CA1153206A - Process and burner for the gasification of solid fuel and gas so prepared - Google Patents
Process and burner for the gasification of solid fuel and gas so preparedInfo
- Publication number
- CA1153206A CA1153206A CA000349115A CA349115A CA1153206A CA 1153206 A CA1153206 A CA 1153206A CA 000349115 A CA000349115 A CA 000349115A CA 349115 A CA349115 A CA 349115A CA 1153206 A CA1153206 A CA 1153206A
- Authority
- CA
- Canada
- Prior art keywords
- burner
- gas
- oxygen
- moderator
- wall
- 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
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
- C10J3/50—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
Abstract
ABSTRACT OF THE DISCLOSURE
Process and burner for preparing hydrogen and carbon monoxide by the partial combustion of finely divided solid fuel with oxygen-containing gas using moderator gas. The reactants are separately supplied to an empty reactor through the burner. The solid fuel is passed in a carrier gas centrally. The oxygen-containing gas is passed concentrically around and separate from the fuel stream. The moderator gas is passed concentrically around and separate from the oxygen-containing gas: in particular the solid fuel in the carrier gas leaves the burner with an exactly axial moment, the oxygen-contain-ing gas and the moderator gas both leaving the burner with axial and inwardly directed radial moments, the burner has a front part with a wall which adjoins, at its front face, the reactor space, and the wall is cooled on the inside of the burner with the moderator gas.
Process and burner for preparing hydrogen and carbon monoxide by the partial combustion of finely divided solid fuel with oxygen-containing gas using moderator gas. The reactants are separately supplied to an empty reactor through the burner. The solid fuel is passed in a carrier gas centrally. The oxygen-containing gas is passed concentrically around and separate from the fuel stream. The moderator gas is passed concentrically around and separate from the oxygen-containing gas: in particular the solid fuel in the carrier gas leaves the burner with an exactly axial moment, the oxygen-contain-ing gas and the moderator gas both leaving the burner with axial and inwardly directed radial moments, the burner has a front part with a wall which adjoins, at its front face, the reactor space, and the wall is cooled on the inside of the burner with the moderator gas.
Description
~ ~3Z~
PROCESS A~D BURNER FOR THE GASIFICATION OF SOLID
FUEL AND GAS SO PREPARED
The inYention relates to the gasification of ~inely divided solid fuel.
This gasification - also known as partial combustion - is carried out by react;on 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 steaim 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 1000 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 flexi-bility 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 disad-vantage.
`~ An alternative process has therefore been developed in which finely divided solid fuel i5 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 1000C. 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 ::
~ ` ~
. ~ .
~ ~3~6 gas is also passed to the reactor through the burner. Since the solid fuel, even if it is $inely divided, is usually less reactive than l;quid or gaseous fuel (it cannot be atomized by the burner) great care is bestowed on the manner in which the fuel and oxygen are mixed. When the mixing in the reactor is insufficient, ~ones of underheating occur in the reactor next to zones of overheating, since part of the fuel does not receive enough oxygen and an other part of the fuel receives too much oxygen. Part of the fuel is then not fully gasi$ied and an other part is converted completely into carbon dioxide and water vapour. A drawback of locally high temper-atures in the reactor is that damage is caused to the refractory lining which is usuall~ provided therein.
In order to check the temperature in the reactor a water vapour-containing moderator gas is o$ten supplied to the reactor.
The water vapour reacts with part of the fuel, with the $ormation of hydrogen and carbon monoxide. The reaction in ~uestion is endo-thermic. The moderator gas can be supplied to the reactor through the burner or otherwise.
In order to ensure a good mixing of fuel and oxygen-containing gas it has already been proposed to have the mixing already take place in or upstream of the burner. A great disadvantage thereof is, however, that - especially when the gasification is carried out at high pressure - the design and operation of an apparatus suitable for said purpose is highly critical. The fact is that the time elapsing between the moment of mixing and the moment when the mixture enters the reactor must invariably be shorter than the combustion ;nduction time o$ said mixture. This induction time decreases substantially at a rise in the gasification pressure. In view of this problem it should be borne i4 mind that the ~uel 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 xcessive 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 : ' ' ~
~` 32~:16 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 re-move these drawbacks and provided 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-contain-ing 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 is 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-con-taining gas.
In particular the solid fuel in the carrier gas leaves the burner with an exactly axial moment, the oxygen-containing gas and the moderator gas both leaving the burner with axial and inwardly directed radial moments, the burner has a front part with a wall which adjoins, at its front face, the reactor space, and the wall is cooled on the inside of the burner with the moderator gas~
;
.
