WO2012073130A2 - Gazéification d'un matériau carboné - Google Patents

Gazéification d'un matériau carboné Download PDF

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Publication number
WO2012073130A2
WO2012073130A2 PCT/IB2011/054885 IB2011054885W WO2012073130A2 WO 2012073130 A2 WO2012073130 A2 WO 2012073130A2 IB 2011054885 W IB2011054885 W IB 2011054885W WO 2012073130 A2 WO2012073130 A2 WO 2012073130A2
Authority
WO
WIPO (PCT)
Prior art keywords
steam
gasifier
pressure
oxygen
ejector
Prior art date
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.)
Ceased
Application number
PCT/IB2011/054885
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English (en)
Other versions
WO2012073130A3 (fr
Inventor
Werner Siegfried Ernst
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sasol Technology Pty Ltd
Original Assignee
Sasol Technology Pty Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Sasol Technology Pty Ltd filed Critical Sasol Technology Pty Ltd
Publication of WO2012073130A2 publication Critical patent/WO2012073130A2/fr
Publication of WO2012073130A3 publication Critical patent/WO2012073130A3/fr
Priority to ZA2013/03923A priority Critical patent/ZA201303923B/en
Anticipated expiration legal-status Critical
Ceased 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
    • C10J3/72—Other features
    • C10J3/78—High-pressure apparatus
    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/06—Continuous processes
    • C10J3/16—Continuous processes simultaneously reacting oxygen and water with the carbonaceous material
    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • 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
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/156—Sluices, e.g. mechanical sluices for preventing escape of gas through the feed inlet
    • 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
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • 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
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • 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
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam

