CN106190333A - Integrated gasification combined TRT based on fine coal air classification pyrolytic gasification - Google Patents

Integrated gasification combined TRT based on fine coal air classification pyrolytic gasification Download PDF

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CN106190333A
CN106190333A CN201610565870.2A CN201610565870A CN106190333A CN 106190333 A CN106190333 A CN 106190333A CN 201610565870 A CN201610565870 A CN 201610565870A CN 106190333 A CN106190333 A CN 106190333A
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gas
outlet
level
fluidized bed
bed
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田原宇
乔英云
谢克昌
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China University of Petroleum East China
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China University of Petroleum East China
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    • 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
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—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
    • C10J3/72—Other features
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
    • F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
    • F01K23/06—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle
    • F01K23/10—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle with exhaust fluid of one cycle heating the fluid in another cycle
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1606—Combustion 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
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
    • C10J2300/1675—Integration of gasification processes with another plant or parts within the plant with the production of electricity making use of a steam turbine
    • 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
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Abstract

The present invention provides Integrated gasification combined TRT based on fine coal air classification pyrolytic gasification, carry circulation fluidized bed front end and be sequentially provided with raw coal pulverizer and pressurization conveying system, bottom is provided with gas distributor and ash releasing tube, returning charge mouth upwards 300 3000mm are provided with air flow bed, and top is provided with two grades of gas-solid separators；Filling heat exchange feed bin under ash releasing tube, bottom is reversely connected with pressurization conveying system by flow control valve；First order separation cinder is connected with carrying circulation fluidized bed returning charge mouth by material returning device, and separation fine ash in the second level is connected with air flow bed by material returning device, and second level gas outlet is connected with high-temperature mobile bed by gas heat-exchanger；Gas turbine and two grades of aerostatic presses, one-level aerostatic press and generator coaxle formula couple linkage successively, and one-level aerostatic press one way outlet is connected with burner, another way outlet accesses two grades of aerostatic presses；Softening water inlet and access steam turbine by heat recovery boiler, steam turbine couples linkage with electromotor；Steam turbine and two grades of aerostatic presses all with gas distributor air inlet pipe UNICOM.

Description

Integrated gasification combined TRT based on fine coal air classification pyrolytic gasification
1. technical field
The present invention provides Integrated gasification combined TRT based on fine coal air classification pyrolytic gasification, belongs to Coal Chemical Industry neck Territory.
2. background technology
But the general knowledge at energy field is exactly coal is the highest energy of low price disposal of pollutants, so exploitation cleaning Coal utilize technology, the target that always countries in the world government and industry are made joint efforts.
Current domestic Coal Clean generation technology has two kinds of schools.A kind of efficiency being to improve conventional coal unit, mainly Method is to improve the temperature of main steam, strengthens acting ability, is an independent Rankine cycle, such as supercritical, ultra supercritical. Another is that IGCC (Integrated Gasification Combined Cycle) i.e. integrated gasification combined cycle plants is sent out Electricity system, is clean Coal Gasification Technology and efficient combustion gas--steam combined cycle power generating system combines, first handle Coal gasification, then promotes combustion engine acting, is equipped with turbine exhaust heat generating simultaneously, namely " makes the plant gas of raw material of coal ". It is how high that the acting ability of any circulation both depends on working gas initial temperature, the main steam temperature of ultra supercritical more than 600 DEG C, And gas turbine acting turbine before temperature be about 1300 DEG C, so IGCC by be next step Coal Clean generating main flow with Trend.
Under state-of-the art, the net efficiency of IGCC generating, up to 43%～45%, is expected to reach higher from now on；And it is dirty The discharge capacity of dye thing is only the 1/10 of conventional coal fired power plant, and desulfuration efficiency is up to 99%, and sulfur dioxide (SO2) emissions are at 25mg/Nm3Left The right side, far below discharge standard 1200mg/Nm3, discharged nitrous oxides only has the 15%～20% of conventional power plant, water consumption only routine The 1/2～1/3 of power station.Therefore, compared with traditional coal power technology, IGCC has that generating efficiency is high, pollutant emission is low, titanium dioxide The advantages such as carbon trapping low cost, are current clean and effective coals that be verified in the world, can be industrialized, most with prospects Power technology.
