GB2237814A - A method and apparatus for co-generating power and hydrocarbons from coal derived synthesis gas using pressure swing absorption - Google Patents

A method and apparatus for co-generating power and hydrocarbons from coal derived synthesis gas using pressure swing absorption Download PDF

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Publication number
GB2237814A
GB2237814A GB8925476A GB8925476A GB2237814A GB 2237814 A GB2237814 A GB 2237814A GB 8925476 A GB8925476 A GB 8925476A GB 8925476 A GB8925476 A GB 8925476A GB 2237814 A GB2237814 A GB 2237814A
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United Kingdom
Prior art keywords
synthesis gas
gas
unit
hydrocarbons
rich stream
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Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
GB8925476A
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GB8925476D0 (en
Inventor
Joachim Ansorge
Columba Kam-Kuen Yeung
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Shell Internationale Research Maatschappij BV
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Shell Internationale Research Maatschappij BV
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Priority to GB8925476A priority Critical patent/GB2237814A/en
Publication of GB8925476D0 publication Critical patent/GB8925476D0/en
Priority to CN90108965A priority patent/CN1026149C/en
Priority to ZA908960A priority patent/ZA908960B/en
Publication of GB2237814A publication Critical patent/GB2237814A/en
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
    • C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
    • C07C1/0485—Set-up of reactors or accessories; Multi-step processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/002—Removal of contaminants
    • C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
    • C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/002—Removal of contaminants
    • C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
    • C10K1/006—Hydrogen cyanide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
    • F02C3/20—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products
    • F02C3/26—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products the fuel or oxidant being solid or pulverulent, e.g. in slurry or suspension
    • F02C3/28—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products the fuel or oxidant being solid or pulverulent, e.g. in slurry or suspension using a separate gas producer for gasifying the fuel before combustion
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1643—Conversion of synthesis gas to energy
    • C10J2300/165—Conversion of synthesis gas to energy integrated with a gas turbine or gas motor
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1656—Conversion of synthesis gas to chemicals

Abstract

A process for producing hydrocarbons and power comprises partially combusting finely divided fuel to produce synthesis gas (H2/CO of 0.25-0.70) and removing particulates, HCN and H2S from the gas at 1, passing part of the gas through a pressure sealing adsorber 2 to remove CO and produce a H2-rich stream 3(H2/CO of 3 to 15), combining the H2-rich gas with part of the synthesis gas to produce a gas having a H2/CO of 1 to 3, which is used at 5 to synthesise hydrocarbons, and desorbing CO from the adsorber 2 and using it, e.g. in gas turbine 4, to produce power. <IMAGE>

