EP0400740A1 - Coal gasification reactor - Google Patents

Coal gasification reactor Download PDF

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Publication number
EP0400740A1
EP0400740A1 EP90201333A EP90201333A EP0400740A1 EP 0400740 A1 EP0400740 A1 EP 0400740A1 EP 90201333 A EP90201333 A EP 90201333A EP 90201333 A EP90201333 A EP 90201333A EP 0400740 A1 EP0400740 A1 EP 0400740A1
Authority
EP
European Patent Office
Prior art keywords
reactor
outlet
stack
quench
diameter ratio
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.)
Granted
Application number
EP90201333A
Other languages
German (de)
French (fr)
Other versions
EP0400740B1 (en
Inventor
Hendrikus Johannes Antonius Hasenack
Petrus H.W.M. Daverveldt
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.)
Shell Internationale Research Maatschappij BV
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Shell Internationale Research Maatschappij BV
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Publication of EP0400740A1 publication Critical patent/EP0400740A1/en
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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
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • C10J3/487—Swirling or cyclonic gasifiers
    • 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
    • C10J3/48—Apparatus; Plants
    • C10J3/50—Fuel charging devices
    • C10J3/506—Fuel charging devices for entrained flow gasifiers
    • 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
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1223—Heating the gasifier by burners
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only

Definitions

  • the present invention relates to a reactor for carrying out a partial oxidation process of a finely divided solid carbon-containing fuel and an oxidant.
  • 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.
  • 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.
  • 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.
  • the fuel is fed from a supply device to a gasifier by means of a suitable carrier fluid.
  • the hot product gas usually contains sticky particles which lose their stickiness upon cooling.
  • the sticky particles in the hot product gas will cause problems in the plant where the product gas is further processed, since undesirable deposits of the particles on, for example, walls, valves or outlets will adversely affect the process. Moreover, such deposits are very hard to remove.
  • the sticky particles may be partly or completely in the molten state; they may comprise metals, salts or ashes, and, in general, these particles lose their stickiness at a temperature below about 800 °C.
  • the hot product gas is quenched in a quench section which is located above the product outlet on top of the reactor.
  • a suitable quench medium such as for example water or a gas is introduced into the product gas in order to cool the product gas.
  • the invention therefore provides a reactor for carrying out a partial oxidation process of a finely divided solid carbon-containing fuel and an oxidant, said reactor comprising a reactor vessel having an outlet for the product gas at its top, a slag outlet at its bottom, a plurality of burner openings in its side wall, a plurality of tangentially directed burners located on the same horizontal level at circumferential spaced points, with a small firing angle, the reactor being provided with a quench above its outlet, wherein a stack having a predetermined length-to-diameter ratio is located between the reactor outlet and the quench inlet.
  • firing angle is defined as the angle between the symmetry axis of the burner jet and the line through the centre of the burner and the centre of the reactor at the same horizontal level.
  • a reactor vessel 1 has been shown.
  • the reactor vessel 1 is provided with a slag outlet 2 at its bottom, a plurality of tangenti­ally fired burners 3, a gas outlet 4 at its top and a quench system 5 comprising a quench inlet 5a above the reactor outlet 4.
  • the tangentially directed burners 3 are located on the same horizontal level at circum­ferental spaced points and cause vortex flow in the reactor vessel 1.
  • the quench system 5 is at its outlet 6 connected to equipment for further treating the synthesis gas. Such equipment is known to those skilled in the art and will not be described in detail.
  • equipment for further treating the synthesis gas.
  • Such equipment is known to those skilled in the art and will not be described in detail.
  • fig. 2 the same reference numerals have been used as in fig. 1.
  • the reactor 1 is provided with an extended pipe or stack 4a at its outlet 4. This extension is located between the reactor outlet 4 and the quench inlet 5a and has a predetermined length-to-diameter ratio Ls/Ds.
  • the quench system 5 is located remote from the reactor outlet.
  • Ls/Ds is 4 to 6 and more in particular Lq/Dq is 5 (as shown in fig. 2).
  • Fig. 3a represents a tangential burner arrangement comprising 4 burners A, B, C, D.
  • the burners are arranged horizontally and are directed to a central point E, which means that the firing angles are 0 degrees.
  • Fig. 3b represents a tangential burner arrangement of the invention comprising 4 burners A′, B′, C′, D′ wherein the firing angles are 5 degrees.
  • the firing angles according to the present invention are in the range of 3 to 5 degrees.
  • the burners are directed to a central circle E′ having a determined area.
  • the stack will also reduce the turbulence of the syngas. This reduction and the fact that the stack wall immediately below the quench inlet is vertical and thus much steeper than the reactor roof in fig. 1 will be beneficial to prevent slag lifting or slag entrainment.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The slagging efficiency of a coal gasification process is increased to 90% by tangential firing at small angles and the installation of a stack of specific length over diameter ratio between the reactor outlet and the quench inlet. In this manner slag lifting and slag entrainment at the quench inlet - stack outlet are prevented.

