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
• • 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
  • C10J3/50—Fuel charging devices
• • 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
  • C10J2200/00—Details of gasification apparatus
  • C10J2200/15—Details of feeding means
• • 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
  • C10J2200/156—Sluices, e.g. mechanical sluices for preventing escape of gas through the feed inlet
• • 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
  • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
  • Y02E50/00—Technologies for the production of fuel of non-fossil origin
  • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
• • 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
  • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
  • Y10T137/00—Fluid handling
  • Y10T137/0318—Processes
  • Y10T137/0324—With control of flow by a condition or characteristic of a fluid
  • Y10T137/0329—Mixing of plural fluids of diverse characteristics or conditions

Definitions

• the invention is directed to a method for supplying an entrainment gasification reactor with fuel from a storage container with the interposition of at least one lock container and at least one storage container, wherein in the entrained flow gasification reactor CO and H 2 - and fly ash containing gas is generated.
• the fuel Since the fuel is initially under ambient pressure, it must first be brought via the supply system to a pressure level above the reactor pressure in order to then be metered to the burners of the pressure gasification reactor.
• An advantageous method provides that the fuel is conveyed from a reservoir in lock container. These are first covered to a pressure level above the reactor pressure, then the fuel over to convey a delivery line by dense phase conveying in a permanently pressurized storage tank for the burner of the gasification reactor. From this storage tank, the burners are continuously supplied in each case with a metered fuel mass flow.
• the transport gas required for dense phase conveying is supplied in or near the outlet of the lock container or in the delivery line.
• the emptied lock containers are then relaxed to be able to absorb more fuel charge under approximately atmospheric pressure. The flash gas is dedusted and released into the atmosphere.
• nitrogen from the air separation plant or carbon dioxide is usually used.
• Carbon dioxide is used when a low-nitrogen synthesis gas or hydrogen and / or CO should be generated.
• Carbon dioxide can be recovered in the gas treatment following gasification. Frequently, the gas flowing out of the gasifier is dedusted and cleaned and subjected to CO conversion in order to adjust the H 2 / CO ratio required by the synthesis or to produce pure hydrogen. CO and water vapor are converted into CO 2 and hydrogen. Thereafter, the gas is cooled, the moisture is condensed out and then CO 2 in a wash with circulating solvent, such as MDEa, Genosorb or methanol, washed out. In a desorber, the CO 2 is expelled from the solution by lowering the pressure or raising the temperature.
• circulating solvent such as MDEa, Genosorb or methanol
• the gas obtained in this way contains not only CO 2 but also other components, eg H 2 , CO, N 2 , methane, hydrogen sulfide, argon, vapors of the solvent used, eg methanol, etc.
• the CO content is for example 0.1%.
• DE 36 90 569 C2 describes a process for removing sulfur-containing compounds from a residual gas.
• the object of the invention is to provide a method for fuel supply of a pressure gasification plant, which ensures in an economical manner that emission of pollutants from the coal sludge and the transport is minimized or completely avoided.
• this object is achieved according to the invention in that for smuggling and / or promotion at least 10 ppm VoI.
• CO preferably 100 ppm to 1000 ppm
• this gas an oxygen-containing gas is mixed, and that this gas mixture is heated to at least 10% of the oxidizing temperature in the gas-containing pollutants.
• the oxygen-containing gas used for smuggling the loosening of the fuel in the reservoir and / or loosening and fluidization of the contents of the lock container and / or for further promotion from the lock container and / or loosening and fluidization in the Georgiabhot- ter is used for supplying the fuel between the system components and from the storage tank and / or to Flugstrom- gasification reactor.
• a particular advantage of the present invention is that all in connection with the lock and the feed of the fuel to the entrained flow gasification reactor gases used may have the claimed criteria.
• the pollutant and oxygen-containing gas mixture is passed through at least one catalyst to accelerate the oxidation of the pollutants.
• the pressure used to increase the pressure in the lock or the container (s) used catalytically oxidized is not catalytically oxidized.
• a gas with an oxygen content of less than 5% is used as lock gas, wherein in a further embodiment can also be provided that the flash gas from the reservoir of the compression stage of a compressor and / or a compression device or the Lock container (s) is supplied.
• 1 is an apparatus diagram of the supply of the fuel to a gasification reactor
• Fig. 2 is a suitably similar system with a plurality of storage containers and in
• FIG. 3 shows a plant essentially according to FIG. modified guidance of the used and emerging gas flows.
