CA1269842A - Process for producing synthesis gas from hydrocarbon fuel - Google Patents
Process for producing synthesis gas from hydrocarbon fuelInfo
- Publication number
- CA1269842A CA1269842A CA000468393A CA468393A CA1269842A CA 1269842 A CA1269842 A CA 1269842A CA 000468393 A CA000468393 A CA 000468393A CA 468393 A CA468393 A CA 468393A CA 1269842 A CA1269842 A CA 1269842A
- Authority
- CA
- Canada
- Prior art keywords
- oxidant
- outlet channel
- stream
- velocity
- burner
- 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 - Fee Related
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/36—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
- C01B3/363—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents characterised by the burner used
-
- 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
- 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
- C10J2300/0926—Slurries comprising bio-oil or bio-coke, i.e. charcoal, obtained, e.g. by fast pyrolysis of biomass
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
- Y02P20/145—Feedstock the feedstock being materials of biological origin
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Inorganic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
ABSTRACT
PROCESS FOR PRODUCING SYNTHESIS GAS FROM HYDROCARBON FUEL
Process for producing synthesis gas by partial combustion of a hydrocarbon fuel being in liquid state or in slurry state with an oxidant consisting of oxygen or an oxygen-containing gas, which process comprises using a burner consisting of a housing enclosing a central outlet channel for low velocity oxidant surrounded by a first annular outlet channel for high velocity oxidant which first annular outlet channel is encompassed by a second annular outlet channel for hydrocarbon fuel, said second annular outlet channel having an inclined outer part directed towards the first annular outlet channel.
PROCESS FOR PRODUCING SYNTHESIS GAS FROM HYDROCARBON FUEL
Process for producing synthesis gas by partial combustion of a hydrocarbon fuel being in liquid state or in slurry state with an oxidant consisting of oxygen or an oxygen-containing gas, which process comprises using a burner consisting of a housing enclosing a central outlet channel for low velocity oxidant surrounded by a first annular outlet channel for high velocity oxidant which first annular outlet channel is encompassed by a second annular outlet channel for hydrocarbon fuel, said second annular outlet channel having an inclined outer part directed towards the first annular outlet channel.
Description
;98~
PROCESS FOR PRODUCING SYMTHESIS GAS FROM HYDROCARBON FVEL
The present invention relates to a process for producing synthesis gas by partial combustion of a hydrocarbon fuel being in liquid state or in slurry state, with an oxidant consisting of oxygen or an oxygen-containing gas.
Hydrocarbon fuels can be converted into synthesis gas, com-prising essentially a mixture of hydrogen and carbon monoxide, by a controlled reaction with a substoichiometric quantity of oxygen or an oxygen-containing gas, such as air. Gases so pro duced may for example be used as feedstock for the manufacture of chemical products, as reducing agent and as a clean fuel~
A primary requirement in processes for producing synthesis gas, also called gasification processes, consists herein that hydrocarbon feedstock is intimately and uniformly mixed with oxidant during the gasification. If the mixing is insufficient, the quality of the formed synthesis gas can be severely impaired in that part Or the feedstock i9 insuffioiently gasified whilst another part is completelg converted into less valuable products, viz. ¢arbon dioxide and water vapour. For meeting the above re-quirement it is essential that the hydrocarbon fuel stream sup-plied i9 broken up into fragments whioh are sufficiently smallfor generating a substantially homogeneous mixture of hydro-carbon fuel and oxidant upon introduction of the oxidant into the fuel stream.
Insufficient contact between the reactants, formed by hydro-carbon fuel and oxidant, may further cause damage to the equip-ment used in the process. If the reactants are not brought into intimate contact with one another oxidant and fuel will ~ollow at least partially independent trajectories inside the reactor in which the process takes place. Since the reactor is filled with mainly hot already formed carbon monoxide and hydrogen, the '~
6~
oxidant ~lll rapidly react with these gases instead of with the fuel. If the oxidant is formed by oxygen or a gas containing free oxygen the reaction will be exothermic and the combustion products, consisting of carbon dioxide and water vapour, will be very hot. These combustion products will also follow independent trajectories, resulting in a poor contact with the relatively cold fuel flow in the reactor. The above phenomenon will result in the formation of local hot spots in the reactor, thereby possibly causing damage to the reactor refractory liming and the used burner(s). The above risk of damage to the process equipment becomeYeven more severe, if relatively heavy hydrocarbon fuels are to be processed, because of the release of a relatively large heat of reaction when such fuels are gasi~ied with free oxygen.