Definitions

  • THIS INVENTION relates to gasification of a carbonaceous material.
  • the invention relates to a method of operating a pressurized gasifier, to a method of upgrading a pressurized gasifier employing steam and oxygen, to a method of operating a gasifier upgraded in accordance with the invention, and to a pressurized gasifier.
  • pressurized gasifiers Numerous kinds of pressurized gasifiers are known in the art and it is recognized that, for pressurized gasifiers, higher operating gasification pressures generally increase the production capacity of the gasifiers.
  • Pressurized gasifiers typically employ a gasification agent comprising an admixture of oxygen and high pressure steam (often high pressure steam from a steam header and steam generated in a jacket of the gasifier itself).
  • the high pressure steam is available at a steam pressure which is higher than the oxygen pressure and the limit on the gasification agent pressure is therefore the oxygen pressure available at the gasification battery limit.
  • the mass flow rate of the steam is significantly higher than the mass flow rate of the oxygen to the gasifier.
  • the oxygen and steam are mixed by controlling the flow of steam and the flow of oxygen to a common mixing point.
  • the steam is available at a pressure significantly higher than that of the oxygen, as is often the case, the steam must be let down from a high pressure across a valve and the excess energy in the steam is not used to perform work.
  • the gasifier is a fixed bed dry bottom gasifier, also known as a moving bed dry ash gasifier, so that dry ash is removed from the gasification vessel.
  • the operating method of the invention is well-suited to gasifiers with a high steam requirement to moderate gasification temperatures, such as fixed bed gasifiers, and is thus unlikely to find application in the operation of gasifiers with a low steam requirement, such as entrained bed gasifiers. It may however be possible to employ the operating method of the invention with gasifiers with a moderate steam requirement, such as fluidized bed gasifiers.
  • the carbonaceous material may be any carbonaceous material suitable for gasification in a pressurized gasifier, particularly a fixed bed or fluidised bed gasifier, such as waste, biomass, petcoke or coal.
  • a pressurized gasifier particularly a fixed bed or fluidised bed gasifier, such as waste, biomass, petcoke or coal.
  • the carbonaceous material will be coal, e.g. lignite, bituminous coal or anthracite.
  • P1 is at least about 20 bar(g), more preferably between about 25 bar(g) and about 100 bar(g), e.g. about 29 bar(g).
  • P2 is at least about 35 bar(g), more preferably between about 45 bar(g) and about 170 bar(g), e.g. about 60 bar(g).
  • P3 is typically at least about 25 bar(g), more typically between about 28 bar(g) and about 1 10 bar(g), e.g. about 29 bar(g).
  • the method of the invention includes generating steam from heat provided by the gasification of the carbonaceous material in the gasifier.
  • the steam may for example be generated in a jacket of the gasification vessel of the gasifier.
  • the steam generated by the gasifier may be at a pressure P4, where P4 > P1 .
  • Steam generated by the gasifier may be used as temperature moderating agent and gasification agent in the gasification vessel.
  • the steam generated by the gasifier is thus mixed with an admixture of steam and oxygen from the steam ejector before being fed into the gasification vessel.
  • the method may include allowing some steam not generated by the gasifier to bypass the steam ejector.
  • steam bypassing the steam ejector is mixed with the steam generated from heat provided by the gasification of the carbonaceous material in the gasifier and is also mixed with the admixture of steam and oxygen from the steam ejector before being fed into the gasification vessel.
  • the method may include letting the steam pressure down, for example across a valve, to reduce the steam pressure to P2.
  • the amount by which the steam pressure will have to be let down for the method of the invention would be less than for a prior art gasification process in which a steam ejector is not used for feeding oxygen to the gasifier.
  • the method may include operating the gasification vessel at said pressure P1 , where said pressure P1 is higher than said pressure P3.
  • said pressure P1 may be between about 0.5 bar and about 1 .5 bar, typically between 0.9 bar and 1 .3 bar higher than said pressure P3.
  • a method of upgrading a pressurized gasifier employing steam and oxygen in a mass/volume ratio of at least 4.8 kg/m n 3 the method including
  • the gasifier may be as hereinbefore described, and may in particular be a fixed bed dry bottom gasifier.
  • the steam supply to the ejector is at a pressure of at least about 35 bar(g), more preferably between about 45 bar(g) and about 170 bar(g), e.g. about 60 bar(g).
  • the gaseous oxygen supply pressure to the steam ejector is typically at least 25 bar(g), more typically between about 28 bar(g) and about 1 10 bar(g), e.g. about 29 bar(g).
  • the gasification vessel may be a jacketed gasification vessel configured to generate steam from heat released during gasification of a carbonaceous material in the jacketed gasification vessel.
  • the method may include connecting the jacket of the gasification vessel in steam flow communication with said outlet of the steam ejector.
  • the invention extends to a method of operating a gasifier upgraded in accordance with the invention, the method including maintaining or operating the gasification vessel of the gasifier at its design operating pressure whilst reducing the oxygen supply pressure to the steam ejector, compared to the oxygen supply pressure to the gasifier prior to upgrading of the gasifier.
  • the invention further extends to a method of operating a gasifier upgraded in accordance with the invention, the method including operating the gasification vessel of the gasifier at a higher pressure than the operating pressure used for the gasification vessel of the gasifier prior to upgrading of the gasifier whilst maintaining the oxygen supply pressure to the steam ejector at least the same as or even higher than the oxygen supply pressure to the gasifier prior to upgrading of the gasifier.
  • the method may include applying a pressure gain of at least 0.5 bar to the oxygen supplied to the steam ejector, by means of the steam ejector.
  • the pressure gain is between 0.5 bar and 1 .5 bar, typically between 0.9 bar and 1 .3 bar.
  • a pressurized gasifier which includes
  • a gasification vessel which is a pressure vessel
  • a steam ejector in flow communication with a steam supply facility, the steam ejector being configured to use steam from the steam supply facility as a motive fluid, the steam ejector also being in flow communication with a gaseous oxygen supply facility and being configured to compress oxygen from the oxygen supply facility to a higher pressure and to deliver an admixture of steam and oxygen to the gasification vessel.
  • the gasifier may be as hereinbefore described, and may in particular be a fixed bed dry bottom gasifier.
  • the gasifier may be a jacketed gasifier configured to generate steam from heat released during gasification of a carbonaceous material.
  • the jacket of the gasifier may be in steam flow communication with an outlet of the steam ejector in use to add steam generated in the jacket to the admixture of steam and oxygen delivered by the steam ejector.
  • the oxygen supply facility may include an air separation plant or unit configured to produce gaseous oxygen at the battery limit of the air separation unit.
  • the gasifier may include a bypass line for steam from the steam supply facility to bypass the steam ejector before entering the gasification vessel.
  • the steam bypass line may be in flow communication with an outlet of the steam ejector, either directly or via a flow line which conveys a mixture of bypass steam and steam generated in the jacket.
  • Figure 1 shows a conventional fixed bed dry bottom gasifier employing an admixture of high pressure steam and oxygen as a gasification agent
  • Figure 2 shows a fixed bed dry bottom gasifier employing a steam ejector in accordance with an embodiment of the invention to provide an admixture of high pressure steam and oxygen as gasification agent to a gasification vessel.
  • reference numeral 10 generally indicates a conventional fixed bed dry bottom gasifier.
  • the gasifier 10 includes a coal lock 12, a gasification vessel 14 and an ash lock 16.
  • the gasification vessel 14 has a jacket (not shown) receiving high pressure boiler feed water by means of a boiler feed water line 18.
  • a jacket steam line 20 is provided to remove steam from the jacket.
  • a coal line 21 delivers coal to the coal lock 12, an ash line 23 removes ash from the ash lock 16 and a synthesis gas line 25 removes raw synthesis gas from the gasification vessel 14.
  • the high pressure steam line 22 is provided with a flow control valve 28 and the gaseous oxygen line 24 is provided with a flow control valve 30.
  • the jacket steam line 20 joins the high pressure steam line 22 downstream of the flow control valve 28.
