the methanol plant reformed gas comprising (1) water in an amount no greater than 2.5 wt %, based on the total weight of the reformed gas, (2) methane in an amount that ranges from 1 wt % to 8 wt %, based on the total weight of the reformed gas, (3) hydrogen, (4) nitrogen, (5) carbon dioxide, and (6) carbon monoxide, to remove at least some of the water from the reformed gas; and b) using the water removed reformed gas as fuel in a steam reformer. 1. A method for recovery of a reformed gas produced in a methanol plant during startup comprising:a) decreasing the temperature of the methanol plant reformed gas comprising (1) water in an amount no greater than 2.5 wt %, based on the total weight of the reformed gas, (2) methane in an amount that ranges from 1 wt % to 8 wt %, based on the total weight of the reformed gas, (3) hydrogen, (4) nitrogen, (5) carbon dioxide, and (6) carbon monoxide, to remove at least some of the water from the reformed gas; andb) using the water removed reformed gas as fuel in a steam reformer.2. The method of claim 1 , wherein the reformed gas comprises hydrogen is present in an amount ranging from 50 wt % to 92.9 wt % hydrogen based on the total weight of the reformed gas; water is present in an amount ranging from 0 wt % to 2.5 wt % based on the total weight of the reformed gas; nitrogen is present in an amount ranging from 0.1 wt % to 5 wt % based on the total weight of the reformed gas; carbon monoxide is present in an amount ranging from 5 wt % to 20 wt % based on the total weight of the reformed gas; carbon dioxide is present in an amount ranging from 1 wt % to 15 wt % based on the total weight of the reformed gas; and methane is present in an amount ranging from 1 ...

MULTISTAGE THERMOLYSIS METHOD FOR SAFE AND EFFICIENT CONVERSION OF E-WASTE MATERIALS

Clean, safe and efficient methods, systems, and processes for utilizing thermolysis methods to processes to convert various e-waste sources into Clean Fuel Gas and Char source are disclosed. The invention processes e-waste sources, such as for example whole circuit boards, to effectively shred and/or grind the waste source, and then process using thermolysis methods to destroy and/or separate halogen and other dangerous components to provide a Clean Fuel Gas and Char source, along with the ability to recover precious metals and other valuable components from the Char. 1. A method for converting an electric and/or electronic waste source to a Clean Fuel Gas and Char source comprising:inputting an electric and electronic waste source into a thermolysis system to generate a Clean Fuel Gas source and Char source;wherein the thermolysis system comprises at least two reactors, an oil/water separator, an oil/tar cracker, and at least two gas scrubbers;wherein the reactors have a process temperature of about 300° C.-800° C. and generate tars and oils;wherein all of the oils and tars are separated in the oil/water separator and at least two gas scrubbers, thereafter cracked in the oil/tar cracker, and send back to the secondary reactor to generate the Clean Fuel Gas source; andwherein the Clean Fuel Gas source and Char source are substantially-free of halogenated organic compounds and do not contain oils and/or tars.2. The method of claim 1 , wherein the electric and electronic waste source comprises printed wiring boards claim 1 , thermoplastic materials claim 1 , flat panel displays claim 1 , printer cartridges and/or cassette claim 1 , or combinations thereof.3. The method of claim 1 , wherein the reactors have a process temperature of about 400° C.-800° C. for the waste source to undergo at least partial gasification.4. (canceled)5. The method of claim 1 , wherein the reactors have a pressure range from about 10 to about 100 millbar.6. The method of claim 1 , wherein the ...

Processes For Producing High Biogenic Concentration Fischer-Tropsch Liquids Derived From Municipal Solid Wastes (MSW) Feedstocks

Processes for producing high biogenic concentration Fischer-Tropsch liquids derived from the organic fraction of municipal solid wastes (MSW) feedstock that contains a relatively high concentration of biogenic carbon (derived from plants) and a relatively low concentration of non-biogenic carbon (derived from fossil sources) wherein the biogenic content of the Fischer-Tropsch liquids is the same as the biogenic content of the feedstock. 1. A transportation fuel or fuel additive derived from biogenic carbon materials , the fuel derived from a process comprising the steps of:a) in a feedstock processing step, removing non-biogenic derived carbon materials and non-carbonaceous materials from municipal solid waste that contain materials that are produced from plant derived carbon (biogenic) as well as non-biogenic derived carbon (fossil based) materials, to produce a feedstock that contains a relatively high concentration of biogenic carbon and a relatively low concentration of non-biogenic carbons along with other non-carbonaceous materials from the municipal solid waste; andb) converting the processed feedstock into Fischer-Tropsch liquids in a bio-refinery while maintaining the relatively high concentration of biogenic carbon and the relatively low concentration of non-biogenic carbon along with other non-carbonaceous materials from the municipal solid waste; andc) upgrading the Fischer-Tropsch liquids into a transportation fuel or fuel additive.2. The transportation fuel or additive derived by the process according to wherein the feedstock processing step includes at least two processing steps.3. The transportation fuel or additive derived by the process according to wherein claim 1 , in the feedstock processing step claim 1 , more than about 10% of the non-biogenic derived carbon materials are purposefully removed from the municipal solid waste.4. The transportation fuel or additive derived by the process according to wherein claim 1 , in the feedstock processing ...

HIGH TAR CONVERSION PERFORMANCE OF A Nl-FE-MGO CATALYST

Disclosed herein, inter alia, are novel nickel-iron-magnesium oxide catalyst compositions and methods of making and using the same. 1. A catalyst comprising nickel (Ni) , iron (Fe) , and magnesium oxide (MgO) , wherein the catalyst comprises about 30 to 60 wt % Ni , about 10 to 30 wt % Fe , and about 20 to 50 wt % MgO.2. The catalyst of claim 1 , wherein the weight ratio is about 40 to 50 wt % Ni claim 1 , 15 to 25 wt % Fe claim 1 , and 30 to 40 wt % MgO.3. The catalyst of claim 1 , wherein the weight ratio is about 45 wt % Ni claim 1 , 20 wt % Fe claim 1 , and 35 wt % MgO.4. The catalyst of claim 1 , wherein the catalyst further comprises a substrate support.5. The catalyst of claim 4 , wherein the substrate support comprises one or more of the ceramic claim 4 , olivine claim 4 , dolomite claim 4 , calcium carbonate claim 4 , aluminum oxide claim 4 , silicon dioxide claim 4 , titanium dioxide claim 4 , and iron oxide.6. The catalyst of claim 4 , wherein the substrate support comprises aluminum oxide claim 4 , silicon dioxide claim 4 , titanium dioxide claim 4 , and iron oxide.7. The catalyst of claim 4 , wherein the catalyst to substrate support weight ratio is 0.5-5.0%.8. The catalyst of claim 4 , wherein the catalyst to substrate support weight ratio is 0.75-1.15%.9. The catalyst of claim 1 , wherein the substrate support is spherical and about 400 to about 600 μm in diameter.10. The catalyst of claim 1 , wherein the catalyst has a honeycomb structure.11. A method of making a nickel-iron-magnesium oxide catalyst claim 1 , said method comprising:(a) mixing nickel nitrate, iron nitrate, and magnesium nitrate in a solvent;(b) combining the solution of step (a) with a substrate support to form a mixture;{'sub': 1', '1, '(c) maintaining the mixture of step (b) at a first temperature (T) for a first duration of time (t);'}{'sub': 2', '2', '2', '1, '(d) increasing the temperature of the mixture in step (c) to a second temperature (T) and maintaining Tfor a second ...

FUELS AND FUEL ADDITIVES THAT HAVE HIGH BIOGENIC CONTENT DERIVED FROM RENEWABLE ORGANIC FEEDSTOCK

Fuel and fuel additives can be produced by processes that provide Fischer-Tropsch liquids having high biogenic carbon concentrations of up to about 100% biogenic carbon. The fuels and fuel additive have essentially the same high biogenic concentration as the Fischer-Tropsch liquids which, in turn, contain the same concentration of biogenic carbon as the feedstock. 1. A high biogenic content fuel derived from renewable organic feedstock sources comprising:At least one of Synthetic Paraffinic Kerosene (SPK) and diesel derived from Fischer-Tropsch liquids and having substantially the same high biogenic concentration as the Fischer-Tropsch liquids and having substantially the same high biogenic concentration as the renewable organic feedstock to the Fischer-Tropsch process that creates the Fischer-Tropsch liquids, wherein the high biogenic concentration is up to 100% biogenic carbons in both the feedstock and the FT liquids, as confirmable by radiocarbon dating and as opposed to non-biogenic carbons derived from fossil sources of carbon.3. A high biogenic content fuel derived from renewable organic feedstock , the high biogenic content fuel comprising:at least one of naphtha, diesel fuel and Synthetic Paraffinic Kerosene (SPK) derived from Fischer-Tropsch liquids and having substantially the same high biogenic concentration as the Fischer-Tropsch liquids and having substantially the same high biogenic renewable organic concentration as the feedstock to the Fischer-Tropsch process that creates the Fischer-Tropsch liquids, wherein the high biogenic concentration is up to 100% biogenic carbons in both the feedstock and the FT liquids, as confirmable by radiocarbon dating and as opposed to non-biogenic carbons derived from fossil sources of carbons.5. A high biogenic content fuel derived from renewable organic feedstock sources according to wherein the high biogenic concentration is the same percentage biogenic carbon in both the feedstock and the FT liquids.6. A high ...

