EP0247504B1 - Verfahren zur Herstellung von Wasserstoff und Kohlenmonoxid enthaltenen Gasen aus festen Brennstoffen - Google Patents

Verfahren zur Herstellung von Wasserstoff und Kohlenmonoxid enthaltenen Gasen aus festen Brennstoffen Download PDF

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Publication number
EP0247504B1
EP0247504B1 EP87107304A EP87107304A EP0247504B1 EP 0247504 B1 EP0247504 B1 EP 0247504B1 EP 87107304 A EP87107304 A EP 87107304A EP 87107304 A EP87107304 A EP 87107304A EP 0247504 B1 EP0247504 B1 EP 0247504B1
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EP
European Patent Office
Prior art keywords
gas
reactor
solid
gasification
recycling conduit
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 - Lifetime
Application number
EP87107304A
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German (de)
English (en)
French (fr)
Other versions
EP0247504A2 (de
EP0247504A3 (en
Inventor
Johannes Dr. Ing. Dipl.-Ing. Lambertz
Wolfgang Dr. Ing. Dipl.-Ing. Adlhoch
Alfred Gustav Dipl.-Ing. Mittelstädt
Wolfgang Hermann
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Rheinbraun AG
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Rheinbraun AG
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Filing date
Publication date
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Publication of EP0247504A2 publication Critical patent/EP0247504A2/de
Publication of EP0247504A3 publication Critical patent/EP0247504A3/de
Application granted granted Critical
Publication of EP0247504B1 publication Critical patent/EP0247504B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • 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
    • C10J3/482—Gasifiers with stationary fluidised bed
    • 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
    • C10J3/523—Ash-removing devices for gasifiers with stationary fluidised bed
    • 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
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—Apparatus; Plants
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/026—Dust removal by centrifugal forces
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/158—Screws
    • 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
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S48/00—Gas: heating and illuminating
    • Y10S48/04—Powdered fuel injection