Description

  • The present invention relates to a reactor for carrying out a partial oxidation process of a finely divided solid carbon-containing fuel and an oxidant.
  • 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.
  • The hot product gas usually contains sticky particles which lose their stickiness upon cooling.
  • The sticky particles in the hot product gas will cause problems in the plant where the product gas is further processed, since undesirable deposits of the particles on, for example, walls, valves or outlets will adversely affect the process. Moreover, such deposits are very hard to remove. The sticky particles may be partly or completely in the molten state; they may comprise metals, salts or ashes, and, in general, these particles lose their stickiness at a temperature below about 800 °C.
  • Therefore, the hot product gas is quenched in a quench section which is located above the product outlet on top of the reactor. In the quench section a suitable quench medium such as for example water or a gas is introduced into the product gas in order to cool the product gas.
  • It is known to apply tangentially fired burners in partial oxidation processes of finely divided solid carbon-containing fuels, i.e. a plurality of tangenti­ally directed burners are located on the same horizontal level at circumferential spaced points of the wall of the reactor vessel and cause vortex flow in the reactor.
  • It has now appeared, however, that present reactor designs still have some disadvantages: the slagging efficiency is rather small (40-50%); there is a possibility for slag lifting to occur at the reactor outlet and short-circuiting of hot synthesis gas out of the reactor into the quench may occur.
  • It is an object of the invention to provide a reactor design which has a slagging efficiency of 90-95%.
  • It is another object of the invention to provide a reactor design wherein slag lifting and slag droplet entrainment is prevented.
  • It is still another object of the invention to provide a reactor design wherein said short-circuiting of synthesis gas is prevented.
  • The invention therefore provides a reactor for carrying out a partial oxidation process of a finely divided solid carbon-containing fuel and an oxidant, said reactor comprising a reactor vessel having an outlet for the product gas at its top, a slag outlet at its bottom, a plurality of burner openings in its side wall, a plurality of tangentially directed burners located on the same horizontal level at circumferential spaced points, with a small firing angle, the reactor being provided with a quench above its outlet, wherein a stack having a predetermined length-to-diameter ratio is located between the reactor outlet and the quench inlet.
  • The term firing angle is defined as the angle between the symmetry axis of the burner jet and the line through the centre of the burner and the centre of the reactor at the same horizontal level.
  • The invention will now be described by way of example in more detail by reference to the accompanying drawings, in which:
    • - fig. 1 represents schematically a longitudinal section of a conventional reactor and quench section;
    • - fig. 2 represents schematically a longitudinal section of a reactor design of the invention;
    • - fig. 3a represents a cross-section along the lines I-I of fig. 1, and
    • - fig. 3b represents a cross-section along the lines II-II of fig. 2.
  • Referring now to fig. 1, a reactor vessel 1 has been shown. The reactor vessel 1 is provided with a slag outlet 2 at its bottom, a plurality of tangenti­ally fired burners 3, a gas outlet 4 at its top and a quench system 5 comprising a quench inlet 5a above the reactor outlet 4. The tangentially directed burners 3 are located on the same horizontal level at circum­ferental spaced points and cause vortex flow in the reactor vessel 1.
  • The quench system 5 is at its outlet 6 connected to equipment for further treating the synthesis gas. Such equipment is known to those skilled in the art and will not be described in detail. In fig. 2 the same reference numerals have been used as in fig. 1.
  • In fig. 2 the reactor 1 is provided with an extended pipe or stack 4a at its outlet 4. This extension is located between the reactor outlet 4 and the quench inlet 5a and has a predetermined length-to-diameter ratio Ls/Ds.
  • The quench system 5 is located remote from the reactor outlet. Advantageously, Ls/Ds is 4 to 6 and more in particular Lq/Dq is 5 (as shown in fig. 2).
  • Further, in fig. 2, the quench system 5 has a length-to-diameter ratio Lg/Dg = 3 and the reactor 1 has a length-to-diameter ratio Lr/Dr = 3.
  • Fig. 3a represents a tangential burner arrangement comprising 4 burners A, B, C, D. The burners are arranged horizontally and are directed to a central point E, which means that the firing angles are 0 degrees.
  • Fig. 3b represents a tangential burner arrangement of the invention comprising 4 burners A′, B′, C′, D′ wherein the firing angles are 5 degrees. Advan­tageously, the firing angles according to the present invention are in the range of 3 to 5 degrees. The burners are directed to a central circle E′ having a determined area.
  • When the reactor design of the invention is used, large centrifugal forces inside the stack will cause a large settling velocity and thus a large slagging efficiency, since most of the slag will be deposited in the lower part of the pipe extension, it is possible to decrease the swirl of the product gas by either installing cross hairs or by a further narrowing of the pipe. This will prevent cold syngas from re-entering the reactor.
  • The stack will also reduce the turbulence of the syngas. This reduction and the fact that the stack wall immediately below the quench inlet is vertical and thus much steeper than the reactor roof in fig. 1 will be beneficial to prevent slag lifting or slag entrainment.
  • Finally the stack will reduce flow short-­circuiting. Thus the breakthrough times toward the reactor outlet increase. Consequently the conversion is enhanced and the outlet temperature may decrease.
  • Various modifications of the present 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 (5)