Description

A METHOD AND APPARATUS FOR CO-GENERATING POWER AND HYDROCARBONS FROM COAL DERIVED SYNTHESIS GAS USING PRESSURE SWING ABSORPTION The present invention relates to a method and apparatus for co-generating power and hydrocarbons from a gasification process wherein synthesis gas (carbon monoxide and hydrogen) is obtained by partial oxidation of a finely divided solid carbon-containing fuel and an oxygen-containing gas.
The oxygen-containing gas used in the partial oxidation may be pure oxygen, mixtures of oxygen and steam, air or mixtures of pure oxygen, air and steam.
In view of the depletion of oil reserves, the production of synthesis gas, which is a feedstock for many chemicals, is a subject of growing interest.
The partial oxidation of finely divided solid carbon-containing fuels can take place according to various established processes.
Finely divided solid carbon-containing fuels are applied in processes for the preparation of synthesis gas by the partial combustion of a finely divided solid carbon-containing fuel with an oxygen-containing gas in a reactor wherein liquid slag formed during the partial combustion process is removed through an outlet in the bottom of the reactor and passed by gravity through a slag discharge means into a water bath or slag quenching vessel where it is solidified by quenching.
The partial combustion of finely divided solid carbon-containing fuel with substantially pure oxygen as oxygen-containing gas yields synthesis gas mainly consisting of carbon monoxide and hydrogen. When the oxygen-containing gas is air or oxygen-enriched air, the synthesis gas formed of course also contains a substantial quantity of nitrogen. By finely divided solid carbon-containing fuel is generally meant coal or another solid fuel, such as brown coal, peat, wood, coke, soot, etc., but mixtures of liquid or gas and particulate solid fuels, are also possible.
Advantageously, a moderator is also introduced into the reactor. The object of the moderator is to exercise a moderating effect on the temperature on the reactor. This is ensured by endothermic reaction between the moderator and the reactants and/or products of the synthesis gas preparation. Suitable moderators are steam and carbon dioxide.
The gasification is advantageously carried out at a temperature in the range from 1200 to 1700 "C and at a pressure in the range from 1 to 200 bar.
The reactor in which the preparation of synthesis gas takes place may have any suitable shape.
The supply of finely divided solid carbon-containing fuel and oxygen-containing gas to the reactor can take place in any manner suitable for the purpose and will not be described in detail.
Liquid slag formed in the partial combustion reaction drops down and is drained through the outlet located in the reactor bottom.
In partial oxidation processes of finely divided solid carbon-containing fuels, such as for example coal gasification, the fuel is fed from a supply device to a gasifier by means of a suitable carrier fluid.
It has already been proposed to convert carbonaceous materials into both gaseous and liquid fuels which can be effectively utilized so as to generate variable amounts of electric power for both industrial and utility needs.
For example, methanol can be applied as peak shaving fuel in combined cycle power generation, but this has many disadvantages (CO-shift, deep sulphur and C02 removal, waste heat generated at 100 C) .
Further, it has already been proposed to apply CO as a peak shaving fuel by capturing, storing and releasing the CO by forming and dissociating a suitable organic molecule i.e. an alkyl formate.
Such a method, however, requires further chemical processes for the synthesis gas from the gasifier which is not desirable.
However, the known methods are not suitable for an advantageous co-generation of electricity and hydrocarbons. As the synthesis of hydrocarbons from coal synthesis gas requires additional hydrogen, a hydrogen manufacturing unit has to be integrated, which is economically not attractive.
Therefore, it is an object of the invention to provide a method and apparatus for co-generation of power and hydrocarbons from coal derived syngas, wherein an additional hydrogen manufacturing unit is not required and a wide range of flexibility in power production is provided whilst offering substantial economic and efficiency advantages.
The invention therefore provides a process for the co-generation of power and hydrocarbons from coal derived synthesis gas in combined cycle power generation, comprising the steps of: a) partially combusting a finely divided solid carbon-containing fuel and an oxygen-containing gas into a synthesis gas possessing an H2/CO ratio ranging from 0.25 to 0.70; b) treating the said synthesis gas to remove particulates, HCN and H2S; c) supplying at least part of the produced synthesis gas to a pressure swing adsorption unit wherein the greater part of the CO is adsorbed and a hydrogen rich stream is produced having an H2/CO ratio ranging from 3 to 15; d) recombining the hydrogen rich stream with part of the synthesis gas from the partial combustion process and using it as feed having an H2/CO ratio ranging from 1 to 3 for a hydrocarbon synthesis unit; e) desorbing the adsorbed CO to produce a CO rich stream having an H2/CO ratio ranging from 0.05 to 0.25 and feeding it to a power generation unit.
The invention further provides an apparatus for the co-generation of power and hydrocarbons from coal derived synthesis gas in combined cycle power generation, comprising: a) means for partially combusting a finely divided solid carbon-containing fuel and an oxygen-containing gas into a synthesis gas possessing an H2/CO ratio ranging from 0.25 to 0.70; b) means for treating the said synthesis gas to remove particulates, HCN and H2S; c) means for supplying at least part of the produced synthesis gas to a pressure swing adsorption unit wherein the greater part of the CO is absorbed; d) means for recombining the hydrogen rich stream with part of the synthesis gas from the partial combustion process and means for using it as feed having an H2/CO ratio ranging from to 3 for a hydrocarbon synthesis unit; and e) means for desorbing the adsorbed CO to produce a CO rich stream having an H2/CO ratio ranging from 0.05 to 0.25 and means for feeding it to a power generation unit.
