EP0021461A1 - Process and burner for the gasification of solid fuel - Google Patents
Process and burner for the gasification of solid fuel Download PDFInfo
- Publication number
- EP0021461A1 EP0021461A1 EP80200355A EP80200355A EP0021461A1 EP 0021461 A1 EP0021461 A1 EP 0021461A1 EP 80200355 A EP80200355 A EP 80200355A EP 80200355 A EP80200355 A EP 80200355A EP 0021461 A1 EP0021461 A1 EP 0021461A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- burner
- gas
- oxygen
- fuel
- moderator
- 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
Links
- 238000000034 method Methods 0.000 title claims abstract description 26
- 239000004449 solid propellant Substances 0.000 title claims abstract description 14
- 238000002309 gasification Methods 0.000 title description 7
- 239000007789 gas Substances 0.000 claims abstract description 67
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 42
- 239000001301 oxygen Substances 0.000 claims abstract description 42
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 42
- 239000000446 fuel Substances 0.000 claims abstract description 35
- 239000012159 carrier gas Substances 0.000 claims abstract description 16
- 239000001257 hydrogen Substances 0.000 claims abstract description 9
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 9
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 8
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 8
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 8
- 238000002485 combustion reaction Methods 0.000 claims abstract description 5
- 238000002360 preparation method Methods 0.000 claims description 2
- 239000000376 reactant Substances 0.000 abstract 1
- 238000002156 mixing Methods 0.000 description 8
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 239000003245 coal Substances 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 238000013021 overheating Methods 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 3
- 230000006698 induction Effects 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229920001131 Pulp (paper) Polymers 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000003077 lignite Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 230000002028 premature Effects 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 230000008961 swelling Effects 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 235000013311 vegetables Nutrition 0.000 description 1
Images
Classifications
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- 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
- C10J3/74—Construction of shells or jackets
-
- 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
- C10J3/74—Construction of shells or jackets
- C10J3/76—Water jackets; Steam boiler-jackets
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/78—High-pressure apparatus
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- 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
- C10J2300/0916—Biomass
- C10J2300/092—Wood, cellulose
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0956—Air or oxygen enriched air
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
-
- 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 invention relates to the gasification of finely divided solid fuel.
- This gasification - also known as partial combustion - is carried out by reaction of solid fuel with an oxygen-containing gas.
- the fuel contains as useful components mainly carbon and hydrogen, which react with the oxygen - and possibly with steam and carbon dioxide - to form carbon monoxide and hydrogen. Depending on the temperature, the formation of methane is also possible.
- the oxygen-containing gas is usually air or oxygen or a mixture thereof.
- coal particles are contacted with the oxygen-containing gas in a reactor in a fixed or fluidized bed at temperatures below 1000 o C.
- the residence time of the coal particles is relatively long (certainly more than one minute).
- a drawback of said processes is that not all types of solid fuel can be gasified in this manner, which limits the flexibility of said processes.
- Highly swelling coal, for example, is unsuitable because it sinters together and clogs the reactor. In some cases the high yield of methane of said processes is a disadvantage.
- the fuel is usually passed in a carrier gas to the reactor through the burner, while the oxygen-containing gas is also passed to the reactor through the burner. Since the solid fuel, even if it is finely divided, is usually less reactive than liquid or gaseous fuel (it cannot be atomized by the burner) great care is bestowed on the manner in which the fuel and oxygen are mixed. When the mixing in the reactor is insufficient, zones of underheating occur in the reactor next to zones of overheating, since part of the fuel does not receive enough oxygen and an other part of the fuel receives too much oxygen. Part of the fuel is then not fully gasified and an other part is converted completely into carbon dioxide and water vapour. A drawback of locally high temperatures in the reactor is that damage is caused to the refractory lining which is usually provided therein.
- a water vapour-containing moderator gas is often supplied to the reactor.
- the water vapour reacts with part of the fuel, with the formation of hydrogen and carbon monoxide.
- the reaction in question is endothermic.