~. ~A . . .
~. ~ ' ', ' 532~6 - 3a -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 mode-rator gas comes intocontact 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 mon-oxide and hydrogen which has formed in the reactor . . .
~;3~6 become prematurely mixed with the stream of oxygen-containing gas (whereby a considerable degree of overheating is prevented in the vicinity of the burner mouth). The formation of a hot flame front at the burner mouth is thus preYented.
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 v), the mass through-put 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 wnen 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 1Ø
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 inwardl~ 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 accord;ng 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 .'. .
' ' ' ~ ' , ' ` , ~ .
.' `~
~LS;3Z~36 present process. Such a burner has a central passage ~or fuel-con-taining carrier gas and concentric passages for oxygen-containing gas and moderator gas around said central passage.
According to the invent;on 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 ~ainl~ parallel with the former openings. Wîth a burner of this type eood results are obtained.
The front part of said burner is provided with a wall having a front face normal to the burner ax;s, 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 inven-tion.
The burner is fitted ;n 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.
~ he passage 7 debouches directl~ into the space 8 within the burner mouth. ~he fronts of the double walls 3,4 are connected by a connecting wall ~. In this wall a number of bores ~0 are provided, the centrelines ~1 of which are located in a conical plane, the apex ~2 of which lies in or even beyond the space 8 seen in the direction of flow 13. ~he 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 :
. ~ ~ , ' ' . ; :
,: , , ~' . ' - . . :
.
~3~6 has also an inwardly directed end 16 which fits loosely in an annular slot 17 of the connecting wall 9. In this manner 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.
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 the annular slot 17 can be replaced by separate bores.
~ .... .
.
. .:
., : ~
PROCESS A~D BURNER FOR THE GASIFICATION OF SOLID
FUEL AND GAS SO PREPARED
The inYention relates to the gasification of ~inely divided solid fuel.
This gasification - also known as partial combustion - is carried out by react;on 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 steaim 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 1000 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 flexi-bility 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 disad-vantage.
`~ An alternative process has therefore been developed in which finely divided solid fuel i5 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 1000C. 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 ::
~ ` ~
. ~ .
~ ~3~6 gas is also passed to the reactor through the burner. Since the solid fuel, even if it is $inely divided, is usually less reactive than l;quid or gaseous fuel (it cannot be atomized by the burner) great care is bestowed on the manner in which the fuel and oxygen are mixed. When the mixing in the reactor is insufficient, ~ones of underheating occur in the reactor next to zones of overheating, since part of the fuel does not receive enough oxygen and an other part of the fuel receives too much oxygen. Part of the fuel is then not fully gasi$ied and an other part is converted completely into carbon dioxide and water vapour. A drawback of locally high temper-atures in the reactor is that damage is caused to the refractory lining which is usuall~ provided therein.
In order to check the temperature in the reactor a water vapour-containing moderator gas is o$ten supplied to the reactor.
The water vapour reacts with part of the fuel, with the $ormation of hydrogen and carbon monoxide. The reaction in ~uestion is endo-thermic. The moderator gas can be supplied to the reactor through the burner or otherwise.
In order to ensure a good mixing of fuel and oxygen-containing gas it has already been proposed to have the mixing already take place in or upstream of the burner. A great disadvantage thereof is, however, that - especially when the gasification is carried out at high pressure - the design and operation of an apparatus suitable for said purpose is highly critical. The fact is that the time elapsing between the moment of mixing and the moment when the mixture enters the reactor must invariably be shorter than the combustion ;nduction time o$ said mixture. This induction time decreases substantially at a rise in the gasification pressure. In view of this problem it should be borne i4 mind that the ~uel 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 xcessive 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 : ' ' ~
~` 32~:16 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 re-move these drawbacks and provided 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-contain-ing 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 is 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-con-taining gas.
In particular the solid fuel in the carrier gas leaves the burner with an exactly axial moment, the oxygen-containing gas and the moderator gas both leaving the burner with axial and inwardly directed radial moments, the burner has a front part with a wall which adjoins, at its front face, the reactor space, and the wall is cooled on the inside of the burner with the moderator gas~
;
.
~. ~A . . .
~. ~ ' ', ' 532~6 - 3a -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 mode-rator gas comes intocontact 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 mon-oxide and hydrogen which has formed in the reactor . . .