IGCC is made up of two parts, i.e. coal gasification and purification part and combustion gas--steam combined cycle power generating part. The capital equipment of Part I has gasification furnace, air separation unit, gas purification equipment (including the retracting device of sulfur)；Part II Capital equipment has gas turbine generating system, waste heat boiler, steam turbine power generating.Multiple key equipments combine and integrated, System is the most complicated, less stable, has had a strong impact on the steady long-term operation of device.General IGCC technical process is: Coal, through being gasificated as middle low-heat value gas, through purifying, removes the pollutant such as the sulfide in coal gas, nitride, dust, becomes The gaseous fuel of cleaning, is then fed into the combustion chambers burn of gas turbine, and heating gas working medium is to drive combustion gas turbine acting, combustion Gas-turbine aerofluxus enters waste heat boiler heating feedwater, produces superheated steam and drives steam turbine acting.
The most in the world, 5 the IGCC power stations built except the U.S., Holland, Spain, Japan and other countries, in Tianjin, state Huaneng Group IGCC Demonstration Station is the 6th IGCC power station, the whole world, and the Edwardsport power station of Indiana, USA is complete The 7th IGCC power station of ball, the kemper power station of Mississippi, America is in the 8th the IGCC power station built, the nearlyest 20 Seat is for the IGCC Plant of Poly-generation.These IGCC overwhelming majority are the high-temperature slag entrained flow gasifications using oxygen to be gasifying agent Stove and wet method low temperature purification.On the one hand air separation unit oxygen energy consumption and investment height, accounts for the investment of coal gasification and operation energy consumption Half, thus increase per kilowatt investment number, have impact on the economic competitiveness of IGCC；On the other hand gasification furnace is high-temperature slag Discharge air flow bed, investment height, oxygen consumption is high, and hot operation status devices degradation, fault rate are increased sharply, and gasification gas waste heat recovery is difficult Degree is big, and slag tap operation easier is big, the difficult recovery of waste heat, Quench sewage disposal difficulty are big；Another further aspect, combustion gas wet method low temperature is clean Changing, high-temperature fuel gas heat utilization rate in lifting repeatedly is low, and secondary sewage quantity is bigger；Finally, air separation unit and gasification furnace, combustion gas The big key equipment of turbine generator group three links, and fault rate will be multiplied, and affect the long period even running of IGCC Plant, as China's Tianjin, Huaneng Group IGCC Demonstration Station runs always unstable after going into operation, just operating is less than half a year, is necessary for stopping production more than two The moon carries out large repairs, thus becomes the bottleneck of IGCC technology industrial application.
In order to save cost and the energy loss of nitrogen oxygen separating, simple flow, overall unit efficiency, reduction are greatly improved The unit K W investment of IGCC power station, coal air gasification technology and efficient combustion gas--steam combined cycle power generating system combines with integrated IGCC technology direction become current study hotspot both domestic and external and emphasis.Send out as the Japan of completion in 2007 does not come (nakoso) Electricity No. 10 machines be exactly the IGCC technology based on air gas of installed capacity 250mw and U.S.'s south electric power based on sky The IGCC technology of gas conveying bed gasification, but owing to fuel gases calorific value is closely related with working gas initial temperature, these air gasization are equal There is the low (1200Kcal/Nm of fuel gases calorific value3Left and right), it is impossible to meet the gas heating value requirement of Modern high throughput gas turbine power generation (more than 1350Kcal/Nm3), the poor efficiency jet dynamic control of would have to the use initial temperature 1200 DEG C that do not generates electricity such as Japan； In addition to eliminate phenol wastewater secondary pollution and the flying dust reduction carbon gasification conversion ratio that gasified tar produces, typically use height Geothermal liquid deslagging, under equipment high temperature, operation easier is big, fault rate is high, and sewage quantity is big and difficult, have impact on based on air gas The competitiveness of the IGCC technology changed.
3. summary of the invention
Deficiency that the purpose of the present invention is contemplated to overcome existing IGCC technology to exist and provide based on fine coal air classification The Integrated gasification combined TRT of pyrolytic gasification, had both solved high, the power transmission high with space division energy loss of existing IGCC technology investment The difficult problem that end efficiency is low and three machines linkage fault rate is high, again can be integrated with the high-efficiency gas turbine of high initial temperature, simple flow, Increase substantially overall unit efficiency, reduce the unit K W investment of IGCC power station, improve the normal utilization of capacity, reduce sewage growing amount.