METHODS AND APPARATUS FOR RECYCLING TAIL GAS IN SYNGAS FERMENTATION TO ETHANOL

The invention present provides a method (and suitable apparatus) to convert biomass to ethanol, comprising gasifying the biomass to produce raw syngas; feeding the raw syngas to an acid-gas removal unit to remove at least some COand produce a conditioned syngas stream; feeding the conditioned syngas stream to a fermentor to biologically convert the syngas to ethanol; capturing a tail gas from an exit of the fermentor, wherein the tail gas comprises at least COand unconverted CO or H; and recycling a first portion of the tail gas to the fermentor and/or a second portion of the tail gas to the acid-gas removal unit. This invention allows for increased syngas conversion to ethanol, improved process efficiency, and better overall biorefinery economics for conversion of biomass to ethanol. 1. A method of converting a carbonaceous feedstock to a syngas-fermentation product , said method comprising:{'sub': ['2', '2;'], '#text': '(a) introducing a carbonaceous feedstock and an oxidant to a gasifier, under suitable gasification conditions to produce a raw syngas stream comprising CO, H, and CO'}(b) optionally feeding at least a portion of said raw syngas stream to a syngas-cleanup unit, to produce an intermediate syngas stream;{'sub': '2', '#text': '(c) feeding at least a portion of said raw syngas stream and/or at least a portion of said intermediate syngas stream, if present, to an acid-gas removal unit, to remove at least some of said COand produce a conditioned syngas stream;'}{'sub': ['2', '2', '2', '2'], '#text': '(d) feeding at least a portion of said conditioned syngas stream to a fermentor, under suitable fermentation conditions and in the presence of suitable microorganisms and nutrients to biologically convert one or more of CO, H, or COto a fermentation product and generate a product stream comprising at least the fermentation product and a tail gas stream comprising at least COand unconverted CO or H;'}(e) recycling at least a first portion of the tail gas to ...

Feedstock Processing Systems And Methods For Producing Fischer-Tropsch Liquids And Transportation Fuels

A method for processing feedstock is described, characterized in that incoming feedstock is processed to selectively recover biogenic carbon material from the incoming feedstock. In some embodiments the incoming feedstock is comprised of mixed solid waste, such as municipal solid waste (MSW). In other embodiments the incoming feedstock is comprised of woody biomass. In some instances, the incoming feedstock is processed to selectively recover biogenic carbon material from the incoming feedstock to produce a processed feedstock having biogenic carbon content of 50% and greater suitable for conversion into biogenic carbon Fischer Tropsch liquids. The high biogenic carbon Fischer Tropsch liquids may be upgraded to biogenic carbon liquid fuels. Alternatively, the incoming feedstock is processed to selectively recover plastic material from the incoming feedstock to produce a processed feedstock having biogenic carbon content of 50% or less. 1. A method for processing feedstock , characterized in that incoming feedstock is processed to selectively recover biogenic carbon material from the incoming feedstock.2. The method of claim 1 , wherein the incoming feedstock is comprised of mixed solid waste.3. The method of claim 1 , wherein in the incoming feedstock is comprised of woody biomass.4. The method of claim 1 , wherein the mixed solid waste is municipal solid waste (MSW).5. The method of claim 2 , wherein the mixed solid waste is comprised of wet organic waste claim 2 , dry organic waste and inorganic waste that is comingled.6. The method of claim 1 , wherein the incoming feedstock is processed to selectively recover biogenic carbon material from the incoming feedstock to produce a processed feedstock having biogenic carbon content of 50% and greater suitable for conversion into biogenic carbon Fischer Tropsch liquids.7. The method of claim 6 , wherein the high biogenic carbon Fischer Tropsch liquids are upgraded to biogenic carbon liquid fuels.8. The method of claim 5 ...

System and Method for Dual Fluidized Bed Gasification

A system, for production of high-quality syngas, comprising a first dual fluidized bed loop having a fluid bed conditioner operable to produce high quality syngas comprising a first percentage of components other than CO and Hfrom a gas feed, wherein the conditioner comprises an outlet for a first catalytic heat transfer stream comprising a catalytic heat transfer material and having a first temperature, and an inlet for a second catalytic heat transfer stream comprising catalytic heat transfer material and having a second temperature greater than the first temperature; a fluid bed combustor operable to combust fuel and oxidant, wherein the fluid bed combustor comprises an inlet connected with the outlet for a first catalytic heat transfer stream of the conditioner, and an outlet connected with the inlet for a second catalytic heat transfer stream of the conditioner; and a catalytic heat transfer material. 1. A method for continuous dry reforming , the method comprising:introducing a feed comprising carbon dioxide and at least one selected from methane and propane into a fluid bed conditioner operated at a conditioning temperature, wherein the fluid bed conditioner is one fluid bed of a dual fluidized bed loop and is configured to convert at least a portion of said feed into synthesis gas components;extracting a first catalytic heat transfer stream comprising a catalytic heat transfer material and having a first temperature from the fluid bed conditioner and introducing at least a portion of the first catalytic heat transfer stream and a flue gas into a fluid bed combustor, wherein the fluid bed combustor is configured to regenerate the catalyst via combustion;extracting a second catalytic heat transfer stream comprising catalytic heat transfer material and having a second temperature from the fluid bed combustor and introducing at least a portion of the second catalytic heat transfer stream into the fluid bed conditioner; andextracting synthesis gas from the fluid ...

MULTISTAGE THERMOLYSIS METHOD FOR SAFE AND EFFICIENT CONVERSION OF E-WASTE MATERIALS

Clean, safe and efficient methods, systems, and processes for utilizing thermolysis methods to processes to convert various e-waste sources into Clean Fuel Gas and Char source are disclosed. The invention processes e-waste sources, such as for example whole circuit boards, to effectively shred and/or grind the waste source, and then process using thermolysis methods to destroy and/or separate halogen and other dangerous components to provide a Clean Fuel Gas and Char source, along with the ability to recover precious metals and other valuable components from the Char. 1. A method for converting an electric and/or electronic waste source to a Clean Fuel Gas and Char source comprising:inputting an electric and electronic waste source into a thermolysis system;undergoing a depolymerization and a cracking reaction of hydrocarbons in the waste source;destroying and/or removing toxic compounds present in the waste sources; andgenerating the Clean Fuel Gas and Char source,wherein the Clean Fuel Gas source is used for power to a system or application;wherein the Char source contains recoverable metals; andwherein the Clean Fuel Gas and Char source are substantially-free of halogenated organic compounds.2. The method of claim 1 , wherein the electric and electronic waste source is an e-waste source selected from the group consisting of printed wiring boards claim 1 , thermoplastic materials claim 1 , flat panel displays claim 1 , printer cartridges and/or cassettes claim 1 , and combinations thereof3. The method of claim 1 , wherein the thermolysis system comprises at least one reactor with a process temperature of from about 300° C.-800° C. for the waste source to undergo at least partial gasification.4. The method of claim 1 , wherein the thermolysis system provides indirect heat in a system that is free of oxygen.5. The method of claim 1 , wherein the thermolysis system has a pressure range from about 10 to about 100 millbar.6. The method of claim 1 , wherein the waste ...

PROCESS AND PLANT FOR SEPARATION OF CONCOMITANTS FROM A RAW SYNTHESIS GAS STREAM AND FOR PRODUCING A SULFUR-FREE BY-PRODUCT

The invention relates to a process and a plant for staged separation of concomitants from a raw synthesis gas stream to produce synthesis gas and a sulfur-free naphtha product as a by-product, To remove naphtha compounds and sulfur-containing concomitants, raw synthesis gas is treated with a scrubbing medium in a prescrubbing stage and withdrawn from the prescrubbing stage, and the laden scrubbing medium is mixed with water to bring about a phase separation into a scrubbing medium-water mixture and naphtha, wherein sulfur-containing concomitants are in solution in naphtha. To remove the sulfur-containing concomitants the naphtha is heated to obtain sulfur-free naphtha as a by-product of the gas scrubbing. 1. Process for staged separation of concomitants from a raw synthesis gas stream to produce synthesis gas by absorption of the concomitants in a physical scrubbing medium run in countercurrent to the raw synthesis gas stream in a plurality of scrubbing stages at elevated pressure , wherein the concomitants comprise at least carbon dioxide (CO) , one or more sulfur compounds of a first type , one or more sulfur compounds of a second type and naphtha , wherein the process comprises the following steps:a) absorbing at least naphtha and sulfur compounds of the first type in a prescrubbing stage to afford a scrubbing medium fraction laden at least with naphtha and sulfur compounds of the first type;b) mixing the laden scrubbing medium fraction obtained in step a) with water to effect a phase separation into two liquid phases, wherein a first liquid phase comprises water and scrubbing medium and a second liquid phase comprises naphtha and sulfur compounds of the first type dissolved therein;c) heating the second liquid phase obtained in step b) to remove the sulfur compounds of the first type and obtain sulfur-free naphtha;d) absorbing carbon dioxide and sulfur compounds of the second type in at least one main scrubbing stage arranged downstream of the prescrubbing stage ...

Hybrid plant for liquid fuel production

A hybrid plant and method for producing liquid fuel product from hydrogen and carbon monoxide containing streams produced by gasifying solid carbonaceous feedstock and steam reforming of light fossil fuels. When a gasification unit in the hybrid plant is operating at reduced capacity or is not operational, oxygen that would have been used in the gasification unit is diverted to a light fossil fuel conversion unit containing an autothermal reformer to increase H 2 -rich syngas flow to a liquid fuel production unit and maintain liquid fuel production at near nameplate capacity.

MULTISTAGE THERMOLYSIS METHOD FOR SAFE AND EFFICIENT CONVERSION OF CARPET/RUG, POLYMERIC MATERIALS AND OTHER WASTE SOURCES

Clean, safe and efficient methods, systems, and processes for utilizing thermolysis methods to processes to convert various carpet, rug, polymeric materials and other waste sources, such as solid waste, tires, manure, auto shredder residue, glass and carbon fiber composite materials, municipal solid wastes, medical wastes, waste wood and the like into a Clean Fuel Gas and Char source are disclosed. The invention processes the carpet, rug, polymeric material to effectively shred and/or grind the waste source, such as post-consumer carpet remnants and waste, and then process using thermolysis methods to destroy and/or separate halogen and other dangerous components to provide a Clean Fuel Gas and Char source. Additional waste sources, such as solid waste, tires, manure, auto shredder residue, glass and carbon fiber composite materials, municipal solid wastes, medical wastes, waste wood and the like, are suitable for the processing of the invention disclosed. 121-. (canceled)22: A method for converting a composite waste source to a Clean Fuel Gas source and Char source comprising:inputting a waste source into a thermolysis system; wherein the thermolysis system comprises at least two reactors, at least two gas scrubbers, an oil/water separator, and an oil/tar cracker;destroying and/or removing toxic compounds present in the waste source; andgenerating the Clean Fuel Gas and Char source,wherein the reactors have a process temperature of about 300° C.-800° C. and generate tars and oils;wherein all of the oils and tars are separated from the Clean Fuel Gas source in the at least two gas scrubbers, thereafter cracked in the oil/tar cracker, and sent back to the secondary reactor to generate more of the Clean Fuel Gas source;wherein the Clean Fuel Gas source and Char source are substantially-free of halogenated organic compounds and do not contain oils and/or tars.23: The method of claim 22 , wherein the composite waste source comprises glass composite claim 22 , carbon ...

