EP0109109B1 - Procédé pour la combustion partielle d'un combustible solide avec recyclage des cendres volantes - Google Patents

Procédé pour la combustion partielle d'un combustible solide avec recyclage des cendres volantes Download PDF

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Publication number
EP0109109B1
EP0109109B1 EP83201501A EP83201501A EP0109109B1 EP 0109109 B1 EP0109109 B1 EP 0109109B1 EP 83201501 A EP83201501 A EP 83201501A EP 83201501 A EP83201501 A EP 83201501A EP 0109109 B1 EP0109109 B1 EP 0109109B1
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EP
European Patent Office
Prior art keywords
fly ash
solid fuel
reactor
ash particles
mixing
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
Application number
EP83201501A
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German (de)
English (en)
Other versions
EP0109109A2 (fr
EP0109109A3 (en
Inventor
Wilhelmus F. J. M. Engelhard
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
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Publication date
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Application filed by Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Publication of EP0109109A2 publication Critical patent/EP0109109A2/fr
Publication of EP0109109A3 publication Critical patent/EP0109109A3/en
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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
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/466—Entrained flow processes
    • 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
    • C10J3/52—Ash-removing devices
    • C10J3/526—Ash-removing 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
    • C10J2300/093—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
    • C10J2300/0953—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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water

Definitions

  • the present invention relates to a process for the partial combustion of a finely divided solid fuel, and more particularly to such a process wherein the generated fly ash is recirculated to the combustion space.
  • finely divided solid fuel is passed into a gasifier at a relatively high pressure.
  • a hot flame is maintained in which the solid fuel reacts with oxygen, supplied as pure oxygen or an oxygen-containing gas, such as air.
  • the solid fuel contains as useful components mainly carbon and hydrogen, which react with the oxygen to form a product gas mainly consisting of coal monoxide and hydrogen.
  • mineral fuel such as coal always contains certain quantities of inorganic, incombustible matter, which is in the combustion process partly collected in the bottom part of the gasifier as slag and partly entrained with the product gas.
  • the product gas may further contain particulates consisting of unconverted coal.
  • the total mass of incombustible matter and unconverted coal entrained with the product gas is normally indicated with the expression fly ash.
  • fly ash For working up or usage of the product gas obtained with the partial combustion of solid fuel, the presence of fly ash in the product gas forms a disadvantage. It is therefore necessary to separate the fly ash from the product gas prior to working up or usage thereof.
  • Various types of equipment are known for separating the fly ash from the product gas, to obtain clean product gas and solid fly ash.
  • the obtained separated solid fly ash has some unfavourable properties. Firstly, fly ash consists of very fine, porous particles - with sizes in the range of 5-60 . 10-6 - having a low bulk density, making storage thereof very inefficient.
  • fly ash normally contains salts of metals, which may leach from the porous fly ash particles, if contacted with water.
  • fly ash normally contains a valuable portion in the form of unconverted coal, which is in fact thrown away if fly ash is merely dumped.
  • US-A-4,319,888 discloses a process for the partial combustion of finely divided solid fuel with fly ash recycle.
  • the fuel is carried in one air stream and the recycled fly ash in another air stream to a riffle plate arrangement.
  • a pneumatic transport takes place before mixing solid fuel and fly ash.
  • the object of the present invention is to overcome the above disadvantages associated with the handling of fly ash, and to make use of the valuable portion in the fly ash in an effective manner.
  • the process for the partial combustion of a finely divided solid fuel with fly ash recycle comprises according to the invention contacting finely divided solid fuel with oxygen in a hot flame in a reactor for partial combustion thereof, withdrawing product gas containing fly ash particles from the reactor, separating the fly ash particles from the product gas, mixing the separated fly ash particles with finely divided solid fuel, forming a fluidized mass of fly ash particles and solid fuel by introducing a gaseous medium therein and transporting the fluidized mass with the gaseous medium to the reactor for partial combustion thereof.
  • the above process according to the invention offers a plurality of advantages over known techniques for fly ash handling. Firstly, by recirculating the fly ash to the reactor, the valuable portion thereof, i.e. unconverted coal, can be converted into product gas, resulting in a better gasification efficiency. Secondly, recirculation of the fly ash to the reactor has a further effect in that at least a portion of the fly ash will be converted into environmentally more acceptable slag, which can be withdrawn from the bottom part of the reactor.
  • fly ash is recycled to the reactor together with solid fuel requiring only a relatively small quantity of carrier gas.
  • Pneumatic transport of merely fly ash through a pipeline system is rather difficult, for two major reasons.
  • the very light and small particles forming the fly ash as well as the rather sticky nature of fly ash easily cause clogging of the valves and other parts of a pipeline system.
  • Pneumatic transport of fly ash is therefore only feasible when extremely large amounts of carrier gas are used.
  • the introduction of such huge amounts of carrier gas into the reactor will have an adverse influence on the combustion process in the reactor, resulting in a less valuable gasification product and in a less effective use of the solid fuel.
  • the total quantity of carrier gas, necessary for transporting the fly ash to the reactor can be considerably reduced by intensively mixing the fly ash with fresh solid fuel prior to further transport to the reactor. It has further been found that, if the fly ash forms about 30 per cent by weight at most of the mixture of fly ash and solid fuel, the total required amount of carrier gas for transporting a mixture of fly ash and solid fuel can be kept substantially equal to the amount of carrier gas necessary for transporting solid fuel only.