~;3~6 become prematurely mixed with the stream of oxygen-containing gas (whereby a considerable degree of overheating is prevented in the vicinity of the burner mouth). The formation of a hot flame front at the burner mouth is thus preYented.
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 v), the mass through-put 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 wnen 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 1Ø
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 inwardl~ 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 accord;ng 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 .'. .
' ' ' ~ ' , ' ` , ~ .
.' `~
~LS;3Z~36 present process. Such a burner has a central passage ~or fuel-con-taining carrier gas and concentric passages for oxygen-containing gas and moderator gas around said central passage.
According to the invent;on 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 ~ainl~ parallel with the former openings. Wîth a burner of this type eood results are obtained.
The front part of said burner is provided with a wall having a front face normal to the burner ax;s, 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 inven-tion.
The burner is fitted ;n 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.
~ he passage 7 debouches directl~ into the space 8 within the burner mouth. ~he fronts of the double walls 3,4 are connected by a connecting wall ~. In this wall a number of bores ~0 are provided, the centrelines ~1 of which are located in a conical plane, the apex ~2 of which lies in or even beyond the space 8 seen in the direction of flow 13. ~he 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 :
. ~ ~ , ' ' . ; :
,: , , ~' . ' - . . :
.
~3~6 has also an inwardly directed end 16 which fits loosely in an annular slot 17 of the connecting wall 9. In this manner 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.
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 the annular slot 17 can be replaced by separate bores.
~ .... .
.
. .:
., : ~
Claims (4)
1. 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 process said three com-ponents are each separately supplied to an empty reactor space through a burner, through which the solid fuel is passed in a carrier gas centrally, leaving the burner with an exactly axial moment, the oxygen-containing gas is passed concentrically around and separate from the fuel stream, leaving the burner with an axial and an inwardly directed radial moment, and the moderator gas is passed concentrically around and separate from the oxygen-con-taining gas, leaving the burner with an axial and an inwardly directed radial moment, said burner having a front part with a wall which adjoins at its front face the reactor space and said wall being cooled on the inside of the burner with the moderator gas.
2. A burner for the partial combustion of a finely divided solid fuel with an oxygen-containing gas using a moderator gas, which burner is provided with a central passage for a fuel-containing fluid and concentric pass-ages for oxygen-containing gas and moderator gas around said central passage, outlet openings for the oxygen-containing gas being directed obliquely forward to one point, and at least one outlet opening for the moderator gas extending mainly parallel with the outlet openings for oxygen-containing gas, and which burner is further provided with a wall having a front face normal to the burner axis, the passage for moderator gas being located along the inside of said wall and said passage changing direction at this point.
3. A burner according to claim 2, wherein the passage for moderator gas along the inside of said wall forms cooling means for said wall.
4. In a reactor for the preparation of a gas com-prising hydrogen and carbon monoxide including a burner and supply means for finely divided solid fuel, oxygen containing gas and a moderator gas the improvement where-in said supply means is housed in said burner, said burner being provided with a central passage for a fuel-containing fluid and concentric passages for oxygen-containing gas and moderator gas around said central passage, outlet openings for the oxygen-containing gas being directed obliquely forward to one point, and at least one outlet opening for the moderator gas extend-ing mainly parallel with the outlet opening for oxygen-containing gas and which burner is further provided with a wall having a front face normal to the burner axis, the passage for moderator gas being located along the inside of said wall and said passage changing direction at this point.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NLAANVRAGE7904625,A NL183096C (en) | 1979-06-13 | 1979-06-13 | BURNER FOR THE PARTIAL BURNING OF A FINE DISTRIBUTED OXYGEN FUEL AND MODERATOR GAS. |
| NL7904625 | 1979-06-13 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1153206A true CA1153206A (en) | 1983-09-06 |
Family
ID=19833350
