EP0780459A2 - Procédé pour la gazéification de solides contenant du carbone en fluidisé et producteur de gaz correspondant - Google Patents

Procédé pour la gazéification de solides contenant du carbone en fluidisé et producteur de gaz correspondant Download PDF

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Publication number
EP0780459A2
EP0780459A2 EP96118067A EP96118067A EP0780459A2 EP 0780459 A2 EP0780459 A2 EP 0780459A2 EP 96118067 A EP96118067 A EP 96118067A EP 96118067 A EP96118067 A EP 96118067A EP 0780459 A2 EP0780459 A2 EP 0780459A2
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EP
European Patent Office
Prior art keywords
fluidized bed
solids
gasified
gasification
section
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.)
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Application number
EP96118067A
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German (de)
English (en)
Other versions
EP0780459A3 (fr
Inventor
Bernd Prof. Dr. Meyer
Wolfgang H. Dr. Adlhoch
Alfred Gustav Mittelstädt
Georg Karkowski
Ingo Schumacher
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.)
Rheinbraun AG
Original Assignee
Rheinbraun AG
Rheinische Braunkohlenwerke AG
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
Priority claimed from DE19548324A external-priority patent/DE19548324C2/de
Application filed by Rheinbraun AG, Rheinische Braunkohlenwerke AG filed Critical Rheinbraun AG
Publication of EP0780459A2 publication Critical patent/EP0780459A2/fr
Publication of EP0780459A3 publication Critical patent/EP0780459A3/fr
Withdrawn legal-status Critical Current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
    • C10J3/56—Apparatus; Plants
    • 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
    • C10J3/54—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
    • 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
    • C10J2200/158—Screws