- the moderator gas can be supplied to the reactor through the burner or otherwise.
- the fuel is supplied in a carrier gas
- that the fuel load of the carrier gas must be high to ensure that the carrier gas does not constitute an excessive thermal ballast and that the quantity of oxygen to be supplied is related to the quantity of fuel supplied, but that in spite of all these limiting factors it should be possible to operate the reactor at a variable production rate, that is to supply fuel in alternately large and small quantities through one and the same burner. It will be obvious that when supplying a small quantity of fuel (carrier gas) together with a small quantity of oxygen-containing gas the velocity in the burner will be low, so that the above-mentioned induction time is reached or exceeded.
- the object of the present invention is to remove these drawbacks and provide a process in which on the one hand the fuel and the oxygen-containing gas are only mixed near the end of the burner and on the other hand an intensive mixing is reached in an early stage, i.e. at the entrance of the fuel and the oxygen-containing gas into the reactor - without causing overheating of the reactor wall near the burner.
- the invention therefore relates to a process for the preparation of a gas comprising hydrogen and carbon monoxide by the partial combustion of a finely divided solid fuel with an oxygen-containing gas using a moderator gas, in which said three components are each separately supplied to an empty reactor space through a burner, which process in characterized in that the solid fuel is passed in a carrier gas centrally through the burner, the oxygen-containing gas is passed through the burner concentrically around and separate from the fuel stream, and the moderator gas is passed through the burner concentrically around and separate from the oxygen-containing gas.
- the moderator gas surrounds the streams of fuel and oxygen-containing gas flowing out of the burner and a degree of tolerance is formed in respect of the velocity at which and the direction in which the moderator gas and the oxygen-containing gas leave the burner, on the one hand an effective mixing of fuel and oxygen-containing gas can be ensured and, on the other hand, satisfactory cooling of the reactor wall near the burner can be effected, since the moderator gas comes into contact therewith.
- the jacket of moderator gas which surrounds the streams of fuel-containing gas and oxygen-containing gas in the reactor immediately beside the burner prevents that the hot mixture of carbon monoxide and hydrogen which has formed in the reactor become prematurely mixed with the stream of oxygen-containing gas (whereby a considerable degree of overheating is prevented in the vicinity of the burner mouthl. The formation of a hot flame front at the burner mouth is thus prevented.
- the fuel-containing carrier gas leaves the burner with an exactly axial moment and that the oxygen-containing gas leaves the burner with an axial moment and an inwardly directed radial moment.
- the stream of oxygen-containing gas is directed to the stream of fuel-containing carrier gas outside the burner.
- mist of a gas stream is meant the. product of the mass throughput and velocity (in vl, the mass throughput being the number of kg of mass of the relevant stream per second leaving the burner.
- the mass throughput is expressed in kg of mass/second and the velocity in m/sec..
- a good mixing is usually obtained in practice when the ratio between the radial moment of the oxygen-containing gas and the axial moment of the fuel-containing carrier gas is between 0.2 and 1.0.
- the process according to the present invention enables the use of a burner of which at the front part a wall adjoins with its front face the reactor space, said wall being cooled on the inside of the burner with the moderator gas. In this manner a satisfactory protection of the front part of the burner is obtained.
- the moderator gas preferably leaves the burner with an axial_ moment and an inwardly directed radial moment. Consequently, it is prevented that the fuel-containing gas and the oxygen-containing gas become mixed in a premature stage with hot carbon monoxide and hydrogen and come into contact with the reactor wall near the burner, so that local overheating is prevented.
- the process according to the invention can of course also be carried out by means of two or more burners debouching into the gasification reactor.
- the invention also relates to a burner for carrying out the present process.
- a burner for carrying out the present process.
- Such a burner has a central passage for fuel-containing carrier gas and concentric passages for oxygen-containing gas and moderator gas around said central passage.
- said burner has outlet openings for the oxygen-containing gas which are directed obliquely forward to one point and one or more outlet openings for the moderator gas running mainly parallel with the former openings.