Sufficient mixing o~ the reactants might be attained in the burner itself. A disadvantage of this option is however that - especially at the usually high pressure gasification - the design and the operation of the burner are highly critical. The reason for this is that the time elapsing between the moment of mixing and the moment the fuel/oxygen mixture enters into the reaction zone should be invariably shorter than the combustion induction time of the mixture. Moreover, the velocity of the mixture inside the burner should be higher than the flame pro-pagation velooity in or-der to avoid flash back. However, the combustion induction time shortens and the flame propagation velocity increase.s at a rise in gasi~ication pressure. If the burner i~ operated at a relatively low ~uel load or, in other words, if the velocity of the ~uel/oxygen mixture in the burner is relatively low, the combustion induction time and/or flash back condition might easily be reached in the burner itself, with as a result overheating and possibly severe damage to the burner.
The above risks of premature combustion and flash back are eliminated if fuel and oxidant are mixed outside the burner in ~269~34X
~ 3 - 63293-2~73 the reaction zone. In thi~ ca~e Qpecial measures are to be taken to ensure a proper mlxing of the reactant~ neces~ary for an effective gaQification of the fuel aa di_cu~sed in the above. A
further complication of mixing fuel and oxidant in the reaction zone outside the burner i~ the risk of overheating of the front part of the burner facing the reaction zone due to a hot flame generated by premature contact of oxygen with already formed synthesiq gas present in the reaction zone. To promote an inti-mate mixing of fuel with oxidant, it ha~ alr~ady been proposed to inject the oxidant aa high velocity jets into a central core flow of fuel. Although such hi~h velocity jet~ are advanta~eous for breaking up the ~uel flow, they may have an adverse effect on the burner ~ront in that they may eaqily cause suction OL` hot reactor ga~eQ along the burner front.
An object of the present invention iQ to provide a process for producing s~ntheai~Q ~aa ~rom hydrocarbon fuel being in liquid state or in Qlurry state, which may be operated at hi~h fuel load~ and wherein the ri~k of product impairment or damage to the equipment u~Qed iQ subatantially eliminated.
The process according to the invention thereto comprises the use o~ at least one burner- consisting of a houQing enclosing a central outlet channel for low velocity oxidant ~urrounded by a first annular outlet channel for high velocity oxidant, whlch firqt annular outlet channel i~ encompassed by a second annular outlet channel for hydrocarbon fuel, said second ~ular outl~t ahannel having an inclined outer part directed towards the first annular outlet channel.
A process for producing synthesis gas by partial combustion o~
3~ a hydrocarbon Euel being in }iquid state or in slurry state, wich an oxidant consisting of oxygen or an oxygen-containing gas, said process comprising the steps of introducing a shielding stream of low velocity hydrocarbon fuel, a scream of high velocity oxidant and a stream of low velocity o~idant via a second annular out ec -`i .. . .
9~
-4- 63~93-~473 channel, a first annular outl~t channol and ~ c~n~ral ou~l~c channel, resp~ctively, o~ one or more burners into a reaction ~one and ~llo~ing ~he hydrocarbon fuel to r~act wich th~ oxidant, said second annular outlet channel having an inclined outer end part directed towards the fi~st annular outlet channel.
~ he low veloclty hydrocarbon fuel ~ream issuing from the second annular outlet charlnel o~ a burner ~o be used acco~dlng to the invention is brsken up by the ~tream of hijh velocity oxidant 1~ ulng from the ~lr~t annular outlet channel, and forms ln fact a ~hield around tho oxid~nt thereby ~reven~ing pre~ature contact of oxldant wlth already ~ormed 6yn~he~is gas.
Slncs accordin~ to the invention the se~ond annular outlet channel has an lnclined out~r part dlrected towards the flrst annular outlet channel and the fu~l is introduced into ~he reaction zone ~ith a low veloclty ~referably in ~he range of between about 5 and about 15 m/~ec whlls~ oxldant ~ro~ the first annular outlet channel enter~ the reaction zone with a substantially hi~her veloclty, c~u~in~ a hlgh ~lip velocity between fuel and oxldant the hydrocarbon fuel stred~ can be e~ectlvely b~oken u~ and mlxed wlth oxidant. ~he veloclty of the oxldant stream from the flr~ annular outlet ahannel ls preferably cho~en in the range of about 50 ~hrough about 90 m/~ec. ~or optlmlzatlo~ of the ~lxln~ o~ the ~uel wl~h oxidant, the fuel stream ~nd therefore the ou~er part o~ tho econd ann~lar outlet channel should preferably be ~o~ltloned at an angle of ~etween about 2û and ~bout 40 with respect ~o the ~lr6t annular outlet channel.
.
, ~ ;
'' ''"' . ~ ' . :'' "'.'.
891;~
-5- 63~g3-2~73 If heavy hydrocarbon fuels are ko be processed, lt may be advantageous to pre-atomize the fuel prior to contact with the oxldant issuing from the first annular outlet channel in order to promote breaking up of the fuel flow by the high velocity oxidant.
The pre-atomization of the fuel is preferably attalned by addiny an atomization fluid, such as steam or carbondioxide, to the fuel prior to entering into the reaction zone.