Definitions

  • the invention relates to a method according to the preamble of claim 1 and a carburetor according to the preamble of claim 15.
  • the carbon-containing solids are gasified under increased pressure in a fluidized bed using endothermic and exothermic reacting gasification agents, with a post-gasification chamber above the fluidized bed and a fixed bed from the gasification residues, the so-called bottom product, underneath the fluidized bed, and fuels are introduced into the fluidized bed and solid Gasification residues are withdrawn from the fixed bed and the gas generated is led out of the post-gasification space and passed through a separator in which at least some of the solid particles entrained in the gas produced are separated and returned to the gasifier via a return line, while the product gas is at least pre-cleaned Condition leaves the separator.
  • Such a carburetor which can be designed as a high-temperature Winkler carburetor (HTW), z. B. depending on the nature of the materials to be gasified at a temperature between about 600 ° and 1300 ° C and under an excess pressure of up to 30 bar and more.
  • These carbonaceous materials can be coal (lignite and / or hard coal), biomass, carbonaceous Residues, e.g. B. sewage sludge, plastics and also mixtures of at least two of these substances.
  • the previously built HTW carburettors can be operated with a thermal output of up to 140 MW.
  • thermal composite power plants with coupled gas and steam generation and conversion of gas and steam into electrical energy - HTW carburettors are provided, which have a much higher thermal output, which can reach up to 900 MW, for example.
  • a power density of 50 MW / m 2 and more is aimed at in relation to the free gasification cross section of the post-gasification zone. Around 25 MW / m 2 are currently realized.
  • the desired power densities can, however, only be achieved if the solids to be gasified and the gaseous gasification agents are distributed as evenly as possible, especially in the fluidized bed, and if the gasification temperature is kept constant over the height of the fluidized bed.
  • the risk of the formation of overheated areas and of irregularly occurring bubbles of different sizes and distributions decreases, so that the temperatures to be observed in some areas of the fluidized bed, for example with regard to the nature of the ash of the solids to be gasified, are not exceeded either when the temperature in the fluidized bed is close to the maximum permissible temperature. This favors the achievement of high thermal performance.
  • a homogeneous fluidized bed leads to a reduction in the formation of undesired gaseous trace substances in the raw gas, for example benzene, naphthalene and other hydrocarbons, so that the effort for removing these trace substances in the downstream gas cleaning is correspondingly lower.
  • the invention has for its object a method for To make gasification of solid carbonaceous materials available using exothermic and endothermic gasification agents and the gasifier used, in which high gasification efficiencies and high power densities can be achieved at low trace substance concentrations in the raw product gas.
  • the substantially uniform radial flow profile of the gases in the fluidized bed is adjusted by appropriate adjustment and distribution of the gasifying agents blown into the fluidized bed and possibly also additionally blown-in gaseous media, for example recycled product gas, which is branched off, for example, in gas cleaning.
  • An absolute uniformity of the radial flow profile cannot, of course, be achieved, especially since the flow velocity in the immediate vicinity of the wall of the reaction space is noticeably lower anyway. The same applies to the average velocity of the gas flow in the direction of the longitudinal axis of the fluidized bed gasifier, which is constant or only increases slightly.
  • the homogeneity is decisively improved, since when approaching a uniform radial flow profile and the conditions mentioned for the speed of the gas flow in the axial direction, uneven flow conditions in the fluidized bed, which can result, for example, in the segregation of specifically heavier mineral components, are largely avoided. which fact can lead to a drop in temperature in the lower region of the fluidized bed. Furthermore, with the homogeneity of the fluidized bed aimed for by the invention, noticeable fluctuations in the height of the fluidized bed in the reaction space are avoided or at least greatly reduced.
  • a homogeneous fluidized bed according to the invention also avoids the occurrence of local flow streaks with significantly higher flow velocities and little moved or dead zones. Avoiding such flow conditions also results in a better exchange of the gaseous and solid components located in the fluidized bed transversely to the longitudinal axis of the reaction space of the gasifier, which fact also contributes to achieving a higher power density.
  • the solids concentration in the fluidized bed is essentially constant. This also reduces undesirable segregation effects, at least noticeably.
  • the upper boundary of the fluidized bed should be below the lower level in the post-gasification room, in which gasification agent is introduced into the post-gasification room.
  • the desired homogeneity of the fluidized bed is generally favored by the fact that gasifying agents are introduced into the fluidized bed in at least two levels that are horizontally spaced apart, the number and distribution of the individual feed nozzles over the circumference of the reaction space and also the distance between the two levels may depend on the particular circumstances, for example the nature of the carbon-containing materials to be gasified, such as grain size, grain size distribution, C content or the like. Of course, it is also possible to feed gasifying agents into the fluidized bed in more than two planes that are vertically spaced apart.
  • any gasification agent supply into the fluidized bed is a disturbance variable, so that it will be important to find a compromise between the desired homogeneity and the unavoidable disturbance of the fluidized bed by the supply of gasifying agents, which approaches an optimum.
  • the fact that the gasification agents are blown into the fluidized bed through nozzles arranged in the wall of the reactor, which if at all protrude with their outflow end from the wall of the reaction space into the fluidized bed, can be avoided in the reactor in the region of the fluidized bed, which fact also favors its homogeneity.
  • the entry points can advantageously be distributed symmetrically over the circumference of the reaction space.
  • Entering the solid materials on the wall of the reaction space delimiting the fluidized bed also has the advantage that the solid materials entered first move down in the immediate vicinity of the wall before they mix intensively with the solid particles in the fluidized bed.
  • This downward movement is essentially due to the fact that, as already mentioned, the speed in the immediate vicinity of the wall is lower due to the friction between the wall and the gas. It increases the residence time of the same and thus the rate of conversion of the solid carbon in the fluidized bed.
  • the fluidized bed volume required for the greatest possible reaction conversion can be accommodated predominantly in the lower, frustoconical section of the reaction chamber, which is favorable for the gasification processes, so that the upper region of the fluidized bed extends only a small amount into the cylindrical section of the reaction chamber.
