CN107723031A - High-pressure gasification and pyrolysis integrated device for pulverized coal - Google Patents
High-pressure gasification and pyrolysis integrated device for pulverized coal Download PDFInfo
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- CN107723031A CN107723031A CN201711185376.4A CN201711185376A CN107723031A CN 107723031 A CN107723031 A CN 107723031A CN 201711185376 A CN201711185376 A CN 201711185376A CN 107723031 A CN107723031 A CN 107723031A
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- gasification
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 114
- 239000003245 coal Substances 0.000 title claims abstract description 102
- 238000002309 gasification Methods 0.000 title claims abstract description 93
- 239000007789 gas Substances 0.000 claims abstract description 104
- 238000010791 quenching Methods 0.000 claims abstract description 45
- 238000000926 separation method Methods 0.000 claims abstract description 33
- 238000001816 cooling Methods 0.000 claims abstract description 17
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 13
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 13
- 239000001257 hydrogen Substances 0.000 claims abstract description 13
- 238000004064 recycling Methods 0.000 claims abstract description 11
- 238000005979 thermal decomposition reaction Methods 0.000 claims description 31
- 230000015572 biosynthetic process Effects 0.000 claims description 23
- 238000003786 synthesis reaction Methods 0.000 claims description 23
- 239000000463 material Substances 0.000 claims description 10
- 239000000498 cooling water Substances 0.000 claims description 7
- 230000008859 change Effects 0.000 claims description 4
- 239000003870 refractory metal Substances 0.000 claims description 4
- 229910010293 ceramic material Inorganic materials 0.000 claims description 3
- 235000008331 Pinus X rigitaeda Nutrition 0.000 claims 1
- 235000011613 Pinus brutia Nutrition 0.000 claims 1
- 241000018646 Pinus brutia Species 0.000 claims 1
- 239000011819 refractory material Substances 0.000 abstract description 3
- 239000000428 dust Substances 0.000 abstract description 2
- 230000000171 quenching effect Effects 0.000 abstract 1
- 238000000034 method Methods 0.000 description 13
- 239000003077 lignite Substances 0.000 description 12
- 238000006243 chemical reaction Methods 0.000 description 10
- 239000011269 tar Substances 0.000 description 10
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 9
- 239000003546 flue gas Substances 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 7
- 239000000571 coke Substances 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 239000007787 solid Substances 0.000 description 6
- 238000002485 combustion reaction Methods 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 238000005984 hydrogenation reaction Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000000843 powder Substances 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- QJZYHAIUNVAGQP-UHFFFAOYSA-N 3-nitrobicyclo[2.2.1]hept-5-ene-2,3-dicarboxylic acid Chemical compound C1C2C=CC1C(C(=O)O)C2(C(O)=O)[N+]([O-])=O QJZYHAIUNVAGQP-UHFFFAOYSA-N 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 239000011280 coal tar Substances 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 239000004021 humic acid Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 230000002269 spontaneous effect Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
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
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
-
- 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
- C10J3/72—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
- C10J3/74—Construction of shells or jackets
-
- 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
- C10J3/78—High-pressure apparatus
-
- 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
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
- C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
- C10J2300/0936—Coal fines for producing producer gas
-
- 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
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
Abstract
The invention relates to a high-pressure gasification and pyrolysis integrated device for pulverized coal, which comprises a gasification section, a quenching section, a pyrolysis section, a cooling separation section and a semicoke recirculation section which are sequentially connected to form a gasification furnace with a closed circulation structure; the gasification section comprises a gasification section shell, a gasification section refractory, a steam nozzle, a raw coal burner and an ash outlet; the chilling section comprises a pressure-bearing chilling section shell positioned on the outer side, a chilling section refractory material positioned in the chilling section shell and used for bearing high temperature, and at least two chilling gas nozzles used for cooling high-temperature gas; the pyrolysis section comprises a pyrolysis section shell, a pyrolysis section refractory, a first section raw coal burner, a pyrolysis section internal member and a second section hydrogen nozzle; the cooling separation section comprises a pressure-bearing shell, refractory materials of the cooling separation section are arranged in the pressure-bearing shell, the semicoke recycling section comprises a semicoke sending tank, and a semicoke conveying pipe is arranged on the semicoke sending tank, so that the treatment capacity is large, the tar yield is high, the light oil content is high, the device height is low, and the dust content of the tar is small.