  • these separating means consists of a cyclone 4, into which product gas is tangentially introduced to bring the gas into a swirling motion. This swirl motion causes a separation of product gas, leaving the cyclone over the top via line 5 and fly ash, removed from the bottom part of the cyclone through line 6.
  • the fly ash is subsequently collected in a storage vessel 7 arranged below cyclone 4, and from there sluiced out to a further veesel 8.
  • This vessel 8 is provided with (not shown) means, for (de)pressurization and for separating entrained gas from the fly ash, for example by aerating or fluidizing the mass of fly ash.
  • the gas separation is essential in order to make sure that no water vapour, which might cause corrosion problems, will condense.
  • the vessel 8 is further provided with a cooling jacket for cooling down the fly ash.
  • the fly ash is sluiced out from vessel 8 via line 10 to a mixing vessel 9, provided with mixing means, such as a stirring device.
  • mixing means such as a stirring device.
  • the fly ash particles are mixed with solid fuel introduced via line 11.
  • the so formed mixture of fly ash particles and solid fuel is subsequently stored in a storage vessel 12. From said storage vessel 12 the mixture is introduced into a further vessel 13 provided with (de)pressurizing means.
  • the solid fuel/fly ash mass is sluiced out from said vessel 13 and introduced into a fluidization vessel 14.
  • the mixture is fluidized in said fluidization vessel 14 by introducing a gaseous medium in the bottom part of the vessel via injection line 15.
  • the fluidized mixture of solid fuel and fly ash is subsequently allowed to flow with gaseous medium to the reactor 1 via line 2 for partial combustion thereof.
  • Tests have been carried out to investigate how fly ash-coal mixtures would fluidize at several fly ash/coal ratios.
  • fly ash particles will substantially behave like the fresh fuel solids, and as a consequence thereof the mixture of fly ash and solid fuel can be easily fluidized.
  • the quantity of gas necessary for fluidizing a mixture of fly ash and solid fuel is substantially the same as the quantity of gas necessary for fluidizing pure solid fuel.
  • the so formed homogeneous mass of solid fuel and fly ash is subsequently allowed to flow via line 2 towards the reactor 1.
  • the amount of fly ash produced in the reactor 1 depends on the type of fuel which is gasified and on the operating conditions in the reactor. When using coal as solid fuel, the amount of fly ash produced will be normally far below 30 per cent by weight of the coal, or in other words far below the upper limit for preparing a sufficiently fluidized mixture of coal and fly ash in the fluidization vessel 14.
  • a possible solution might be for example increasing the throughput of fresh solid fuel either or not in combination with intermittently processing solid fuel with a low fly ash production for diminishing the surplus of fly ash obtained from the solid fuel with high fly ash production.
  • composition of the formed fly ash can be examined for example by sampling the flow through line 10, to determine the amount of oxygen necessary for an optimal gasification process in reactor 1.
  • FIG. 2 showing a second flow scheme according to the invention.
  • the mixing vessel 9 has been replaced by a direct transport system of fly ash to the fluidization vessel 14.
  • Fly ash, separated from product gas and brought in vessel 8 at the operating pressure of reactor 1 is pneumatically transported from vessel 8 to a further vessel 20 via transport line 21.
  • a carrier gas such as for example nitrogen is injected into line 21 via an injector 22.
  • Vessel 20 is formed by a cyclone, into which the fly ash and carrier gas are tangentially introduced.
  • the carrier gas separated from the fly ash in cyclone 20 is withdrawn through line 23.
  • the fly ash, collected in the bottom part of vessel 20 is subsequently dosed to fluidization vessel 14 via a rotary valve 24 positioned in a connecting line 25.
  • the fluidization vessel 14 is arranged at a lower level than cyclone vessel 20 and at a rather acute angle a with respect to the vertical.
  • the angle of inclination with the vertical of line 25 is preferably not greater than about 20 degrees.
  • Fresh solid fuel from storage vessel 26, brought at the required reactor operating pressure in vessel 27, is introduced via transfer line 28 into the fludiza- tion vessel 14.
  • Carrier gas, withdrawn from line 23, is transported via line 29 into the bottom part of vessel 14. In this manner the solid fuel and fly ash particles are fluidized, while these components are simultaneously mixed with one another to form a substantially homogeneous mixture of solid fuel particles and recirculated fly ash particles.
  • the so formed mixture of solid and fly ash particles is subsequently allowed to flow with the gaseous medium to the reactor 1 via line 2.
  • the amount of fly ash supplied into fluidization vessel 14 can be controlled by regulating rotation of rotary valve 24. Further, the fly ash can be continuously or intermittently dosed to vessel 14.
  • Rotary valve 24 can be replaced by another suitable dosing system, such as a set of sluicing valves, wherein an appropriate fly ash sluicing volume is available between said valves.
  • the fluidization vessel 14 is suitably provided with a level control system for regulating the level of solids in said vessel 14.
  • a level control system for regulating the level of solids in said vessel 14.
  • a signal is given to increase the supply of fresh solid fuel from the solid fuel storage vessels, to maintain a stable reactor operation.
  • Pressure losses occurring during the transport of fly ash from the reactor 1 to the fluidization vessel 14 can be overcome by pressurizing the fly ash in one or more of the fly ash vessels in the system, for example by injecting gas into said vessel(s).
  • the shown system for fly ash recycle can be further provided with means, not shown, for sluicing out minor amounts of fly ash, which might be necessary when processing solid fuel with an excessive high fly ash production.
  • the gaseous medium for the transport of fly ash and the formation transport of the solid fuel fly ash mixture from fluidization vessel 14 to the reactor may be for example a suitable inert gas, such as nitrogen, or cooled product gas produced in the reactor.
  • the reactor 1 may be provided with a plurality of burners for solid fuel, wherein a part of these burners is used in the above described recycling process.