Methods, Systems, And Apparatuses For Utilizing A Fischer-Tropsch Purge Stream

Systems, apparatuses and methods of utilizing a Fischer-Tropsch (“FT”) tail gas purge stream for recycling are disclosed. One or more methods include removing an FT tail gas purge stream from an FT tail gas produced by an FT reactor, treating the FT tail gas purge stream with steam in a water gas shift (“WGS”) reactor, having a WGS catalyst, to produce a shifted FT purge stream including carbon dioxide and hydrogen, and removing at least a portion of the carbon dioxide from the shifted FT purge stream, producing a carbon dioxide stream and a treated purge stream. Other embodiments are also disclosed. 1. A system for producing Fischer Tropsch (“FT”) hydrocarbons , the system comprising:a. a syngas preparation unit configured to produce a syngas comprising hydrogen and carbon monoxide from a carbonaceous feedstock, wherein the syngas preparation unit is a steam methane reformer;b. a syngas conditioning unit, fluidly connected to an output of the syngas preparation unit, configured to condition the syngas to remove a process condensate stream from the syngas and produce a conditioned syngas;c. an FT reactor, fluidly connected to an output of the syngas conditioning unit, and having an FT catalyst, configured to operate under FT conditions to receive the conditioned syngas as an input and to make FT liquid hydrocarbons, with an FT tail gas and an FT water stream as by-products;d. an FT tail gas flowline to transport the FT tail gas from the FT reactor to the syngas preparation unit for use as a feed;e. a diverting line configured to remove an FT tail gas purge stream, comprising a portion of the FT tail gas, from the FT tail gas in the FT tail gas flowline;f. a water gas shift (“WGS”) reactor fluidly connected to the diverting line to receive the FT tail gas purge stream, and having a water gas shift catalyst positioned therein, configured to convert carbon monoxide and water in the FT purge stream exposed to the water gas shift catalyst under WGS conditions at least in ...

SYSTEM AND METHOD FOR POWER PRODUCTION USING PARTIAL OXIDATION

The present disclosure relates to a power production system that is adapted to achieve high efficiency power production using partial oxidation of a solid or liquid fuel to form a partially oxidized stream that comprises a fuel gas. This fuel gas stream can be one or more of quenched, filtered, and cooled before being directed to a combustor of a power production system as the combustion fuel. The partially oxidized stream is combined with a compressed recycle COstream and oxygen. The combustion stream is expanded across a turbine to produce power and passed through a recuperator heat exchanger. The expanded and cooled exhaust stream can be further processed to provide the recycle COstream, which is compressed and passed through one or more recuperator heat exchangers in a manner useful to provide increased efficiency to the combined systems. 1. A process for the production of power using a combination of a partial oxidation (POX) system and a power production system (PPS) , the process comprising:combining a solid or liquid fuel and oxygen in a POX reactor under conditions sufficient to partially oxidize the fuel and form a POX stream comprising a fuel gas at a first temperature;removing from the POX stream comprising the fuel gas at least a portion of any solid components or gaseous components that do not form part of the fuel gas;cooling the POX stream comprising the fuel gas in a POX heat exchanger to a second, lower temperature;purifying the POX stream comprising the fuel gas by removing at least a portion of any liquid water and acid gases therefrom and thus forming a stream of the fuel gas;compressing the stream of the fuel gas to a pressure of about 12 MPa or greater;combusting the stream of the fuel gas in a PPS combustor to form a combustion product stream at a pressure of at least about 10 MPa and a temperature of at least about 800° C.;expanding the combustion product stream across a PPS turbine to generate power and form an expanded PPS combustion ...

Integrated biorefinery for production of liquid fuels

A system including a mixing apparatus configured to produce a reformer feedstock and comprising one or more cylindrical vessel having a conical bottom section, an inlet for superheated steam within the conical bottom section and an inlet for at least one carbonaceous material at or near the top of the cylindrical vessel, wherein the one or more cylindrical vessel is a pressure vessel configured for operation at a pressure in the range of from about 5 psig (34.5 kPa) to about 50 psig (344.7 kPa); a reformer configured to produce, from the reformer feedstock, a reformer product comprising synthesis gas, and also producing a hot flue gas; a synthesis gas conversion apparatus configured to catalytically convert at least a portion of the synthesis gas in the reformer product into synthesis gas conversion product, and to separate, from the synthesis gas conversion product, a spent catalyst stream and a tailgas.

NOVEL BETA-HYDROXYLATED TERTIARY DIAMINES, A PROCESS FOR THEIR SYNTHESIS AND THEIR USE FOR ELIMINATING ACID COMPOUNDS A GASEOUS EFFLUENT

The invention relates to novel nitrogen compounds belonging to the family of tertiary diamines of general formula (I) below, wherein R is an alkanediyl radical —(CH)n- with n=2, 3, 4, 5 or 6. 4. A synthesis method of a nitrogen compound as claimed in claim 1 , comprising the following reactions:a first reaction of epoxidation of an alpha-omega-diene to achieve epoxidation of each one of the alkene functions of the alpha-omega-diene to oxirane functions so as to produce a diepoxyalkane,{'claim-ref': {'@idref': 'CLM-00001', 'claim 1'}, 'a second reaction of addition of two moles of dimethylamine and one molecule of the diepoxyalkane so as to produce the nitrogen compound as claimed in .'}5. A method as claimed in claim 4 , wherein:the first reaction is an epoxidation reaction of 1,5-hexadiene to produce 1,2,5,6-diepoxyhexane,the second reaction is an addition reaction of two moles of dimethylamine and one molecule of 1,2,5,6-diepoxyhexane to produce N,N,N′,N′-(tetramethyl)-1,6-diamino-2,5-hexanediol.6. A method as claimed in claim 4 , wherein:the first reaction is an epoxidation reaction of 1,7-octadiene to produce 1,2,7,8-diepoxyoctane,the second reaction is an addition reaction of two moles of dimethylamine and one molecule of 1,2,7,8-diepoxyoctane to produce N,N,N′,N′-(tetramethyl)-1,8-diamino-2,7-octanediol.7. A method as claimed in claim 4 , wherein the first epoxidation reaction consists in reacting the alpha-omega-diene with a peracid or a peroxide or a hydroperoxide or oxygen associated with a suitable catalytic system claim 4 , and said peracid can be generated in situ by reaction between a carboxylic acid and a hydrogen peroxide.8. A method as claimed in claim 4 , wherein the second addition reaction is carried out in the presence of excess dimethylamine.9. A method as claimed in claim 4 , wherein the first epoxidation reaction and the second addition reaction are carried out in two successive stages.10. A method of removing acid compounds contained in a ...

A process and relating apparatus to make pure hydrogen from a syngas originated from wastes gasification

A raw syngas coming from HT gasification of organic wastes, once cooled in a proper heat recovery boiler or in a quencher is treated in a scrubbing section where, by adding an acidic solution followed by alkaline solution and by a WESP, particulate and chlorine compounds are removed and the syngas is ready for conversion, after its compression. In the conversion step CO is converted into C02 and H2 by adding steam; H2S is reduced to sulphur in a solid form, C02 is removed via cryogenic unit or an amine unit and pure H2 is produced.

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.

PLANT AND METHOD FOR GENERATION OF SYNTHESIS GAS

Method and plant for generation of synthesis gas, comprising the steps of air fractionation to give oxygen, nitrogen and tail gas, gasification of a hydrocarbonaceous fuel to give crude synthesis gas and cleaning of the crude synthesis gas by removal of acid gas by means of cryogenic absorption, wherein the absorbent is cooled by means of a compression coolant circuit and the cooling water used is cooled by evaporative cooling by means of the tail gas obtained in the air fractionation. 13-. (canceled)4. A method of generating a synthesis gas which consists essentially of carbon monoxide and hydrogen and has been purified of acid gases , proceeding from a hydrocarbonaceous fuel , and also air and steam , the method comprising the steps of:a) fractionating air by low-temperature rectification to give an oxygen stream, a tail gas stream and a nitrogen stream, wherein the tail gas stream and the nitrogen stream are at ambient temperature and the nitrogen stream is at elevated pressure;b) converting a hydrocarbonaceous fuel at elevated pressure and elevated temperature with the oxygen stream generated in step a) and the steam to a synthesis gas;c) removing the acid gases from the synthesis gas generated in step b) by low-temperature absorption in an absorption column with a liquid absorbent;d) cooling the absorbent used in step c) to the low temperature needed for the low-temperature absorption by means of a compression refrigeration plant, wherein the compression refrigeration plant comprises a coolant circuit in which the coolant is compressed and hence heated and is cooled and condensed by subsequent heat exchange with cooling water; ande) cooling the cooling water before it exchanges heat with the coolant in step d) by evaporative cooling,wherein the evaporative cooling in step e) is conducted with the tail gas stream generated in step a) and/or, after the tail gas stream has been expanded, with the nitrogen stream generated in step a).5. Method according to claim 4 ...