Description
Technical field
The present invention relates to bed pulverized coal gasification technology field, the sub-prime for being related to coal is classified clean and effective comprehensive utilization technique, specifically
It is related to a kind of high-pressure gasified thermal decomposition integrated makeup of fine coal to put.
Background technology
Coal resources in China rich reserves, and oil, natural gas resource relative shortage, China's oil in 2010 it is external according to
Degree of depositing is up to 55%.In addition, 20% is there are about inside the oil that China consumes every year is used as industrial chemicals production chemical industry production
Product.Therefore, oil product, chemical products and coal gas are substituted using the coal resources production of reserves relative abundance, alleviates China's oil and enter
Mouth pressure and natural gas consumption pressure, tool are of great significance.And worldwide using lignite, jet coal as representative
Low-order coal occupies very big ratio again.According to measuring and calculating, whole world lignite oil in place is about 4,000,000,000,000 tons, and lignite guarantor has verified in China
It is 1311.42 hundred million tons to have reserves, accounts for the 13% of coal reserves.Chinese lignite resource is mainly distributed on Inner Mongolia Autonomous Region
East and Yunnan Province are domestic.Brown moisture in coal, ash content and oxygen content, oil content are higher, and phosphorus content, sulfur content are low, volatile matter one
As 45%~55%, no cohesiveness, heat endurance is poor, and chemical reaction is strong, the humic acid containing inequality, calorific value during burning
Low, easy-weathering spontaneous combustion during storage, unit energy cost of transportation is high, is unfavorable for long-distance transportation and storage.Based on lignite property
Particularity, its processing and utilization mode mainly have：Combustion power generation, gasification, liquefaction, pyrolysis, coking, produce chemical products humic acid
Deng.It is relatively low near coal-mine generating calorific value because lignite moisture is high, produce a large amount of powder when reducing the utilization rate of lignite, and burning
Dirt and CO, environment is seriously polluted, therefore lignite upgrading turns into the primary premise that lignite utilizes.Particularly to a large amount of in low-order coal
How fine coal realizes that comprehensive utilization more turns into insoluble problem.
Fixation of the technology that lignite upgrading mainly uses in the prior art using upright square stove, revolving bed and moving bed as representative
Bed, this technology has had certain application case (such as praising magnificent stove), but this kind of technology can only utilize more than 3-8mm block
Coal.And at present for the low-order coal of powdery, main method is including using pulverized coal friring as thermal source and using low pressure syn-gas as heat at present
Two methods of source.A certain amount of semicoke can be consumed using flue gas or by pulverized coal pyrolysis technology of the flue gas semicoke as thermal source, and
And the semicoke after being pyrolyzed must also be cooled to room temperature, this process can cause the ash content in semicoke to greatly increase.And closed with low pressure
Into the pyrolytic process that gas is thermal source, because the size of capacity of low pressure gasifying stove is limited, cause the thermal source of pyrolysis oven is limited can not increase
On a large scale, therefore the pyrolysis oven production capacity of this method is limited.