During operation of the burner to be used in the process according to the invention the space laterally enclosed by the oxidant stream from the first annular outlet channel is filled with low velocity oxidant issuing from the central outlet channel, thereby preventing the generation of wakes which miyht cause flame attachment to the front of the burner. The central oxidant stream preferably has a low velocity in the range of about 10 throuyh about 30 m/sec. The fuel and oxidant streams issuing from the first and second annular outlet channels may be laterally enclosed by a stream of a low velocity moderator gas, sultably comprislny steam or carbon dioxlde. Thls stream of modorator yas fulfills two different ob~ectlves, namely it lifts the flame, formed after lgnition o~ the fuel/ox.tdant mixture, from the ~ront of ~he burner and it reduces the burner front heat fluxe%.
It will be understood that a shielding moderator gas stream is partlcularly preferred lf heavier hydrocarbon fuels, causing the release of much heat of reaction when gasified, are used as feedstock for the production of synthesis gas. The velocity of the stream of moderator gas is preferably chosen in the range of about 10 through about 40 m/sec. For reducing the outflow veloclty of the moderator gas s~ream, the burner is . . . = , ~2~89l~
-5a- 63293-247 preferably provlded with a moderator ga~ outlet channel widening towards the frQnt of the hurner. The central outlet channel and the fir~t outlet channel may be supplied with oxidant via a common oxidant supply channel substantially coaxially arranged with the central outlet channel. Al~ernatively, these two channels are independently fed via two separate oxidant supply channels. In the first variant the velocity dlfference between the oxidant stream lssuing from the central outlet channel and the oxidant stream from the first annular outlet channel is achieved by using a central outlet channel which widens towards the front of the burner. The second variant, in whlch the oxidant outlet channels are connected to separate supply channels, may be preferred over the flrst one, if the burner is to ~e used over a wide range of fuel loads and fuel conditions. The application of two separate oxidant supply channels enables lndependent control of the low velocity oxidan~ stream and the high velocity oxidant. The ma~s flow ratio of high veloci~y oxidant and low velocity oxidant is pre~erably about 30,70.
" ,~ .
9~
For minimizing the risk of overheating of` the burner, the central outlet channel, the first and the second annular outlet channel are preferably retracted from the front of the burner.
By this arrangement of the burner internals the heat flux near the internals is considerably lower than the heat flux in the reaction zone. The rate of retraction should preferably not ex-ceed about 10 mm.
The invention will now be further elucidated by way of ex-ample only with reference to the accompanying drawings, in which Figure 1 shows a longitudinal section of a first burner to be used in the process according to the invention; and Figure 2 shows a longitudinal section of a second burner to be used in the process according to the invention.
Re~erring to Figure 1, a burner 1 for the gasification of a hydrocarbon fuel being in the liquid state or in the slurry state, is shown which burner comprises a cylindrical hollow wall member 2 having an enlarged endpart forming a front face 3 which is sub-stantially normal to the longitudinal axis 4 of the burner. The interior of the hollow wall member 2 is provided with a concentric wall 5, dividing the interior of said wall member 2 into pas3ages 6 and 7 for cooling fluid supplied and discharged via not shown conduit means. The hollow wall rnember 2 laterally encompasses a plurality of substantially coaxially arranged channels for fuel and oxidant, viz. a central outlet channel 8 for low velocity oxidant, a first annular outlet channel 9 for high velocity oxi-dant and a second annular outlet channel 10 for low velocity f`uel.
Between the wall of said second annular outlet channel 10 and the inner surface of wall member 2 an annular space is left forming a channel for a moderator gas. As shown in Figure 1~ the outer end-part of fuel channel 10 is arranged at a forward angle of about30 degrees with respect to the high velocity oxidant channel 9, to promote breaking up the fuel stream issuing from channel 10 during operation of the burner. The first annular outlet channel 9 and the central outlet channel 8 are both in fluid communication ;9~
- 7, with a substantially centrally arranged oxidant supply channel 11.
For reducing the velocity of the oxidant stream passing through the central outlet channel 8 during operation of the burner, the cross-section of said channel widens in downstream direction.
For minimizing flow turbulences, the widening of the channel should preferably be gradual. The rate of increase of the cross-section depends on the desired velocity difference between the oxidant stream from the central channel 8 and the oxidant stream from the annular channel 9. The slit width of the fuel channel 10 should be rather small, in the order of magnitude of about 5 mm, to keep the fuel stream from said channel sufficiently thin for being easily broken up by high velocity oxidant. The annular space, indicated with reference number 12, between the second annular channel 10 and the hollow wall member 2, has an in downstream direction widening endpart 13, to promote outflow of moderator gas with a low velocity.
As shown in Figure 1, the burner internals forming the channels 8, 9 and 10, are slightly retracted from the front face 3, to protect chese internals against excess heat fluxes. Preferably these internals are additionally cooled by passing cooling medium through a channel 12, arranged between the first and second annu-lar outlet channels 9 and 10. It should be noted that also the oxidant passing through the first annular channel 9 and the mode~
rator gas passin~ through the annular space 12 form an important contribution to the cooling of the burner internals.