- the front part of said burner is provided with a wall having a front face normal to the burner axis, along the inside of said wall the passage for moderator gas is located, which passage changes direction at this point. In this manner a satisfactory cooling of the burner front is obtained.
- the drawing shows diagrammatically an axial cross-section of the front part of a burner according to an embodiment of the invention.
- the burner is fitted in an opening of the reactor wall 1, which is shown diagrammatically and comprises an outer wall 2 and an inner double wall 3,4. Between the outer wall 2 and the outer double wall 3 is an annular space 5 for the passage of the moderator gas. Between the double walls 3 and 4 is an annular space 6 for the passage of oxygen-containing gas and within the inner double wall 4 is an axial passage 7 for carrier gas with finely divided solid fuel.
- the passage 7 debouches directly into the space 8 within the burner mouth.
- the fronts of the double walls 3,4 are connected by a connecting wall 9.
- a number of bores 10 are provided, the centrelines 11 of which are located in a conical plane, the apex J2 of which lies in or even beyond the space 8 seen in the direction of flow 13.
- the bores 10 form the connection between the space 6 and the space 8.
- the front of the outer wall 2 is provided with a front face 14 which is directed normal to the centreline 15 of the burner and has also an inwardly directed end 16 which fits loosely in an annular slot 17 of the connecting wall 9.
- the space 5 extends near the burner front along the inside of the front face 14 and said space 5 nevertheless debouches into the space 8 in a direction which is substantially parallel to the bores 10.
- the burner injects a well-mixed stream of fuel and oxygen, surrounded by a jacket of moderator gas, into the reactor, the front part of the burner being cooled by moderator gas.
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
Abstract
Description
- The invention relates to the gasification of finely divided solid fuel.
- This gasification - also known as partial combustion - is carried out by reaction of solid fuel with an oxygen-containing gas. The fuel contains as useful components mainly carbon and hydrogen, which react with the oxygen - and possibly with steam and carbon dioxide - to form carbon monoxide and hydrogen. Depending on the temperature, the formation of methane is also possible. In principle, all possible solid materials of vegetable and animal origin, such as coal, brown coal, wood pulp, etc. are suitable as fuel. The oxygen-containing gas is usually air or oxygen or a mixture thereof.
- In existing coal gasification processes, coal particles are contacted with the oxygen-containing gas in a reactor in a fixed or fluidized bed at temperatures below 1000oC. The residence time of the coal particles is relatively long (certainly more than one minute). A drawback of said processes is that not all types of solid fuel can be gasified in this manner, which limits the flexibility of said processes. Highly swelling coal, for example, is unsuitable because it sinters together and clogs the reactor. In some cases the high yield of methane of said processes is a disadvantage.
- An alternative process has therefore been developed in which finely divided solid fuel is passed into a reactor through a burner at a relatively high velocity and in which process the fuel reacts there in the flame with the oxygen-containing gas at temperatures above 1000oC. In the latter process the residence time of the fuel in the reactor is relatively short (usually less than 10 seconds). By this process it is possible to gasify all types of solid fuel. The methane yield is low. The process can be carried out at high pressure.
- In the latter process the fuel is usually passed in a carrier gas to the reactor through the burner, while the oxygen-containing gas is also passed to the reactor through the burner. Since the solid fuel, even if it is finely divided, is usually less reactive than liquid or gaseous fuel (it cannot be atomized by the burner) great care is bestowed on the manner in which the fuel and oxygen are mixed. When the mixing in the reactor is insufficient, zones of underheating occur in the reactor next to zones of overheating, since part of the fuel does not receive enough oxygen and an other part of the fuel receives too much oxygen. Part of the fuel is then not fully gasified and an other part is converted completely into carbon dioxide and water vapour. A drawback of locally high temperatures in the reactor is that damage is caused to the refractory lining which is usually provided therein.
- In order to check the temperature in the reactor a water vapour-containing moderator gas is often supplied to the reactor. The water vapour reacts with part of the fuel, with the formation of hydrogen and carbon monoxide. The reaction in question is endothermic. The moderator gas can be supplied to the reactor through the burner or otherwise.
- In order to ensure a good mixing of fuel and oxygen-containing gas it has already been proposed to have the mixing already take place in or upstream of the burner. A great disadvantage thereof is, however, that - especially when the gasification is carried out at high pressure - the design and operation of an apparatus suitable for said purpose is highly critical. The fact is that the time elapsing between the moment of mixing and the moment when the mixture enters the reactor must invariably be shorter than the combustion induction time of said mixture. This induction time decreases substantially at a rise in the gasification pressure. In view of this problem it should be borne in mind that the fuel is supplied in a carrier gas, that the fuel load of the carrier gas must be high to ensure that the carrier gas does not constitute an excessive thermal ballast and that the quantity of oxygen to be supplied is related to the quantity of fuel supplied, but that in spite of all these limiting factors it should be possible to operate the reactor at a variable production rate, that is to supply fuel in alternately large and small quantities through one and the same burner. It will be obvious that when supplying a small quantity of fuel (carrier gas) together with a small quantity of oxygen-containing gas the velocity in the burner will be low, so that the above-mentioned induction time is reached or exceeded.
- The object of the present invention is to remove these drawbacks and provide a process in which on the one hand the fuel and the oxygen-containing gas are only mixed near the end of the burner and on the other hand an intensive mixing is reached in an early stage, i.e. at the entrance of the fuel and the oxygen-containing gas into the reactor - without causing overheating of the reactor wall near the burner.
- The invention therefore relates to a process for the preparation of a gas comprising hydrogen and carbon monoxide by the partial combustion of a finely divided solid fuel with an oxygen-containing gas using a moderator gas, in which said three components are each separately supplied to an empty reactor space through a burner, which process in characterized in that the solid fuel is passed in a carrier gas centrally through the burner, the oxygen-containing gas is passed through the burner concentrically around and separate from the fuel stream, and the moderator gas is passed through the burner concentrically around and separate from the oxygen-containing gas.
- Now that the moderator gas surrounds the streams of fuel and oxygen-containing gas flowing out of the burner and a degree of tolerance is formed in respect of the velocity at which and the direction in which the moderator gas and the oxygen-containing gas leave the burner, on the one hand an effective mixing of fuel and oxygen-containing gas can be ensured and, on the other hand, satisfactory cooling of the reactor wall near the burner can be effected, since the moderator gas comes into contact therewith.
- Moreover, the jacket of moderator gas which surrounds the streams of fuel-containing gas and oxygen-containing gas in the reactor immediately beside the burner, prevents that the hot mixture of carbon monoxide and hydrogen which has formed in the reactor become prematurely mixed with the stream of oxygen-containing gas (whereby a considerable degree of overheating is prevented in the vicinity of the burner mouthl. The formation of a hot flame front at the burner mouth is thus prevented.
- In order to obtain a good mixing of fuel-containing gas and oxygen-containing gas, according to the invention it is preferably ensured that the fuel-containing carrier gas leaves the burner with an exactly axial moment and that the oxygen-containing gas leaves the burner with an axial moment and an inwardly directed radial moment. In this way, the stream of oxygen-containing gas is directed to the stream of fuel-containing carrier gas outside the burner.
- In this specification by "moment" of a gas stream is meant the. product of the mass throughput and velocity (in vl, the mass throughput being the number of kg of mass of the relevant stream per second leaving the burner. The mass throughput is expressed in kg of mass/second and the velocity in m/sec..
- A good mixing is usually obtained in practice when the ratio between the radial moment of the oxygen-containing gas and the axial moment of the fuel-containing carrier gas is between 0.2 and 1.0.
- The process according to the present invention enables the use of a burner of which at the front part a wall adjoins with its front face the reactor space, said wall being cooled on the inside of the burner with the moderator gas. In this manner a satisfactory protection of the front part of the burner is obtained.