The U of Publication No. CN 203373318 Chinese utility model document discloses a kind of PC-FB pyrolysis system,
It includes fluidized bed pyrolysis stove, gas distributor, semicoke hopper, multi-cyclone, decontaminating separator, coke guidance tube, gas
Distributor is located in fluidized bed pyrolysis stove, and multi-cyclone is connected with gas distributor, semicoke hopper by coke guidance tube with
Gas distributor is connected, and decontaminating separator is connected with multi-cyclone.The PC-FB pyrolysis system utilizes High Temperature Gas
Thermal source of the sensible heat of body as fluidized bed pyrolysis, solve the problems, such as the utilization ratio of high-temperature gas sensible heat, while pulverized coal pyrolysis is divided
Level upgrading is converted into coal gas, semicoke and coal tar.The PC-FB pyrolysis system utilizes bottom by optimizing in fluid bed
Coal and oxygen generating unit divided combustion, are pyrolyzed using the sensible heat of flue gas, reduce high-temperature gas conveying problem, while pass through gas
Body directly contacts with fine coal and increases heat exchange efficiency；But because the patent employs the partially combusted method combustion process of fine coal
In can produce substantial amounts of lime-ash, and these lime-ash mix common discharge with semicoke, can greatly increase the ash content in semicoke
Content, secondly because the higher particle diameter that can cause coke breeze of ignition temperature increases, so as to increase the utilization difficulty of later stage semicoke；Finally
Because burning can produce substantial amounts of flue gas, this can substantially reduce the quality of pyrolysis gas.
Publication No. CN 106987281A Chinese invention patent document discloses pulverized coal pyrolysis gasification integrated reactor
With the method for processing fine coal.Pulverized coal pyrolysis gasification integrated reactor includes：Body of heater is pyrolyzed, more pyrolysis chambers are defined in it,
Multiple radiant tubes are provided with pyrolysis chamber, being pyrolyzed the top of body of heater has fine coal entrance, and the bottom for being pyrolyzed body of heater has semicoke
Outlet, being pyrolyzed on body of heater has syngas outlet, and being pyrolyzed the side wall of body of heater, there is the fuel inlet of connection radiant tube and flue gas to go out
Mouthful；Gasify body of heater, and gasification chamber is defined in it, has gasification agent inlet on the body of heater that gasifies, and the top for the body of heater that gasifies has partly
Burnt entrance, the bottom for the body of heater that gasifies have lime-ash outlet, and gasification furnace body is below pyrolysis body of heater, and semicoke entrance is with exporting phase
Even.The semicoke that can be obtained pulverized coal pyrolysis using pulverized coal pyrolysis gasification integrated reactor is converted into synthesis gas, and
The sensible heat of synthesis gas is made full use of, while solves the Utilizing question of semicoke.Pulverized coal pyrolysis gasification integrated reactor make use of
Pyrolysis oven and gasification furnace are coupled to have obtained integrated apparatus, can be made full use of the sensible heat of synthesis gas and be made full use of partly
It is burnt.But first, the device causes the heat transfer efficiency of device relatively low using the mode of indirectly heat, single stove treating capacity by
To certain limitation, fast pyrogenation can not be realized.Secondly, the device pyrolysis oven passes through itself weight in the top of gasification furnace, material
Power, which is realized to fall, enters gasification furnace, and therefore, the device can not handle the foam coal that particle diameter reaches tens micron levels, and this is also by rear
10mm Particle size requirements are confirmed in the patent requirements in face；Finally, two bodies of heater are arranged up and down can cause single unit system very
High (overall height is in 100m or so), builds for framework and ensure that installation security adds difficulty.
The content of the invention
Can realizing the efficient cascade utilization of low-order coal it is an object of the invention to provide one kind, output coal tar is gentle simultaneously
The fine coal high-pressure gasified thermal decomposition integrated makeup for changing gas is put, to solve in the presence of prior art with flue gas or added by flue gas
Hot semicoke can consume a certain amount of semicoke for the pulverized coal pyrolysis technology of thermal source, and the semicoke after pyrolysis must also be cooled to room
Temperature, this process can cause the ash content in semicoke to greatly increase, or the pyrolytic process using low pressure syn-gas as thermal source, due to low pressure
The size of capacity of gasification furnace is limited, causes the thermal source of pyrolysis oven is limited can not increase scale, causes what its pyrolysis oven production capacity was limited
Problem.