1. A reactor for carrying out a partial oxidation process of a finely divided solid carbon-containing fuel and an oxidant, said reactor comprising a reactor vessel having an outlet for the product gas at its top, a slag outlet at its bottom, a plurality of burner openings in its side wall, a plurality of tangentially directed burners located on the same horizontal level at circumferential spaced points, with a small firing angle, the reactor being provided with a quench above its outlet, wherein a stack having a predetermined length-to-diameter ratio is located between the reactor outlet and the quench inlet.
2. The reactor as claimed in claim 1 wherein the stack has a length-to-diameter ratio of 4 to 6.
3. The reactor as claimed in claim 2 wherein the stack has a length-to-diameter ratio of 5.
4. The reactor as claimed in any one of claims 1-3 wherein the firing angle is 3 to 5 degrees.
5. Reactor for carrying out a partial oxidation process of a finely divided solid carbon-containing fuel and an oxidant, substantially as described in the specification by reference to fig. 2 and 3B of the accompanying drawings.
EP90201333A 1989-05-30 1990-05-23 Coal gasification reactor Expired - Lifetime EP0400740B1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB898912316A GB8912316D0 (en) 1989-05-30 1989-05-30 Coal gasification reactor
GB8912316 1989-05-30

Publications (2)

Publication Number Publication Date
EP0400740A1 true EP0400740A1 (en) 1990-12-05
EP0400740B1 EP0400740B1 (en) 1994-08-03

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EP90201333A Expired - Lifetime EP0400740B1 (en) 1989-05-30 1990-05-23 Coal gasification reactor

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EP (1) EP0400740B1 (en)
JP (1) JP2932198B2 (en)
CN (1) CN1025345C (en)
AU (1) AU618195B2 (en)
CA (1) CA2017635C (en)
DE (1) DE69011216T2 (en)
DK (1) DK0400740T3 (en)
ES (1) ES2058754T3 (en)
GB (1) GB8912316D0 (en)
ZA (1) ZA904064B (en)

Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0699734A1 (en) * 1994-08-31 1996-03-06 Mitsubishi Jukogyo Kabushiki Kaisha Coal firing device
WO2006117355A1 (en) 2005-05-02 2006-11-09 Shell Internationale Research Maatschappij B.V. Method and system for producing synthesis gas
EP1918352A1 (en) 2006-11-01 2008-05-07 Shell Internationale Researchmaatschappij B.V. Solid carbonaceous feed to liquid process
DE102007027601A1 (en) 2007-06-12 2008-12-18 Uhde Gmbh Production and cooling of gaseous coal gasification products
WO2009130292A2 (en) * 2008-04-24 2009-10-29 Shell Internationale Research Maatschappij B.V. Process to prepare an olefin-containing product or a gasoline product
WO2009118082A3 (en) * 2008-03-27 2010-01-07 Uhde Gmbh Device for producing synthesis gas with a gasification reactor and connecting quenching chamber
US7741377B2 (en) 2006-11-01 2010-06-22 Shell Oil Company Solid carbonaceous feed to liquid process
US20110174683A1 (en) * 2008-10-09 2011-07-21 Synfuels China Co., Ltd Method and equipment for multistage liquefying of carbonaceous solid fuel
US8012436B2 (en) 2007-09-04 2011-09-06 Shell Oil Company Quenching vessel
US8048178B2 (en) 2007-11-20 2011-11-01 Shell Oil Company Process for producing a purified synthesis gas stream
US8083815B2 (en) 2008-12-22 2011-12-27 Shell Oil Company Process to prepare methanol and/or dimethylether
US8182561B2 (en) 2008-01-16 2012-05-22 Shell Oil Company Process to provide a particulate solid material to a pressurised reactor
US8308983B2 (en) 2008-10-08 2012-11-13 Shell Oil Company Process to prepare a gas mixture of hydrogen and carbon monoxide
US8360342B2 (en) 2010-04-30 2013-01-29 General Electric Company Fuel injector having differential tip cooling system and method
US8444061B2 (en) 2007-09-04 2013-05-21 Shell Oil Company Spray nozzle manifold
US8490635B2 (en) 2008-09-01 2013-07-23 Shell Oil Company Self cleaning nozzle arrangement
US9079199B2 (en) 2010-06-14 2015-07-14 General Electric Company System for increasing the life of fuel injectors
US9890341B2 (en) 2007-09-18 2018-02-13 Thyssenkrupp Industrial Solutions Ag Gasification reactor and process for entrained-flow gasification
DE102008057410B4 (en) 2008-11-14 2019-07-04 Thyssenkrupp Industrial Solutions Ag Apparatus for the production of synthesis gas with a gasification reactor followed by quenching

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CN101003755B (en) * 2006-01-19 2010-09-29 神华集团有限责任公司 Gasification stove with multi nozzle, and gasification method
US9051522B2 (en) 2006-12-01 2015-06-09 Shell Oil Company Gasification reactor
DE102006059149B4 (en) 2006-12-14 2009-06-25 Siemens Ag Residual flow reactor for the gasification of solid and liquid energy sources
DE102007044726A1 (en) 2007-09-18 2009-03-19 Uhde Gmbh Synthesis gas producing method, involves drying and cooling synthesis gas in chamber, arranging water bath below another chamber, and extracting produced and cooled synthesis gas from pressure container below or lateral to latter chamber
DE102008012734A1 (en) 2008-03-05 2009-09-10 Uhde Gmbh Method for obtaining synthesis gas by gasification of liquid or finely comminuted solid fuels, involves producing synthesis gas in reaction chamber arranged over reactor, in which ingredients are supplied
DE102008015801B4 (en) 2008-03-27 2019-02-28 Thyssenkrupp Industrial Solutions Ag Apparatus for the production of synthesis gas with a gasification reactor followed by a quenching chamber
DE102009005464A1 (en) 2009-01-21 2010-08-05 Uhde Gmbh Device for producing crude gas containing carbon monoxide or hydrogen by gasification of an ash-containing fuel with oxygen-containing gas in a gasification reactor, comprises connected gas cooling chamber, and tapered connecting channel
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US8960651B2 (en) 2008-12-04 2015-02-24 Shell Oil Company Vessel for cooling syngas

