EP0447632B1 - Verfahren zum Betrieb einer Anlage für die Vergasung fester Brennstoffe - Google Patents

Verfahren zum Betrieb einer Anlage für die Vergasung fester Brennstoffe Download PDF

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Publication number
EP0447632B1
EP0447632B1 EP19900123157 EP90123157A EP0447632B1 EP 0447632 B1 EP0447632 B1 EP 0447632B1 EP 19900123157 EP19900123157 EP 19900123157 EP 90123157 A EP90123157 A EP 90123157A EP 0447632 B1 EP0447632 B1 EP 0447632B1
Authority
EP
European Patent Office
Prior art keywords
gasification
flydust
dust
burners
bulk density
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
EP19900123157
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0447632A1 (de
Inventor
Hans-Richard Baumann
Norbert Ullrich
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.)
Krupp Koppers GmbH
Original Assignee
Krupp Koppers GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Krupp Koppers GmbH filed Critical Krupp Koppers GmbH
Publication of EP0447632A1 publication Critical patent/EP0447632A1/de
Application granted granted Critical
Publication of EP0447632B1 publication Critical patent/EP0447632B1/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
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • 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
    • C10J3/485—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
    • 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
    • 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
    • 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
    • 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
    • C10K1/024—Dust removal by filtration
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1223—Heating the gasifier by burners