  • the return line is inclined at an angle between 10 ° and 30 ° with respect to the inner wall of the frusto-conical lower section of the fluidized bed gasifier.
  • a particularly intensive mixing of the recycled solids with the solids in the fluidized bed can be achieved in that the recycled solids are introduced into the fluidized bed with an entry pulse following the inclination of the wall. This could, for. B. the device disclosed in DE-OS 36 17 802 of the applicant.
  • Feed screws, gravity-operated inclined tubes and pneumatically operated feed members can be used as suitable feed members for the solids, different feed members being able to be provided on the same carburetor. If there are several junctions for the entry of the solids to be gasified, a symmetrical distribution of the entry points, possibly including the entry point for the returned solids, is advantageous in order to achieve a uniform charge over the circumference.
  • the nozzles of the first nozzle plane above the fluidized bed for supplying gaseous gasification agent within the cylindrical upper section of the reaction space which may have a diameter of the order of 2 m, for example, are preferably slightly inclined downwards in the direction of the fluidized bed.
  • the vertically downward flow component of the gaseous medium which is brought about in this way counteracts the prevailing upward directed axial gas flow, as a result of which part of the solid emerging from the fluidized bed is moved back into the fluidized bed. This results in an extension of the reaction time and thus an improvement in the reaction turnover.
  • Nozzles of a further nozzle plane in the post-reaction space which may be arranged above it, can be directed upwards with their orifices, in order to allow through them caused vertically upward flow component to increase the gas velocity in the upper region of the post-gasification space.
  • a minimum residence time of the C-containing solid in the fluidized bed is required.
  • the residence time of the solid particles in the fluidized bed essentially depends on the volume which the fluidized bed occupies.
  • a larger fluidized bed volume with the same diameter of the cylindrical section is achieved if the half cone angle is reduced and the height of the truncated cone - and with it the height of the fluidized bed - is increased. It may be advantageous to choose half the cone angle of the frustoconical section of the reaction chamber so that the fluidized bed is covered with a maximum of twice the diameter of the cylindrical upper section.
  • the section of the fluidized bed which is located in the cylindrical region of the reaction space, has an axial extent which corresponds at most to twice the diameter of the cylindrical upper section.
  • the overlap can be, for example, 3 m.
  • Feedstocks with lower reactivity e.g. B. hard coal
  • the speed with which the C-fix portion of the solids is converted in the gasifier also depends on the partial pressure of the exothermic and endothermic gasifying agents - mainly O 2 , H 2 O, CO 2 . If the partial pressure of the gasifying agent in the gasifier is reduced by lowering the pressure and / or by using inert gas, a longer minimum dwell time is required.
  • the method according to the invention can be carried out using air to provide the necessary exothermic gasifying agent.
  • air it is also possible to use a mixture of O 2 on the one hand and air on the other hand, ie enriched air, or mixtures of O 2 and other gasifying agents.
  • the HTW carburetor 1 shown in the drawing is provided with an upper cylindrical section 2 with the inside diameter d.
  • the lower section 3 connects to the upper section 2 and has the shape of an inverted truncated cone having. Its larger diameter corresponds to the diameter d of the upper cylindrical section 2. Its smallest diameter 4 is determined by the cross section of the two devices 5 for the floor extraction. For a given half cone angle 11, this results in a specific axial length h for the lower section 3 of the HTW carburetor 1.
  • an entry 6 opens laterally into the lower section 3, via which the carbon-containing solid 7 is introduced into the fluidized bed 8.
  • the return line 9 opens into the lower section 3. Via the return line 9, dust 10 separated from the product gas is returned to the fluidized bed 8 in a cyclone or the like. If, in the exemplary embodiment shown in FIG. 1, the half cone angle 11 of the lower section 3 is 8 °, the return line 9 is inclined at an angle 12 of 22 ° with respect to the wall of the lower section 3.
  • the fluidized bed 8 is acted upon by recycle gas 13, which also serves as a sealing and cooling gas, by means of the device 5 for the floor extraction.
  • recycle gas 13 which also serves as a sealing and cooling gas
  • the fluidized bed 8 is supplied with water vapor via the feed line 14.
  • a small axial flow is formed in the lower part of the fluidized bed 8.
  • Gas flows 19 and 20 experience further increases by the supply of further air or exothermic gasification agent 21 or 22 and the progressive conversion of the starting material 7 into coal gas.
  • the upper limit 23 of the fluidized bed 8 is located at an axial distance above the largest diameter d of the lower section 3, so that the part of the fluidized bed delimited on the upper side by the upper limit 23 covers the part 25 of the lower section 3 thereof by the dimension u .
  • the dimension of the overlap ü is 1 m in the selected example, in which the cylindrical section 2 of the HTW carburetor 1 has an inner diameter d of 2.8 m.
  • exothermic gasification agent 26 is blown in at an angle 27 of approximately 60 ° in the direction of the fluidized bed 8.
  • the air flow 26 causes the solid emerging from the fluidized bed in the form of bubbles to react immediately with the added gasifying agent and the unreacted solid experiences an impulse in the direction of the fluidized bed.
  • An increase in the speed of the gases emerging from the top of the fluidized bed 8 and flowing into the post-gasification zone is achieved by gasifying agent nozzles 36 arranged higher up, which are directed upwards at an angle 37, which is also approximately 60 °.
  • FIG. 2 shows the outflow of the gas flow profile in the radial direction in the individual horizontal planes of the lower section 3 of the HTW carburetor.
  • the speed indicated in FIG. 1 by arrows 15, 18, 19 and 20 is in each case the average speed of the gas speed prevailing in the individual injection planes 145, 16, 21 and 22.
  • the increase in this gas velocity is represented on the right side of FIG. 2 by line 28.
  • the dash-colon line 30 represents the average gas velocity if one turns the speed arrows 34, 15, 18, 19 and 20 to the right and imagines it as the basis on line 35. Based on the initial speed 15, the speed 20 in the last injection plane 22 experiences an increase between 130 and 300%.
  • the return line 9 opens into the lower section 3 of the HTW gasifier 1 in the horizontal plane III-III from the right.
  • the return line 9 is opposite an entry 6 for the feedstock 7 to be gasified lateral distances 31 of equal size in the same horizontal plane III-III, two further entries 32 and 33 are provided for the feedstock 7 to be gasified. 3, the four entry points corresponding to the feed lines 6 for the solid to be gasified and the return line 9 as a whole, so that they have a spacing of 90 ° in radians. In the case of two feed lines for the solid to be gasified, the distances between them and the return line would accordingly be 120 °.
  • the recycling gas 13 also causes a small gas flow 34 in the lowermost part of the fluidized bed 8, as shown in FIG. 2.