  • a sized coal feed is fed by means of the coal line 21 into the gasification vessel 14 through the coal lock 12 and moves down through a bed formed inside the gasification vessel 14.
  • the coal feed has coal particles greater than 5mm.
  • Gasification agent comprising an admixture of oxygen and steam enters at a bottom of the bed through a rotating grate (not shown) from the gasification agent line 26.
  • Oxygen is required to combust some of the coal to supply energy for the endothermic gasification reactions.
  • Steam is required to moderate the temperatures inside the gasification vessel 14, as well as to act as gasification agent.
  • Part of the steam that is used is generated in the gasifier jacket from boiler feed water fed into the jacket by means of the boiler feed water line 18.
  • the steam generated in the gasifier jacket is saturated and has a pressure of about 29 bar(g) and the gaseous oxygen is available at a pressure of about 30 bar(g) and a temperature of about 1 10°C.
  • reaction zones are distinguishable from top to bottom, namely a drying zone where moisture is released, a devolatisation zone where pyrolysis takes place, a reduction zone or gasification zone where mainly endothermic reactions occur, an exothermic oxidation or combustion zone, and an ash bed at the bottom of the gasifier bed.
  • hot ash exchanges heat with cold incoming reagents, such as steam and oxygen, while at the same time hot raw gas, i.e. raw synthesis gas, exchanges heat with cold incoming coal.
  • tars, oils and pitches and the like are released. These pyrolysis products are not destroyed, in view of the relatively low operating temperature of the pressurized dry ash moving bed gasifier 10.
  • the pyrolysis products can be used to create valuable co-products, such as ammonia, sulphur, cresols and phenols. The following are some of the reactions that take place in the gasifier:
  • the temperature profile in the gasifier 10 varies between about 800°C and about 1350°C as the coal moves through the different zones in the gasification vessel 14.
  • the raw gas or raw synthesis gas stream in the synthesis gas line 25 leaves the gasification vessel 14 typically at a temperature between about 460°C and 600°C, but may be lower.
  • the maximum temperature in the gasification vessel 14 is limited by the ash fusion temperature of the coal feed as ash fusion creates removal problems of the ash at the bottom of the gasifier 10.
  • the high pressure steam in the high pressure steam line 22 is typically available at a much higher pressure than the gaseous oxygen pressure in the gaseous oxygen line 24.
  • the high pressure steam may be available at about 40 bar(g) whereas the gaseous oxygen is available at about 30 bar(g).
  • the high pressure steam is let down across the flow control valve 28 to about 29 bar(g).
  • the gaseous oxygen pressure is let down across the flow control valve 30 to about 29 bar(g) and the gasification agent formed by an admixture of the let down high pressure steam and the gaseous oxygen is then fed into the gasification vessel 14 at a pressure of about 29 bar(g), which is then also the operating pressure of the gasification vessel 14.
  • Steam generated in the jacket of the gasification vessel 14 is maintained at a pressure of about 29 bar(g) by being in flow communication with the let down high pressure steam downstream of the flow control valve 28 and the jacket steam from the jacket steam line 20 is thus fed with the let down high pressure steam and the gaseous oxygen as part of the gasification agent admixture into the gasification vessel 14.
  • FIG. 1 a fixed bed dry bottom gasifier upgraded in accordance with the invention, and operated in accordance with the invention, is shown and generally indicated by reference numeral 100.
  • the gasifier 100 is in many respects similar to the gasifier 10, the same components or features are indicated by the same reference numerals, unless otherwise indicated.
  • the gasifier 100 is provided with a steam ejector 102 (typically one of a few) downstream of the steam flow control valve 28 and the gaseous oxygen flow control valve 30.
  • a high pressure steam bypass line 104 with a steam flow control valve 106 is provided to allow for high pressure steam to bypass the steam ejector 102 and to be let down to a lower pressure.
  • the jacket steam line 20 and the high pressure steam bypass line 104 join the gasification agent line 26 downstream of the steam ejector 102.
  • the gasifier 100 is operated in similar fashion to the gasifier 10. However, an important difference is that the gaseous oxygen is supplied at a pressure of 29 bar(g) and not at a pressure of 30 bar(g), as is the case with the gasifier 10.
  • the high pressure steam, let down to a pressure P2 of about 39 bar(g) is supplied to the steam ejector 102 as a motive fluid and performs work in the steam ejector 102 to draw in the gaseous oxygen from the gaseous oxygen line 24 at a pressure P3 and to compress the gaseous oxygen to a pressure slightly higher than 29 bar(g).
  • a mixture of steam and gaseous oxygen thus exits the steam ejector 102 and this mixture is fed as the gasification agent by means of the gasification agent line 26 into the gasification vessel 14.
  • This mixture is at a pressure of about 29 bar(g), which is also the operating pressure P1 of the gasification vessel 14.
  • the flow of oxygen through the flow control valve 30 can be maintained even though the gaseous oxygen is supplied at a pressure of 29 bar(g) and not at a pressure of 30 bar(g).
  • Jacket steam at a pressure P4 of about 29 bar(g) from the jacket steam line 20 joins the gasification agent line 26, as is the case with the gasifier 10.
  • the gasifier 100 requires more steam than can be fed through the steam ejector(s) 102.
  • the additional high pressure steam is let down by means of the steam flow control valve 106 to a pressure of about 29 bar(g) and is fed into the gasification agent line 26 to form part of the gasification agent being fed into the gasification vessel 14.
  • the steam flow control valve 28 would not be required.
  • the steam flow through the steam ejector(s) 102 would remain fairly constant. Consequently, it would not be necessary to let the high pressure steam in the high pressure steam line 22 down to a lower pressure across the flow control valve 28, and thus the flow control valve 28 would not be required.
  • the total steam to the gasifier 100 would be controlled via the steam flow control valve 106. Should the flow of gaseous oxygen in the gaseous oxygen line 24 be reduced for any reason, the pressure increase of gaseous oxygen across the steam ejector 102 would simply be higher, thus resulting in the gasifier pressure P1 further being increased.
  • a steam ejector in accordance with the invention to provide gasification agent to a gasifier is ideally suited to gasifiers requiring a large ratio of steam to oxygen in the gasification agent, such as fixed bed and possibly fluidized bed gasifiers.
  • Table 1 reflects the differences between the operation of a conventional gasifier of the art as depicted in Figure 1 (the base case) and two simulated cases (case A and case B) of a gasifier operating in accordance with an embodiment of the invention as depicted in Figure 2.
  • Case A reflects the method of operating the gasifier by applying a pressure gain to the oxygen supplied to the steam ejector, by means of the steam ejector.
  • Case B reflects the method of operating the gasifier by maintaining or operating the gasification vessel of the gasifier at its design operating pressure whilst reducing the oxygen supply pressure to the steam ejector, compared to the oxygen supply pressure to the gasifier prior to upgrading of the gasifier. Table 1
  • the oxygen pressure increases were estimated using vendor-supplied tables for commercially available steam ejectors and the utility savings were determined by proprietary simulation models describing and predicting the operation of a Sasol® FBDBTM gasifier and associated systems.
  • the normalized steam and oxygen flows depicted in Table 1 reflect the ratios of the steam mass flow and oxygen mass flow to the base case steam mass flow and oxygen mass flow respectively.
  • the suction ratio is the ratio of the oxygen mass flow to the steam mass flow entering the steam ejector.
  • the same steam ejector 102 can also be employed in an alternative embodiment of the invention.
  • the gasifier operating pressure P1 is maintained at the design operating pressure of 30 bar(g), whilst the oxygen supply pressure P3 to the steam ejector is reduced to 28.9 bar(g), compared to the oxygen supply pressure of 30 bar(g) in the base case (i.e. prior to upgrading the gasifier).
  • the utility requirements e.g. compression and pumping duties
  • case selected for commercial implementation would be determined by the specific requirements of the facility. For example, should scope exist for greater production at higher gasifier pressures, case A would be selected. However, should there be no scope for pressure increase due, inter alia, to equipment design limitations, utility savings could still be realized in the air separation unit or plant through the implementation of case B.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