- The moderator gas preferably leaves the burner with an axial_ moment and an inwardly directed radial moment. Consequently, it is prevented that the fuel-containing gas and the oxygen-containing gas become mixed in a premature stage with hot carbon monoxide and hydrogen and come into contact with the reactor wall near the burner, so that local overheating is prevented.
- The process according to the invention can of course also be carried out by means of two or more burners debouching into the gasification reactor.
- The invention also relates to a burner for carrying out the present process. Such a burner has a central passage for fuel-containing carrier gas and concentric passages for oxygen-containing gas and moderator gas around said central passage.
- According to the invention said burner has outlet openings for the oxygen-containing gas which are directed obliquely forward to one point and one or more outlet openings for the moderator gas running mainly parallel with the former openings. With a burner of this type good results are obtained.
- The front part of said burner is provided with a wall having a front face normal to the burner axis, along the inside of said wall the passage for moderator gas is located, which passage changes direction at this point. In this manner a satisfactory cooling of the burner front is obtained.
- The invention will be further illustrated below with reference to the appertaining drawing.
- The drawing shows diagrammatically an axial cross-section of the front part of a burner according to an embodiment of the invention.
- The burner is fitted in an opening of the reactor wall 1, which is shown diagrammatically and comprises an
outer wall 2 and an innerdouble wall outer wall 2 and the outerdouble wall 3 is an annular space 5 for the passage of the moderator gas. Between thedouble walls annular space 6 for the passage of oxygen-containing gas and within the innerdouble wall 4 is anaxial passage 7 for carrier gas with finely divided solid fuel. - The
passage 7 debouches directly into thespace 8 within the burner mouth. The fronts of thedouble walls bores 10 are provided, thecentrelines 11 of which are located in a conical plane, the apex J2 of which lies in or even beyond thespace 8 seen in the direction offlow 13. Thebores 10 form the connection between thespace 6 and thespace 8. - The front of the
outer wall 2 is provided with afront face 14 which is directed normal to thecentreline 15 of the burner and has also an inwardly directedend 16 which fits loosely in anannular slot 17 of the connecting wall 9. In this manner the space 5 extends near the burner front along the inside of thefront face 14 and said space 5 nevertheless debouches into thespace 8 in a direction which is substantially parallel to thebores 10. - During operation the burner injects a well-mixed stream of fuel and oxygen, surrounded by a jacket of moderator gas, into the reactor, the front part of the burner being cooled by moderator gas.
- It will be obvious that numerous alterations can be made to the burner shown. For example, the number of
bores 10 may be varied or replaced by an annular slit and theannular slot 17 can be replaced by separate bores. ;
Claims (8)
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
NL7904625 | 1979-06-13 | ||
NLAANVRAGE7904625,A NL183096C (en) | 1979-06-13 | 1979-06-13 | BURNER FOR THE PARTIAL BURNING OF A FINE DISTRIBUTED OXYGEN FUEL AND MODERATOR GAS. |
Publications (3)
Publication Number | Publication Date |
---|---|
EP0021461A1 true EP0021461A1 (en) | 1981-01-07 |
EP0021461B1 EP0021461B1 (en) | 1983-08-17 |
EP0021461B2 EP0021461B2 (en) | 1990-12-27 |