To achieve the above object, the present invention provides a kind of fine coal high pressure gas that can realize high pressure direct hydrogenation pyrolytic gasification
Change thermal decomposition integrated makeup to put, including be sequentially connected the gasification section of gasification furnace for forming closed cycle structure, Quench section, pyrolysis section,
Refrigerated separation section and semicoke recycling section；
The gasification section includes gasification piece housing, gasification section refractory matter, steam jet, raw coal burner and lime-ash outlet；
The gasification section refractory matter is arranged on the inside of the gasification piece housing, the steam jet, the raw coal burner and described
Lime-ash outlet is separately positioned on the gasification piece housing；
The Quench section includes the Quench piece housing of the pressure-bearing positioned at outside and the use inside the Quench piece housing
In the Quench section refractory matter for bearing high temperature, and at least two Quench gas jets for cooling down high-temperature gas；The Quench gas blowout
Mouth is arranged on the Quench piece housing；
The pyrolysis section includes pyrolysis piece housing, pyrolysis section refractory matter, one section of raw coal burner, pyrolysis section inner member and two sections
Hydrogen nozzle；The pyrolysis section refractory matter is arranged in the pyrolysis piece housing, in one section of raw coal burner, the pyrolysis section
Component and two sections of hydrogen nozzles are from top to bottom successively set on the pyrolysis piece housing；
Refrigerated separation section includes pressure-bearing shell, and refrigerated separation section refractory matter, the pressure-bearing are provided with the pressure-bearing shell
The top perforate of housing is connected with the inner cylinder of pyrolysis section bottom, is divided into two chambers by dividing plate inside the pressure-bearing shell,
The chamber top is provided with least two internal cyclones being connected with the inner cylinder of pyrolysis section；The gas vent of internal cyclone is arranged on
Described in top at chamber, discharged after gas collection by the gas vent of pyrolysis gas and synthesis gas；The dipleg of internal cyclone is worn
The dividing plate is crossed to stretch into the bed of material of chamber described in bottom；Cloth on the bed of material described in bottom as semicoke cooling in chamber
Provided with coil pipe or comb cooler, to be cooled down indirectly to semicoke by the cooling water in pipe, with according to semicoke discharge valve
It is required that semicoke is cooled, chamber described in bottom is connected with loosening gas by loosening gas entrance and loosening gas outlet；
The semicoke recycling section includes semicoke sending cans, and semicoke delivery pipe is provided with the semicoke sending cans, described
The top of semicoke sending cans is provided with semicoke entrance, and conveying gas entrance, the semicoke are provided with the middle part of the semicoke sending cans
The bottom of sending cans is provided with the emergent discharge port of semicoke.
Alternatively, the gasification section of the gasification of high-pressure pulverized coal thermal decomposition integrated is used with pyrolysis section and is arranged in juxtaposition, gasification section
Using air upflow bed, pyrolysis section uses descending air flow bed operative combination.
Alternatively, the Quench section is arranged at the top position of the gasification section.
Alternatively, the pyrolysis section is arranged in juxtaposition at the right positions of the Quench section with gasification section.
Alternatively, the refrigerated separation section is arranged on the lower position of the pyrolysis section.
Alternatively, the semicoke recycling section is arranged on the lower position of the refrigerated separation section.
Alternatively, internal cyclone is arranged to refractory metal or ceramic material.
Alternatively, coil pipe or the comb cooler is cooled down indirectly by the cooling water in pipe to semicoke, by semicoke
It is cooled to DEG C.
Alternatively, the steam jet and the raw coal burner are from top to bottom successively set on the gasification piece housing
Bottom.
Alternatively, the lime-ash outlet is arranged on the bottom of the gasification piece housing.
The invention has the advantages that：
The fine coal high-pressure gasified thermal decomposition integrated makeup of the present invention is put, can solve the problem that in the presence of prior art with flue gas or
A certain amount of semicoke can be consumed for the pulverized coal pyrolysis technology of thermal source by flue gas semicoke, and the semicoke after pyrolysis must also
Room temperature is cooled to, this process can cause the ash content in semicoke to greatly increase, or the pyrolytic process using low pressure syn-gas as thermal source,
Because the size of capacity of low pressure gasifying stove is limited, causes the thermal source of pyrolysis oven is limited can not increase scale, cause its pyrolysis oven to produce
Can be limited the problem of；It realizes low-order coal by the way that the gasification of air upflow bed and the pyrolysis of descending air flow bed are carried out into organic assembling
High-voltage high-speed is pyrolyzed and gasification integration, obtains the advantages that single stove treating capacity is high, and tar yield is high, and light oil constituents is more, simultaneously
The big oily dirt separation of product gas dustiness is significantly reduced by adding the part such as gas solid separation and semicoke cooling in device interior
The difficulty of difficult and semicoke conveying, the last present apparatus are combined by the unique mode of operation of pyrolysis oven and gasification furnace so that pyrolysis
Stove and gasification furnace can be run side by side, greatly shorten the fed distance of high-temperature gas and semicoke, improve the safety of equipment
Property, and reduce the height of integral device.
