CA2017635C - Coal gasification reactor - Google Patents
Coal gasification reactor Download PDFInfo
- Publication number
- CA2017635C CA2017635C CA002017635A CA2017635A CA2017635C CA 2017635 C CA2017635 C CA 2017635C CA 002017635 A CA002017635 A CA 002017635A CA 2017635 A CA2017635 A CA 2017635A CA 2017635 C CA2017635 C CA 2017635C
- Authority
- CA
- Canada
- Prior art keywords
- reactor
- outlet
- quench
- stack
- slag
- 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.)
- Expired - Lifetime
Links
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
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The slugging 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
2~1'~Ea COAL GASIFICATION REACTOR
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 2o 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 3o are steam and carbon dioxide.
201'i f The gasification is advantageously carried out at a temperature in the range from 1200 to 3700 °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.
~t11'if~ a It is known to apply tangentially fired burners in partial oxidation processes of finely divided solid carbon-containing fuels, i.e. a plurality of tangenti-ally 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.
20~~0~~
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 2o 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 3o are steam and carbon dioxide.
201'i f The gasification is advantageously carried out at a temperature in the range from 1200 to 3700 °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.
~t11'if~ a It is known to apply tangentially fired burners in partial oxidation processes of finely divided solid carbon-containing fuels, i.e. a plurality of tangenti-ally 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.
20~~0~~
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. l, a reactor vessel 1 has been shown. The reactor vessel 1 is provided with a slag outlet 2 at its bottom, a plurality of tangenti-ally fired burners 3, a gas outlet 4 at its top and a 2o 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 circum-ferental spaced points and cause vortex flow in the reactor vessel 1.
25 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.
30 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.
20~.'~6~
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. l, a reactor vessel 1 has been shown. The reactor vessel 1 is provided with a slag outlet 2 at its bottom, a plurality of tangenti-ally fired burners 3, a gas outlet 4 at its top and a 2o 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 circum-ferental spaced points and cause vortex flow in the reactor vessel 1.
25 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.
30 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.
20~.'~6~
The quench system 5 is located remote from the reactor outlet. Advantageously, Ls/Ds is 4 to 6 and more in particular Ls/Ds is 5 (as shown in fig. 2).
Further, in fig. 2, the quench system 5 has a length-to-diameter ratio Lq/Dq = 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. Advan-tageously, 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 ' ~,0~.'a ~~ a 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.
Further, in fig. 2, the quench system 5 has a length-to-diameter ratio Lq/Dq = 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. Advan-tageously, 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 ' ~,0~.'a ~~ a 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 (4)
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 a top, a bottom and a side wall, a reactor outlet for the product gas at said top, a slag outlet at said bottom, a plurality of burner openings in said side wall, and 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 said reactor outlet, said quench having a quench inlet and wherein a stack having a length-to-diameter ratio of 4 to 6:1 is located between the reactor outlet and the quench inlet.
a reactor vessel having a top, a bottom and a side wall, a reactor outlet for the product gas at said top, a slag outlet at said bottom, a plurality of burner openings in said side wall, and 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 said reactor outlet, said quench having a quench inlet and wherein a stack having a length-to-diameter ratio of 4 to 6:1 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 5:1.
3. The reactor as claimed in claim 1 or 2, wherein the firing angle is 3 to 5 degrees.
4. The reactor as claimed in claim 1, 2 or 3, wherein cross hairs are installed in the stack.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB8912316.0 | 1989-05-30 | ||
| GB898912316A GB8912316D0 (en) | 1989-05-30 | 1989-05-30 | Coal gasification reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2017635A1 CA2017635A1 (en) | 1990-11-30 |
| CA2017635C true CA2017635C (en) | 2000-05-09 |
Family
ID=10657536
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002017635A Expired - Lifetime CA2017635C (en) | 1989-05-30 | 1990-05-28 | Coal gasification reactor |