Technical scheme:
Integrated gasification combined TRT based on fine coal air classification pyrolytic gasification, by carrying circulation fluidized bed, gas distribution Device, pressurization conveying system, pulverizer, first order gas-solid separator, material returning device, second level gas-solid separator, air flow bed, returning charge Mouthful, carry a reactor, turbulent fluidized bed, gas heat-exchanger, high-temperature mobile bed, burner, gas turbine, air intake, one Level aerostatic press, two grades of aerostatic presses, softening water inlet, heat recovery boiler, steam turbine, electromotor, cooling water inlet, cooling water go out Mouth, heat exchange feed bin, flow control valve and chimney etc. form；The front end carrying circulation fluidized bed is sequentially provided with raw coal pulverizer and pressurizes defeated Material system, the outlet of pressurization conveying system accesses carries the feeding-in solid body mouth in the middle part of circulation fluidized bed；Carry and bottom circulation fluidized bed, be provided with gas Body distributor and ash releasing tube, the position away from bottom 300-1000mm is provided with returning charge mouth, away from the position of returning charge mouth upwards 300-3000mm Installing the air flow bed of Y type connection, the position away from air flow bed upwards 500-3000mm is provided with feeding-in solid body mouth, and top is provided with two grades Gas-solid separator；Equipped with heat exchange feed bin under ash releasing tube, heat exchange feed bin side arranges cooling water inlet and coolant outlet, and bottom leads to Inflow-rate of water turbine controlling valve is reversely connected with pressurization conveying system；The cinder circulation pipe of first order gas-solid separator passes through material returning device and takes Being connected with the returning charge mouth bottom circulation fluidized bed, the fine ash circulation pipe of second level gas-solid separator passes through material returning device and air flow bed phase Even, second level gas-solid separator gas outlet is connected with high-temperature mobile bed by gas heat-exchanger；Burner, gas turbine and two Level aerostatic press, one-level aerostatic press and electromotor composition Gas Turbine Generating Units；The outlet of high-temperature mobile bed and one-level compressor A way outlet all with burner connect, burner outlet access gas turbine, gas turbine outlet pass through heat recovery boiler Access smoke stack emission；Gas turbine and two grades of aerostatic presses, one-level aerostatic press and generator coaxle formula couple linkage successively, and air enters Mouth accesses one-level aerostatic press, and a way outlet of one-level aerostatic press is connected with burner, another way outlet accesses two grades of aerostatic presses；Soft Changing water inlet and accessed the entrance of steam turbine by heat recovery boiler, steam turbine couples linkage with electromotor；The outlet of steam turbine With the outlet of two grades of aerostatic presses all with the gas distributor air inlet pipe UNICOM carried bottom circulation fluidized bed.
Carrying circulation fluidized bed is carrying reactor and carrying reactor lower part Y of the turbulent fluidized bed by bottom and top The air flow bed of type connection combines, and turbulent fluidized bed equivalent diameter is relatively big, and it is less to carry reactor equivalent diameter, diameter ratio It is 2～3:1；Carrying reactor both can be the homogeneous straight tube reactor of equivalent diameter, it is also possible to be by a diameter of different equivalents The size straight tube of diameter multiple is formed by connecting by concentric reducer pipe fitting, and the diameter ratio of size straight tube is 1.2～2:1；Air flow bed Equivalent diameter is only the 10%-50% of turbulent fluidized bed equivalent diameter.
The reaction temperature of turbulent fluidized bed is 800-1200 DEG C, and the reaction temperature of air flow bed is 1200-1600 DEG C, carries anti- Answering the reaction temperature at the feeding-in solid body mouth of device to be 700-1000 DEG C, the reaction temperature carrying reactor top is 600-900 DEG C, The reaction temperature of heat exchange bin outlet is no more than 100 DEG C.
The feed coal that pulverizer is pulverized is the one in brown coal, long bituminous coal or bituminous coal or mixture, and after pulverizing, granularity is little Coal dust in 5mm.
Pressurization conveying system is dry powder force (forcing) pump or coal lock pressurizing feeder.