Claims (6)

1. Procédé pour la combustion partielle d'un combustible solide très divisé avec recyclage des cendres volantes, qui comprend la mise en contact d'un combustible solide très divisé avec de l'oxygène, dans une flamme chaude, dans un réacteur pour la combustion partielle de celui-ci, le retrait du gaz de production contenant tes particules de cendres volantes du réacteur, la séparation des particules des cendres volantes du gaz de production, le mélange des particules séparées de cendres volantes avec du combustible solide très divisé, la formation d'une masse fluidisée de particules de cendres volantes et de combustible solide par l'introduction dans celle-ci d'un milieu gazeux, et le transport de la masse fluidisée avec le milieu gazeux vers le réacteur pour sa combustion partielle.
2. Procédé selon la revendication 1, dans lequel le poids total des particules de cendres volantes dans la masse fluidisée est d'au plus 30 pour cent du poids total des particules de cendres volantes et de combustible solide dans ladite masse.
3. Procédé selon la revendication 1 ou 2, dans lequel le milieu gazeux est l'azote ou le gaz de production froid.
4. Procédé selon l'une quelconque des revendications 1 à 3, dans lequel le mélange et la formation d'une masse fluidisée sont des étapes distinctes du procédé.
5. Procédé selon l'une quelconque des revendications 1 à 3, dans lequel le mélange et la formation d'une masse fluidisée s'effectuent en une étape unique du procédé.
6. Procédé selon la revendication 4, dans lequel le mélange des particules séparées de cendres volantes et du combustible solide s'effectue dans une cuve de mélange pourvue à l'intérieur de moyens de mélange, et ayant des moyens distincts d'admission pour les particules de cendres volantes et pour le combustible solide et des moyens d'évacuation pour le mélange formé.
EP83201501A 1982-11-11 1983-10-18 Procédé pour la combustion partielle d'un combustible solide avec recyclage des cendres volantes Expired EP0109109B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB8232282 1982-11-11
GB8232282 1982-11-11