Reference is now made to Figure 2, showing a suitable variant of the burner described above. It should be noted that identical elements have been indicated in the Figures with the same reference numeral. In the embodiment shown in Figure 2, the oxidant supply means are formed by a central oxidant chan-nel 20 and an annular oxidant channel 21, which are not in fluid communication with one another as in the first shown burner em-bodiment. The channels 20 and 21 are each connected to a seParate oxidant source for the supply of low velocity oxidant and for the 38~
supply of high velocity oxidant, respectively, so that the oxi-dant supply to each of said channels can be controlled and varied independently from one another. On account of the absence of a separate moderator gas channel and a cooling channel between the fuel and oxidant channels, this second burner is of a more simple construction than the first one. It should however be noted that this second burner should be used for gasification of hydrocarbon fuels causing release of only a moderate reaction of heat upon gasification.
PROCESS FOR PRODUCING SYMTHESIS GAS FROM HYDROCARBON FVEL
The present invention relates to a process for producing synthesis gas by partial combustion of a hydrocarbon fuel being in liquid state or in slurry state, with an oxidant consisting of oxygen or an oxygen-containing gas.
Hydrocarbon fuels can be converted into synthesis gas, com-prising essentially a mixture of hydrogen and carbon monoxide, by a controlled reaction with a substoichiometric quantity of oxygen or an oxygen-containing gas, such as air. Gases so pro duced may for example be used as feedstock for the manufacture of chemical products, as reducing agent and as a clean fuel~
A primary requirement in processes for producing synthesis gas, also called gasification processes, consists herein that hydrocarbon feedstock is intimately and uniformly mixed with oxidant during the gasification. If the mixing is insufficient, the quality of the formed synthesis gas can be severely impaired in that part Or the feedstock i9 insuffioiently gasified whilst another part is completelg converted into less valuable products, viz. ¢arbon dioxide and water vapour. For meeting the above re-quirement it is essential that the hydrocarbon fuel stream sup-plied i9 broken up into fragments whioh are sufficiently smallfor generating a substantially homogeneous mixture of hydro-carbon fuel and oxidant upon introduction of the oxidant into the fuel stream.
Insufficient contact between the reactants, formed by hydro-carbon fuel and oxidant, may further cause damage to the equip-ment used in the process. If the reactants are not brought into intimate contact with one another oxidant and fuel will ~ollow at least partially independent trajectories inside the reactor in which the process takes place. Since the reactor is filled with mainly hot already formed carbon monoxide and hydrogen, the '~
6~
oxidant ~lll rapidly react with these gases instead of with the fuel. If the oxidant is formed by oxygen or a gas containing free oxygen the reaction will be exothermic and the combustion products, consisting of carbon dioxide and water vapour, will be very hot. These combustion products will also follow independent trajectories, resulting in a poor contact with the relatively cold fuel flow in the reactor. The above phenomenon will result in the formation of local hot spots in the reactor, thereby possibly causing damage to the reactor refractory liming and the used burner(s). The above risk of damage to the process equipment becomeYeven more severe, if relatively heavy hydrocarbon fuels are to be processed, because of the release of a relatively large heat of reaction when such fuels are gasi~ied with free oxygen.
Sufficient mixing o~ the reactants might be attained in the burner itself. A disadvantage of this option is however that - especially at the usually high pressure gasification - the design and the operation of the burner are highly critical. The reason for this is that the time elapsing between the moment of mixing and the moment the fuel/oxygen mixture enters into the reaction zone should be invariably shorter than the combustion induction time of the mixture. Moreover, the velocity of the mixture inside the burner should be higher than the flame pro-pagation velooity in or-der to avoid flash back. However, the combustion induction time shortens and the flame propagation velocity increase.s at a rise in gasi~ication pressure. If the burner i~ operated at a relatively low ~uel load or, in other words, if the velocity of the ~uel/oxygen mixture in the burner is relatively low, the combustion induction time and/or flash back condition might easily be reached in the burner itself, with as a result overheating and possibly severe damage to the burner.
The above risks of premature combustion and flash back are eliminated if fuel and oxidant are mixed outside the burner in ~269~34X
~ 3 - 63293-2~73 the reaction zone. In thi~ ca~e Qpecial measures are to be taken to ensure a proper mlxing of the reactant~ neces~ary for an effective gaQification of the fuel aa di_cu~sed in the above. A
further complication of mixing fuel and oxidant in the reaction zone outside the burner i~ the risk of overheating of the front part of the burner facing the reaction zone due to a hot flame generated by premature contact of oxygen with already formed synthesiq gas present in the reaction zone. To promote an inti-mate mixing of fuel with oxidant, it ha~ alr~ady been proposed to inject the oxidant aa high velocity jets into a central core flow of fuel. Although such hi~h velocity jet~ are advanta~eous for breaking up the ~uel flow, they may have an adverse effect on the burner ~ront in that they may eaqily cause suction OL` hot reactor ga~eQ along the burner front.