Definitions

  • the invention relates to a process for producing hydrogen and carbon monoxide-containing gases from solid fuels at elevated pressure in a fluidized bed using gasifying agents, a fixed bed of solid gasification residues from which the solid gasification residues are drawn off possibly being located below the fluidized bed, and A post-gasification space is arranged above the fluidized bed and the synthesis gas generated is drawn off from the post-gasification space and passed through a separator in which at least some of the entrained solid particles are separated and returned to the fluidized bed via a return line, while the synthesis gas in at least the pre-cleaned state passes the separator leaves.
  • a gasification reactor which has a lower, conical part in which the fuel to be gasified is whirled up by the gasification agent.
  • the resulting fluidized bed within which the fuel particles are in constant motion, has a lower and an upper limit, which are normally not sharp.
  • the lower limit is formed by the fixed bed, which consists of finer and coarser, possibly sintered solid gasification residues.
  • the axis is withdrawn from the reactor.
  • the solid particles separated in the cyclone still contain so much carbon that it is worth returning them to the reactor.
  • an increased supply of gasification agents into the fluidized bed an operating state can even be reached which is referred to as a "circulating fluidized bed".
  • An upper limit of the fluidized bed is no longer formed. Rather, so much gasifying agent is supplied that the majority of the fuel particles enter the post-gasification chamber and from there into the separator and must therefore be recycled anyway if a sufficient degree of gasification is to be achieved.
  • the return line through which the particulate matter deposited in the cyclone is returned to the reactor extends between the cyclone, generally between the lower part thereof, and the reactor, the arrangement normally being such that the return line is in the region of the fluidized bed, that is, in the lower region of the reactor opens into this.
  • the return line runs obliquely at least in some areas, that is to say at an acute angle to the vertical. In any case, the interior of the reactor, the separator and the return line form a coherent system.
  • the risk that the solid matter in the return line gets stuck in it, with the result that after a short time the solid matter accumulating in the return line reaches the separator is particularly due to the fact that the return line has a small diameter in relation to its length .
  • the length will generally be determined by the distance to be bridged between the separator and the area of the fluidized bed reactor into which the solid to be returned is to be brought Distance.
  • An increase in the diameter of the return line, which would counteract the risk of blockages occurring, is ruled out, since this would undesirably influence the pressure and flow conditions in the overall device, possibly to a point at which the system does not more works.
  • a fluidized bed combustion device is known from SE-A 8 206 888, the flue gases of which are cleaned in a cyclone.
  • the dust separated in the cyclone is returned to the combustion device via a pneumatic transport system.
  • flue gas ducts that run parallel to a shaft within the combustion device, in the lower area of which the fluidized bed is located.
  • the flue gas ducts also serve as a collecting space for dust-like solids separated from the flue gases within the combustion device and deposited on the floor of the respective flue gas duct. This floor is provided with nozzles which are operated continuously or intermittently in order to return a certain amount of the dust into the fluidized bed in order to adjust the temperature of the same.
  • the invention has for its object to improve the process of the type described in the introduction so that, regardless of the amount of solid particles to be returned from the separator to the reactor, proper continuous operation of the gasification reactor is ensured.
  • the solid particles to be returned can be returned to the reactor in a controllable manner depending on the particular circumstances, that is to say on the gasification pressure, quantity and time.
  • the invention proposes that gas be introduced in pulses in the return line at least at one point to loosen up the solid particles therein.
  • a procedure has been found to be particularly expedient in which gas is blown into the return line at a plurality of points spaced apart in the longitudinal direction of the return line, these points should be arranged in the region in which the solid particles to be returned accumulate. It is therefore the area which is adjacent to the reactor or the fluidized bed located therein.
  • Some of the gas streams blown into the return line at different points can be blown continuously.
  • the pulsed blowing of at least some of the gas streams into the return line also has the advantage that less gas is used to achieve the same effect. This is also important because an excessively large amount of gas that is blown into the return line and that at least predominantly flows upwards towards the cyclone reduces the separation efficiency of the cyclone.
  • An mode of operation has been found to be expedient in which the gas is blown into the return line at the lowest, i.e. the mouth of the return line into the reactor, and the gas is blown into the return line intermittently, i.e. in pulses, at all other locations above it.
  • a mode of operation in which the pulse-like injection of the gas at the injection points is at least temporarily offset is particularly advantageous in such a way that from two injection points at a distance in the longitudinal direction of the return line, the injection begins earlier and possibly also at the injection point positioned closer to the reactor ends earlier than at the injection point positioned further away from the reactor. It is thereby achieved that the solid column located in the return line progressively loosens from bottom to top, that is to say counter to the direction of flow of the solid in the return line, which once leads to. that below the area of the solid column which has been loosened by a gas pulse at a certain position, the solid has also already been loosened, possibly already drained off.
  • the flow process within the return line can be influenced well in terms of quantity and time in this way, so that the speed at which the solid flows out of the return line into the reactor can be determined by controlling the gas pulses, in particular their time offset.
  • the amount of gas to be blown in may depend on the amount of the solid present in the return line or of the solid to be returned to the reactor.
  • the number of gas pulses can also depend on the amount of the solid in the return line or the solid to be returned to the reactor. It is possible to increase the amount of gas to be injected by increasing the number of gas pulses per unit of time, although this dependency is not mandatory, since it is readily possible to distribute a certain gas volume over a smaller or larger number of gas pulses. the gas volume injected per pulse then changes.
  • the duration of a pulse can be 0.1 to 2 s, preferably 1 s. In general, it is expedient to provide a pause between two successive pulses which lasts 1 s, preferably 0.1 s.
  • the time shift between the pulses of two adjacent blowing points can be so great that the pulse on the in each case in the chronological order second blowing point only begins after the pulse in the preceding blowing point has ended.
  • the amount of gas injected or the number of gas pulses can be controlled as a function of the temperature in the return line.
  • Inert gas e.g. B. Co 2 or nitrogen or recycled process gas can be used.
  • the gasification process for producing a product gas takes place in a reactor 10, in whose lower region 12, which tapers conically from top to bottom, is the fluidized bed 14.
  • the conical region is adjoined at the top by a cylindrical region 16 which contains the post-gasification zone 18.
  • the reactor 10 merges into a short shaft 20, at the end of which a conveyor and cooling screw 22 is arranged.
  • the solid gasification residues which predominantly contain ashes and collect in a fixed bed 24 below the fluidized bed 14, are drawn off through the shaft 20 and the screw 22.
  • the solid fuel to be gasified is introduced into the reactor 10 from a reservoir 28 by a screw 26. In the embodiment shown in the drawing, the solid fuel enters the latter below the upper limit 30 of the fluidized bed 14.
  • the fuel can e.g. B. pre-dried lignite, which has a water content of 12-18% and a grain size between 0 and 5 mm.
  • other carbon-containing fuels can also be used, e.g. Peat or coals that are more coalized than brown coal.