After carrying the pressure of circulation fluidized bed, the outlet pressure of two-stage compressor, exhaust steam in steam turbine pressure and coal dust pressurization conveying Pressure is identical, the outlet pressure 0.1-0.6MPa higher than the outlet pressure of one-level compressor of two-stage compressor.
One-level compressor forced air is 2:1-0.7 with the mass ratio of two-stage compressor forced air.
Embodiment is described the feature of the present invention by the present invention in detail.
4. accompanying drawing explanation
Accompanying drawing is the process schematic representation of the present invention.
The drawing of accompanying drawing sets bright as follows:
1, circulation fluidized bed 2, gas distributor 3, pressurization conveying system 4, pulverizer 5, first order gas-solid separator are carried 6, material returning device 7, second level gas-solid separator 8, air flow bed 9, returning charge mouth, 10, carry a reactor 11, turbulent fluidized bed 12, gas heat-exchanger 13, high-temperature mobile bed 14, burner 15. gas turbine 16, air intake 17, one-level aerostatic press 18, two grades of aerostatic presses 19, softening water inlet 20, heat recovery boiler 21, steam turbine 22, electromotor 23, cooling water inlets 24, coolant outlet 25, heat exchange feed bin 26, flow control valve 27, chimney
Assembly of the invention feature is described in detail in detail with embodiment below in conjunction with the accompanying drawings.
5. detailed description of the invention
Embodiment, Integrated gasification combined TRT based on fine coal air classification pyrolytic gasification, by carry circulation fluidized bed 1, Gas distributor 2, pressurization conveying system 3, pulverizer 4, first order gas-solid separator 5, material returning device 6, second level gas-solid separator 7, air flow bed 8, returning charge mouth 9, carry a reactor 10, turbulent fluidized bed 11, gas heat-exchanger 12, high-temperature mobile bed 13, burning Device 14, gas turbine 15, air intake 16,17, two grades of aerostatic presses 18 of one-level aerostatic press, softening water inlet 19, Waste Heat Recovery pot Stove 20), steam turbine 21), electromotor 22), cooling water inlet 23), coolant outlet 24), heat exchange feed bin 25), flow control valve 26) and the composition such as chimney 27；The front end carrying circulation fluidized bed 1 is sequentially provided with pulverizer 4 and pressurization conveying system 3, the pressurization of raw coal The outlet of conveying system 3 accesses carries the feeding-in solid body mouth in the middle part of circulation fluidized bed 1；Carry and bottom circulation fluidized bed 1, be provided with gas distributor 2 And ash releasing tube, the position away from bottom 300-1000mm is provided with returning charge mouth 6, and the position away from returning charge mouth 6 upwards 300-3000mm is provided with Y The air flow bed 8 of type connection, the position away from air flow bed 8 upwards 500-3000mm is provided with feeding-in solid body mouth, and top is provided with two grades of gas-solids Separator；The cinder circulation pipe of first order gas-solid separator 5 is connected with the returning charge mouth 9 carried bottom circulation fluidized bed 1 by material returning device 6 Logical, the fine ash circulation pipe of second level gas-solid separator 7 is connected with air flow bed 8 by material returning device 6, second level gas-solid separator 7 gas Body outlet is connected with high-temperature mobile bed 13 by gas heat-exchanger 12；Burner 14, gas turbine 15 and two grades of aerostatic presses 18, Level aerostatic press 17 and electromotor 22 form Gas Turbine Generating Units；The outlet of high-temperature mobile bed 13 and the one of one-level compressor 17 Way outlet is all connected with burner 14, and burner 14 outlet accesses gas turbine 15, and Waste Heat Recovery is passed through in gas turbine 15 outlet Boiler 20 accesses chimney 27 and discharges；Gas turbine 15 and two grades of aerostatic presses 18, one-level aerostatic press 17 and electromotor 22 coaxial-type depend on Secondary connection links, and air intake 16 accesses one-level aerostatic press 17, and a way outlet of one-level aerostatic press 17 is connected with burner 14, separately One way outlet accesses two grades of aerostatic presses 18；Soften water inlet 19 and accessed the entrance of steam turbine 21, vapour by heat recovery boiler 20 Turbine 21 couples linkage with electromotor 22；The outlet of steam turbine 21 and two grades of aerostatic presses 18 export all with carry bottom circulation fluidized bed 1 Gas distributor 2 air inlet pipe UNICOM；Equipped with heat exchange feed bin 25 under ash releasing tube, heat exchange feed bin 25 side arranges cooling water inlet 23 With coolant outlet 24, bottom is reversely connected with pressurization conveying system 3 by flow control valve 26.