An object of the present invention iQ to provide a process for producing s~ntheai~Q ~aa ~rom hydrocarbon fuel being in liquid state or in Qlurry state, which may be operated at hi~h fuel load~ and wherein the ri~k of product impairment or damage to the equipment u~Qed iQ subatantially eliminated.
The process according to the invention thereto comprises the use o~ at least one burner- consisting of a houQing enclosing a central outlet channel for low velocity oxidant ~urrounded by a first annular outlet channel for high velocity oxidant, whlch firqt annular outlet channel i~ encompassed by a second annular outlet channel for hydrocarbon fuel, said second ~ular outl~t ahannel having an inclined outer part directed towards the first annular outlet channel.
A process for producing synthesis gas by partial combustion o~
3~ a hydrocarbon Euel being in }iquid state or in slurry state, wich an oxidant consisting of oxygen or an oxygen-containing gas, said process comprising the steps of introducing a shielding stream of low velocity hydrocarbon fuel, a scream of high velocity oxidant and a stream of low velocity o~idant via a second annular out ec -`i .. . .
9~
-4- 63~93-~473 channel, a first annular outl~t channol and ~ c~n~ral ou~l~c channel, resp~ctively, o~ one or more burners into a reaction ~one and ~llo~ing ~he hydrocarbon fuel to r~act wich th~ oxidant, said second annular outlet channel having an inclined outer end part directed towards the fi~st annular outlet channel.
~ he low veloclty hydrocarbon fuel ~ream issuing from the second annular outlet charlnel o~ a burner ~o be used acco~dlng to the invention is brsken up by the ~tream of hijh velocity oxidant 1~ ulng from the ~lr~t annular outlet channel, and forms ln fact a ~hield around tho oxid~nt thereby ~reven~ing pre~ature contact of oxldant wlth already ~ormed 6yn~he~is gas.
Slncs accordin~ to the invention the se~ond annular outlet channel has an lnclined out~r part dlrected towards the flrst annular outlet channel and the fu~l is introduced into ~he reaction zone ~ith a low veloclty ~referably in ~he range of between about 5 and about 15 m/~ec whlls~ oxldant ~ro~ the first annular outlet channel enter~ the reaction zone with a substantially hi~her veloclty, c~u~in~ a hlgh ~lip velocity between fuel and oxldant the hydrocarbon fuel stred~ can be e~ectlvely b~oken u~ and mlxed wlth oxidant. ~he veloclty of the oxldant stream from the flr~ annular outlet ahannel ls preferably cho~en in the range of about 50 ~hrough about 90 m/~ec. ~or optlmlzatlo~ of the ~lxln~ o~ the ~uel wl~h oxidant, the fuel stream ~nd therefore the ou~er part o~ tho econd ann~lar outlet channel should preferably be ~o~ltloned at an angle of ~etween about 2û and ~bout 40 with respect ~o the ~lr6t annular outlet channel.
.
, ~ ;
'' ''"' . ~ ' . :'' "'.'.
891;~
-5- 63~g3-2~73 If heavy hydrocarbon fuels are ko be processed, lt may be advantageous to pre-atomize the fuel prior to contact with the oxldant issuing from the first annular outlet channel in order to promote breaking up of the fuel flow by the high velocity oxidant.
The pre-atomization of the fuel is preferably attalned by addiny an atomization fluid, such as steam or carbondioxide, to the fuel prior to entering into the reaction zone.
During operation of the burner to be used in the process according to the invention the space laterally enclosed by the oxidant stream from the first annular outlet channel is filled with low velocity oxidant issuing from the central outlet channel, thereby preventing the generation of wakes which miyht cause flame attachment to the front of the burner. The central oxidant stream preferably has a low velocity in the range of about 10 throuyh about 30 m/sec. The fuel and oxidant streams issuing from the first and second annular outlet channels may be laterally enclosed by a stream of a low velocity moderator gas, sultably comprislny steam or carbon dioxlde. Thls stream of modorator yas fulfills two different ob~ectlves, namely it lifts the flame, formed after lgnition o~ the fuel/ox.tdant mixture, from the ~ront of ~he burner and it reduces the burner front heat fluxe%.
It will be understood that a shielding moderator gas stream is partlcularly preferred lf heavier hydrocarbon fuels, causing the release of much heat of reaction when gasified, are used as feedstock for the production of synthesis gas. The velocity of the stream of moderator gas is preferably chosen in the range of about 10 through about 40 m/sec. For reducing the outflow veloclty of the moderator gas s~ream, the burner is . . . = , ~2~89l~
-5a- 63293-247 preferably provlded with a moderator ga~ outlet channel widening towards the frQnt of the hurner. The central outlet channel and the fir~t outlet channel may be supplied with oxidant via a common oxidant supply channel substantially coaxially arranged with the central outlet channel. Al~ernatively, these two channels are independently fed via two separate oxidant supply channels. In the first variant the velocity dlfference between the oxidant stream lssuing from the central outlet channel and the oxidant stream from the first annular outlet channel is achieved by using a central outlet channel which widens towards the front of the burner. The second variant, in whlch the oxidant outlet channels are connected to separate supply channels, may be preferred over the flrst one, if the burner is to ~e used over a wide range of fuel loads and fuel conditions. The application of two separate oxidant supply channels enables lndependent control of the low velocity oxidan~ stream and the high velocity oxidant. The ma~s flow ratio of high veloci~y oxidant and low velocity oxidant is pre~erably about 30,70.
" ,~ .
9~
For minimizing the risk of overheating of` the burner, the central outlet channel, the first and the second annular outlet channel are preferably retracted from the front of the burner.
By this arrangement of the burner internals the heat flux near the internals is considerably lower than the heat flux in the reaction zone. The rate of retraction should preferably not ex-ceed about 10 mm.
The invention will now be further elucidated by way of ex-ample only with reference to the accompanying drawings, in which Figure 1 shows a longitudinal section of a first burner to be used in the process according to the invention; and Figure 2 shows a longitudinal section of a second burner to be used in the process according to the invention.
Re~erring to Figure 1, a burner 1 for the gasification of a hydrocarbon fuel being in the liquid state or in the slurry state, is shown which burner comprises a cylindrical hollow wall member 2 having an enlarged endpart forming a front face 3 which is sub-stantially normal to the longitudinal axis 4 of the burner. The interior of the hollow wall member 2 is provided with a concentric wall 5, dividing the interior of said wall member 2 into pas3ages 6 and 7 for cooling fluid supplied and discharged via not shown conduit means. The hollow wall rnember 2 laterally encompasses a plurality of substantially coaxially arranged channels for fuel and oxidant, viz. a central outlet channel 8 for low velocity oxidant, a first annular outlet channel 9 for high velocity oxi-dant and a second annular outlet channel 10 for low velocity f`uel.
Between the wall of said second annular outlet channel 10 and the inner surface of wall member 2 an annular space is left forming a channel for a moderator gas. As shown in Figure 1~ the outer end-part of fuel channel 10 is arranged at a forward angle of about30 degrees with respect to the high velocity oxidant channel 9, to promote breaking up the fuel stream issuing from channel 10 during operation of the burner. The first annular outlet channel 9 and the central outlet channel 8 are both in fluid communication ;9~
- 7, with a substantially centrally arranged oxidant supply channel 11.
For reducing the velocity of the oxidant stream passing through the central outlet channel 8 during operation of the burner, the cross-section of said channel widens in downstream direction.
For minimizing flow turbulences, the widening of the channel should preferably be gradual. The rate of increase of the cross-section depends on the desired velocity difference between the oxidant stream from the central channel 8 and the oxidant stream from the annular channel 9. The slit width of the fuel channel 10 should be rather small, in the order of magnitude of about 5 mm, to keep the fuel stream from said channel sufficiently thin for being easily broken up by high velocity oxidant. The annular space, indicated with reference number 12, between the second annular channel 10 and the hollow wall member 2, has an in downstream direction widening endpart 13, to promote outflow of moderator gas with a low velocity.
As shown in Figure 1, the burner internals forming the channels 8, 9 and 10, are slightly retracted from the front face 3, to protect chese internals against excess heat fluxes. Preferably these internals are additionally cooled by passing cooling medium through a channel 12, arranged between the first and second annu-lar outlet channels 9 and 10. It should be noted that also the oxidant passing through the first annular channel 9 and the mode~
rator gas passin~ through the annular space 12 form an important contribution to the cooling of the burner internals.
Reference is now made to Figure 2, showing a suitable variant of the burner described above. It should be noted that identical elements have been indicated in the Figures with the same reference numeral. In the embodiment shown in Figure 2, the oxidant supply means are formed by a central oxidant chan-nel 20 and an annular oxidant channel 21, which are not in fluid communication with one another as in the first shown burner em-bodiment. The channels 20 and 21 are each connected to a seParate oxidant source for the supply of low velocity oxidant and for the 38~
supply of high velocity oxidant, respectively, so that the oxi-dant supply to each of said channels can be controlled and varied independently from one another. On account of the absence of a separate moderator gas channel and a cooling channel between the fuel and oxidant channels, this second burner is of a more simple construction than the first one. It should however be noted that this second burner should be used for gasification of hydrocarbon fuels causing release of only a moderate reaction of heat upon gasification.