  • the reactor 10 is provided with a plurality of feed lines for gaseous media, which serve as gasifying agents.
  • the leads 32 located at the bottom open into the shaft 20 and serve to supply a gaseous medium to loosen the fixed bed 24.
  • This medium can be an endothermic gasifying agent, for example steam or CO 2 , but also an inert medium, for . B. nitrogen act.
  • nozzles are provided for the supply of gasification agent in planes which are at vertical distances from one another.
  • Gasification agent which brings about endothermic reactions is preferably supplied through the feed lines 34, 36 in the lower levels.
  • Oxygen-containing gasification agents are supplied in the feed lines 40, 41.
  • feed lines 44, 45 and 46 open into the after-reaction space 18. Gasification agents which bring about exothermic and endothermic reactions are normally introduced into the after-reaction space 18 via these feed lines.
  • the fuel to be gasified is introduced into the reactor 10 by the screw 26 in the region of the fluidized bed 14.
  • the fuel particles are fluidized by the gasification agents, the degassing products, the vapor produced by the evaporation of the water contained in the fuel and the reaction products.
  • the very small, almost dust-like components of the solid fuel introduced into the fluidized bed are entrained relatively quickly by the gas flowing upward through the upper boundary of the Wibel bed 30 into the after-reaction space 18, in which they are largely converted.
  • the extent to which gasification agents are fed through the feed lines 44, 45, 46 into the post-reaction space 18 depends in particular on the amount of solid carbon to be converted in the post-reaction space 18.
  • the heavy particles within the fluidized bed 14 sink through the latter and thus reach the fixed bed 24.
  • These heavier particles can be coarser, predominantly carbon-containing particles that are too large for the fluidized bed to move from below to the bottom gas flowing through the top could be carried.
  • such particles sediment down through the fluidized bed 14 onto the fixed bed 24, the weight of which is too high in relation to the grain size. It can be both carbon-containing particles with a high ash content and particles that consist exclusively of non-gasifiable substances.
  • the product gas 65 generated in the reactor 10 is withdrawn through a line 50 extending from the reactor 10 near the upper end thereof and, after pre-cleaning in a cyclone 52, downstream devices, e.g. B. supplied for gas cleaning.
  • the solid particles separated in the cyclone 52 which generally still contain carbon, pass via the lower outlet 66 of the cyclone into a return line 69, the lower, obliquely extending section 62 end 62 of which is connected to the reactor 10 in the region of the fluidized bed 14.
  • the gas 65 cleaned from the separated solid particles leaves cyclone 52 through a dip tube 67 via a line 68.
  • the return line 69 for the solid particles deposited in the cyclone 52 opens into the reactor 10 at about the level of the screw 26.
  • the solid particles flow downward from the lower region of the cyclone 66 into the return line 69, the cross section of which in the region 62 between the mouth 60 into the reactor 10 and about level 61 is filled by the solid particles.
  • the column of solid particles thus formed within the return line 69 constitutes a barrier which prevents solid particles and gas from the reactor 10 from passing through the return line 69 directly into the area of the separator 52 designed as a cyclone.
  • the return line 69 has a relatively small cross-section and, moreover, the pressure prevailing in the area of the cyclone 52 is noticeably lower than the pressure in the fluidized bed 14, so that a pressure gradient which counteracts gravity between the mouth 60 of the return line 69 into the reactor 10 on the one hand and the On the other hand, cyclone 52 exists, without special measures there is no guarantee that as much solid particles from the return line 69 will enter the reactor 10 over longer periods of time as will pass from the cyclone 52 into the return line above.
  • the small cross section of the return line 69 means that the particles contained therein can settle, so that even if a solid column formed in the return line 69, the height and weight of which is sufficient, the pressure drop to compensate for a proper and undisturbed outflow of the solid particles forming this column into the reactor 10 would not be guaranteed.
  • nozzles 81 opening into the return line 69 are provided for a gaseous medium. These nozzles 81 are arranged at intervals from one another in the longitudinal direction of the return line 69. They are fed via a control valve 70 to 77 from a common pressure medium source 78 with a gas, which can be, for example, C0 2 or also recirculated product gas which is branched off from the gas stream 65 at a suitable point.
  • the control valves 71-77 are operated by a common controller 79, to which they are connected via a line 80.
  • the pressure level of the gas 78 will be somewhat higher than the pressure level in the fluidized bed 14.
  • the controller 79 controls the individual valves 71 - 77 and in each case briefly releases a gas flow of a certain amount, which flows through the nozzles 81 into the lower region of the pulse Return line 69 arrives. It can be done in such a way that the valves 70-77 successively cause a short-term gas pulse such that a gas pulse is first passed through the valve 70 or the associated nozzle 81 into the mouth 60 of the return line 69 and then gas pulses are delayed by the others Valves are introduced into the return line 69, the time interval from the first gas pulse caused by the valve 70 increasing with increasing distance of the respective valve from the first valve 70.
  • valve 70 it is also possible to allow a longer pause to occur after actuation of the last valve 77 before the next pulse cycle begins by actuation of the valve 70. This depends on the amount of solid that comes from the cyclone 52 into the return line 69 and thus on the speed at which the solid particles from the return line 69 have to be introduced into the reactor 10. It is also possible, if necessary, not to allow the pulse cycle to run over the entire number of valves 70-77 present, but rather, for example, to only give gas pulses into return line 69 through valves 70-75. How the process is carried out depends on the particular circumstances, in particular the amount of solids collected in the return line 69 per unit of time.
  • the individual valves 70-77 can be actuated in a simple manner via the controller 79, to which the temperature sensors 57-59 detecting the temperature in the return line 69 are assigned, which are assigned to that region of the return line 69 in which the nozzles 81 of the valves 70 -77 are.
  • a temperature level is established within the latter which is not substantially below the temperature level within the fluidized bed 14 and usually in the range between 800 and 1000 ° C. If the return of the solid slows down, a direct drop in the temperature level to lower values can be determined at the temperature measuring points 57-59. This change in temperature indicates that the return of the solid from line 69 into fluidized bed 14 is too slow.
  • the controller is prompted to accelerate the pulse train by signals supplied to the controller 79 via the line 64 from the temperature measuring points.
  • the pulse train can be slowed down.
  • valves 70-77 or 71-77 instead of actuating the valves 70-77 or 71-77 via the temperature, there is also the possibility of actuating the valves and thus the gas pulses caused by them via the pressure prevailing at the respective points on the return line.
  • the nozzles 81 consist of customary, heat-resistant materials. Commercially available pneumatic switching valves can be used for valves 70 - 77. It is expedient to arrange them at equally large distances from and along the return line 69, it being possible to provide 1-3 nozzles / m of the return line.
  • the nozzles 81 will normally be arranged predominantly in the area of the return line which is not vertical.
  • the diameter of the return line 69 can be 20 cm, for example.
  • the amount of gas to be blown into the return line is small.
  • the quantitative ratio between this gas to be blown in and the product gas produced in the gasification reactor can be approximately 2: 500.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Industrial Gases (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
EP87107304A 1986-05-27 1987-05-19 Verfahren zur Herstellung von Wasserstoff und Kohlenmonoxid enthaltenen Gasen aus festen Brennstoffen Expired - Lifetime EP0247504B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3617802 1986-05-27
DE19863617802 DE3617802A1 (de) 1986-05-27 1986-05-27 Verfahren zur herstellung von wasserstoff und kohlenmonoxid enthaltenen gasen aus festen brennstoffen