Brief description of the drawings
Fig. 1 is the structural representation that the high-pressure gasified thermal decomposition integrated makeup of fine coal of the present invention is put.
Fig. 2 is the structural representation for the gasification section that the high-pressure gasified thermal decomposition integrated makeup of fine coal of the present invention is put.
Fig. 3 is the structural representation for the Quench section that the high-pressure gasified thermal decomposition integrated makeup of fine coal of the present invention is put.
Fig. 4 is the structural representation for the pyrolysis section that the high-pressure gasified thermal decomposition integrated makeup of fine coal of the present invention is put.
Fig. 5 is the structural representation for the refrigerated separation section that the high-pressure gasified thermal decomposition integrated makeup of fine coal of the present invention is put.
Fig. 6 is the structural representation for the semicoke recycling section that the high-pressure gasified thermal decomposition integrated makeup of fine coal of the present invention is put.
Fig. 7 is the operation principle schematic diagram that the high-pressure gasified thermal decomposition integrated makeup of fine coal of the present invention is put.
In figure, 1 is gasification section, and 2 be Quench section, and 3 be pyrolysis section, and 4 be refrigerated separation section, and 5 be that semicoke recycles section；1-1
For the piece housing that gasifies, 1-2 is gasification section refractory matter, and 1-3 is steam jet.1-4 is raw coal burner, and 1-5 exports for lime-ash；2-
1 is Quench piece housing, and 2-2 is Quench section refractory matter, and 2-3 is Quench gas jets；3-1 is pyrolysis piece housing, and 3-2 is that pyrolysis section is resistance to
Fire material, 3-3 is one section of raw coal burner, and 3-4 is pyrolysis section inner member, and 3-5 is two sections of hydrogen nozzles；4-1 is inner cylinder, and 4-2 is to hold
Pressure shell body, 4-3 are refrigerated separation section refractory matter, and 4-4 is internal cyclone, and 4-5 is dividing plate, and 4-6 is coil pipe or comb cooler, 4-7
To loosen gas entrance, 4-8 be semicoke discharge valve, and 4-9 exports to loosen gas, and 4-10 is gas vent, and 5-1 is semicoke entrance, 5-2
For semicoke sending cans, 5-3 is conveying gas entrance, and 5-4 is the emergent discharge port of semicoke, and 5-5 is semicoke delivery pipe.
Embodiment
Following examples are used to illustrate the present invention, but are not limited to the scope of the present invention.