• 1 shows the fuel supply designated 1 in a storage container 2, wherein the fuel path drawn in a stronger line leads from the reservoir 2 into a lock container 3, from there via a line 4b into a storage container 5 and from there via lines 6a the burners 6 of the gasification reactor. 7
• the effluent during filling of the lock container gas is fed via a line 3e a filter 10, wherein after filtering the gas is discharged via the line 10e either in the environment or for further use.
• the filter dust is returned to the reservoir 2.
• the displaced during filling of the reservoir 2 gas is also supplied to the filter 10 in the line 2e.
• Slag and solids-containing water are carried out at 7b from the entrained flow gasification reactor, and the gas is passed via line 7a to a gas treatment 8, the synthesis gas being discharged from the gas treatment 8 via line 8a.
• the recovered carbon dioxide can be divided into two streams, as shown in FIG. 1, a stream 8b supplied to a compression and a pipe 8c supplied to the gas export.
• the dust-like fuel 1 is temporarily stored in the storage container 2 and transferred from there via a connecting line to the lock container 3.
• the lock container 3 To be able to absorb fuel from the reservoir 2, the lock container 3 must first be relaxed. The effluent from the lock containers gas 3e is dedusted in the filter 10 and released into the atmosphere. Then the locks are filled with fuel and pressurized with gas 3a and 3b. Thereafter, the outlet line of the lock is rinsed with 3c and the dust-like fuel from the lock container 3 via line 4b conveyed into the storage tank 5. In this case, loosening and fluidizing gas 3b and transport gas 4a are added.
• the storage tank 5 is permanently at operating pressure and continuously supplies the gasifier 7 via a plurality of lines 6a.
• the delivery from the storage container is effected by adding loosening and fluidizing gas 5b into the outlet region of the container and of further transport gas 5c into the burner line 6a.
• the Brennstoffström 6a is continuously and regulated transported by dense phase conveying in the gasification 7 via the burner 6.
• the flash gas 5e from the feed tank is returned to an appropriate pressure stage of the compressor 18 to reduce the required gas amount 8b and the compression power.
• the gasification 7 comprises a gasification reaction tor, a gas cooling and dedusting and a cooling and discharge of the slag 7b and the solids-containing water.
• the gas treatment 8 part of the carbon monoxide and water vapor is converted into carbon dioxide and hydrogen.
• the gas is purified with a solvent (eg MDEa or methanol) and carbon dioxide is separated from the synthesis gas 8a (predominantly H 2 and CO).
• a solvent eg MDEa or methanol
• carbon dioxide is separated from the synthesis gas 8a (predominantly H 2 and CO).
• the carbon dioxide-containing gas obtained in the gas purification has a low pressure and usually contains small amounts of pollutants, such as carbon monoxide ⁇ 1%, hydrogen sulfide ⁇ 10 ppmv, traces of hydrocarbons, etc.
• the recovered carbon dioxide may have one or more qualities.
• Fig. 1 shows two CO 2 streams, 8b for densification and 8c for export.
• the exported stream may often contain CO, H 2 S and methanol, eg if the gas is used to displace underground crude oil. If the pollutant content should also be reduced in this stream, this can also be done by oxidation, as shown in FIG.
• An oxygen-containing gas 16c preferably air
• the stream 8b is compressed in the compressor 18 and used for the transfer, fluidization and pneumatic transport of the fuel into the gasifier. Part of this gas is released to the environment, in the exemplary embodiment of FIG. 1 that is the flow 10e.
• an oxygen-containing gas 16 is added to the pollutant-containing gas 8b and the mixture is compressed adiabatically or polytropically with only slight intercooling.
• the oxygen addition, stream 16a may occur after compression 18.
• the compressed hot gas can optionally be further heated with heat exchangers (not shown) and dwell for a certain time at the temperature so that the pollutants, in particular CO and methanol, can react with the oxygen in the gas mixture.
• heat exchangers not shown
• the gas in the heat exchanger 19, e.g. an evaporator to be cooled to the desired temperature.
• the admixture of the oxygen 16 in front of the compressor 18 brings a further advantage in the carburetor.
• the gasification media fuel 6a and oxygen are fed into the gasifier through separate, concentric passages of the burners 6 and initially form separate strands in the gasifier which are gradually mixed together.