La présente invention concerne un procédé de mise en œuvre d'un réacteur de gazéification sous pression (100), comprenant les étapes consistant à introduire un matériau carboné (21) dans la cuve de gazéification sous pression (14) du réacteur de gazéification (100), alors que la cuve de gazéification est à une pression P1. De la vapeur (22) servant tout à la fois d'agent de modération de la température et d'agent de gazéification est introduite par un éjecteur à vapeur (102) dans la cuve de gazéification (14), la vapeur pénétrant dans l'éjecteur (102) sous une pression P2 et faisant office de fluide moteur pour l'éjecteur à vapeur (102). De l'oxygène (24) est également introduit dans la cuve de gazéification par l'intermédiaire de l'éjecteur à vapeur (102), l'oxygène pénétrant dans l'éjecteur à vapeur (102) sous une pression P3, et P2 > P1 > P3. Le matériau carboné est gazéifié en présence de vapeur et d'oxygène sous une pression P1, le processus produisant des cendres et du gaz de synthèse contenant au moins du CO et de l'H2, les cendres (23) et le gaz de synthèse (25) étant ensuite extraits de la cuve de gazéification.
PCT/IB2011/054885 2010-12-03 2011-11-03 Gazéification d'un matériau carboné Ceased WO2012073130A2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
ZA2013/03923A ZA201303923B (en) 2010-12-03 2013-05-29 Gasification of a carbonaceous material