In this manner hydrocarbons can be co-produced together with electricity without an additional hydrogen manufacturing unit for the hydrocarbon synthesis being required.
The invention will now be described by way of example in more detail by reference to the accompanying drawing in which the figure represents a block scheme of the invention.
According to the present invention a gasifier carbon feedstock such as coal, lignite, petroleum residue and the like is gasified under appropriate conditions using a gasifying agent essentially consisting of oxygen, possibly in combination with steam.
The synthesis gas will contain mostly carbon monoxide (CO) and hydrogen (H2) along with smaller concentrations of carbon dioxide, methane, hydrogen sulphide, argon and other inerts. The H2/CO ratio will range from 0.25 to 0.70.
The invention is based upon the following idea.
Power generation needs combustible gas. Presence of hydrogen is not essential. Carbon monoxide is more suitable because of its higher heating value per mole compared to hydrogen. Hydrocarbon synthesis needs a synthesis gas with a hydrogen to carbon monoxide ratio of about two to perform the hydrocarbon synthesis to produce valuable hydrocarbons.
If a pressure swing absorption (PSA) unit is applied as a connecting link between the gasifier and the hydrocarbon synthesis, the PSA unit splitting the synthesis gas from the partial combustion unit into a CO-rich stream and an H2-rich stream acts as a kind of selector: the CO rich stream is sent to power generation whereas the H2 rich stream is sent to where the hydrogen is essential, i.e. to the hydrocarbon synthesis. The principles of operation of pressure swing adsorption and hydrocarbon synthesis are known as such and will not be described in detail. The main application would be with a big power station. The hydrogen available in the synthesis gas from coal would be used for high added value hydrocarbons. The power generating ability of the remaining gas is hardly affected or even slightly increased.
This configuration is more efficient and less expensive compared to a configuration which, for example, uses conventional CO-shift technology as a connecting link.
Referring to the figure, in the simplified scheme shown, the configuration of the invention consists of: a) a coal gasification unit 1 producing synthesis gas which is lean in hydrogen; b) a pressure swing adsorption unit 2 (PSA) in which most of the carbon monoxide of the coal synthesis gas is adsorbed and a hydrogen rich stream is produced. This hydrogen rich stream is combined via a line 3 with part of the coal synthesis gas to form a heavy paraffin synthesis (HPS) gas with the desired H2/CO ratio. The carbon monoxide is desorbed and fed to a gas-turbine 4 for power generation; and c) a synthesis unit 5 in which paraffinic hydrocarbons are synthesized, isomerized and fractionated according to the requirements.
Coal is supplied through a line A and gasified in the coal gasifier 1 with a pressurized stream of for example 95% molar purity oxygen, supplied through a line B for example from a cryogenic air separation unit (not shown). The coal feed rate is for example approximately 4000 t/d and the gasification pressure for example 25 bara at a temperature appropriate for the coal to give a high thermal efficiency.
The synthesis gas is passed through an appropriate process (not shown) to remove a high proportion of the solids present. This can be a dry process involving the use of one or more cyclone filters or other means. Thereafter the net gas is stripped off its acid gas components, most notably hydrogen sulphide, in an acid gas removal step (not shown), whilst at the same time removing the remaining solids and some of the carbon dioxide and water formed in the process. This is carried out in a series of wash columns, absorbers and flashes, making use in part of a physical or chemical absorbent such as Sulfinol or Selexol. The offgas stream is directed to a sulphur recovery process (not shown) where the sulphur is collected.
The cleaned gas, which has essentially a 0.25 to 0.70 ratio of H2 to CO is at some 40 deg. C and 20 bara pressure.
Example 4000 t/d coal were gasified with oxygen resulting in about 3 8x106 Nm3/d synthesis gas with a hydrogen to carbon monoxide ratio of about 0.25-0.70. The synthesis gas is treated to remove particulates, HCN and H2S.
Advantageously, 20-30% of the coal synthesis gas was treated in a CO-shift and a CO2 removal unit 6 to produce about 1z10 Nm3 towngas 6a which fulfils to the CO and heating value specifications. The remaining part was fed to the PSA unit 2.
60-70% of the synthesis gas produced in the coal gasification unit was splitted in the PSA unit 2 into two streams: - a CO rich stream (H2/CO about 0.14-0.06) used for power generation 4, 4a and - an H2 rich stream (H2/CO about 10.5-4.5) which was combined with the remaining 15-58 of the coal synthesis gas to form the heavy paraffins synthesis (HPS) gas with an H2/CO ratio of 2.1.
A small part of the raw hydrogen could be further purified by pressure swing adsorption (PSA) for use in the hydro-finishing steps of the products (see below).
The synthesis gas was first converted by heavy paraffin synthesis (HPS) into a range of linear hydrocarbons 5a.
Subsequently, linear paraffins in the range C5 to C17 were separated from the total hydrocarbon stream and after hydrotreating to remove olefins and oxygenates used for paraffinic solvents and detergent feedstocks.
The remaining stream of linear hydrocarbons is converted in a heavy paraffins conversion (HPC) unit into naphtha, kerosene and gasoil.
The overall thermal efficiency of this scheme results to about 48-50%. Besides the advantage of lower capital investment the presented concept achieves a slightly higher thermal efficiency than the corresponding complex using conventional CO-shift technology.
It will be appreciated that the step of producing towngas is optional and should not be considered an indispensable feature of the present invention.
Various modifications of the invention will become apparent to those skilled in the art from the foregoing description and accompanying drawings. Such modifications are intended to fall within the scope of the appended claims.