Definitions

  • German patent application P 38 37 587.7 which does not belong to the prior art, relates to a method for operating a plant for the gasification of fine-grained to dust-like solid fuels
  • Gasification reactor equipped with gasification burners.
  • Dust collection container and device for returning dust to the gasification reactor wherein the gasification burners burn into the gasification reactor with a fuel / reagent jet which is rotationally symmetrical at the gasification burner outlet, a primary reaction zone of high temperature is formed by the fuel / reagent jets in the gasification reactor and the flue dust with its raw gas content and its residual carbon through a conveying gas flow into the axis introduced by at least one fuel / reactant jet, from which the fuel / reactant jet is introduced into the primary reaction zone and is melted down therein.
  • the method according to this earlier patent application is based on the object of carrying out the method in such a way that the fly dust separated dry from the raw gas is completely incorporated into the slag without special treatment and without interfering influence on the gasification process, and at the same time the residual carbon contained in the flying dust is to be burned completely.
  • This is achieved in that the flue dust with its raw gas and residual carbon is introduced through a conveying gas stream into the axis of at least one fuel / reactant jet of a gasification burner, introduced by this into the primary reaction zone and melted in it.
  • the present invention now relates to a further embodiment of the method of operation according to the earlier patent application, by means of which, in particular, the process conditions for the return of airborne dust are to be improved. It is provided according to the invention that the bulk density of the separated dust is determined and taken into account when regulating the mass flow of the dust supplied to the gasification burners, the supply of the dust to the gasification burners being continuously and controlled with a delivery density in the order of 60 to 90% of the dust dust density he follows.
  • the invention is based on the knowledge that the bulk density of the fly dust can vary within wide limits between about 150 kg / m3 and 600 kg / m3 depending on the residual carbon contained therein. If the bulk density is low, there is a fly dust with an excessive residual carbon content, which indicates incomplete gasification in the gasification reactor. If this is the case, then according to the invention the mass flow of the fly dust supplied to the gasification burners is increased accordingly. If the residual carbon content in the fly dust is too low, ie high bulk density, the mass flow can conversely be reduced will. In order to increase the economic efficiency of the dust collection and at the same time to achieve a high uniformity of the dosage, according to the invention, a conveying density of the order of 60 to 90% of the bulk dust density is used.
  • the system shown in the figure consists of the gasification reactor 1, which is equipped, for example, with four gasification burners 2.
  • the raw gas generated in the gasification reactor 1 is drawn off via the line 3 and cooled to a temperature between 200 and 400 ° C. in a waste heat boiler, not shown in the figure, which normally forms a structural unit with the gasification reactor 1.
  • the raw gas loaded with fly dust arrives in the separator 4, in which the carried fly dust is separated dry.
  • a filter can also be used.
  • the separated flying dust falls into the collecting container 5, which is directly connected to the separator 4.
  • a quantity of flying dust can be stored in the collecting container 5. which corresponds approximately to an operating time of the gasification reactor 1 of 1 to 3 hours.
  • the raw gas freed from the bulk of the fly dust is fed via line 6 to its further treatment.
  • the intermediate container 7 is arranged below the collecting container 5 and is connected to the collecting container 5 via the distributor 8 and the line 9.
  • the collecting container 5 is emptied in the gravity flow after pressure equalization.
  • a fluidizing gas can be introduced into the outlet area of the collecting container 5 via the line 10.
  • the intermediate container 7 can of course also be arranged next to the collecting container 5. In this case, the collection container 5 is then emptied due to the pressure difference between the collection container 5 and the intermediate container 7.
  • the fluidizing gas supplied via the line 10 is withdrawn from the intermediate container 7 via the line 11 after separation of the airborne dust conveyed in the dense flow.
  • the fluidizing gas passes via line 13 into the buffer container 14. From there, the fludging gas can be withdrawn via line 15 and added to the raw gas stream in line 3 or used as a conveying gas via line 26 at the outlet of the supply container 16 .
  • the intermediate container 7 is filled cyclically as required, that is to say at a maximum fill level in the collecting container 5 or at a minimum fill level in the supply container 16.
  • the filling of the intermediate container 7 is controlled by the measuring devices 17 and 18.
  • the measuring device 17 is used to determine the vacancy and the measuring device 18 that of the full level.
  • the dust supply via the line 9 is interrupted and by supplying gas via lines 19 and 20, the required excess pressure for the conveyance to the supply container 16 is built up.
  • the lines 19 and 20 two gene from line 10.
  • a CO2- or N2-rich gas is preferably used as the gas in this line, which gas is supplied via line 10 from a source located outside the system, for example a gas supply device.
  • the dust can be conveyed from the intermediate container 7 via the line 35 into the allotment container 16 as soon as the fill level of the allotment container 16 makes this necessary.
  • the conveyance is carried out with a high delivery density between 100 and 550 kg / m3, so that the delivery density is in the order of 60 to 90% of the fly dust bulk density.
  • a screen (not shown in the figure) is installed in the line 35, if necessary, which serves to separate these impurities.
  • the allocation container 16 is dimensioned such that it can accommodate the entire filling content of the intermediate container 7.
  • the feed container 16 is equipped with a weighing device 21 and the radiometric fill level measurements 22a and 22b, which record the cylindrical part of the feed container 16. With the aid of the weighing device 21, the weight difference between the beginning and the end of the filling of the allotment container 16 can be determined.
  • the mass flow of the flying dust, which is conveyed from the feed container 16 to the gasification burners 2 during the filling process, must also be added to this value.
  • the mean bulk density of the dust can be calculated after completion of the filling process, which - as already explained above - required for a controlled operation becomes.
  • the bulk density is too low, there is a risk that the feed container 16 will be overfilled.
  • the differential pressure between the feed container 16 and the gasification reactor 1 is increased accordingly with the aid of additional gas supply via line 23.
  • the supply of conveying gas in the outlet area of the supply container 16 via the line 24 and in the central outlet line 25 via the line 26 must be increased accordingly in order to set a lower conveying density in the line 27 leading to the gasification burner 2 which is adapted to the reduced bulk density.
  • the delivery density in the central outlet line 25 can be measured and monitored by the radiometric density measurement 28.
  • An increase in the calculated bulk density of the flying dust above the normal value determined under optimized process conditions is not critical for the refilling process of the supply container 16.
  • metering can also be carried out with a lower differential pressure between the feed container 16 and the gasification reactor 1 and a higher delivery density in the central outlet line 25.
  • knowing the bulk density of the fly dust also allows a check of the gasification conditions.
  • the system according to the invention additionally the radiometric level measurements 22a and 22b are provided.
  • 22a and 22b are arranged, for example, at a distance of one meter from one another on the cylindrical part of the distribution container 16. This measuring range is only flowed through once during each filling and emptying process.
  • the bulk density when filling and emptying the distribution container 16 can be calculated if the weight difference between the maximum radiometric level measurement 22b and the minimum radiometric level measurement 22a is determined and at the same time the value for the mass flow of the Airborne dust returned to the gasification reactor 1 is taken into account. There is therefore another method for determining the bulk density to disposal.
  • the system according to the invention differs from the system according to the earlier patent application in that the fly dust is fed to the gasification reactor 1 only from a single supply container 16, the differential pressure between the supply container 16 and the gasification reactor 1 to adapt the gasification reactor 1 supported dust can be changed.
  • the guide variable for the change in the differential pressure is the ratio between the total mass of the fuel which is fed to the gasification reactor 1, that is to say all four gasification burners 2, and the mass flow of the airborne dust which is returned to the gasification reactor 1.
  • the ratio of fuel to recycled flying dust is primarily dependent on the ash content of the fuel used, the degree of C-conversion during gasification and the degree of separation of the flying dust in separator 4, to name only the main influencing factors. This dependence on the individual factors is determined by preliminary tests during the commissioning phase of the system and programmed in the control system of the system.
  • the mass flow can in each case through a Venturi tube installed in the lines 27 with the help a differential pressure meter 30 are checked. This is particularly necessary if, in deviation from the normal case, the fly dust should not be supplied to all gasification burners 2 in an evenly distributed manner, for example because the gasification burners 2 have a different construction or fuel supply in some cases.
  • the required regulation of the mass flow of dust can be carried out with the help of the control valve 31 installed in the line 27.
  • a further radiometric density measurement 32 can be installed in the central outlet line 25.
  • the residual carbon content of the returned fly dust can also be determined.
  • the residual carbon content can serve as a reference variable for the change in the oxygen / carbon ratio in the gasification reactor caused by the fly dust recirculation.
  • the disposal line 33 is connected to the distributor 8. This line is provided for the event of a fault if the fly dust separated in the separator 4 cannot be returned to the gasification reactor 1 as a result of a malfunction and must therefore be removed from the system via the disposal line 33.
  • this flue dust can, if necessary, be passed together with the raw gas drawn off via line 6 into a separator (not shown in the figure), in which the flue dust is separated by moisture, the resulting slurry being thickened and then melted or deposited into a slag.