Carrying circulation fluidized bed 1 is carrying reactor 10 and carrying reactor 10 of the turbulent fluidized bed 11 by bottom and top The air flow bed 8 of bottom Y type connection combines, and turbulent fluidized bed 11 equivalent diameter is relatively big, carries reactor 10 equivalent diameter relatively Little, diameter ratio is 2～3:1；Carrying reactor 10 both can be the homogeneous straight tube reactor of equivalent diameter, it is also possible to be by directly Footpath is that the size straight tube of different equivalent diameter multiple is formed by connecting by concentric reducer pipe fitting, and the diameter ratio of size straight tube is 1.2 ～2:1；(8 equivalent diameters are only the 10%-50% of turbulent fluidized bed (11) equivalent diameter to air flow bed.
The reaction temperature of turbulent fluidized bed (11) is 800-1200 DEG C, and the reaction temperature of air flow bed (8) is 1200-1600 DEG C, (reaction temperature at the feeding-in solid body mouth of 10 is 700-1000 DEG C, carries the reactor (reaction on 10 tops to carry reactor Temperature is 600-900 DEG C, and (reaction temperature of 25 outlets is no more than 100 DEG C to heat exchange feed bin.
The feed coal that pulverizer 4 is pulverized is the one in brown coal, long bituminous coal or bituminous coal or mixture, and after pulverizing, granularity is little Coal dust in 5mm.
Pressurization conveying system 3 is dry powder force (forcing) pump or coal lock pressurizing feeder.
Carry the pressure of circulation fluidized bed 1, the outlet pressure of two-stage compressor 18, steam turbine 21 exhaust steam pressure and coal dust pressurization defeated After material, pressure is identical, the outlet pressure 0.1-0.6MPa higher than the outlet pressure of one-level compressor 17 of two-stage compressor 18.
One-level compressor 17 forced air is 2:1-0.7 with the mass ratio of two-stage compressor 18 forced air.
During carrying out practically, feed coal is ground into the coal dust of 0～6mm, then by pressurization conveying system by pulverizer 4 3 entrance are carried circulation fluidized bed 1 middle and lower part and are mixed with High Temperature Gas activating QI and circulating ash, carry out fine coal hydrocracking at 700-1000 DEG C Reaction, generates a large amount of methane and a little tar, and flows up formation Matter Transfer together；Cracking oil and gas and gasification gas and circulation Grey mixing in carrying a reactor is lifted up, and proceeds hydrogenation of tar pyrolysis at 600-900 DEG C, produces methane with light Hydrocarbon；Carrying circulation fluidized bed 1 top through gas solid separation, the high temperature big-and-middle particulate carbonaceous heat ash that first order gas-solid separator 5 separates Being returned from returning charge mouth 9 by material returning device 6 carries bottom circulation fluidized bed 1, with two-stage pressurizing hot-air and exhaust steam in steam turbine at 800- At 1200 DEG C occur char Gasification reaction, gasification gas with the overwhelming majority high-temp circulating ash again together with flow up formation material follow Ring；The high-temperature fine carbon containing ash that second level gas-solid separator 7 separates is delivered to and carries the air flow bed 8 that circulation fluidized bed 1 middle and lower part Y type connects In, air gasification reaction at 1200～1600 DEG C, generates High Temperature Gas and liquid lime-ash effluent stream bed 8 enters and carries circulation fluidized bed In 1, High Temperature Gas ramps up entrance and carries circulation fluidized bed 1 middle and lower part, and in order to carry circulation fluidized bed, (1 fine coal and hydrogenation of tar cracking provide heat Amount；Liquid lime-ash flows downwardly into the circulating ash bed of material carrying circulation fluidized bed 1 bottom, and heat exchange is solidified as solid lime-ash, with carrying circulation The solid material of bed 1 participates in circulation or ash discharge is discharged；Second level gas-solid separator 7 separates gas as combustion gas through combustion gas heat exchange After device 12 heat exchange homoiothermic, purified by high-temperature mobile bed 13 dust-removal and desulfurizing dechlorination and removing heavy-metal；After purification, combustion gas is at burner With one-level forced air high efficient mixed and burning in 14, propelling gas turbine engine high speed rotating, drive two grades of aerostatic presses 18, one-level gas Press 17 and electromotor 22 operate；Dust-collecting air enters one-level aerostatic press 17 from air intake 16 and pressurizes, rear section conduct of pressurizeing The combustion air of gas turbine 15, is partially into two grades of aerostatic press 18 repressurizations；The high-temperature flue gas of gas turbine 15 is by useless After the water that softening water inlet 19 adds is heated into high steam by thimble-tube boiler 20, discharged by chimney 27；High steam pushes away Dynamic steam turbine 21 rotates and drives electromotor 22 to generate electricity, and the electricity that gas electricity generator and steam turbine generator produce is sent outside as product； Steam turbine 21 exhaust steam and secondary high-pressure hot-air enter by carrying the gas distributor 2 bottom circulation fluidized bed 1, and semicoke is at 800- Generating gasification reaction at 1200 DEG C；Small part high-temp circulating ash enters heat exchange feed bin 25 from the ash releasing tube carried bottom circulation fluidized bed 1, Entered from cooling water inlet 23, cooling water heat exchange that coolant outlet 24 is discharged cools to less than 100 DEG C, from heat exchange feed bin 25 Bottom regulates and controls the timing of cold cycle ash by pressurization conveying system reversely outer row by flow control valve 26.