• the rate of reaction of the oxygen with the hot gas in the gasifier is several orders of magnitude higher than that with the first relatively cold fuel, so that the majority of the oxygen reacts with the gas, forming an extremely hot gas flame and a relatively long cold fuel strand. Only by mixing and radiation, the fuel temperature is raised, so that the gasification of the fuel can take place. If, on the other hand, part of the oxygen is fed together with the fuel, the exothermic oxygen reactions take place in the immediate vicinity of the fuel particles, which shortens the cold fuel strand and thus also the flame. The practical consequences are a higher fuel consumption and a higher carburetor output, since the maximum fuel throughput of a gasification burner is usually limited by the flame length.
• FIG. 2 shows in more detail an alternative embodiment of the emission-reduced fuel discharge and delivery, wherein, as already mentioned above, functionally identical plant components have the same reference symbols of FIG. 1.
• the dust-like fuel 1 is temporarily stored in the storage container 2 and from there via connecting lines to e.g. passed three lock container 3.
• the lines are flushed with 2c before opening the lock valves.
• fluidizing gas 2b is fed into the discharge cones of the reservoir.
• the lock containers are used offset in time to promote the fuel, so that there is a quasi-continuous supply of the storage container 5.
• the fuel-filled lock containers are pressed with 3a and 3b. Then, the fuel is transported into the receiver tank 5, whereby fluidizing gas 3b are fed into the outlet cones and transport gas 3c and 4a. Thereafter, the emptied containers are relaxed over 3e.
• the expansion gases 3e are heated, for example, in the heat exchanger 11, in order to avoid icing and condensation during the expansion and in the filter 10.
• Some of the gases can be collected in the buffer 9 and used further, for example in the storage tank, streams 2a, 2b, 2c and for inerting the grinding plant. At least some of the gases will be in the Filter 10 dedusted and released into the atmosphere.
• the buffer 9 is additionally supplied with the gas 9a, for example during the start-up phase. Part of the transport gas introduced into the feed tank 5 with the fuel is also discharged via 5e.
• the pressure of the expansion gases 5e is reduced by means of a compression device, e.g. an injector, which is driven by propellant gas 18d raised, so that the gases can be returned to the lock or used as a transport gas.
• a compression device e.g. an injector, which is driven by propellant gas 18d raised, so that the gases can be returned to the lock or used as a transport gas.
• the predominantly CO 2 -containing cold gas 8b separated in the gas treatment 8 is compressed using a compressor with interstage cooling to reduce the compression capacity.
• a portion of the compressed gas, for example, with the parameters 60 bar and 100 0 C, is fed into the buffer 17, in which a constant pressure with PC (pressure control) is regulated and then in the fuel delivery between the outlet cones of the locks and the carburetor used.
• PC pressure control
• the mixture can be heated, for example, in a gas / gas heat exchanger 15 and heated with external heat Q heater 14 further heated and contacted with a catalyst 13.
• the gas is heated by the egzotherme oxidation, so that the heat exchanger 14 at sufficiently high Concentration of the oxidizable substances H 2 , CO, H 2 S, etc., eg> 1%, can be omitted.
• the gas is heated for example in the heat exchanger 15 to 190 0 C and in the heater 14 to 220 0 C.
• CO, methanol and others are converted into significantly less toxic gases.
• the effluent from the reactor 13 gas is cooled in the heat exchanger 15 to about 130 0 C and passed into the buffer 12.
• FC flow control
• the recirculated and compressed gas 20a may alternatively be e.g. be used as transport gas 4a and 5c or as Fluidisiergas.
• the optimum parameters of oxidation of CO, methanol and the like, the temperature, the oxygen concentration, the amount of catalyst or the residence time in the high temperature range, if no catalyst is used, must be determined by economic analysis. Since the required residence time and the amount of catalyst are reduced with increasing oxygen concentration, an optimum in the case of excess oxygen is to be expected. High levels of oxygen in the lock gas, however, could result in ignition and explosion of the mixture with dusty fuel, particularly when using reactive fuels such as lignite or biofuels. The oxygen concentration should therefore not be higher than 5%.
• FIG. 3 shows a further variant of the inventive emission reduction with three C0 2 fractions with different pressures.
• the oxygen flow 16 is here the fraction 8b mixed with the lowest, for example, approximately atmospheric pressure, the mixture is adiabatically compressed until the pressure of the second fraction 8c, eg 5 bar in 18 LP, whereby the gas is heated to about 200 0 C and mixed with 8c.