Claims (7)

1. A process for the co-generation of power and hydrocarbons from coal derived synthesis gas in combined cycle power generation, comprising the steps of: a) partially combusting a finely divided solid carbon-containing fuel and an oxygen-containing gas into a synthesis gas possessing an H2/CO ratio ranging from 0.25 to 0.70; b) treating the said synthesis gas to remove particulates, HCN and H2S; c) supplying at least part of the produced synthesis gas to a pressure swing adsorption unit wherein the greater part of the CO is adsorbed and a hydrogen rich stream is produced having an H2/CO ratio ranging from 3 to 15; d) recombining the hydrogen rich stream with part of the synthesis gas from the partial combustion process and using it as feed having an H2/CO ratio ranging from 1 to 3 for a hydrocarbon synthesis unit; e) desorbing the adsorbed CO to produce a CO rich stream having an H2/CO ratio ranging from 0.05 to 0.25 and feeding it to a power generation unit.
2. The process as claimed in claim 1 wherein part of the synthesis gas from step a) and b) is treated in a CO-shift and a CO2 removal unit to produce town gas and wherein the remaining part of the said synthesis gas is fed to the pressure swing absorption unit.
3. The process as claimed in claim 2 wherein said part from step a) and b) is 20-30%.
4) The process as claimed in claim 3 wherein 60-70% of the synthesis gas produced in the coal gasification unit is splitted in the PSA unit into two streams: a CO rich stream (H2/CO about 0.14-0.06) used for power generation and an H2 rich stream (H2/CO about 10.5-4.5) which is combined with the remaining 15-5% of the coal synthesis gas to form the heavy paraffins synthesis (HPS) gas with an H2/CO ratio of 2.1.
5. An apparatus for the co-generation of power and hydrocarbons from coal derived synthesis gas in combined cycle power generation, comprising: a) means for partially combusting a finely divided solid carbon-containing fuel and an oxygen-containing gas into a synthesis gas possessing an H2/CO ratio ranging from 0.25 to 0.70; b) means for treating the said synthesis gas to remove particulates, HCN and H2S; c) means for supplying at least part of the produced synthesis gas to a pressure swing adsorption unit wherein the greater part of the CO is absorbed; d) means for recombining the hydrogen rich stream with part of the synthesis gas from the partial combustion process and means for using it as feed having an H2/CO ratio ranging from 1 to 3 for a hydrocarbon synthesis unit; and e) means for desorbing the adsorbed CO to produce a CO rich stream having an H2/CO ratio ranging from 0.05 to 0.25 and means for feeding it to a power generation unit.
6. Process for co-production of power and hydrocarbons from coal derived synthesis gas substantially as described in the description by reference to the Example.
7. Apparatus for co-production of power and hydrocarbons from coal derived synthesis gas substantially as described in the description by reference to the figure.
GB8925476A 1989-11-10 1989-11-10 A method and apparatus for co-generating power and hydrocarbons from coal derived synthesis gas using pressure swing absorption Withdrawn GB2237814A (en)