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GB718410A (en) * 1953-01-05 1954-11-10 Babcock & Wilcox Co Method of and apparatus for gasification of a solid fuel containing carbon
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GB718410A (en) * 1953-01-05 1954-11-10 Babcock & Wilcox Co Method of and apparatus for gasification of a solid fuel containing carbon
GB840699A (en) * 1958-06-20 1960-07-06 Sumitomo Chemical Co Method of gasifying pulverised coal in vortex flow
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US5755165A (en) * 1994-08-31 1998-05-26 Mitsubishi Jukogyo Kabushiki Kaisha Coal firing device
EP0699734A1 (en) * 1994-08-31 1996-03-06 Mitsubishi Jukogyo Kabushiki Kaisha Coal firing device
US8685119B2 (en) 2005-05-02 2014-04-01 Shell Oil Company Method and system for producing synthesis gas, gasification reactor, and gasification system
WO2006117355A1 (en) 2005-05-02 2006-11-09 Shell Internationale Research Maatschappij B.V. Method and system for producing synthesis gas
EP1918352A1 (en) 2006-11-01 2008-05-07 Shell Internationale Researchmaatschappij B.V. Solid carbonaceous feed to liquid process
US7741377B2 (en) 2006-11-01 2010-06-22 Shell Oil Company Solid carbonaceous feed to liquid process
CN101200650B (en) * 2006-11-01 2012-01-18 国际壳牌研究有限公司 Method of solid carbonaceous feed to liquid process
DE102007027601A1 (en) 2007-06-12 2008-12-18 Uhde Gmbh Production and cooling of gaseous coal gasification products
US8012436B2 (en) 2007-09-04 2011-09-06 Shell Oil Company Quenching vessel
US8444061B2 (en) 2007-09-04 2013-05-21 Shell Oil Company Spray nozzle manifold
US9890341B2 (en) 2007-09-18 2018-02-13 Thyssenkrupp Industrial Solutions Ag Gasification reactor and process for entrained-flow gasification
US8048178B2 (en) 2007-11-20 2011-11-01 Shell Oil Company Process for producing a purified synthesis gas stream
US9149779B2 (en) 2008-01-16 2015-10-06 Shell Oil Company Process to provide a particulate solid material to a pressurised reactor
EP2764910A2 (en) 2008-01-16 2014-08-13 Shell Internationale Research Maatschappij B.V. System to provide a particulate solid material to a pressurised reactor
US8182561B2 (en) 2008-01-16 2012-05-22 Shell Oil Company Process to provide a particulate solid material to a pressurised reactor
US8562698B2 (en) 2008-03-27 2013-10-22 Thyssenkrupp Uhde Gmbh Device for production of synthesis gas with a gasification reactor with a subsequent quenching space
RU2482165C2 (en) * 2008-03-27 2013-05-20 Тиссенкрупп Уде Гмбх Device for obtaining synthesis gas with reactor-gasifier and adjacent quick cooling chamber
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WO2009130292A3 (en) * 2008-04-24 2010-01-21 Shell Internationale Research Maatschappij B.V. Process to prepare an olefin-containing product or a gasoline product
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CN1047688A (en) 1990-12-12
AU618195B2 (en) 1991-12-12
DE69011216D1 (en) 1994-09-08
CN1025345C (en) 1994-07-06
GB8912316D0 (en) 1989-07-12
DK0400740T3 (en) 1994-08-29
ES2058754T3 (en) 1994-11-01
DE69011216T2 (en) 1995-02-16
JP2932198B2 (en) 1999-08-09
JPH0324195A (en) 1991-02-01
ZA904064B (en) 1991-02-27
EP0400740B1 (en) 1994-08-03
AU5602290A (en) 1990-12-06
CA2017635A1 (en) 1990-11-30
CA2017635C (en) 2000-05-09

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