Integrated gasification combined TRT based on fine coal air classification pyrolytic gasification provided by the present invention, by carrying Circulation fluidized bed fine coal classification pyrolytic gasification produces the combustion gas rich in methane and dry ash extraction and high-temperature mobile bed gas-purification, it is possible to Meet the requirement of the combustion gas heat of the high-efficiency gas turbine of high initial temperature, both solved existing IGCC technology and invested too high and space division energy The difficult problem that source loss is high, sending end efficiency is low and three machines linkage fault rate is high, again can be with the high-efficiency gas turbine of high initial temperature Integrated, simple flow, increase substantially overall unit efficiency, reduce the unit K W investment of IGCC power station, improve the normal utilization of capacity, subtract Few water consumption and sewage growing amount；Additionally gasifier operation is easy, and oxygen consumption is low, gasification efficiency is high, and the intensity of gasification is big, equipment body Long-pending little, steel consumption is low, and fixed investment is substantially reduced, and ash discharge process is simple.

Claims (7)

1. Integrated gasification combined TRT based on fine coal air classification pyrolytic gasification, by carry circulation fluidized bed, gas distributor, Pressurization conveying system, pulverizer, first order gas-solid separator, material returning device, second level gas-solid separator, air flow bed, returning charge mouth, take Band bed reactor, turbulent fluidized bed, gas heat-exchanger, high-temperature mobile bed, burner, gas turbine, air intake, one-level air pressure Machine, two grades of aerostatic presses, soften water inlet, heat recovery boiler, steam turbine, electromotor, cooling water inlet, coolant outlet, change Hot aggregate bin, flow control valve and chimney etc. form, and its technical characteristic is that the front end carrying circulation fluidized bed is sequentially provided with raw coal pulverizer With pressurization conveying system, the outlet of pressurization conveying system accesses carries the feeding-in solid body mouth in the middle part of circulation fluidized bed；Carry at the bottom of circulation fluidized bed Portion is provided with gas distributor and ash releasing tube, and the position away from bottom 300-1000mm is provided with returning charge mouth, away from returning charge mouth upwards 300- The position of 3000mm is provided with the air flow bed of Y type connection, and the position away from air flow bed upwards 500-3000mm is provided with feeding-in solid body mouth, top Portion is provided with two grades of gas-solid separators；Equipped with heat exchange feed bin under ash releasing tube, heat exchange feed bin side arranges cooling water inlet and cooling water Outlet, bottom is reversely connected with pressurization conveying system by flow control valve；The cinder circulation pipe of first order gas-solid separator leads to The returning charge mouth crossing material returning device and carry bottom circulation fluidized bed is connected, and the fine ash circulation pipe of second level gas-solid separator passes through material returning device Being connected with air flow bed, second level gas-solid separator gas outlet is connected with high-temperature mobile bed by gas heat-exchanger；Burner, combustion Gas-turbine and two grades of aerostatic presses, one-level aerostatic press and electromotor composition Gas Turbine Generating Units；The outlet of high-temperature mobile bed and One way outlet of one-level compressor is all connected with burner, and burner outlet accesses gas turbine, and gas turbine outlet is by useless Thimble-tube boiler accesses smoke stack emission；Gas turbine and two grades of aerostatic presses, one-level aerostatic press and generator coaxle formula couple successively Linkage, air intake accesses one-level aerostatic press, and a way outlet of one-level aerostatic press is connected with burner, another way outlet accesses two Level aerostatic press；Softening water inlet and accessed the entrance of steam turbine by heat recovery boiler, steam turbine couples linkage with electromotor；Vapour The outlet of turbine and the outlet of two grades of aerostatic presses all with the gas distributor air inlet pipe UNICOM carried bottom circulation fluidized bed.