METHOD AND DEVICE FOR FISCHER-TROPSCH SYNTHESIS

A method for Fischer-Tropsch synthesis, the method including: 1) gasifying a raw material to obtain a crude syngas including H, CO and CO; 2) electrolyzing a saturated NaCl solution using a chloralkali process to obtain a NaOH solution, Hand H; 3) removing the COin the crude syngas using the NaOH solution obtained in 2) to obtain a pure syngas; and 4) insufflating the Hobtained in 2) to the pure syngas to adjust a mole ratio of CO/Hin the pure syngas, and then introducing the pure syngas for Fischer-Tropsch synthesis reaction. A device for Fischer-Tropsch synthesis includes a gasification device, an electrolyzer, a first gas washing device, and a Fischer-Tropsch synthesis reactor. 1. A method for Fischer-Tropsch synthesis , the method comprising:{'sub': 2', '2, '1) gasifying a raw material to obtain a crude syngas comprising H, CO and CO;'}{'sub': 2', '2, '2) electrolyzing a saturated NaCl solution using a chloralkali process to obtain a NaOH solution, Cland H;'}{'sub': '2', '3) removing the COin the crude syngas using the NaOH solution obtained in 2) to obtain a pure syngas; and'}{'sub': 2', '2, '4) insufflating the Hobtained in 2) into the pure syngas to adjust a mole ratio of CO/Hin the pure syngas, and then using the pure syngas for Fischer-Tropsch synthesis reaction.'}2. The method of claim 1 , wherein in 3) claim 1 , the COin the crude syngas is removed through a direct gas-liquid contact between the NaOH solution and the crude syngas to yield the pure syngas.3. The method of claim 1 , wherein in 3) claim 1 , the COis first separated from the crude syngas to yield the pure syngas claim 1 , and then the COis absorbed using the NaOH solution.4. The method of claim 1 , wherein in 3) claim 1 , a remaining of the NaOH solution after absorbing COin the crude syngas is condensed and crystallized as a by-product.5. The method of claim 1 , wherein in 3) claim 1 , a remaining of the NaOH solution after absorbing COin the crude syngas is used for removing COin an ...

AMINO-SILOXANE COMPOSITION AND METHODS OF USING THE SAME

An amino-siloxane composition is presented. The amino-siloxane composition includes structure (I): 5. The amino-siloxane composition according to claim 1 , wherein X comprises an RO— group; a RS group; an (R)N— group; or a morpholine group claim 1 , wherein Ris independently at each occurrence a C-Caliphatic radical.6. The amino-siloxane composition according to claim 1 , wherein X comprises a CHO— group; a CHO— group; a (CH)N— group; a (CH)N— group claim 1 , or a morpholine group.7. A reaction product of the amino-siloxane composition of with carbon dioxide.12. The method according to claim 8 , wherein X comprises a RO— group; a (R)N— group; a RS group; or a morpholine group claim 8 , wherein Ris independently at each occurrence a C-Caliphatic radical.13. The method according to claim 8 , wherein X comprises a CHO— group; a CHO— group; a (CH)N— group; a (CH)N— group claim 8 , or a morpholine group.14. The method according to claim 8 , wherein the carbon dioxide absorbent composition is substantially free of a co-solvent.15. The method according to claim 8 , further comprising forming a reaction product of the amino-siloxane with carbon dioxide claim 8 , wherein the reaction product is substantially liquid at room temperature.16. The method according to claim 8 , wherein the process stream is generated from at least one of a combustion process claim 8 , a gasification process claim 8 , a landfill claim 8 , a furnace claim 8 , a steam generator claim 8 , and a boiler.17. The method according to claim 8 , wherein the process stream is generated from processing of a fuel.18. The method according to claim 17 , wherein the fuel comprises coal.19. The method according to claim 8 , wherein the process stream comprises syn-gas. This invention was made with Government support under grant number DE-AR-0000084 awarded by the Department of Energy. The Government has certain rights in the invention.Power generating processes that are based on combustion of carbon containing fuel ...

LOW TEMPERATURE SULFUR TOLERANT TAR AND SULFUR REMOVAL WITH CONCOMITANT SYNTHESIS GAS CONDITIONING

A catalyst comprising of NiO; AlO; and ZnO. The catalyst is capable of greater than 5% sulfur removal from a synthesis gas at a temperature range from 300° C. to 600° C. 2. (canceled)3. (canceled)4. (canceled)5. (canceled)6. (canceled)7. The catalyst of claim 1 , wherein the catalyst is capable of removal of tar is greater than 55% tar conversion at 350° C.8. The catalyst of claim 1 , wherein NiO is present from 1 to 10 wt %.9. The catalyst of claim 1 , wherein the catalyst is capable of sulfur removal from the synthesis gas at greater than 10%.10. (canceled)1220.-. (canceled)21. The catalyst of claim 1 , wherein the catalyst comprises 0.5 to 15 wt % ZnO.22. The catalyst of claim 11 , wherein the catalyst comprises 0.5 to 15 wt % ZnO.23. The catalyst of claim 1 , wherein the catalyst comprises 7.5 to 12.5 wt % NiO and 7.5 to 12.5 wt % ZnO.23. The catalyst of claim 11 , wherein the catalyst comprises 7.5 to 12.5 wt % NiO and 7.5 to 12.5 wt % ZnO.24. The catalyst of claim 1 , wherein the catalyst is configured to be used in a circulating fluidized bed reactor.25. The catalyst of claim 11 , wherein the catalyst is configured to be used in a circulating fluidized bed reactor.26. The catalyst of claim 1 , wherein at least one of Ni and Zn are present as both reduced metal sites and metal oxide sites.27. The catalyst of claim 26 , wherein the reduced metal sites comprise the hydride form of the metal.28. The catalyst of claim 11 , wherein at least one of Ni and Zn are present as both reduced metal sites and metal oxide sites.29. The catalyst of claim 28 , wherein the reduced metal sites comprise the hydride form of the metal.30. A catalyst for treating a raw synthesis gas claim 28 , the catalyst comprising:(a) a mixture of nickel oxide and nickel hydride;(b) a mixture of zinc oxide and zinc hydride; and{'sub': 2', '3, '(c) AlO.'}31. The catalyst of claim 30 , wherein claim 30 , at a temperature in a range from 300° C. to 600° C. claim 30 , the catalyst is simultaneously ...

PRODUCTION OF RENEWABLE FUELS AND ENERGY BY STEAM/CO2 REFORMING OF WASTES

This invention relates to a power recovery process in waste steam/COreformers in which a waste stream can be made to release energy without having to burn the waste or the syngas. This invention in some embodiments does not make use of fuel cells as a component but makes use of exothermic chemical reactors using syngas to produce heat, such as Fischer-Tropsch synthesis. It also relates to control or elimination of the emissions of greenhouse gases in the power recovery process of this invention with the goal of producing energy in the future carbonless world economy. 1. A waste reformation system comprising:a hydrocarbon synthesis reactor for producing a first stream of synthesized hydrocarbon gas;a waste reforming conversion system for receiving at least organic waste and for producing a second stream of synthesized hydrocarbon gas;wherein the hydrocarbon synthesis reactor is in fluid communication with the waste reforming conversion system such that a first portion of the first stream is mixed with the organic waste prior to the organic waste being received by the waste reforming conversion system; andwherein the waste reforming conversion system is in fluid communication with the hydrocarbon synthesis reactor such that the second stream is used for producing the first stream.2. The waste reformation system of claim 1 , wherein the hydrocarbon synthesis reactor is at least one of a Fischer-Tropsch reactor claim 1 , a methanol synthesis reactor claim 1 , a methanation reactor claim 1 , and a shift converter.3. The waste reformation system of claim 2 , wherein the hydrocarbon synthesis reactor is a Fischer-Tropsch unit and a shift converter.4. The waste reformation system of claim 3 , further comprising a pressure shift adsorption (PSA) unit in fluid communication with the shift converter claim 3 , the PSA unit for producing hydrogen fuel.5. The waste reformation system of claim 2 , wherein the hydrocarbon synthesis reactor is a shift converter.6. The waste ...

PROCESS AND DEVICE FOR REACTING ORGANIC MATERIALS TO GIVE HYDROGEN GAS

A device for reacting an organic starting material to yield a gas that includes hydrogen has a feed device, a tubular furnace with an entry zone, an interior space, an axis of rotation and an exit side, and a water feed arranged by the feed device or entry zone and controllable as a function of the content of hydrogen in the gas mixture. The feed device feeds the starting material in the region of the entry zone into the interior space of the tubular furnace, from which a solid material and a gas mixture is discharged. The tubular furnace has a compensator for different thermal expansions of a first zone and a second zone. A gas-conducting system includes a gas monitor for the content of hydrogen in the gas mixture. 2. The apparatus according to wherein the compensator is arranged in a transition area between the first zone and the second zone.3. The apparatus according to and further comprising a stationary bearing claim 1 , wherein the compensator is connected to the tubular furnace and designed to slide in relation to the stationary bearing claim 1 , wherein in the event of thermally-induced expansion the compensator is configured to be displaced relative to the bearing.4. The apparatus according to claim 1 , wherein the tubular furnace is supported in a sliding manner in the region of the entry zone and/or the exit zone in order to permit thermally-induced expansion of the tubular furnace in the direction of the axis of rotation.5. The apparatus according to claim 1 , further comprising in the area of the water feed an actuator is arranged and configured to regulate the water feed by way of a control variable which is provided by the gas monitor.6. The apparatus according to claim 1 , further comprising in the region of the first zone of the tubular furnace a preheating system that is configured to bring the starting material in the region of the first zone up to a temperature of between 300 degrees Celsius and 900 degrees Celsius.7. The apparatus according to ...

Method and Systems for Treating Synthesis Gas

The present invention relates to a method for treating synthesis gas, from an indirect or direct gasifier; the method including steps for: allowing the gas within a predetermined entry temperature range to flow into a first heat exchanger, allowing the gas to flow through the first heat exchanger while exchanging heat to a first medium, allowing the gas to transfer from the first heat exchanger to a subsequent last heat exchanger, allowing the gas to flow though the last heat exchanger while exchanging heat to a last medium, and allowing the gas to exit the last heat exchanger for being available to a further treatment, such as a cleaning treatment, within a predetermined exit temperature range, preferably below an ash or mineral solidification point. Furthermore, the present invention relates to a cooling system for cooling of synthesis gas and to a gasification system.