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000349115A Expired CA1153206A (en) | 1979-06-13 | 1980-04-02 | Process and burner for the gasification of solid fuel and gas so prepared |
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) |
Families Citing this family (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4282010A (en) * | 1979-07-17 | 1981-08-04 | The United States Of America As Represented By The United States Department Of Energy | Fluidized bed injection assembly for coal gasification |
| GB2060158A (en) * | 1979-10-02 | 1981-04-29 | Shell Int Research | Solid fuel combustion |
| US4391611A (en) * | 1981-03-05 | 1983-07-05 | The United States Of America As Represented By The United States Department Of Energy | Gasification system |
| DE3373915D1 (en) * | 1982-08-12 | 1987-11-05 | Texaco Development Corp | Coal gasification burner and apparatus |
| DE3371405D1 (en) * | 1982-08-23 | 1987-06-11 | Shell Int Research | Burner for the partial combustion of finely divided solid fuel |
| CA1218903A (en) * | 1982-10-19 | 1987-03-10 | Ian Poll | Process and burner for the partial combustion of solid fuel |
| GB8307519D0 (en) * | 1983-03-18 | 1983-04-27 | Shell Int Research | Burner |
| 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 |
| DE3440088A1 (en) * | 1984-11-02 | 1986-05-07 | Veba Oel Entwicklungs-Gesellschaft mbH, 4650 Gelsenkirchen | BURNER |
| 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 |
Family Cites Families (9)
| 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 |
| GB737070A (en) * | 1952-12-11 | 1955-09-21 | Basf Ag | Improvements in the gasification of pulverulent to granular fuels |
| 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 |
| DE1076868B (en) * | 1958-04-30 | 1960-03-03 | Koppers Gmbh Heinrich | Device for generating fuel gas by gasifying 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 |
| US3929429A (en) * | 1974-09-26 | 1975-12-30 | Texaco Inc | Fuel gas from solid carbonaceous fuels |
| 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 CA CA000349115A patent/CA1153206A/en not_active Expired
- 1980-04-02 IN IN381/CAL/80A patent/IN152671B/en unknown
- 1980-04-03 ZA ZA00802014A patent/ZA802014B/en unknown
- 1980-04-07 JP JP4553980A patent/JPS56907A/en active Granted
- 1980-04-17 EP EP80200355A patent/EP0021461B2/en not_active Expired - Lifetime
- 1980-04-17 DE DE8080200355T patent/DE3064565D1/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0240716B2 (en) | 1990-09-12 |
| AU5705280A (en) | 1980-12-18 |
| JPS56907A (en) | 1981-01-08 |
| ZA802014B (en) | 1981-04-29 |
| EP0021461B2 (en) | 1990-12-27 |
| DE3064565D1 (en) | 1983-09-22 |
| EP0021461B1 (en) | 1983-08-17 |
| NL7904625A (en) | 1980-12-16 |
| NL183096C (en) | 1988-07-18 |
| AU533204B2 (en) | 1983-11-10 |
| IN152671B (en) | 1984-03-10 |
| EP0021461A1 (en) | 1981-01-07 |
| NL183096B (en) | 1988-02-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP0107225B1 (en) | Process and burner for the partial combustion of solid fuel | |
| CA1153206A (en) | Process and burner for the gasification of solid fuel and gas so prepared | |
| US4353712A (en) | Start-up method for partial oxidation process | |
| US4865542A (en) | Partial combustion burner with spiral-flow cooled face | |
| CA1308306C (en) | Partial combustion burner with spiral-flow cooled face | |
| US4858538A (en) | Partial combustion burner | |
| US4887962A (en) | Partial combustion burner with spiral-flow cooled face | |
| CA1190046A (en) | Partial oxidation burner | |
| CA1301458C (en) | Process for partial oxidation of a hydrocarbon-containing fuel | |
| US4458607A (en) | Process and burner for the partial combustion of finely divided solid fuel | |
| US4400179A (en) | Partial oxidation high turndown apparatus | |
| CN101605876B (en) | Method and device for the entrained-flow gasification of solid fuels under pressure | |
| CA1269842A (en) | Process for producing synthesis gas from hydrocarbon fuel | |
| US4392869A (en) | High turndown partial oxidation process | |
| JPH0526085B2 (en) | ||
| US4351645A (en) | Partial oxidation burner apparatus | |
| CA1063503A (en) | Process and burner for the partial combustion of a liquid or gaseous fuel | |
| CN101788146A (en) | Multi-lance combination burner | |
| US4364744A (en) | Burner for the partial oxidation of slurries of solid carbonaceous fuels | |
| US4479810A (en) | Partial oxidation system | |
| US4371379A (en) | Partial oxidation process using a swirl burner | |
| US4371378A (en) | Swirl burner for partial oxidation process | |
| US2702743A (en) | Method and apparatus for preheating gaseous and vaporous reagents in powdered fuel gasification | |
| CA1131028A (en) | Method for heating oxygen containing gas in conjunction with a gasification system | |
| CA1162046A (en) | Burner and process for the partial oxidation of slurries of solid carbonaceous fuels |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |