GB2151348A - Burner and process for producing synthesis gas from hydrocarbon fuel - Google Patents

Burner and process for producing synthesis gas from hydrocarbon fuel Download PDF

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Publication number
GB2151348A
GB2151348A GB08332945A GB8332945A GB2151348A GB 2151348 A GB2151348 A GB 2151348A GB 08332945 A GB08332945 A GB 08332945A GB 8332945 A GB8332945 A GB 8332945A GB 2151348 A GB2151348 A GB 2151348A
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GB
United Kingdom
Prior art keywords
outlet channel
oxidant
burner
annular outlet
stream
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
Application number
GB08332945A
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GB8332945D0 (en
GB2151348B (en
Inventor
Hendrikus Johannus An Hasenack
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shell Internationale Research Maatschappij BV
Original Assignee
Shell Internationale Research Maatschappij BV
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Priority to GB08332945A priority Critical patent/GB2151348B/en
Publication of GB8332945D0 publication Critical patent/GB8332945D0/en
Priority to CA000468393A priority patent/CA1269842A/en
Priority to KR1019840007693A priority patent/KR920000778B1/en
Priority to PT79633A priority patent/PT79633B/en
Priority to FR8418616A priority patent/FR2556332B1/en
Priority to ES538324A priority patent/ES8507418A1/en
Priority to DD84270383A priority patent/DD229982A5/en
Priority to CS849451A priority patent/CS269965B2/en
Priority to JP59256633A priority patent/JPH0694361B2/en
Priority to BR8406227A priority patent/BR8406227A/en
Priority to DE3444590A priority patent/DE3444590C2/en
Publication of GB2151348A publication Critical patent/GB2151348A/en
Priority to CN198585105729A priority patent/CN85105729A/en
Application granted granted Critical
Publication of GB2151348B publication Critical patent/GB2151348B/en
Expired legal-status Critical Current

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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)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

A burner for producing synthesis gas by partial combustion of a hydrocarbon fuel in liquid state or in slurry state with an oxidant consisting of oxygen or an oxygen- containing gas, comprises a housing enclosing a central outlet channel (8) for low velocity oxidant surrounded by a first annular outlet channel (9) for high velocity oxidant which first annular outlet channel is encompassed by a second annular outlet channel (10) for hydrocarbon fuel, said second annular outlet channel (10) having an inclined outer part directed towards the first annular outlet channel (9). <IMAGE>

Description

SPECIFICATION Burner and process for producing synthesis gas from hydrocarbon fuel The present invention relates to a burner 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. The invention further relates to a process for producing synthesis gas from hydrocarbon fuel, in which process one or more of such burners are used.
Hydrocarbon fuels can be converted into synthesis gas, comprising 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 produced may for example be used as feedstock for the manufacture of chemical products, as reducing agent for 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 of the feedstock is insufficiently gasified whilst another part is completely converted into less valuable products, viz. carbon dioxide and water vapour. For meeting the above requirement it is essential that the hydrocarbon fuel stream supplied is broken up into fragments which are sufficiently small for generating a substantially homogeneous mixture of hydrocarbon fuel and oxidant upon introduction of the oxidant into the fuel stream.
Insufficient contact between the reactants, formed by hydrocarbon fuel and oxidant, may further cause damage to the equipment used in the process. If the reactants are not brought into intimate contact with one another oxidant and fuel will follow 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 oxidant will 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 becomes even more servere, if relatively heavy hydrocarbon fuels are to be processed, because of the release of a relatively large heat of reaction when such fuels are gasified with free oxygen.
Sufficient mixing of 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 propagation velocity in order to avoid flash back. However, the combustion induction time shortens and the flame propagation velocity increases at a rise in gasification pressure.If the burner is operated at a relatively low fuel load or, in other words, if the velocity of the fuel/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 the reaction zone. In this case special measures are to be taken to ensure a proper mixing of the reactants necessary for an effective gasification of the fuel as discussed in the above. A further complication of mixing fuel and oxidant in the reaction zone outside the burner is 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 synthesis gas present in the reaction zone. To promote an intimate mixing of fuel with oxidant, it has already been proposed to inject the oxidant as high velocity jets into a central core flow of fuel.
Although such high velocity jets are advantageous for breaking up the fuel flow, they may have an adverse effect on the burner front in that they may easily cause suction of hot reactor gases along the burner front.
An object of the present invention is to provide a burner for producing synthesis gas from hydrocarbon fuel being in liquid state or in slurry state, which may be operated at high fuel loads and wherein the risk of product impairment or damage to the equipment used is substantially eliminated.
The burner according to the invention thereto comprises 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.
Apart from a burner a process is provided 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 according to the invention comprises introducing a stream of low velocity hydrocarbon fuel, a stream of high velocity oxidant and a stream of low velocity oxidant, via the second annular outlet channel, the first annular outlet channel and the central outlet channel, respectively, of one or more burners according the invention, into a reaction zone and allowing the stream of hydrocarbon fuel to react with the oxidant.
The low velocity hydrocarbon fuel stream issuing from the second annular outlet channel of a burner according to the invention is broken up by the stream of high velocity oxidant issuing from the first annular outlet channel, and forms in fact a shield around the oxidant thereby preventing premature contact of oxidant with already formed synthesis gas.
Since according to the invention the second annular outlet channel has an inclined outer part directed towards the first annular outlet channel and the fuel is introduced into the reaction zone with a low velocity preferably in the range of between about 5 and about 1 5 m/sec whilst oxidant from the first annular outlet channel enters the reaction zone with a substantially higher velocity, causing a high slip velocity between fuel and oxidant, the hydrocarbon fuel stream can be effectively broken up and mixed with oxidant. The velocity of the oxidant stream from the first annular outlet channel is preferably chosen in the range of about 50 through about 90 m/sec.
For optimization of the mixing of the fuel with oxidant, the fuel stream and therefore the outer part of the second annular outlet channel should preferably be positioned at an angle of between about 20 and about 40 with respect to the first annular outlet channel.
If heavy hydrocarbon fuels are to be processed, it may be advantageous to pre-atomize the fuel prior to contact with the oxidant 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 attained by adding an atomization fluid, such as steam or carbondioxide, to the fuel prior to entering into the reaction zone.
During operation of the proposed burner 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 might cause flame attachment to the front of the burner. The central oxidant stream preferably has a low velocity in the range of about 10 through 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, suitably comprising steam or carbon dioxide. This stream of moderator gas fulfills two different objectives, namely it lifts the flame, formed after ignition of the fuel/oxidant mixture, from the front of the burner and it reduces the burner front heat fluxes.
It will be understood that a shielding moderator gas stream is particularly preferred if 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 outfiow velocity of the moderator gas stream, the burner is preferably provided with a moderator gas outlet channel widening towards the front of the burner. The central outlet channel and the first outlet channel may be supplied with oxidant via a common oxidant supply channel substantially coaxially arranged with the central outlet channel. Alternatively, these two channels are independently fed via two separate oxidant supply channels. In the first variant the velocity difference between the oxidant stream issuing 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 which the oxidant outlet channels are connected to separate supply channels, may be preferred over the first one, if the burner is to be used over a wide range of fuel loads and fuel conditions. The application of two separate oxidant supply channels enables independent control of the low velocity oxidant stream and the high velocity oxidant.
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 internais the heat flux near the internals is considerably lower than the heat flux in the reaction zone. The rate of retraction should preferably not exceed about 10 mm.
The invention will now be further elucidated by way of example only with reference to the accompanying drawings, in which Figure 1 shows a longitudinal section of a first burner according to the invention; and Figure 2 shows a longitudinal section of a second burner according to the invention.
Referring to Fig. 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 substantially 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 passages 6 and 7 for cooling fluid supplied and discharged via not shown conduit means. The hollow wall member 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 oxidant and a second annular outlet channel 10 for low velocity fuel.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 Fig. 1, the outer endpart of fuel channel 10 is arranged at a forward angle of about 30 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 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 crosssection 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 crosssection depends on the desired velocity difference between the oxidant stream for 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 Fig. 1, the burner internals forming the channels 8, 9 and 10, are slightly retracted from the front face 3, to protect these internals against excess heat fluxes.
Preferably these internals are additionally cooled by passing cooling medium through a channel 1 2, arranged between the first and second annular outlet channels 9 and 10. It should be noted that also the oxidant passing through the first annular channel 9 and the moderator gas passing through the annular space 1 2 form an important contribution to the cooling of the burner internals.
Reference is now made to Fig. 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 Fig. 2, the oxidant supply means are formed by a central oxidant channel 20 and an annular oxidant channel 21, which are not in fluid communication with one another as in the first shown burner embodiment. The channels 20 and 21 are each connected to a separate oxidant source for the supply of low velocity oxidant and for the supply of high velocity oxidant, respectively, so that the oxidant 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 (17)

1. Burner 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 oxygencontaining gas, which burner comprises 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.
2. Burner as claimed in claim 1, wherein the outer ends of the central outlet channel and the first and second annular outlet channels are retracted from the front of the housing.
3. Burner as claimed in claim 2, wherein the outer ends of the central outlet channel and the first and second annular outlet channels are retracted over a distance of at most about 10 mm from the front of the housing.
4. Burner as claimed in any one of the claims 1-3, wherein the outer part of the second annular outlet channel is arranged at an angle of between about 20 and about 40 degrees with respect to the first annular outlet channel.
5. Burner as claimed in any one of the claims 1-4, wherein the burner further comprises a central oxidant supply channel connected to the central outlet channel and the first annular outlet channel, the central outlet channel having an outwardly diverging shape for the issue of low velocity oxidant.
6. Burner as claimed in any one of the claims 1-4, wherein the central outlet channel and the first annular outlet channel are connected to separate supply channels for supplying low velocity oxidant and high velo city oxidant, respectively.
7. Burner as claimed in any one of the claims 1-6, wherein the second annular outlet channel is surrounded by a third annular outlet channel for low velocity moderator gas.
8. Burner as claimed in claim 7, wherein the third outlet channel has an outer end part with a cross sectional area increasing towards the front of the housing.
9. 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 oxygencontaining gas, which process comprises introducing a stream of low velocity hydrocarbon fuel, a stream of high velocity oxidant and a stream of low velocity oxidant via the second annular outlet channel, the first annular outlet channel and the central outlet channel, respectively, of one or more burners as claimed in any one of the preceding claims into a reaction zone and allowing the hydrocarbon fuel to react with the oxidant.
10. Process as claimed in claim 9, wherein the stream of hydrocarbon fuel is admixed with an atomizing medium prior to introduction into the reaction zone.
11. Process as claimed in claim 9 or 10, wherein the stream of hydrocarbon fuel is introduced into the reaction zone with a velocity in the range of about 5 through about 1 5 m/sec.
1 2. Process as claimed in any one of the claims 9-11, wherein the mass flow ratio of high velocity oxidant and low velocity oxidant is about 30:70.
1 3. Process as claimed in any one of the claims 9-12, 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.
14. Process as claimed in any one of the claims 9-13, 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.
15. Process as claimed in any one of the claims 9-14, wherein a stream of low velocity moderator gas is formed around the oxidant and fuel streams.
1 6. Process as claimed in claim 1 5, wherein the moderator gas is formed by steam, carbon dioxide, nitrogen cold reactor gas or mixtures thereof.
17. Process as claimed in claim 1 5 or 16, 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.
1 8. Burner for producing synthesis gas by partial combustion of a hydrocarbon fuel being in liquid state or in slurry state hydrocarbon fuel substantially as described with parti cular reference to the accompanying drawings.
1 9. Process for producing synthesis gas by partial combustion of a hydrocarbon fuel being in liquid state or in slurry state substantially as described with particular reference to the accompanying drawings.
GB08332945A 1983-12-09 1983-12-09 Burner and process for producing synthesis gas from hydrocarbon fuel Expired GB2151348B (en)

Priority Applications (12)

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
CA000468393A CA1269842A (en) 1983-12-09 1984-11-22 Process for producing synthesis gas from hydrocarbon fuel
DD84270383A DD229982A5 (en) 1983-12-09 1984-12-06 METHOD FOR PRODUCING SYNTHESEGAS FROM A HYDROCARBON FUEL
BR8406227A BR8406227A (en) 1983-12-09 1984-12-06 PROCESS FOR THE PRODUCTION OF SYNTHESIS GAS BY PARTIAL COMBUSTION OF HYDROCARBON FUEL IN LIQUID OR SEMI-LIQUID STATE
FR8418616A FR2556332B1 (en) 1983-12-09 1984-12-06 PROCESS FOR THE PRODUCTION OF SYNTHESIS GAS FROM A HYDROCARBON FUEL
ES538324A ES8507418A1 (en) 1983-12-09 1984-12-06 Burner and process for producing synthesis gas from hydrocarbon fuel
KR1019840007693A KR920000778B1 (en) 1983-12-09 1984-12-06 Process for producing synthesis gas from hydrocarbon fuel
CS849451A CS269965B2 (en) 1983-12-09 1984-12-06 Method of synthesis gas production from hydrocarbon fuel
JP59256633A JPH0694361B2 (en) 1983-12-09 1984-12-06 Method for producing synthesis gas from hydrocarbon fuel
PT79633A PT79633B (en) 1983-12-09 1984-12-06 Process for producing synthesis gas from hydrocarbon fuel
DE3444590A DE3444590C2 (en) 1983-12-09 1984-12-06 Process for the production of synthesis gas from a hydrocarbon fuel
CN198585105729A CN85105729A (en) 1983-12-09 1985-07-27 Method with producing synthetic gas from hydrocarbon fuel

Applications Claiming Priority (1)

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

Publications (3)

Publication Number Publication Date
GB8332945D0 GB8332945D0 (en) 1984-01-18
GB2151348A true GB2151348A (en) 1985-07-17
GB2151348B GB2151348B (en) 1986-08-06

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Family Applications (1)

Application Number Title Priority Date Filing Date
GB08332945A Expired GB2151348B (en) 1983-12-09 1983-12-09 Burner and 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) ES8507418A1 (en)
FR (1) FR2556332B1 (en)
GB (1) GB2151348B (en)
PT (1) PT79633B (en)

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0255748A2 (en) * 1986-08-05 1988-02-10 Shell Internationale Researchmaatschappij B.V. Process for partial oxidation of a hydrocarbon-containing fuel
EP0291111A1 (en) * 1987-05-12 1988-11-17 Shell Internationale Researchmaatschappij B.V. Process for partial oxidation of a hydrocarbon-containing gaseous fuel
US4865542A (en) * 1988-02-17 1989-09-12 Shell Oil Company Partial combustion burner with spiral-flow cooled face
US4887962A (en) * 1988-02-17 1989-12-19 Shell Oil Company Partial combustion burner with spiral-flow cooled face
WO1995032148A1 (en) * 1994-05-19 1995-11-30 Shell Internationale Research Maatschappij B.V. A process for the manufacture of synthesis gas by partial oxidation of a liquid hydrocarbon-containing fuel using a multi-orifice (co-annular) burner
WO1996038690A1 (en) * 1995-06-01 1996-12-05 Voest-Alpine Industrieanlagenbau Gmbh Burner
EP0997433A1 (en) * 1998-10-30 2000-05-03 Casale Chemicals SA Process and burner for the partial oxidation of hydrocarbons
EP1607370A1 (en) * 2004-06-18 2005-12-21 Casale Chemicals S.A. Process and burner for hydrocarbon partial oxidation
EP1411296A3 (en) * 2002-10-14 2006-08-02 Thermoselect Aktiengesellschaft Oxygen lance for the high-temperature gasification of waste and method of operation
WO2009019271A1 (en) * 2007-08-06 2009-02-12 Shell Internationale Research Maatschappij B.V. Method of manufacturing a burner front face
US9546784B2 (en) 2007-08-06 2017-01-17 Shell Oil Company Burner
WO2017217889A1 (en) * 2016-06-16 2017-12-21 Алексей Александрович НИКИФОРОВ Chemical compression reactor

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JP2928299B2 (en) * 1989-09-22 1999-08-03 株式会社神戸製鋼所 Generation method of reducing gas
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
JP4739090B2 (en) * 2006-04-06 2011-08-03 大陽日酸株式会社 Burner or lance cooling structure
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
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

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EP0255748A2 (en) * 1986-08-05 1988-02-10 Shell Internationale Researchmaatschappij B.V. Process for partial oxidation of a hydrocarbon-containing fuel
EP0255748A3 (en) * 1986-08-05 1988-09-07 Shell Internationale Research Maatschappij B.V. Process for partial oxidation of a hydrocarbon-containing fuel
EP0291111A1 (en) * 1987-05-12 1988-11-17 Shell Internationale Researchmaatschappij B.V. Process for partial oxidation of a hydrocarbon-containing gaseous fuel
US4865542A (en) * 1988-02-17 1989-09-12 Shell Oil Company Partial combustion burner with spiral-flow cooled face
US4887962A (en) * 1988-02-17 1989-12-19 Shell Oil Company Partial combustion burner with spiral-flow cooled face
WO1995032148A1 (en) * 1994-05-19 1995-11-30 Shell Internationale Research Maatschappij B.V. A process for the manufacture of synthesis gas by partial oxidation of a liquid hydrocarbon-containing fuel using a multi-orifice (co-annular) burner
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
WO1996038690A1 (en) * 1995-06-01 1996-12-05 Voest-Alpine Industrieanlagenbau Gmbh Burner
EP0997433A1 (en) * 1998-10-30 2000-05-03 Casale Chemicals SA Process and burner for the partial oxidation of hydrocarbons
US6692661B1 (en) 1998-10-30 2004-02-17 Casale Chemicals Sa Process for partial oxidation of hydrocarbons
EP1411296A3 (en) * 2002-10-14 2006-08-02 Thermoselect Aktiengesellschaft Oxygen lance for the high-temperature gasification of waste and method of operation
EP1607370A1 (en) * 2004-06-18 2005-12-21 Casale Chemicals S.A. Process and burner for hydrocarbon partial oxidation
WO2009019271A1 (en) * 2007-08-06 2009-02-12 Shell Internationale Research Maatschappij B.V. Method of manufacturing a burner front face
AU2008285637B2 (en) * 2007-08-06 2011-03-17 Air Products And Chemicals, Inc. Method of manufacturing a burner front face
US9032623B2 (en) 2007-08-06 2015-05-19 Shell Oil Company Method of manufacturing a burner front face
US9546784B2 (en) 2007-08-06 2017-01-17 Shell Oil Company Burner
WO2017217889A1 (en) * 2016-06-16 2017-12-21 Алексей Александрович НИКИФОРОВ Chemical compression reactor
RU2640079C2 (en) * 2016-06-16 2017-12-26 Алексей Александрович Никифоров Chemical compression reactor

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CS269965B2 (en) 1990-05-14
GB8332945D0 (en) 1984-01-18
JPH0694361B2 (en) 1994-11-24
PT79633B (en) 1986-10-21
KR850004259A (en) 1985-07-11
ES538324A0 (en) 1985-09-01
DD229982A5 (en) 1985-11-20
DE3444590A1 (en) 1985-06-20
FR2556332A1 (en) 1985-06-14
CN85105729A (en) 1987-03-04
FR2556332B1 (en) 1988-10-21
CA1269842A (en) 1990-06-05
PT79633A (en) 1985-01-01
KR920000778B1 (en) 1992-01-23
BR8406227A (en) 1985-10-01
GB2151348B (en) 1986-08-06
DE3444590C2 (en) 1996-02-29
ES8507418A1 (en) 1985-09-01
JPS60141602A (en) 1985-07-26
CS945184A2 (en) 1989-10-13

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