• the mixture in Figs. 22 and 23 may be further heated. Then the oxidation of the pollutants in 24 and the recovery of the heat in 22.
• the most of the pollutants liberated low pressure gas is used in the low pressure part of the coal treatment 22a, by other consumers 22b, in the smuggling and promotion 22c after prior compression in the high pressure compressor 18HP, however the rest is relaxed in expander 25, recovering mechanical or electrical energy.
• the expanded gas 25a can be used, for example, for the inertization of the coal grinding plant or released into the atmosphere. Further heat exchangers, eg for heating the streams 8c, 22d, 25a or cooling the streams 18a, 18b, 22a to 22c, should be considered in consideration of the technical and economic aspects.
• Part of the gas 8 produced in the gas treatment 8, consisting mainly of CO 2 gas 8d no oxygen-containing gas is added. This gas, if necessary after compression, is exported and / or used downstream of the carburetor, for example in the gas dedusting, fly ash treatment and as flushing or sealing gas, to avoid Nutzgasppee by oxidation of H 2 and CO.
• the gas Upon release of the lock 3, the gas is significantly cooled due to the isenotropic or polytropic relaxation, whereby ice formation from the water vapor, which originates from the residual moisture of the coal, and condensation of CO 2 could disturb the process.
• the lock container is cyclically cally confronted with low temperatures, whereby the container wall is subjected to mechanical stress, resulting in a cyclic process fatigue of the material.
• the lock container is heated from the outside electrically or with a medium.
• Other apparatus of fuel extraction 2, 4, 5, 9, 10 and the connecting pipelines should also be heated in order to avoid a dew point.
• exemplary advantageous embodiments of the invention are shown to illustrate the path of pollutants into the atmosphere and the method of reducing emissions.
• the emission control according to the invention is also applicable to alternative designs of fuel injection and delivery, gasification and gas treatment, e.g.
• the oxygen-containing gas 16 may have the same composition as the oxygen flow for the gasifier.
• Common to gasification is a cryogenically recovered gas containing from 85 to 99.8% O 2 to 3% Ar and nitrogen.
• air, oxygen-enriched air or nitrogen with an oxygen content of, for example, 2% can also be used.
• gas 8b which consists predominantly of carbon dioxide
• gas 8b is generally obtained in gasification plants from the downstream gas scrubber
• an imported gas is required for the start-up operation of the entire plant, for example CO 2 or nitrogen.
• nitrogen is preferred, which can be stored for this purpose, for example in the liquid phase.
• the flow 18c shows that the compressed and low-pollutant gas 18 can also be used for other purposes, eg as lock and purge gas in the fly ash treatment.
• An export gas at medium pressure can be withdrawn from the buffer 9 and the current 1Oe is available under a slight overpressure.
• the illustrated in Fig. 2 embodiment of the reservoir 2, the lock container 3 and the Nachré effet 4b is an example that is used here to illustrate the basic processes. It is envisaged that the number of lock containers can be larger. It is also provided that the lock containers supply the feed tank 5 via a plurality of feed lines.

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• Chemical & Material Sciences (AREA)
• Engineering & Computer Science (AREA)
• Combustion & Propulsion (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• Organic Chemistry (AREA)
• Industrial Gases (AREA)
• Carbon And Carbon Compounds (AREA)
• Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
• Hydrogen, Water And Hydrids (AREA)

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• 2009
  • 2009-01-28 DE DE200910006384 patent/DE102009006384A1/de not_active Ceased
  • 2009-12-23 WO PCT/EP2009/009240 patent/WO2010086008A2/de active Application Filing
  • 2009-12-23 KR KR1020117019015A patent/KR101626185B1/ko not_active IP Right Cessation
  • 2009-12-23 CA CA 2750927 patent/CA2750927A1/en not_active Abandoned
  • 2009-12-23 RU RU2011135415/05A patent/RU2513404C2/ru not_active IP Right Cessation
  • 2009-12-23 BR BRPI0924226A patent/BRPI0924226A2/pt not_active Application Discontinuation
  • 2009-12-23 AP AP2011005832A patent/AP3458A/xx active
  • 2009-12-23 US US13/138,280 patent/US8900334B2/en not_active Expired - Fee Related
  • 2009-12-23 CN CN2009801556676A patent/CN102300963A/zh active Pending
  • 2009-12-23 EP EP09801945A patent/EP2391696A2/de not_active Withdrawn
  • 2009-12-23 UA UAA201110280A patent/UA108984C2/uk unknown
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