MULTISTAGE THERMOLYSIS METHOD FOR SAFE AND EFFICIENT CONVERSION OF CARPET/RUG, POLYMERIC MATERIALS AND OTHER WASTE SOURCES

Clean, safe and efficient methods, systems, and processes for utilizing thermolysis methods to processes to convert various carpet, rug, polymeric materials and other waste sources, such as solid waste, tires, manure, auto shredder residue, glass and carbon fiber composite materials, municipal solid wastes, medical wastes, waste wood and the like into a Clean Fuel Gas and Char source are disclosed. The invention processes the carpet, rug, polymeric material to effectively shred and/or grind the waste source, such as post-consumer carpet remnants and waste, and then process using thermolysis methods to destroy and/or separate halogen and other dangerous components to provide a Clean Fuel Gas and Char source. Additional waste sources, such as solid waste, tires, manure, auto shredder residue, glass and carbon fiber composite materials, municipal solid wastes, medical wastes, waste wood and the like, are suitable for the processing of the invention disclosed. 120-. (canceled)21. A Clean Fuel Gas and Char source produced by the method ofinputting a carpet, rug, and/or other polymeric material waste source into a thermolysis system;optionally increasing the moisture content of the waste source by injecting steam into the system or drying the waste source to decrease the moisture contentundergoing a depolymerization and a cracking reaction of hydrocarbons in the carpet, rug and/or other polymeric material waste source;destroying and/or removing toxic compounds present in the carpet, rug and/or other polymeric material waste source; andgenerating the Clean Fuel Gas and Char source,wherein the Clean Fuel Gas and Char contain less than about 10 ppb of halogenated organic compounds.22. The Clean Fuel Gas and Char source of claim 21 , wherein the Clean Fuel Gas and Char source generated are free of the halogenated organic compounds.23. The Clean Fuel Gas and Char source of claim 21 , wherein the Clean Fuel Gas and Char source generated are free tars and/or oils.24. The Clean ...

CONVERSION OF SOLID BIOMASS INTO A LIQUID HYDROCARBON MATERIAL

The present invention provides a process for producing liquid hydrocarbon products from a solid biomass feedstock, said process comprising the steps of: 1. A process for producing liquid hydrocarbon products from a solid biomass feedstock , said process comprising the steps of:a) providing in a first hydropyrolysis reactor vessel a first hydropyrolysis catalyst composition, said composition comprising one or more active metals selected from cobalt, molybdenum, nickel, tungsten, ruthenium, platinum, palladium, iridium and iron on an oxide support, wherein the active metals are present in a partially sulfided form to the extent that the first hydropyrolysis catalyst composition contains sulfur in an amount of from 10 to 90% of a full stoichiometric amount;{'sub': 2', '2', '2', '1', '3, 'b) contacting the solid biomass feedstock with said first hydropyrolysis catalyst composition and molecular hydrogen in said first hydropyrolysis reactor vessel at a temperature in the range of from 350 to 600° C. and a pressure in the range of from 0.50 to 7.50 MPa, to produce a product stream comprising partially deoxygenated hydropyrolysis product, HO, H, CO, CO, C-Cgases, char and catalyst fines;'}c) removing said char and catalyst fines from said product stream;{'sub': 2', '2', '2', '1', '3', '2', '2', '1', '3, 'd) hydroconverting said partially deoxygenated hydropyrolysis product in a hydroconversion reactor vessel in the presence of one or more hydroconversion catalyst and of the HO, CO, CO, H, and C-Cgas generated in step a), to produce a vapour phase product comprising substantially fully deoxygenated hydrocarbon product, HO, CO, CO, hydrogen and C-Cgases.'}2. A process according to claim 1 , wherein the active metals are selected from one or more of cobalt claim 1 , molybdenum claim 1 , nickel claim 1 , tungsten claim 1 , and iron.3. A process according to claim 1 , wherein the hydroconversion catalyst is selected from sulfided catalysts comprising one or more metals from the ...

Process and system for converting waste to energy without burning

This invention relates to a power recovery process in waste steam/CO 2 reformers whereby a waste stream can be made to release energy without having to burn the waste or the syngas. This invention does not make use of fuel cells as its critical component but makes use of highly exothermic chemical reactors using syngas to produce large amounts of heat, such as Fischer-Tropsch. It also relates to control or elimination of the emissions of greenhouse gases in the power recovery process of this invention with the goal of producing energy in the future carbonless world economy. A New Concept for a duplex kiln was developed that has the combined functionality of steam/CO 2 reforming, heat transfer, solids removal, filtration, and heat recovery. New methods of carbon-sequestering where the syngas produced by steam/CO 2 reforming can be used in Fischer-Tropsch processes that make high-carbon content compounds while recycling the methane and lighter hydrocarbons back to the reformer to further produce syngas at a higher H 2 /CO ratio.

Method and Systems for Treating Synthesis Gas

The present invention relates to a method for treating synthesis gas, from an indirect or direct gasifier; the method including steps for: allowing the gas within a predetermined entry temperature range to flow into a first heat exchanger, allowing the gas to flow through the first heat exchanger while exchanging heat to a first medium, allowing the gas to transfer from the first heat exchanger to a subsequent last heat exchanger, allowing the gas to flow though the last heat exchanger while exchanging heat to a last medium, and allowing the gas to exit the last heat exchanger for being available to a further treatment, such as a cleaning treatment, within a predetermined exit temperature range, preferably below an ash or mineral solidification point. Furthermore, the present invention relates to a cooling system for cooling of synthesis gas and to a gasification system. 1. A method for treating synthesis gas , such as gasification gas , such as between initial production and cleaning thereof , from an indirect or direct gasifier; the method comprising steps for:allowing the gas within a predetermined entry temperature range to flow into a first heat exchanger,allowing the gas to flow through the first heat exchanger while exchanging heat to a first medium, preferably a steam medium,allowing the gas to transfer from the first heat exchanger to a subsequent last heat exchanger,allowing the gas to flow though the last heat exchanger while exchanging heat to a last medium, preferably also a steam medium, andallowing the gas to exit the last heat exchanger for being available to a further treatment, such as a cleaning treatment, within a predetermined exit temperature range, preferably below an ash or mineral solidification point.2. The method according to claim 1 , in which the heat exchangers operate on steam cooling claim 1 , preferably fully operate on steam cooling.3. The method according to claim 1 , in which the heat exchangers operate on superheated steam ...

Removal of monocyclic aromatic compounds (BTEX) from a gas

The present invention relates to an improved process and system for purifying a gas, preferably an energy gas, containing aromatic compounds and isolating a fraction of aromatic compounds from said gas. In the process according to the invention, the gas is contacted with a washing liquid in step (a), at a temperature of 15-250° C., to obtain a purified gas, which is depleted in aromatic compounds, and a spent washing liquid wherein the aromatic compounds are dissolved. The spent washing liquid is stripped in step (b) with a stripping gas comprising at least 50 vol. % steam, to obtain a stripped washing liquid which is advantageously reused in step (a) and a loaded stripping gas comprising the aromatic compounds. The aromatic compounds are separated from the loaded stripping gas in step (c) by condensation of the steam and/or the aromatic compounds comprised in the loaded stripping gas to obtain an immiscible composition and isolating the aromatic compounds therefrom. The cleared stripping gas which is advantageously reused in step (b).

METHOD AND SYSTEM FOR GASIFICATION OF BIOMASS

A system for gasifying biomass is disclosed. The system comprises a water storage tank, a water pump, a heat exchanger, a plasma torch heater, a gasifier, an ash cooler, a spray tower, a dust collector, a deacidification tower, and a desiccator. The water storage tank is connected to the water inlet of the heat exchanger; the vapor outlet of the heat exchanger is connected to the vapor inlet of the plasma torch heater; the vapor outlet of the plasma torch heater is connected to the vapor nozzle of the gasifier; the ash outlet of the gasifier is connected to the ash inlet of the ash cooler; the gas outlet of the gasifier is connected to the gas inlet of the spray tower; and the gas outlet of the spray tower is connected to the gas inlet of the heat exchanger. 246. The system of claim 1 , wherein said system further comprises a nitrogen protecting device () connected to a feed inlet of said gasifier ().36. The system of claim 1 , wherein said system further comprises a plurality of vapor nozzles claim 1 , said vapor nozzles are arranged on said gasifier () and grouped into 3-4 height levels claim 1 , and said vapor nozzles of each level are evenly and tangentially arranged along a circumferential direction.46. The system of claim 2 , wherein said system further comprises a plurality of vapor nozzles claim 2 , said vapor nozzles are arranged on said gasifier () and grouped into 3-4 height levels claim 2 , and said vapor nozzles of each level are evenly and tangentially arranged along a circumferential direction. This application is a divisional of U.S. Ser. No. 13/745,858 filed on Jan. 20, 2013, now pending, which is a continuation-in-part of International Patent Application No. PCT/CN2011/076843 with an international filing date of Jul. 5, 2011, designating the United States, and which further claims priority benefits to Chinese Patent Application No. 201010234086.6 filed Jul. 20, 2010. The contents of all of the aforementioned applications, including any intervening ...

Methods and apparatus for recycling tail gas in syngas fermentation to ethanol

The invention present provides a method (and suitable apparatus) to convert biomass to ethanol, comprising gasifying the biomass to produce raw syngas; feeding the raw syngas to an acid-gas removal unit to remove at least some CO 2 and produce a conditioned syngas stream; feeding the conditioned syngas stream to a fermentor to biologically convert the syngas to ethanol; capturing a tail gas from an exit of the fermentor, wherein the tail gas comprises at least CO 2 and unconverted CO or H 2 ; and recycling a first portion of the tail gas to the fermentor and/or a second portion of the tail gas to the acid-gas removal unit. This invention allows for increased syngas conversion to ethanol, improved process efficiency, and better overall biorefinery economics for conversion of biomass to ethanol.