Family
ID=19833350
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP80200355A Expired - Lifetime EP0021461B2 (en) | 1979-06-13 | 1980-04-17 | Process and burner for the gasification of solid fuel |
Country Status (8)
Country | Link |
---|---|
EP (1) | EP0021461B2 (en) |
JP (1) | JPS56907A (en) |
AU (1) | AU533204B2 (en) |
CA (1) | CA1153206A (en) |
DE (1) | DE3064565D1 (en) |
IN (1) | IN152671B (en) |
NL (1) | NL183096C (en) |
ZA (1) | ZA802014B (en) |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0026509A2 (en) * | 1979-10-02 | 1981-04-08 | Shell Internationale Researchmaatschappij B.V. | Process for the partial combustion of solid fuel and burner for carrying out the process |
EP0022897B1 (en) * | 1979-07-17 | 1983-11-30 | Westinghouse Electric Corporation | Fluidized bed injection assembly for coal gasification |
EP0101213A2 (en) * | 1982-08-12 | 1984-02-22 | Texaco Development Corporation | Coal gasification burner and apparatus |
EP0107225A1 (en) * | 1982-10-19 | 1984-05-02 | Shell Internationale Researchmaatschappij B.V. | Process and burner for the partial combustion of solid fuel |
EP0120517A2 (en) * | 1983-03-18 | 1984-10-03 | Shell Internationale Researchmaatschappij B.V. | Burner and process for the partial combustion of solid fuel |
EP0180249A2 (en) * | 1984-11-02 | 1986-05-07 | VEBA OEL Technologie GmbH | Method of operating a burner |
Families Citing this family (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4391611A (en) * | 1981-03-05 | 1983-07-05 | The United States Of America As Represented By The United States Department Of Energy | Gasification system |
EP0108425B1 (en) * | 1982-08-23 | 1987-05-06 | Shell Internationale Researchmaatschappij B.V. | Burner for the partial combustion of finely divided solid fuel |
GB8317251D0 (en) * | 1983-06-24 | 1983-07-27 | Shell Int Research | Burner for gasification of solid fuel |
JPS6138313A (en) * | 1984-07-30 | 1986-02-24 | Babcock Hitachi Kk | Burner for jet stream bed coal gasification furnace |
JPS63142095A (en) * | 1986-12-05 | 1988-06-14 | Babcock Hitachi Kk | Jet-layer coal gasification furnace |
JPH086102B2 (en) * | 1989-10-20 | 1996-01-24 | バブコツク日立株式会社 | Spouted bed gasifier |
JP4936817B2 (en) * | 2006-08-07 | 2012-05-23 | 大陽日酸株式会社 | Combustion device for synthesis gas production and synthesis gas production method |
Citations (7)
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LU35569A1 (en) * | ||||
FR978135A (en) * | 1947-12-29 | 1951-04-10 | Koppers Co Inc | Apparatus for the continuous production of combustible gases |
FR1089366A (en) * | 1952-12-11 | 1955-03-16 | Basf Ag | Process for gasification of fuels ranging from pulverulent to granular |
FR1203262A (en) * | 1957-09-13 | 1960-01-18 | Bataafsche Petroleum | Process for preparing gas mixtures containing hydrogen and carbon monoxide and apparatus for carrying out the process |
GB911374A (en) * | 1958-04-30 | 1962-11-28 | Koppers Gmbh Heinrich | Device for the gasification of finely divided fuels |
US3847564A (en) * | 1970-01-23 | 1974-11-12 | Texaco Development Corp | Apparatus and process for burning liquid hydrocarbons in a synthesis gas generator |
FR2286104A1 (en) * | 1974-09-26 | 1976-04-23 | Texaco Development Corp | PROCESS FOR THE CONTINUOUS PRODUCTION OF HYDROGEN AND CARBON MONOXIDE |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2520883B2 (en) * | 1975-05-10 | 1979-07-05 | Eisenwerk-Gesellschaft Maximilianshuette Mbh, 8458 Sulzbach-Rosenberg | Process and device for the continuous gasification of coal or carbonaceous fuels in an iron bath reactor |
JPS5333601A (en) * | 1976-09-10 | 1978-03-29 | Pioneer Electronic Corp | Stereophonic system |