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ZA2010/08724 2010-12-03
ZA201008724 2010-12-03

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Publication Number Publication Date
WO2012073130A2 true WO2012073130A2 (fr) 2012-06-07
WO2012073130A3 WO2012073130A3 (fr) 2012-08-30

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ZA (1) ZA201303923B (fr)

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CN110105985A (zh) * 2019-05-13 2019-08-09 安徽华尔泰化工股份有限公司 一种固定床造气增氧制气工艺
CN112707371A (zh) * 2021-02-27 2021-04-27 上海浦名能源科技有限公司 一种高温焦炉荒煤气加压直接水蒸汽重整制氢的装置及方法

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CA2596542C (fr) * 2005-02-01 2013-05-28 Sasol-Lurgi Technology Company (Proprietary) Limited Procede d'utilisation d'un reacteur de gazeification sec a lit fixe

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110105985A (zh) * 2019-05-13 2019-08-09 安徽华尔泰化工股份有限公司 一种固定床造气增氧制气工艺
CN112707371A (zh) * 2021-02-27 2021-04-27 上海浦名能源科技有限公司 一种高温焦炉荒煤气加压直接水蒸汽重整制氢的装置及方法

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CN102533338A (zh) 2012-07-04
WO2012073130A3 (fr) 2012-08-30
ZA201303923B (en) 2014-02-26

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