PRODUCTION OF RENEWABLE FUELS AND ENERGY BY STEAM/CO2 REFORMING OF WASTES

This invention relates to a power recovery process in waste steam/COreformers in which a waste stream can be made to release energy without having to burn the waste or the syngas. This invention in some embodiments does not make use of fuel cells as a component but makes use of exothermic chemical reactors using syngas to produce heat, such as Fischer-Tropsch synthesis. It also relates to control or elimination of the emissions of greenhouse gases in the power recovery process of this invention with the goal of producing energy in the future carbonless world economy. 1. A method of reforming of organic waste material , comprising:producing a first stream of synthesized hydrocarbon gas;providing to a waste reforming conversion system a supply of organic waste;mixing the organic waste with a first portion of the first stream;reforming the mixture of the first stream and the waste with steam and carbon dioxide and producing a second stream of synthesized hydrocarbon gas and heat; andusing a second portion from the second stream for said producing a first stream.2. The method of wherein said reforming does not include burning the waste or the portion of the first stream.3. The method of wherein said reforming is without the use of a catalyst.4. The method of which further comprises using the heat from said reforming to drive a heat engine and generator to produce electricity.5. The method of wherein said producing a first stream is with a hydrocarbon synthesis reactor.6. The method of wherein the hydrocarbon synthesis reactor further produces a carbon-containing liquid or solid product.7. The method of wherein the carbon-containing liquid or solid product is paraffin.8. The method of wherein the organic waste includes carbon and wherein substantially all of the carbon in the organic waste is sequestered in the carbon-containing liquid or solid product.9. The method of wherein said reforming is at a temperature not greater than one thousand eight hundred degrees F.10. ...

Demetallization of hydrocarbons

The present disclosure refers to a process and a process plant for extraction of metals from a hydrocarbon mixture obtained from a gasification or pyrolysis process, comprising the steps of combining said hydrocarbon mixture with an aqueous acid forming a mixture, mixing said mixture, separating said mixture in a contaminated aqueous phase and a purified hydrocarbon phase, with the associated benefit of said aqueous acid being able to release metals bound in such gasification and pyrolysis processes.

Multistage thermolysis method for safe and efficient conversion of e-waste materials

Clean, safe and efficient methods, systems, and processes for utilizing thermolysis methods to processes to convert various e-waste sources into Clean Fuel Gas and Char source are disclosed. The invention processes e-waste sources, such as for example whole circuit boards, to effectively shred and/or grind the waste source, and then process using thermolysis methods to destroy and/or separate halogen and other dangerous components to provide a Clean Fuel Gas and Char source, along with the ability to recover precious metals and other valuable components from the Char.

METHODS, SYSTEMS, AND APPARATUSES FOR UTILIZING A FISCHER-TROPSCH PURGE STREAM

Systems, apparatuses and methods of utilizing a Fischer-Tropsch (“FT”) tail gas purge stream for recycling are disclosed. One or more methods include removing an FT tail gas purge stream from an FT tail gas produced by an FT reactor, treating the FT tail gas purge stream with steam in a water gas shift (“WGS”) reactor, having a WGS catalyst, to produce a shifted FT purge stream including carbon dioxide and hydrogen, and removing at least a portion of the carbon dioxide from the shifted FT purge stream, producing a carbon dioxide stream and a treated purge stream. Other embodiments are also disclosed. 1. A method of producing Fischer-Tropsch (“FT”) hydrocarbons via FT synthesis in an FT reactor having an FT synthesis catalyst , the method comprising:a) producing a syngas comprising hydrogen and carbon monoxide in a syngas preparation unit using a carbonaceous feed;b) producing a liquid FT hydrocarbon stream, an FT tail gas stream and an FT water stream using the syngas gas as a feed in the FT reactor under FT operating conditions;c) removing an FT tail gas purge stream from the FT tail gas stream, leaving a remainder FT tail gas stream;d) treating the FT tail gas purge stream with steam in a water gas shift (“WGS”) reactor, having a WGS catalyst, to produce carbon dioxide and hydrogen, which form a shifted FT purge stream; ande) treating the shifted FT purge stream in a carbon dioxide removal unit, which removes carbon dioxide from the shifted FT purge stream, producing a carbon dioxide stream and a treated purge stream.2. The method of claim 1 , further comprising recycling the carbon dioxide stream as an input to the syngas preparation unit.3. The method of claim 1 , further comprising recycling the carbon dioxide stream as an input to the FT reactor.4. The method of claim 1 , wherein the syngas preparation unit is a steam methane reformer.5. The method of claim 1 , wherein the syngas preparation unit is an autothermal reformer.6. The method of claim 1 , wherein ...

SYSTEMS AND METHODS FOR FORMALDEHYDE CONTROL

Methods are provided to use water-free quench liquids to obtain pyrolytic liquid products with reduced formaldehyde content. Products include liquids with improved hydroxyacetaldehyde content. 1. A method for producing a low-formaldehyde product having a ratio of no more than 150 ppm formaldehyde per 1° BX of the low-formaldehyde product , comprising:i) pyrolyzing biomass to form gaseous pyrolysis products;ii) condensing a portion of the gaseous pyrolysis products to form the low-formaldehyde product, comprising: contacting the gaseous pyrolysis products with a nonaqueous coolant; andiii) separating at least a portion of the low-formaldehyde product from the nonaqueous coolant.2. A method for producing a low-formaldehyde liquid product having a ratio of no more than 150 ppm formaldehyde per 1° BX of the low-formaldehyde liquid product , comprising:i) pyrolyzing one or more biomass components to form gaseous pyrolysis products;ii) introducing the gaseous pyrolysis products into a separation unit;iii) recirculated a liquid coolant having a water solubility at 25° C. of less than 100 ppm water from an outlet of the separation unit to an inlet of the separation unit; andiv) recovering the liquid product comprising at least 50 wt. % of the gaseous pyrolysis products from the separation unit.3. A method for producing a low-formaldehyde liquid product having a ratio of no more than 150 ppm formaldehyde per 1° BX of the low-formaldehyde liquid product , comprising:i) pyrolyzing biomass in a biomass-containing stream to form a gaseous pyrolytic stream comprising water;ii) introducing the gaseous pyrolytic stream into a separation unit;iii) recirculating a substantially water-free liquid coolant stream from an outlet of the separation unit to an inlet of the separation unit; andiv) recovering substantially all of the water present in the gaseous pyrolytic stream from the separation unit in a first stream consisting of the liquid product and a second stream consisting of a non ...

METHODS AND APPARATUS FOR RECYCLING TAIL GAS IN SYNGAS FERMENTATION TO ETHANOL

The invention present provides a method (and suitable apparatus) to convert biomass to ethanol, comprising gasifying the biomass to produce raw syngas; feeding the raw syngas to an acid-gas removal unit to remove at least some COand produce a conditioned syngas stream; feeding the conditioned syngas stream to a fermentor to biologically convert the syngas to ethanol; capturing a tail gas from an exit of the fermentor, wherein the tail gas comprises at least COand unconverted CO or H; and recycling a first portion of the tail gas to the fermentor and/or a second portion of the tail gas to the acid-gas removal unit. This invention allows for increased syngas conversion to ethanol, improved process efficiency, and better overall biorefinery economics for conversion of biomass to ethanol. 1. A method of converting a carbonaceous feedstock to a syngas-fermentation product , said method comprising:{'sub': 2', '2, '(a) introducing a carbonaceous feedstock and an oxidant to a gasifier, under suitable gasification conditions to produce a raw syngas stream comprising CO, H, and CO, wherein said carbonaceous feedstock is selected from the group consisting of biomass, cellulose, hydrocarbons, carbohydrates, coal, petroleum coke, charcoal, lignite, carbon-rich waste materials, natural gas, and combinations thereof, and wherein said oxidant comprises one or more of air, oxygen, and steam;'}(b) optionally feeding at least a portion of said raw syngas stream to a syngas-cleanup unit, to produce an intermediate syngas stream;{'sub': '2', '(c) feeding at least a portion of said raw syngas stream and/or at least a portion of said intermediate syngas stream, if present, to an acid-gas removal unit, to remove at least some of said COand produce a conditioned syngas stream;'}{'sub': 2', '2, '(d) feeding at least a portion of said conditioned syngas stream to a fermentor, under suitable fermentation conditions and in the presence of suitable microorganisms and nutrients to biologically ...

PRODUCTION OF PRODUCTS FROM BIOMASS

A process for producing products from biomass comprises pyrolysing biomass at a selected temperature and producing a bio-syngas, processing bio-syngas from pyrolysis step (a) to remove condensable constituents from the bio-syngas, and processing the non-condensable bio-syngas from bio-syngas processing step (b) and producing one or more than one product, such as bio-fuels, bio-chemicals, bio-solvents and bio-plastics. 1. A process for producing products , such as bio-fuels , bio-chemicals , bio-solvents and bio-plastics , from biomass that comprises the following steps:(a) pyrolysing a feed material in the form of biomass at a selected temperature and decomposing the feed material and producing a bio-syngas and a solid char,(b) processing bio-syngas from pyrolysis step (a) to remove condensable constituents from the bio-syngas and producing a condensed bio-liquid, such as a bio-tar, and a non-condensable bio-syngas; and(c) processing the non-condensable bio-syngas from bio-syngas processing step (b) in a bio-hydrocarbons synthesis process step and producing one or more than one product, such as bio-fuels, bio-chemicals, bio-solvents and bio-plastics.2. The process defined in wherein the selected temperature for the pyrolysis step (a) is >500° C.3. The process defined in wherein the selected temperature for the pyrolysis step (a) is >600° C.4. The process defined in wherein the bio-liquids includes bio-tar.5. The process defined in includes a drying step of drying the feed material for the pyrolysis step (a) to a required moisture content for the pyrolysis step.6. The process defined in includes a cooling step for bio-syngas when an end use of bio-syngas is for use as an engine fuel and/or for direct combustion.7. The process defined in wherein the cooling step includes a gas storage (buffer) step.8. The process defined in includes transferring Ofrom the bio-hydrocarbons synthesis process step (c) to the pyrolysis step (a) to substitute at least a part of the air ...

METHOD AND SYSTEM FOR PURIFYING SYNTHESIS GAS, IN PARTICULAR FOR AMMONIA SYNTHESIS

The invention relates to a method for purifying synthesis gas, in particular for ammonia synthesis, wherein a partial stream () of an H-rich, CO-containing synthesis gas stream is burned, in particular to generate electrical energy, and wherein at least one component contained in the remaining H-rich, CO-containing synthesis gas stream (), in particular in the form of carbon dioxide, methanol and/or water, is absorbed by an adsorber at low temperatures, after which said absorbed component is desorbed from the adsorber by flushing using nitrogen () at higher temperatures. According to the invention the H-rich partial stream () is diluted using the nitrogen () used for the flushing before being burned. The invention further relates to a system () for purifying synthesis gas, in particular for ammonia synthesis. 1. A method for purifying synthesis gas , in particular for ammonia synthesis , wherein{'b': '26', 'sub': '2', 'a partial stream () of an H-rich, CO-containing synthesis gas stream is burnt, in particular for generating electrical energy, and wherein'}{'sub': '2', 'b': 26', '14', '14', '33, 'i': 'a', 'at least one component contained in the remaining H-rich, CO-containing synthesis gas stream (), in particular in the form of carbon dioxide, methanol and/or water, is adsorbed at low temperatures by an adsorber () and then said at least one adsorbed component is desorbed from the adsorber () by purging with nitrogen () at higher temperatures,'}{'sub': '2', 'b': 26', '35, 'characterized in that, prior to combustion, the H-rich partial stream () is diluted with the nitrogen used for purging ().'}2311426313317. The method as claimed in claim 1 , characterized in that additionally nitrogen () claim 1 , which has not been used previously for purging the adsorber () claim 1 , is added to the H-rich partial stream () prior to combustion claim 1 , to dilute it claim 1 , and in particular the nitrogen used for dilution ( claim 1 , ) is produced by cryogenic separation () ...

Plasma-assisted method and system for treating raw syngas comprising tars

This disclosure provides a system and method for conversion of raw syngas and tars into refined syngas, while optionally minimizing the parasitic losses of the process and maximizing the usable energy density of the product syngas. The system includes a reactor including a refining chamber for refining syngas comprising one or more inlets configured to promote at least two flow zones: a central zone where syngas and air/process additives flow in a swirling pattern for mixing and combustion in the high temperature central zone; at least one peripheral zone within the reactor which forms a boundary layer of a buffering flow along the reactor walls, (b) plasma torches that inject plasma into the central zone, and (c) air injection patterns that create a recirculation zone to promotes mixing between the high temperature products at the core reaction zone of the vessel and the buffering layer, wherein in the central zone, syngas and air/process additives mixture are ignited in close proximity to the plasma arc, coming into contact with each other, concurrently, at the entrance to the reaction chamber and method of using the system.

Feed injector tip cap

A system includes a gasification feed injector. The gasification feed injector includes a tip portion disposed at a fluid exit region of the gasification feed injector, and a tip cap coupled to the tip portion of the gasification feed injector and configured to serve as a thermal barrier for the tip portion during gasification reactions.

SYNTHETIC FUELS AND CHEMICALS PRODUCTION WITH IN-SITU CO2 CAPTURE

Novel redox based systems for fuel and chemical production with in-situ COcapture are provided. A redox system using one or more chemical intermediates is utilized in conjunction with liquid fuel generation via indirect Fischer-Tropsch synthesis, direct hydrogenation, or pyrolysis. The redox system is used to generate a hydrogen rich stream and/or COand/or heat for liquid fuel and chemical production. A portion of the byproduct fuels and/or steam from liquid fuel and chemical synthesis is used as part of the feedstock for the redox system. 114.-. (canceled)15. A method for producing a liquid fuel from a solid carbonaceous fuel comprising:pyrolizing a first portion of the solid carbonaceous fuel to form the liquid fuel; and{'sub': '2', 'claim-text': [{'sub': '2', 'reducing metal oxide containing particles in a first reaction zone with the second portion of the solid carbonaceous fuel thereby forming the COrich gases and reduced metal oxide containing particles;'}, 'directly sending a first portion of the reduced metal oxide containing particles from the first reaction zone to a second reaction zone, and a second portion of the reduced metal oxide containing particles from the first reaction zone to a third reaction zone;', 'oxidizing the first portion of the reduced metal oxide containing particles in the second reaction zone with steam thereby generating the hydrogen rich gases and at least partially oxidized metal oxide containing particles;', 'sending the at least partially oxidized metal oxide containing particles from the second reaction zone to the third reaction zone;', 'oxidizing the at least partially oxidized metal oxide containing particles from the second reaction zone and the second portion of the reduced metal oxide containing particles from the first reaction zone in the third reaction zone with an oxygen containing gas, thereby generating oxidized metal oxide containing particles; and', 'returning the oxidized metal oxide containing particles from the ...

PROCESS AND A SYSTEM FOR PRODUCING SYNTHESIS GAS

The present disclosure relates to a process and a system for producing synthesis gas. The carbonaceous feedstock is gasified, in the presence of at least one of oxygen and steam, in a first reactor to obtain a gaseous mixture comprising H2, CO, CH4, CO2, H2O, tar and char. The gaseous mixture is treated in a second, reactor, in the presence of a catalyst, to obtain synthesis gas. The system comprises a first reactor, a connecting conduit, a second reactor, at least one cyclone separator, at least one heat exchanger and at least one synthesis gas filter unit. The process and the system of the present disclosure are capable of producing synthesis gas with comparatively higher conversion of the unreacted char. 1. A process for producing synthesis gas with increased Hto CO molar ratio from a carbonaceous feedstock , said process comprising the following steps:{'b': '100', 'sub': 2', '4', '2', '2', '2, 'gasifying said carbonaceous feedstock in a first reactor (), in the presence of at least one of oxygen and steam, at a temperature in the range of 850° C. to 1800° C. and at a pressure in the range of 1 bar to 60 bar, to obtain a gaseous mixture comprising H, CO, CH, CO, HO, tar and char where the Hto CO molar ratio is less than 1.2; and'}{'b': '300', 'sub': 2', '2, 'further gasifying said gaseous mixture in a second reactor () with at least one of steam, CO, CO and hydrogen, in the presence of a catalyst comprising alkali metal salt impregnated on silica-alumina support and, at a temperature in the range of 600° C. to 850° C. and at a pressure in the range of 1 bar to 60 bar, to obtain synthesis gas with H/CO molar ratio being in the range of 1.5 to 6.'}2. The process as claimed in claim 1 , wherein:{'b': '100', 'i. said carbonaceous feedstock is gasified in a primary zone of said first reactor () having a temperature in the range of 900° C. to 1800° C.; and'}{'b': '100', 'ii. an additional portion of said carbonaceous feedstock is gasified in a secondary zone of said ...

INTEGRATED PROCESSES FOR REFINING SYNGAS AND BIOCONVERSION TO OXYGENATED ORGANIC COMPOUND

Integrated processes are provided for syngas refining and bioconversion of syngas to oxygenated organic compound. In the integrated processes ammonia contained in the syngas is recovered and used as a source of nitrogen and water for the fermentation. The integrated processes first remove tars from syngas by scrubbing using a first aqueous medium under conditions that ammonium bicarbonate is unstable. With tars removed, contact between the syngas and a second aqueous medium enables ammonia and carbon dioxide to be removed from the syngas without undue removal of components adverse to the fermentation, processing or oxygenated product such as benzene, toluene, xylene, ethylene, acetylene, and hydrogen cyanide. At least a portion of the second aqueous medium is supplied as a source of water and ammonia for the fermentation. 1. A process for generating a syngas comprising:(a) continuously gasifying carbonaceous feedstock at a temperature in excess of about 1000° C. to provide a syngas stream containing hydrogen sulfide, carbonyl sulfide, methane, ethylene, acetylene, benzene, toluene, xylene, tars including naphthalene, ammonia, and hydrogen cyanide;(b) cooling the syngas stream to a temperature below the temperature at which uncatalyzed water gas shift reactions occur;(c) scrubbing the syngas, said scrubbing by contact with a first aqueous medium at a temperature that is a sufficiently high temperature such that less than 40 percent of the ammonia contained in the syngas is absorbed by the aqueous medium and a pressure sufficient to provide aqueous medium in the liquid phase to provide a scrubbed syngas and an aqueous medium containing tars, wherein the contacting is for a duration sufficient such that the scrubbed syngas contains less than about 5 ppm(mole) naphthalene;(d) contacting the aqueous medium containing tars with stripping gas under stripping conditions sufficient to remove tars from the aqueous medium and provide a lean aqueous medium containing tars and a ...

PRODUCTION OF RENEWABLE FUELS AND ENERGY BY STEAM/CO2 REFORMING OF WASTES

This invention relates to a power recovery process in waste steam/COreformers in which a waste stream can be made to release energy without having to burn the waste or the syngas. This invention in some embodiments does not make use of fuel cells as a component but makes use of exothermic chemical reactors using syngas to produce heat, such as Fischer-Tropsch synthesis. It also relates to control or elimination of the emissions of greenhouse gases in the power recovery process of this invention with the goal of producing energy in the future carbonless world economy. 1. A waste reformation system comprising:a hydrocarbon synthesis reactor for producing a first stream of synthesized hydrocarbon gas;a waste reforming conversion system for receiving organic waste, steam, and carbon dioxide and for producing a second stream of synthesized hydrocarbon gas;wherein the hydrocarbon synthesis reactor is in fluid communication with the waste reforming conversion system such that a first portion of the first stream is mixed with the organic waste prior to the organic waste being received by the waste reforming conversion system; andwherein the waste reforming conversion system is in fluid communication with the hydrocarbon synthesis reactor such that a second portion of the second stream is used for producing the first stream.2. The waste reformation system of claim 1 , further comprising means for cooling the second portion prior to said producing the first stream.3. The waste reformation system of claim 2 , wherein the means for cooling is a Brayton cycle turbine.4. The waste reformation system of claim 1 , further comprising means for pressurizing the second portion prior to said producing the first stream.5. The waste reformation system of claim 1 , wherein the hydrocarbon synthesis reactor is at least one of a Fischer-Tropsch unit and a shift converter.6. The waste reformation system of claim 1 , wherein the hydrocarbon synthesis reactor is a Fischer-Tropsch unit and a ...