-
1979
- 1979-06-13 NL NLAANVRAGE7904625,A patent/NL183096C/en not_active IP Right Cessation
-
1980
- 1980-04-01 AU AU57052/80A patent/AU533204B2/en not_active Ceased
- 1980-04-02 IN IN381/CAL/80A patent/IN152671B/en unknown
- 1980-04-02 CA CA000349115A patent/CA1153206A/en not_active Expired
- 1980-04-03 ZA ZA00802014A patent/ZA802014B/en unknown
- 1980-04-07 JP JP4553980A patent/JPS56907A/en active Granted
- 1980-04-17 DE DE8080200355T patent/DE3064565D1/en not_active Expired
- 1980-04-17 EP EP80200355A patent/EP0021461B2/en not_active Expired - Lifetime
Patent Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
LU35569A1 (en) * | ||||
FR978135A (en) * | 1947-12-29 | 1951-04-10 | Koppers Co Inc | Apparatus for the continuous production of combustible gases |
FR1089366A (en) * | 1952-12-11 | 1955-03-16 | Basf Ag | Process for gasification of fuels ranging from pulverulent to granular |
FR1203262A (en) * | 1957-09-13 | 1960-01-18 | Bataafsche Petroleum | Process for preparing gas mixtures containing hydrogen and carbon monoxide and apparatus for carrying out the process |
GB911374A (en) * | 1958-04-30 | 1962-11-28 | Koppers Gmbh Heinrich | Device for the gasification of finely divided fuels |
US3847564A (en) * | 1970-01-23 | 1974-11-12 | Texaco Development Corp | Apparatus and process for burning liquid hydrocarbons in a synthesis gas generator |
FR2286104A1 (en) * | 1974-09-26 | 1976-04-23 | Texaco Development Corp | PROCESS FOR THE CONTINUOUS PRODUCTION OF HYDROGEN AND CARBON MONOXIDE |
Cited By (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0022897B1 (en) * | 1979-07-17 | 1983-11-30 | Westinghouse Electric Corporation | Fluidized bed injection assembly for coal gasification |
EP0026509A2 (en) * | 1979-10-02 | 1981-04-08 | Shell Internationale Researchmaatschappij B.V. | Process for the partial combustion of solid fuel and burner for carrying out the process |
EP0026509A3 (en) * | 1979-10-02 | 1981-10-14 | Shell Internationale Research Maatschappij B.V. | Process for the partial combustion of solid fuel and burner for carrying out the process |
EP0101213A2 (en) * | 1982-08-12 | 1984-02-22 | Texaco Development Corporation | Coal gasification burner and apparatus |
EP0101213A3 (en) * | 1982-08-12 | 1984-11-28 | Texaco Development Corporation | Coal gasification burner and apparatus |
EP0107225A1 (en) * | 1982-10-19 | 1984-05-02 | Shell Internationale Researchmaatschappij B.V. | Process and burner for the partial combustion of solid fuel |
US4523529A (en) * | 1982-10-19 | 1985-06-18 | Shell Oil Company | Process and burner for the partial combustion of solid fuel |
EP0120517A2 (en) * | 1983-03-18 | 1984-10-03 | Shell Internationale Researchmaatschappij B.V. | Burner and process for the partial combustion of solid fuel |
EP0120517A3 (en) * | 1983-03-18 | 1985-07-10 | Shell Internationale Research Maatschappij B.V. | Burner and process for the partial combustion of solid fuel |
EP0180249A2 (en) * | 1984-11-02 | 1986-05-07 | VEBA OEL Technologie GmbH | Method of operating a burner |
EP0180249A3 (en) * | 1984-11-02 | 1987-01-21 | Veba Oel Entwicklungs-Gesellschaft Mbh | Burner |
Also Published As
Publication number | Publication date |
---|---|
DE3064565D1 (en) | 1983-09-22 |
JPS56907A (en) | 1981-01-08 |
AU5705280A (en) | 1980-12-18 |
CA1153206A (en) | 1983-09-06 |
NL183096B (en) | 1988-02-16 |
IN152671B (en) | 1984-03-10 |
EP0021461B1 (en) | 1983-08-17 |
JPH0240716B2 (en) | 1990-09-12 |
AU533204B2 (en) | 1983-11-10 |
NL183096C (en) | 1988-07-18 |
NL7904625A (en) | 1980-12-16 |
ZA802014B (en) | 1981-04-29 |
EP0021461B2 (en) | 1990-12-27 |
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