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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)
EP96118067A 1995-12-22 1996-11-12 Procédé pour la gazéification de solides contenant du carbone en fluidisé et producteur de gaz correspondant Withdrawn EP0780459A3 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19548324A DE19548324C2 (de) 1994-12-23 1995-12-22 Verfahren zum Vergasen von kohlenstoffhaltigen Feststoffen in der Wirbelschicht sowie dafür verwendbarer Vergaser
DE19548324 1995-12-22

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EP0780459A2 true EP0780459A2 (fr) 1997-06-25
EP0780459A3 EP0780459A3 (fr) 1997-09-10

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EP96118067A Withdrawn EP0780459A3 (fr) 1995-12-22 1996-11-12 Procédé pour la gazéification de solides contenant du carbone en fluidisé et producteur de gaz correspondant

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EP (1) EP0780459A3 (fr)
AU (1) AU7429696A (fr)

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3617802A1 (de) 1986-05-27 1987-12-03 Rheinische Braunkohlenw Ag Verfahren zur herstellung von wasserstoff und kohlenmonoxid enthaltenen gasen aus festen brennstoffen

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3840353A (en) * 1971-07-30 1974-10-08 A Squires Process for gasifying granulated carbonaceous fuel
DE2643298A1 (de) * 1976-09-25 1978-04-06 Davy Bamag Gmbh Verfahren zur kontinuierlichen vergasung von feinteiligem, kohlenstoffhaltigem material

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3617802A1 (de) 1986-05-27 1987-12-03 Rheinische Braunkohlenw Ag Verfahren zur herstellung von wasserstoff und kohlenmonoxid enthaltenen gasen aus festen brennstoffen

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AU7429696A (en) 1997-06-26
EP0780459A3 (fr) 1997-09-10

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