Publications (3)

Publication Number Publication Date
EP0109109A2 EP0109109A2 (fr) 1984-05-23
EP0109109A3 EP0109109A3 (en) 1985-05-15
EP0109109B1 true EP0109109B1 (fr) 1987-08-05

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ID=10534210

Family Applications (1)

Application Number Title Priority Date Filing Date
EP83201501A Expired EP0109109B1 (fr) 1982-11-11 1983-10-18 Procédé pour la combustion partielle d'un combustible solide avec recyclage des cendres volantes

Country Status (6)

Country Link
EP (1) EP0109109B1 (fr)
JP (1) JPS59100303A (fr)
AU (1) AU559776B2 (fr)
CA (1) CA1242887A (fr)
DE (1) DE3372867D1 (fr)
ZA (1) ZA838337B (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3837587C1 (fr) * 1988-11-05 1990-05-23 Krupp Koppers Gmbh, 4300 Essen, De
DE4004874A1 (de) * 1990-02-16 1991-08-29 Krupp Koppers Gmbh Verfahren zum betrieb einer anlage fuer die vergasung fester brennstoffe

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH01310219A (ja) * 1988-06-07 1989-12-14 Kawasaki Heavy Ind Ltd 石炭部分燃焼炉ボイラ設備の灰及びチャーの回収方法
JPH02133702A (ja) * 1988-08-19 1990-05-22 Kawasaki Heavy Ind Ltd 石炭部分燃焼炉ガス生成設備の爆発防止方法
DE4105227A1 (de) * 1991-02-20 1992-08-27 Krupp Koppers Gmbh Verfahren und vorrichtung zur vergasung eines feinkoernigen bis staubfoermigen brennstoffes mit flugascherueckfuehrung
CN108753367A (zh) * 2018-07-25 2018-11-06 上海正申建设工程有限公司 一种飞灰零排放的流化床粉煤气化装置及工艺
CN109694752A (zh) * 2019-03-01 2019-04-30 江苏普格机械有限公司 流化床的返粉方法及基于该方法的流化床气化炉
CN112798457A (zh) * 2020-12-23 2021-05-14 华能（天津）煤气化发电有限公司 一种用于igcc的飞灰再循环判定方法

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2113774A (en) * 1934-11-26 1938-04-12 Schmalfeldt Hans Process for the gasification of dust or fine-grained fuels with circulating gas
DE737641C (de) * 1936-04-29 1943-07-20 Julius Pintsch Kom Ges Verfahren zur Wassergaserzeugung aus feuchtem Brennstaub
GB803234A (en) * 1953-07-28 1958-10-22 Gas Council Process for the gasification of solid carbonaceous material in suspension
JPS5420431A (en) * 1977-07-15 1979-02-15 Mitsubishi Heavy Ind Ltd Pulverized coal combustion boiler
DE2751911B2 (de) * 1977-11-21 1980-11-06 Davy International Ag, 6000 Frankfurt Verfahren und Gas-Generator für die Vergasung von Kohlenstaub
JPS5852410B2 (ja) * 1979-09-27 1983-11-22 日立電線株式会社 架空配電線
US4319888A (en) * 1980-12-12 1982-03-16 Combustion Engineering, Inc. Apparatus for mixing char-ash into coal stream

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3837587C1 (fr) * 1988-11-05 1990-05-23 Krupp Koppers Gmbh, 4300 Essen, De
DE3941816A1 (de) * 1988-11-05 1991-06-20 Krupp Koppers Gmbh Verfahren zum betrieb einer anlage fuer die vergasung fester brennstoffe
DE4004874A1 (de) * 1990-02-16 1991-08-29 Krupp Koppers Gmbh Verfahren zum betrieb einer anlage fuer die vergasung fester brennstoffe

Also Published As

Publication number Publication date
AU559776B2 (en) 1987-03-19
CA1242887A (fr) 1988-10-11
ZA838337B (en) 1984-06-27
EP0109109A2 (fr) 1984-05-23
EP0109109A3 (en) 1985-05-15
AU2110683A (en) 1984-05-17
JPS59100303A (ja) 1984-06-09
DE3372867D1 (en) 1987-09-10

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