Claims (9)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A process for producing synthesis gas by partial combustion of a hydrocarbon fuel being in liquid state or in slurry state, with an oxidant consisting of oxygen or an oxygen-containing gas, said process comprising the steps of introducing a shielding stream of low velocity hydrocarbon fuel, a stream of high velocity oxidant and a stream of low velocity oxidant via a second annular outlet channel, a first annular outlet channel and a central outlet channel, respectively, of one or more burners into a reaction zone and allowing the hydrocarbon fuel to react with the oxidant, said second annular outlet channel having an inclined outer end part directed towards the first annular outlet channel.
2. Process as claimed in claim 1, wherein the stream of hydrocarbon fuel is admixed with an atomizing medium prior to introduction into the reaction zone.
3. process as claimed in claim 1, wherein the stream of hydrocarbon fuel is introduced into the reaction zone with velocity in the range of about 5 through about 15 m/sec.
4. Process as claimed in claim 1, wherein the mass flow ratio of high velocity oxidant and low velocity oxidant is about 30:70.
5. Process as claimed in claim 1, wherein the stream of high velocity oxidant is issued from the burner with a velocity in the range of about 50 through about 90 m/sec.
6. Process as claimed in claim 1, wherein the stream of low velocity oxidant is issued from the burner with a velocity in the range of about 10 through about 30 m/sec.
7. Process as claimed in claim 1, wherein a stream of low velocity moderator gas is formed around the oxidant and fuel streams.
8. Process as claimed in claim 7, wherein the moderator gas is selected from the group consisting of steam, carbon dioxide, nitrogen cold reactor gas or mixtures thereof.
9. Process as claimed in claim 7 or 8, wherein the stream of moderator gas has a velocity upon leaving the burner(s) in the range of about 10 through about 40 m/sec.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB08332945A GB2151348B (en) | 1983-12-09 | 1983-12-09 | Burner and process for producing synthesis gas from hydrocarbon fuel |
| GB8332945 | 1983-12-09 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1269842A true CA1269842A (en) | 1990-06-05 |
Family
ID=10553100
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000468393A Expired - Fee Related CA1269842A (en) | 1983-12-09 | 1984-11-22 | Process for producing synthesis gas from hydrocarbon fuel |
Country Status (12)
| Country | Link |
|---|---|
| JP (1) | JPH0694361B2 (en) |
| KR (1) | KR920000778B1 (en) |
| CN (1) | CN85105729A (en) |
| BR (1) | BR8406227A (en) |
| CA (1) | CA1269842A (en) |
| CS (1) | CS269965B2 (en) |
| DD (1) | DD229982A5 (en) |
| DE (1) | DE3444590C2 (en) |
| ES (1) | ES538324A0 (en) |
| FR (1) | FR2556332B1 (en) |
| GB (1) | GB2151348B (en) |
| PT (1) | PT79633B (en) |
Families Citing this family (19)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB8619076D0 (en) * | 1986-08-05 | 1986-09-17 | Shell Int Research | Partial oxidation of fuel |
| GB8711156D0 (en) * | 1987-05-12 | 1987-06-17 | Shell Int Research | Partial oxidation of hydrocarbon-containing fuel |
| US4887962A (en) * | 1988-02-17 | 1989-12-19 | Shell Oil Company | Partial combustion burner with spiral-flow cooled face |
| US4865542A (en) * | 1988-02-17 | 1989-09-12 | Shell Oil Company | Partial combustion burner with spiral-flow cooled face |
| JP2928299B2 (en) * | 1989-09-22 | 1999-08-03 | 株式会社神戸製鋼所 | Generation method of reducing gas |
| CN1043028C (en) * | 1994-05-19 | 1999-04-21 | 国际壳牌研究有限公司 | Process for manufacture of synthesis gas by partial oxidation of liquid hydrocarbon-containing fuel using multi-orifice (coannular) burner |
| AT402440B (en) * | 1995-06-01 | 1997-05-26 | Voest Alpine Ind Anlagen | BURNER |
| DE69822635T2 (en) | 1998-10-30 | 2005-02-10 | Casale Chemicals Sa | Process and burner for the partial oxidation of hydrocarbons |
| DE19941978B4 (en) * | 1999-09-03 | 2005-09-22 | Stiebel Eltron Gmbh & Co. Kg | Method and device for producing a synthesis gas |
| JP4851027B2 (en) * | 2001-06-22 | 2012-01-11 | 大陽日酸株式会社 | Combustion apparatus and burner for carbon monoxide and hydrogen generation |