Publications (3)

Publication Number Publication Date
EP0247504A2 EP0247504A2 (de) 1987-12-02
EP0247504A3 EP0247504A3 (en) 1988-04-06
EP0247504B1 true EP0247504B1 (de) 1990-10-03

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ID=6301727

Family Applications (1)

Application Number Title Priority Date Filing Date
EP87107304A Expired - Lifetime EP0247504B1 (de) 1986-05-27 1987-05-19 Verfahren zur Herstellung von Wasserstoff und Kohlenmonoxid enthaltenen Gasen aus festen Brennstoffen

Country Status (8)

Country Link
US (1) US4852994A (es)
EP (1) EP0247504B1 (es)
CN (1) CN1011417B (es)
AU (1) AU594463B2 (es)
DE (2) DE3617802A1 (es)
ES (1) ES2017959B3 (es)
FI (1) FI86075C (es)
GR (1) GR3001127T3 (es)

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CN102911741B (zh) * 2012-10-18 2013-12-25 东南大学 循环流化床煤气化的装置
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Also Published As

Publication number Publication date
EP0247504A2 (de) 1987-12-02
US4852994A (en) 1989-08-01
GR3001127T3 (en) 1992-06-25
DE3765311D1 (de) 1990-11-08
DE3617802A1 (de) 1987-12-03
ES2017959B3 (es) 1991-03-16
DE3617802C2 (es) 1992-09-10
AU594463B2 (en) 1990-03-08
CN1011417B (zh) 1991-01-30
FI86075C (fi) 1992-07-10
FI872321A (fi) 1987-11-28
CN87103895A (zh) 1987-12-16
FI86075B (fi) 1992-03-31
EP0247504A3 (en) 1988-04-06
AU7331487A (en) 1987-12-03
FI872321A0 (fi) 1987-05-26

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