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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)
  • Processing Of Solid Wastes (AREA)
  • Gasification And Melting Of Waste (AREA)
EP19900123157 1990-02-16 1990-12-04 Verfahren zum Betrieb einer Anlage für die Vergasung fester Brennstoffe Expired - Lifetime EP0447632B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE4004874 1990-02-16
DE19904004874 DE4004874A1 (de) 1990-02-16 1990-02-16 Verfahren zum betrieb einer anlage fuer die vergasung fester brennstoffe

Publications (2)

Publication Number Publication Date
EP0447632A1 EP0447632A1 (de) 1991-09-25
EP0447632B1 true EP0447632B1 (de) 1993-06-30

Family

ID=6400319

Family Applications (1)

Application Number Title Priority Date Filing Date
EP19900123157 Expired - Lifetime EP0447632B1 (de) 1990-02-16 1990-12-04 Verfahren zum Betrieb einer Anlage für die Vergasung fester Brennstoffe

Country Status (7)

Country Link
EP (1) EP0447632B1 (enrdf_load_stackoverflow)
CN (1) CN1030464C (enrdf_load_stackoverflow)
DE (2) DE4004874A1 (enrdf_load_stackoverflow)
DK (1) DK0447632T3 (enrdf_load_stackoverflow)
ES (1) ES2043222T3 (enrdf_load_stackoverflow)
PL (1) PL164897B3 (enrdf_load_stackoverflow)
ZA (1) ZA9010026B (enrdf_load_stackoverflow)

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4113447A1 (de) * 1991-04-25 1992-10-29 Krupp Koppers Gmbh Verfahren zur steuerung des betriebsablaufes eines vergasungsreaktors
DE102010018108A1 (de) * 2010-04-24 2011-10-27 Uhde Gmbh Vorrichtung zur Versorgung mehrerer Brenner mit feinkörnigem Brennstoff
US8721747B2 (en) * 2010-08-11 2014-05-13 General Electric Company Modular tip injection devices and method of assembling same
WO2012151625A1 (en) 2011-05-09 2012-11-15 Hrl Treasury (Idgcc) Pty Ltd Improvements in integrated drying gasification
DE102011083850A1 (de) * 2011-09-30 2013-04-04 Siemens Aktiengesellschaft Pneumatische Brennstoffzuführung von einem Dosiergefäß zu einem Vergasungsreaktor mit hohem Differenzdruck

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL171691C (nl) * 1973-02-26 1983-05-02 Shell Int Research Werkwijze voor de bereiding van waterstof en/of koolmonoxide bevattende gassen door onvolledige verbranding van brandstoffen en afscheiding van de daarbij gevormde vaste stofdeeltjes.
US4158552A (en) * 1977-08-29 1979-06-19 Combustion Engineering, Inc. Entrained flow coal gasifier
DD147188A3 (de) * 1977-09-19 1981-03-25 Lutz Barchmann Verfahren und vorrichtung zur druckvergasung staubfoermiger brennstoffe
DE3132506A1 (de) * 1981-08-18 1983-03-03 Hoechst Ag, 6000 Frankfurt Verfahren und vorrichtung zur herstellung von synthesegas
DE3372867D1 (en) * 1982-11-11 1987-09-10 Shell Int Research Process for the partial combustion of solid fuel with fly ash recycle
DE3810404A1 (de) * 1988-03-26 1989-10-12 Krupp Koppers Gmbh Verfahren und vorrichtung zum pneumatischen foerdern eines feinkoernigen bis staubfoermigen brennstoffes in einen unter erhoehtem druck stehenden vergasungsreaktor
DE3823773A1 (de) * 1988-07-14 1990-01-18 Krupp Koppers Gmbh Verfahren zur ermittlung und steuerung des brennstoff-massenstromes bei der partialoxidation (vergasung) von feinkoernigen bis staubfoermigen brennstoffen

Also Published As

Publication number Publication date
ES2043222T3 (es) 1993-12-16
DE59001892D1 (de) 1993-08-05
DK0447632T3 (da) 1993-11-22
EP0447632A1 (de) 1991-09-25
CN1030464C (zh) 1995-12-06
PL288331A3 (en) 1991-12-02
ZA9010026B (en) 1991-10-30
PL164897B3 (pl) 1994-10-31
DE4004874A1 (de) 1991-08-29
CN1054095A (zh) 1991-08-28
DE4004874C2 (enrdf_load_stackoverflow) 1992-11-19

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