| DE10248530B4 (en) * | 2002-10-14 | 2004-08-12 | Thermoselect Ag | Oxygen lance for high-temperature gasification of waste, and method for operating the same |
| DK1607370T3 (en) * | 2004-06-18 | 2011-11-21 | Casale Chemicals Sa | Process and burner for partial oxidation of hydrocarbons |
| JP4739090B2 (en) * | 2006-04-06 | 2011-08-03 | 大陽日酸株式会社 | Burner or lance cooling structure |
| CN101363626B (en) * | 2007-08-06 | 2015-05-20 | 国际壳牌研究有限公司 | Method of manufacturing a burner front face |
| CN101363624B (en) | 2007-08-06 | 2011-05-25 | 国际壳牌研究有限公司 | Burner |
| CN202835334U (en) * | 2012-04-02 | 2013-03-27 | 国际壳牌研究有限公司 | Burner used for gasified solid fuel |
| CN104560210A (en) * | 2015-01-19 | 2015-04-29 | 清华大学 | Coal water slurry atomizing nozzle and gasification furnace with same |
| RU2640079C2 (en) * | 2016-06-16 | 2017-12-26 | Алексей Александрович Никифоров | Chemical compression reactor |
| CN114231320B (en) * | 2021-11-29 | 2023-04-14 | 北京航化节能环保技术有限公司 | Coal gasification device capable of operating under variable load |
Family Cites Families (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB218701A (en) * | 1923-02-14 | 1924-07-14 | Ludwig Grote | Burner for pulverulent fuel |
| GB227479A (en) * | 1923-07-17 | 1925-01-19 | Cornelis Zulver | Improvements in or relating to liquid fuel burners or atomizers |
| GB298080A (en) * | 1927-10-01 | 1929-08-29 | Witkowitzer Bergb Gewerkschaft | Coal dust, gas and oil burner for constant velocities of ejection under variable loads |
| GB1266072A (en) * | 1969-02-11 | 1972-03-08 | ||
| US3743606A (en) * | 1970-01-23 | 1973-07-03 | Texaco Development Corp | Synthesis gas generation |
| FR2230583A1 (en) * | 1973-05-24 | 1974-12-20 | Texaco Development Corp | Synthesis gas generation - using triple orifice burner designed to prevent heat induced damage |
| JPS5246192A (en) * | 1975-10-11 | 1977-04-12 | Hideo Furukawa | Discharge printing method and apparatus |
| JPS5525122A (en) * | 1978-08-11 | 1980-02-22 | Hitachi Ltd | Multiple digital control method |
| GB2094969B (en) * | 1981-03-13 | 1985-01-03 | Kawasaki Heavy Ind Ltd | Method of combustion of pulverised coal by pulverised coal burner |
| DE3219316A1 (en) * | 1982-05-22 | 1983-11-24 | Ruhrchemie Ag, 4200 Oberhausen | METHOD AND DEVICE FOR PRODUCING SYNTHESIS GAS BY PARTIAL OXIDATION OF COAL-WATER SUSPENSIONS |
| US4502633A (en) * | 1982-11-05 | 1985-03-05 | Eastman Kodak Company | Variable capacity gasification burner |
-
1983
- 1983-12-09 GB GB08332945A patent/GB2151348B/en not_active Expired
-
1984
- 1984-11-22 CA CA000468393A patent/CA1269842A/en not_active Expired - Fee Related
- 1984-12-06 FR FR8418616A patent/FR2556332B1/en not_active Expired
- 1984-12-06 BR BR8406227A patent/BR8406227A/en not_active IP Right Cessation
- 1984-12-06 DD DD84270383A patent/DD229982A5/en not_active IP Right Cessation
- 1984-12-06 ES ES538324A patent/ES538324A0/en active Granted
- 1984-12-06 JP JP59256633A patent/JPH0694361B2/en not_active Expired - Lifetime
- 1984-12-06 DE DE3444590A patent/DE3444590C2/en not_active Expired - Fee Related
- 1984-12-06 PT PT79633A patent/PT79633B/en not_active IP Right Cessation
- 1984-12-06 CS CS849451A patent/CS269965B2/en unknown
- 1984-12-06 KR KR1019840007693A patent/KR920000778B1/en not_active IP Right Cessation
-
1985
- 1985-07-27 CN CN198585105729A patent/CN85105729A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| GB2151348A (en) | 1985-07-17 |
| FR2556332A1 (en) | 1985-06-14 |
| ES8507418A1 (en) | 1985-09-01 |
| PT79633A (en) | 1985-01-01 |
| ES538324A0 (en) | 1985-09-01 |
| DD229982A5 (en) | 1985-11-20 |
| KR850004259A (en) | 1985-07-11 |
| FR2556332B1 (en) | 1988-10-21 |
| CN85105729A (en) | 1987-03-04 |
| GB2151348B (en) | 1986-08-06 |
| CS269965B2 (en) | 1990-05-14 |
| PT79633B (en) | 1986-10-21 |
| DE3444590C2 (en) | 1996-02-29 |
| JPH0694361B2 (en) | 1994-11-24 |
| KR920000778B1 (en) | 1992-01-23 |
| BR8406227A (en) | 1985-10-01 |
| GB8332945D0 (en) | 1984-01-18 |
| JPS60141602A (en) | 1985-07-26 |
| DE3444590A1 (en) | 1985-06-20 |
| CS945184A2 (en) | 1989-10-13 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKLA | Lapsed |