Priority Applications (3)

Application Number Priority Date Filing Date Title
GB8925476A GB2237814A (en) 1989-11-10 1989-11-10 A method and apparatus for co-generating power and hydrocarbons from coal derived synthesis gas using pressure swing absorption
CN90108965A CN1026149C (en) 1989-11-10 1990-11-08 Method and apparatus for co-generating power and hydrocarbons from coal derived synthesis gas using pressure swing absorption
ZA908960A ZA908960B (en) 1989-11-10 1990-11-08 A method and apparatus for co-generating power and hydrocarbons from coal derived synthesis gas using pressure wing absorption

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Application Number Priority Date Filing Date Title
GB8925476A GB2237814A (en) 1989-11-10 1989-11-10 A method and apparatus for co-generating power and hydrocarbons from coal derived synthesis gas using pressure swing absorption

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GB8925476D0 GB8925476D0 (en) 1989-12-28
GB2237814A true GB2237814A (en) 1991-05-15

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0884099A2 (en) * 1997-06-09 1998-12-16 Daido Hoxan Inc. Gas generating apparatus and gas generation process using the same
US6162373A (en) * 1995-10-03 2000-12-19 Exxon Research And Engineering Company Removal of hydrogen cyanide from synthesis gas (Law322)
EP2145665A2 (en) 2008-07-17 2010-01-20 Air Products and Chemicals, Inc. Gas purification by adsorption of hydrogen sulfide
US8247462B2 (en) 2007-02-12 2012-08-21 Sasol Technology (Proprietary) Limited Co-production of power and hydrocarbons

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7500997B2 (en) * 2002-02-05 2009-03-10 The Regents Of The University Of California Steam pyrolysis as a process to enhance the hydro-gasification of carbonaceous materials
CN1733873B (en) * 2004-08-11 2010-05-26 日本气体合成株式会社 Method for producing liquefied petroleum gas
CN101663377B (en) * 2007-02-12 2013-05-01 沙索技术有限公司 Co-production of power and hydrocarbons

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2165551A (en) * 1984-10-10 1986-04-16 Shell Int Research Production of synthesis gas

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2165551A (en) * 1984-10-10 1986-04-16 Shell Int Research Production of synthesis gas

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6162373A (en) * 1995-10-03 2000-12-19 Exxon Research And Engineering Company Removal of hydrogen cyanide from synthesis gas (Law322)
EP0884099A2 (en) * 1997-06-09 1998-12-16 Daido Hoxan Inc. Gas generating apparatus and gas generation process using the same
EP0884099A3 (en) * 1997-06-09 2000-04-19 Daido Hoxan Inc. Gas generating apparatus and gas generation process using the same
US8247462B2 (en) 2007-02-12 2012-08-21 Sasol Technology (Proprietary) Limited Co-production of power and hydrocarbons
US8552073B2 (en) 2007-02-12 2013-10-08 Sasol Technology (Proprietary) Limited Co-production of power and hydrocarbons
EP2145665A2 (en) 2008-07-17 2010-01-20 Air Products and Chemicals, Inc. Gas purification by adsorption of hydrogen sulfide
US7909913B2 (en) 2008-07-17 2011-03-22 Air Products And Chemicals, Inc. Gas purification by adsorption of hydrogen sulfide
US8197580B2 (en) 2008-07-17 2012-06-12 Air Products And Chemicals, Inc. Gas purification by adsorption of hydrogen sulfide
US8551229B2 (en) 2008-07-17 2013-10-08 Air Products And Chemicals, Inc. Gas purification by adsorption of hydrogen sulfide

Also Published As

Publication number Publication date
CN1026149C (en) 1994-10-05
GB8925476D0 (en) 1989-12-28
CN1051619A (en) 1991-05-22
ZA908960B (en) 1991-08-28

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