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
- 239000003245 coal Substances 0.000 title abstract description 5
- 238000002309 gasification Methods 0.000 title abstract description 5
- 238000010791 quenching Methods 0.000 claims abstract description 22
- 239000002893 slag Substances 0.000 claims abstract description 15
- 238000010304 firing Methods 0.000 claims abstract description 8
- 238000000034 method Methods 0.000 claims abstract description 8
- 229910052799 carbon Inorganic materials 0.000 claims description 11
- 239000000446 fuel Substances 0.000 claims description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 10
- 239000007787 solid Substances 0.000 claims description 10
- 230000003647 oxidation Effects 0.000 claims description 5
- 238000007254 oxidation reaction Methods 0.000 claims description 5
- 239000007800 oxidant agent Substances 0.000 claims description 3
- 230000001590 oxidative effect Effects 0.000 claims description 3
- 210000004209 hair Anatomy 0.000 claims description 2
- 238000009434 installation Methods 0.000 abstract 1
- 238000009491 slugging Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 23
- 230000015572 biosynthetic process Effects 0.000 description 8
- 238000003786 synthesis reaction Methods 0.000 description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- 238000002485 combustion reaction Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000000171 quenching effect Effects 0.000 description 2
- 239000004449 solid propellant Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 235000002918 Fraxinus excelsior Nutrition 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000003077 lignite Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000003415 peat Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
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)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (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 |
| WO2006117355A1 (en) | 2005-05-02 | 2006-11-09 | Shell Internationale Research Maatschappij B.V. | 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 |
| 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 |
| 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 |
| US8012436B2 (en) | 2007-09-04 | 2011-09-06 | Shell Oil Company | Quenching vessel |
| AU2008294832B2 (en) | 2007-09-04 | 2011-05-19 | Air Products And Chemicals, Inc. | Spray nozzle manifold and process for quenching a hot gas using such an arrangement |
| 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 |
| KR101568433B1 (en) | 2007-09-18 | 2015-11-11 | 티센크루프 인더스트리얼 솔루션스 아게 | Gasification reactor and method for entrained-flow gasification |
| 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 |
| US8048178B2 (en) | 2007-11-20 | 2011-11-01 | Shell Oil Company | Process for producing a purified synthesis gas stream |
| WO2009090216A2 (en) | 2008-01-16 | 2009-07-23 | Shell Internationale Research Maatschappij B.V. | Process to provide a particulate solid material to a pressurised reactor |
| 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 |
| 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 |
| 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 |
| 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 |
| CN102046566B (en) * | 2008-04-24 | 2014-10-01 | 国际壳牌研究有限公司 | Process for the preparation of olefin-containing products or gasoline products |
| EP2133414A1 (en) * | 2008-06-11 | 2009-12-16 | Basf Se | Uses and methods for preventing and /or treating oral malodour |
| CN102171314B (en) | 2008-09-01 | 2013-07-24 | 国际壳牌研究有限公司 | Self cleaning arrangement |
| EP2334765A2 (en) | 2008-10-08 | 2011-06-22 | Shell Internationale Research Maatschappij B.V. | Process to prepare a gas mixture of hydrogen and carbon monoxide |
| AU2009301573B2 (en) * | 2008-10-09 | 2013-09-26 | Synfuels China Technology Co., Ltd. | Method and equipment for multistage liquefying of carbonaceous solid fuel |
| US8960651B2 (en) | 2008-12-04 | 2015-02-24 | Shell Oil Company | Vessel for cooling syngas |
| AU2009331847B2 (en) | 2008-12-22 | 2012-06-07 | Air Products And Chemicals, Inc. | 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 |
| GB840700A (en) * | 1958-06-20 | 1960-07-06 | Sumitomo Chemical Co | A method of gasifying pulverised coal |
| GB840699A (en) * | 1958-06-20 | 1960-07-06 | Sumitomo Chemical Co | Method of gasifying pulverised coal in vortex flow |
| 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 DK DK90201333.3T patent/DK0400740T3/en active
- 1990-05-23 EP EP90201333A patent/EP0400740B1/en not_active Expired - Lifetime
- 1990-05-23 DE DE69011216T patent/DE69011216T2/en not_active Expired - Fee Related
- 1990-05-28 CA CA002017635A patent/CA2017635C/en not_active Expired - Lifetime
- 1990-05-28 CN CN90103807A patent/CN1025345C/en not_active Expired - Lifetime
- 1990-05-28 AU AU56022/90A patent/AU618195B2/en not_active Ceased
- 1990-05-28 ZA ZA904064A patent/ZA904064B/en unknown
- 1990-05-28 JP JP2135525A patent/JP2932198B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| DE69011216T2 (en) | 1995-02-16 |
| CA2017635A1 (en) | 1990-11-30 |
| JP2932198B2 (en) | 1999-08-09 |
| ZA904064B (en) | 1991-02-27 |
| CN1047688A (en) | 1990-12-12 |
| EP0400740A1 (en) | 1990-12-05 |
| EP0400740B1 (en) | 1994-08-03 |
| AU618195B2 (en) | 1991-12-12 |
| GB8912316D0 (en) | 1989-07-12 |
| CN1025345C (en) | 1994-07-06 |
| ES2058754T3 (en) | 1994-11-01 |
| AU5602290A (en) | 1990-12-06 |
| DE69011216D1 (en) | 1994-09-08 |
| JPH0324195A (en) | 1991-02-01 |
| DK0400740T3 (en) | 1994-08-29 |
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| EEER | Examination request | ||
| MKLA | Lapsed | ||
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Effective date: 20121202 |