Integrated gasification combined TRT based on fine coal air classification pyrolytic gasification the most according to claim 1, it is special Levy that to be to carry circulation fluidized bed be carrying reactor and carrying reactor lower part Y type of the turbulent fluidized bed by bottom and top The air flow bed of connection combines, and turbulent fluidized bed equivalent diameter is relatively big, and it is less to carry reactor equivalent diameter, and diameter ratio is 2～3:1；Carrying reactor both can be the homogeneous straight tube reactor of equivalent diameter, it is also possible to be straight by a diameter of different equivalents The size straight tube of footpath multiple is formed by connecting by concentric reducer pipe fitting, and the diameter ratio of size straight tube is 1.2～2:1；Air flow bed is worked as Amount diameter is only the 10%-50% of turbulent fluidized bed equivalent diameter.
Integrated gasification combined TRT based on fine coal air classification pyrolytic gasification the most according to claim 1, it is special Levying and be that the reaction temperature of turbulent fluidized bed is 800-1200 DEG C, the reaction temperature of air flow bed is 1200-1600 DEG C, carries reaction Reaction temperature at the feeding-in solid body mouth of device is 700-1000 DEG C, and the reaction temperature carrying reactor top is 600-900 DEG C, changes The reaction temperature of hot aggregate bin outlet is no more than 100 DEG C.
Integrated gasification combined TRT based on fine coal air classification pyrolytic gasification the most according to claim 1, it is special Levy and be that pressurization conveying system is dry powder force (forcing) pump or coal lock pressurizing feeder.
Integrated gasification combined TRT based on fine coal air classification pyrolytic gasification the most according to claim 1, it is special Levying and be that the feed coal that pulverizer is pulverized is the one in brown coal, long bituminous coal or bituminous coal or mixture, after pulverizing, granularity is for being less than The coal dust of 5mm.
Integrated gasification combined TRT based on fine coal air classification pyrolytic gasification the most according to claim 1, it is special Levy and press after being to carry the pressure of circulation fluidized bed, the outlet pressure of two-stage compressor, exhaust steam in steam turbine pressure and coal dust pressurization conveying Power is identical, the outlet pressure 0.1-0.6MPa higher than the outlet pressure of one-level compressor of two-stage compressor.
Integrated gasification combined TRT based on fine coal air classification pyrolytic gasification the most according to claim 1, it is special Levy and be that one-level compressor forced air is 2:1-0.7 with the mass ratio of two-stage compressor forced air.
CN201610565870.2A 2016-07-18 2016-07-18 Integrated gasification combined TRT based on fine coal air classification pyrolytic gasification Withdrawn CN106190333A (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106701205A (en) * 2017-03-22 2017-05-24 中国石油大学(华东) Integrated gasification combined power generating device based on air staging pyrolysis gasification of pulverized coal
CN108504394A (en) * 2017-02-23 2018-09-07 中国石油化工股份有限公司 It is catalyzed pyrolysis-gasification integrated reacting device and method

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108504394A (en) * 2017-02-23 2018-09-07 中国石油化工股份有限公司 It is catalyzed pyrolysis-gasification integrated reacting device and method
CN108504394B (en) * 2017-02-23 2020-07-07 中国石油化工股份有限公司 Catalytic pyrolysis-gasification integrated reaction device and method
CN106701205A (en) * 2017-03-22 2017-05-24 中国石油大学(华东) Integrated gasification combined power generating device based on air staging pyrolysis gasification of pulverized coal

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