Gas clean-up unit and gas purification method

A gas clean-up unit includes a first conversion unit configured to perform a first conversion process of converting hydrogen cyanide contained in gas to be treated to ammonia, in presence of a first catalyst and at a first predetermined temperature; a second conversion unit configured to perform a second conversion process of converting carbonyl sulfide in the gas that has been subjected to the first conversion process to hydrogen sulfide, in presence of a second catalyst and at a second predetermined temperature lower than the first predetermined temperature; a cleaning unit configured to perform a cleaning process of bringing the gas into gas-liquid contact with cleaning liquid to remove the ammonia by cleaning; and a desulfurization unit configured to absorb and remove hydrogen sulfide in the gas by bringing the gas that has been subjected to the cleaning process into gas-liquid contact with absorbent.

Method and apparatus for separating a synthesis gas by cryogenic distillation

In a process for separating a mixture containing carbon monoxide, hydrogen and carbon dioxide, the mixture cooled in a heat exchanger is contacted by a stream of liquid methanol at a temperature below −40° C. to produce carbon dioxide enriched methanol and a carbon dioxide depleted gas relative to the cooled mixture, the carbon dioxide depleted gas is cooled in the heat exchanger and is sent to a separation unit to produce a carbon monoxide enriched stream and a hydrogen enriched stream and the streams enriched in carbon monoxide and hydrogen are heated in the heat exchanger by exchanging heat with the mixture.

Methods and system for decreasing gas emissions from landfills

A method of diverting municipal solid waste (MSW) from a landfill that includes receiving, at a MSW processing system, a quantity of MSW, gasifying the quantity of MSW in a gasification unit to yield a syngas stream and biochar stream, converting at least a portion of the syngas to mixed alcohols in an alcohol synthesis unit, separating the mixed alcohols into one or more alcohol products, and determining a carbon offset for diverting the MSW from the landfill to the MSW processing system.

QUENCH CHAMBER WITH INTEGRATED SCRUBBER SYSTEM

The present application provides a gasifier for creating a flow of a syngas. The gasifier may include a reaction chamber and a quench chamber. The quench chamber may include a number of integrated scrubber trays therein such that the syngas first enters a quench pool via a dip tube and then passes through the scrubber trays before leaving the quench chamber. 1. A gasifier for creating a flow of a syngas , comprising:a reaction chamber; anda quench chamber;the quench chamber comprising a plurality of integrated scrubber trays therein.2. The gasifier of claim 1 , wherein the quench chamber comprises a quench ring therein.3. The gasifier of claim 2 , wherein the quench chamber comprises a dip tube extending from the quench ring.4. The gasifier of claim 3 , wherein the quench chamber comprises a flow of water extending from the quench ring and down the dip tube.5. The gasifier of claim 4 , wherein the flow of water comprises an outer film and an inner film along the dip tube.6. The gasifier of claim 4 , wherein the flow of water is in a counter flow arrangement with a flow of cooled syngas.7. The gasifier of claim 3 , wherein the quench chamber comprises a quench pool downstream of the dip tube.8. The gasifier of claim 3 , wherein the plurality of scrubber trays are positioned about the dip tube.9. The gasifier of claim 3 , wherein the dip tube comprises a downward path for a flow of hot syngas.10. The gasifier of claim 1 , wherein the quench chamber comprises a syngas outlet.11. The gasifier of claim 1 , wherein the plurality of scrubber trays comprises a plurality of perforations therein.12. The gasifier of claim 11 , wherein the plurality of scrubber trays comprises a plurality of protrusions positioned about the plurality of perforations.13. The gasifier of claim 12 , wherein the plurality of protrusions comprises a sharp claim 12 , pin-like shape.14. The gasifier of claim 1 , wherein the plurality of scrubber trays comprises an upward path for a flow of cooled ...

Feed injector for a gasification system

The present disclosure provides a feed injector for a gasification system. The feed injector may include an inner tube defining an inner feed passage therein, an intermediate tube defining an intermediate feed passage therein, and an outer tube defining an outer feed passage therein. The outer tube may include an outer tube pipe portion and an outer tube tip portion attached to one another, and the outer tube tip portion may be formed of a ceramic matrix composite, a sintered Silicon Carbide, or a sintered Silicon Nitride. The present disclosure also provides a related method of operating a feed injector of a gasification system as well as a related integrated gasification combined cycle power plant.

PROCESS FOR DEVOLATIZING A FEEDSTOCK

Provided herein is a method for devolatizing a solid feedstock. The solid feedstock is treated to a produce a particle size laying between 1 cmand 100 cm. The solid feedstock is passed into a device connected to an outlet of a compaction screw auger comprising an assembly including a solid feedstock injector, a retort, a side arm for injecting a heated gas comprising hydrogen, and a process auger. The solid feedstock is contacted with the heated gas at a temperature of 500° C. to 1000° C. for a time of 60 seconds to 120 seconds, whereby the solid feedstock is converted into a gas stream and a solid stream. 1. A method for devolatizing a solid feedstock , comprising carbon-based waste selected from the group consisting of hazardous material , biomass , animal manure , tires , municipal solid waste and refuse derived fuel , wherein the method comprises:{'sup': 3', '3, 'treating the solid feedstock to a produce a particle size laying between 1 cmand 100 cm;'} [{'sub': 1', '2', '1', '2', '1', '2, 'the injector having a cylindrical body defined by an inner cylindrical surface and an outer cylindrical surface with a thickness between the inner and outer cylindrical surfaces, an inner cavity, an inside diameter D, and an outside diameter D; an inlet end of the injector having an inlet opening and injector flange radially disposed around the inlet opening and extending radially outward from the cylindrical body of the injector; an outlet end of the injector having an outlet opening and an injector ring radially disposed around the outlet opening and extending radially outward from the cylindrical body of the injector; an internal sealing shoulder being disposed on the outer cylindrical surface of the injector at a distance Lfrom the injector ring and at a distance Lfrom the injector flange, wherein the distance Lis less than the distance L;'}, {'sub': 3', '4', '3', '2, 'the retort having a cylindrical body defined by an inner cylindrical surface and an outer cylindrical ...

HYDROGEN CHLORIDE REMOVING AGENT

The present invention provides a new hydrogen chloride removing agent that exhibits a good hydrogen chloride removal effect at a relatively low temperature. The present invention preferably provides a new hydrogen chloride removing agent for removing hydrogen chloride contained in a hydrogen-chloride-containing gas, such as a pyrolysis gas, a combustion exhaust gas, a dry distillation gas, etc., especially hydrogen chloride contained in a biomass pyrolysis gas. The present invention relates to a hydrogen chloride removing agent characterized by containing a mixture of a calcium carbonate and an imogolite and/or a synthetic imogolite, and relates to a method for removing, by using said hydrogen chloride removing agent, hydrogen chloride contained in a hydrogen-chloride-containing gas, especially hydrogen chloride contained in a biomass pyrolysis gas. 1. A hydrogen chloride removing agent containing a mixture of calcium carbonate and imogolite and/or synthetic imogolite.2. The hydrogen chloride removing agent according to claim 1 , wherein a mass ratio of calcium carbonate to imogolite and/or synthetic imogolite in the mixture is 100:5 to 100:50.3. The hydrogen chloride removing agent according to claim 1 , wherein the hydrogen chloride removing agent is for removing hydrogen chloride contained in a hydrogen chloride-containing gas.4. The hydrogen chloride removing agent according to claim 1 , wherein the hydrogen chloride removing agent is for removing hydrogen chloride contained in a biomass pyrolysis gas.5. A method for removing hydrogen chloride from a hydrogen chloride-containing gas using a hydrogen chloride removing agent claim 1 , wherein the hydrogen chloride removing agent contains a mixture of calcium carbonate and imogolite and/or synthetic imogolite.6. The method according to claim 5 , wherein a mass ratio of calcium carbonate to imogolite and/or synthetic imogolite in the mixture is 100:5 to 100:50.7. The method according to claim 5 , wherein the removal ...

TWO-STAGE METHOD FOR REMOVING CO2 FROM SYNTHESIS GAS

A plant for removing COfrom a fluid stream via an aqueous absorption medium contains a) a first absorption zone for treating the fluid stream with a partially regenerated absorption medium, b) a second absorption zone for treating the treated fluid stream with a regenerated absorption medium, c) a first flash vessel for depressurizing the loaded absorption medium, d) a second flash vessel for depressurizing the sub-partially regenerated absorption medium, e) a stripper for thermally regenerating the partially regenerated absorption medium, f) a conduit for feeding a substream of the partially regenerated absorption medium into the first absorption zone and a conduit for feeding a further substream of the partially regenerated absorption medium into a stripper, g) a conduit for recirculating the regenerated absorption medium to the second absorption zone, and h) a jet pump for compressing the water vapor-comprising, second CO-comprising gas stream. 110-. (canceled)11. A plant for removing COfrom a fluid stream with an aqueous absorption medium , the plant comprising:a) a first absorption zone for treating the fluid stream with a partially regenerated absorption medium,{'sub': '2', 'b) a second absorption zone for treating the treated fluid stream with a regenerated absorption medium, giving a fluid stream which has been freed of COand a loaded absorption medium,'}{'sub': '2', 'c) a first flash vessel for depressurizing the loaded absorption medium to a pressure of from 1.2 to 3 bar absolute, giving a sub-partially regenerated absorption medium and a first CO-comprising gas stream,'}{'sub': '2', 'd) a second flash vessel for depressurizing the sub-partially regenerated absorption medium to a pressure of from 1 to 1.2 bar absolute, giving the partially regenerated absorption medium and a water vapor-comprising, second CO-comprising gas stream,'}{'sub': '2', 'e) a stripper for thermally regenerating the partially regenerated absorption medium, with the regenerated ...

System and process for the manufacture of hydrocarbons and upgraded coal by catalytic mild temperature pyrolysis of coal

A process for upgrading a solid carbonaceous material includes heating the solid carbonaceous material in the presence of a catalyst under partial pyrolysis conditions and obtaining an upgraded solid carbonaceous product, a gaseous product, and a spent catalyst.