Embodiment
A kind of high-pressure gasified thermal decomposition integrated makeup of fine coal is put, and referring to Fig. 1, including is sequentially connected and is formed closed cycle structure
Gasification section 1, Quench section 2, pyrolysis section 3, refrigerated separation section 4 and the semicoke recycling section 5 of gasification furnace；
Referring to Fig. 2, the gasification section 1 includes gasification piece housing 1-1, gasification section refractory matter 1-2, steam jet 1-3, original
Coal burner 1-4 and lime-ash outlet 1-5；The gasification section refractory matter 1-2 is arranged on the inside of the gasification piece housing 1-1, described
Steam jet 1-3, the raw coal burner 1-4 and lime-ash outlet 1-5 are separately positioned on the gasification piece housing 1-1；
Referring to Fig. 3, the Quench section 2 includes the Quench piece housing 2-1 of the pressure-bearing positioned at outside and positioned at the Quench section
The Quench section refractory matter 2-2 for being used to bear high temperature inside housing 2-1, and at least two Quench gas for cooling down high-temperature gas
Nozzle 2-3；The Quench gas jets 2-3 is arranged on the Quench piece housing 2-1；
Referring to Fig. 4, the pyrolysis section 3 include pyrolysis piece housing 3-1, pyrolysis section refractory matter 3-2, one section of raw coal burner 3-3,
Pyrolysis section inner member 3-4 and two sections of hydrogen nozzle 3-5；The pyrolysis section refractory matter 3-2 is arranged on the pyrolysis piece housing 3-1
Interior, one section of raw coal burner 3-3, the pyrolysis section inner member 3-4 and two sections of hydrogen nozzles 3-5 are from top to bottom set successively
Put on the pyrolysis piece housing 3-1；
Referring to Fig. 5, refrigerated separation section 4 includes being provided with refrigerated separation section in pressure-bearing shell 4-2, the pressure-bearing shell 4-2
Refractory matter 4-3, the pressure-bearing shell 4-2 top perforate are connected with the inner cylinder 4-1 of the bottom of pyrolysis section 3, the pressure-bearing shell
It is two chambers to be divided inside 4-2 by dividing plate 4-5, and the chamber top is provided with least two inner cylinder 4-1 phases with pyrolysis section 3
The internal cyclone 4-4 of connection；Internal cyclone 4-4 gas vent is arranged on described in top at chamber, passes through pyrolysis gas after gas collection
Discharged with the gas vent 4-10 of synthesis gas；Internal cyclone 4-4 dipleg stretches into chamber described in bottom through the dividing plate 4-5
The bed of material in；Coil pipe or comb cooler 4-6 are laid with the bed of material described in bottom as semicoke cooling in chamber, with
Semicoke is cooled down indirectly by the cooling water in pipe, so that semicoke to be cooled according to semicoke discharge valve 4-8 requirement, bottom institute
State chamber and be connected with loosening gas by loosening gas entrance 4-7 and loosening gas outlet 4-9；
Referring to Fig. 6, the semicoke recycling section 5 includes being provided with semicoke sending cans 5-2, the semicoke sending cans 5-2
Semicoke delivery pipe 5-5, the semicoke sending cans 5-2 top are provided with semicoke entrance 5-1, the semicoke sending cans 5-2
The bottom that portion is provided with conveying gas entrance 5-3, the semicoke sending cans 5-2 is provided with the emergent discharge port 5-4 of semicoke.
The high-pressure gasified thermal decomposition integrated makeup of fine coal of the present embodiment is put, and gasification piece housing 1-1 is mainly used in bearing pressure, and
There is certain thickness gasification section refractory material 1-2 to be used for the high temperature and air flow bed for bearing gasification reaction inside gasification section 1
Quickly wash away.The Quench piece housing 2-1 of Quench section 2 is located at outside and is used for pressure-bearing, Quench section refractory matter 2-2 it is internally positioned and
For bearing high temperature, Quench gas jets 2-3 is used for cooling down high-temperature gas.It is pyrolyzed piece housing 3-1 and pyrolysis section refractory matter 3-2 work
To be washed away with the high temperature and fine coal of respectively pressure-bearing and tolerance pyrolysis, one section of raw coal burner 3-3 effect mainly sprays into raw coal, with
High-temperature synthesis gas mixing is pyrolyzed, and pyrolysis section inner member 3-4 effect mainly lifts mixing efficiency, improves heat-transfer effect,
Two sections of hydrogen nozzle 3-5 effect is to improve hydrogen partial pressure, realizes that high-temperature hydrogenation is pyrolyzed, improves light oil constituents content.Pyrolysis section 3
The refrigerated separation section 4 and semicoke recycling section 5 of lower end connection, its main function is to realize gas and semicoke at high temperature and pressure
The pre-separation of fine coal and the cooling of semicoke.Internal cyclone 4-4 mainly plays gas solid separation, because whirlwind inside and outside differential pressure is little,
Therefore, internal cyclone 4-4 is not subject to pressure substantially, and refractory metal can be selected or ceramics are used as material.The bottom of refrigerated separation section 4
Chamber main function is the cooling of semicoke, and the bed of material in lower chamber is furnished with coil pipe or comb cooler 4-6, by pipe
Cooling water semicoke is cooled down indirectly, semicoke is cooled to 300 DEG C or so to meet semicoke discharge valve 4-8 requirement,
Simultaneously in order to improve the heat transfer coefficient of semicoke and mobility, 4-9 is exported by loosening gas entrance 4-7 and loosening gas in lower chamber
It is connected with loosening gas.