Country Status (10)
| Country | Link |
|---|---|
| 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) |
Families Citing this family (28)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3364013B2 (en) * | 1994-08-31 | 2003-01-08 | 三菱重工業株式会社 | Coal combustor |
| CN101166813B (en) | 2005-05-02 | 2011-11-23 | 国际壳牌研究有限公司 | Method and system for producing synthesis gas |
| 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 |
| AU2007231719B2 (en) | 2006-11-01 | 2012-02-02 | Air Products And Chemicals, Inc. | Solid carbonaceous feed to liquid process |
| EP1918352B1 (en) | 2006-11-01 | 2009-12-09 | Shell Internationale Researchmaatschappij B.V. | Solid carbonaceous feed to liquid process |
| 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 |
| DE102007027601A1 (en) | 2007-06-12 | 2008-12-18 | Uhde Gmbh | Production and cooling of gaseous coal gasification products |
| WO2009030674A2 (en) | 2007-09-04 | 2009-03-12 | Shell Internationale Research Maatschappij B.V. | Quenching vessel |
| ES2384130T3 (en) | 2007-09-04 | 2012-06-29 | Shell Internationale Research Maatschappij B.V. | Spray nozzle manifold and process for cooling a hot gas using such an arrangement |
| 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 |
| CA2699714C (en) | 2007-09-18 | 2016-04-19 | Uhde Gmbh | Gasification reactor and process for entrained-flow gasification |
| 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 |
| EP2222595B1 (en) | 2007-11-20 | 2011-07-06 | Shell Internationale Research Maatschappij B.V. | Process for producing a purified synthesis gas stream |
| EP2764910B1 (en) | 2008-01-16 | 2019-02-27 | Air Products and Chemicals, Inc. | System to start-up a process for providing a particulate solid material to a pressurised reactor |
| 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 |
| 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 |
| CA2719230C (en) | 2008-03-27 | 2016-02-16 | Uhde Gmbh | Device for production of synthesis gas with a gasification reactor with a subsequent quenching space |
| 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 |
| EP2133414A1 (en) * | 2008-06-11 | 2009-12-16 | Basf Se | Uses and methods for preventing and /or treating oral malodour |
| WO2010023306A2 (en) | 2008-09-01 | 2010-03-04 | Shell Internationale Research Maatschappij B.V. | Self cleaning arrangement |
| WO2010040764A2 (en) | 2008-10-08 | 2010-04-15 | Shell Internationale Research Maatschappij B.V. | Process to prepare a gas mixture of hydrogen and carbon monoxide |
| RU2460757C1 (en) * | 2008-10-09 | 2012-09-10 | Синфьюэлс Чайна Текнолоджи Ко., Лтд. | Method and equipment for multi-stage liquefying of carbon-containing solid fuel |
| US8960651B2 (en) | 2008-12-04 | 2015-02-24 | Shell Oil Company | Vessel for cooling syngas |
| EP2373602B1 (en) | 2008-12-22 | 2013-08-21 | Shell Internationale Research Maatschappij B.V. | Process to prepare methanol and/or dimethylether |
| US8360342B2 (en) | 2010-04-30 | 2013-01-29 | General Electric Company | Fuel injector having differential tip cooling system and method |
| US9079199B2 (en) | 2010-06-14 | 2015-07-14 | General Electric Company | System for increasing the life of fuel injectors |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE911313C (en) * | 1943-11-21 | 1954-05-13 | Koppers Gmbh Heinrich | Device for gasifying dust-like or fine-grain fuels |
| 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 |
| GB840700A (en) * | 1958-06-20 | 1960-07-06 | Sumitomo Chemical Co | A method of gasifying pulverised coal |
| EP0050863A1 (en) * | 1980-10-24 | 1982-05-05 | Hitachi, Ltd. | Process of and apparatus for gasifying coals |
-
1989
- 1989-05-30 GB GB898912316A patent/GB8912316D0/en active Pending
-
1990
- 1990-05-23 ES ES90201333T patent/ES2058754T3/en not_active Expired - Lifetime
- 1990-05-23 EP EP90201333A patent/EP0400740B1/en not_active Expired - Lifetime
- 1990-05-23 DK DK90201333.3T patent/DK0400740T3/en active
- 1990-05-23 DE DE69011216T patent/DE69011216T2/en not_active Expired - Fee Related
- 1990-05-28 CN CN90103807A patent/CN1025345C/en not_active Expired - Lifetime
- 1990-05-28 JP JP2135525A patent/JP2932198B2/en not_active Expired - Lifetime
- 1990-05-28 ZA ZA904064A patent/ZA904064B/en unknown
- 1990-05-28 CA CA002017635A patent/CA2017635C/en not_active Expired - Lifetime
- 1990-05-28 AU AU56022/90A patent/AU618195B2/en not_active Ceased
Also Published As
| Publication number | Publication date |
|---|---|
| AU5602290A (en) | 1990-12-06 |
| GB8912316D0 (en) | 1989-07-12 |
| AU618195B2 (en) | 1991-12-12 |
| JPH0324195A (en) | 1991-02-01 |
| JP2932198B2 (en) | 1999-08-09 |
| DE69011216D1 (en) | 1994-09-08 |
| EP0400740A1 (en) | 1990-12-05 |
| CA2017635A1 (en) | 1990-11-30 |
| ZA904064B (en) | 1991-02-27 |
| DE69011216T2 (en) | 1995-02-16 |
| CN1025345C (en) | 1994-07-06 |
| CN1047688A (en) | 1990-12-12 |
| DK0400740T3 (en) | 1994-08-29 |
| ES2058754T3 (en) | 1994-11-01 |
| EP0400740B1 (en) | 1994-08-03 |
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