The high-pressure gasified thermal decomposition integrated makeup of fine coal of the present embodiment is put, and referring to Fig. 7, raw coal and oxygen pass through the side of gasification section 1
Multiple raw coal burner 1-4 of wall are entered, and high-temp combustion occurs in gasification section 1, so as to provide thermal source for device, then unreacted
Raw coal and semicoke from semicoke delivery pipe and vapor gasification reaction occurs, generation high-temperature synthesis gas main component is CO
And H2, W-response are carried out under the conditions of pressure 4MPa, 1100-1400 DEG C of temperature, the slag produced in gasification reaction is with liquid shape
Formula is discharged downwards from outlet at bottom, and 1300 DEG C or so high-temperature synthesis gas are upwardly into Quench section 2.High temperature into Quench section 2 closes
Into gas 800 DEG C or so are progressively cooled to by being mixed with 200 DEG C or so of the Quench gas from multiple Quench gas jets 2-3
By entering pyrolysis section after top elbows.Pass through in 800 DEG C or so of synthesis gas of pyrolysis section 3 with one section of raw coal nozzle 3-3's
Raw coal hybrid cooling occurs fast pyrogenation to 500 DEG C or so and reacted, and pyrolytic reaction is the descending cocurrent air flow bed reaction of gas-solid, is reacted
Residence time is about 4s, while is passed through high-temperature hydrogen in pyrolysis section 3 and hydrogenation reaction occurs, and carries out tar lighting.It is reacted
Gas and semicoke carry out gas solid separation by the multiple internal cyclone 4-4 being connected with the lower end of pyrolysis section 3, and gas passes through internal cyclone 4-4
The gas vent on top is discharged after being pooled to the upper-part centralized air chamber of refrigerated separation section 4 from product gas outlet, carries out further gas-solid point
Clean synthesis gas and tar are obtained from tar cooling.The semicoke isolated is discharged into refrigerated separation by internal cyclone 4-4 dipleg
4 bottom dust storage chambers of section, then cooled down by the way that indirect heat exchange occurs with the coil pipe or comb cooler 4-6 for being embedded to feed bin, it is cold
But the semicoke to about 300 DEG C is discharged into semicoke sending cans by semicoke discharge valve 4-8, and being conveyed into gasification furnace by conveying gas is used as gas
Change feed coal and carry out gasification reaction.
The high-pressure gasified thermal decomposition integrated makeup of the fine coal of the present embodiment is put, by will dry coal powder airflow bed up gasification furnace and under
Promoting the circulation of qi fluidized bed fast pyrogenation is combined, and realizes the pyrolysis of fine coal high-voltage high-speed and the high-pressure gasified coupling integrated Poly-generation of semicoke.
The device has the characteristics that fine coal treating capacity is big, operation is mature and stable, hydrogen-rich fast pyrogenation, tar yield is high, light oil content is high,
Gasification reaction generation HTHP synthesis gas, and the heat of this strand of synthesis gas can be particularly carried out using high-temperature semi-coke caused by pyrolysis
Thermal source of the and can as low-order coal pyrolytic reaction is measured, energy directly rationally utilizes, and consumption is low.The present apparatus with upright square stove, rotation
Rotated bed and moving bed are compared for the fixed bed of representative and with gas with the fluidized bed pyrolysis of solid thermal carriers, and it is first by by gas
Change stove and pyrolysis oven has carried out organic assembling, it is up by gasification furnace synthesis gas, the descending scheme of pyrolysis oven raw coal, realize to powder
The processing of coal and scale is big；Secondly, present apparatus product gas only has 5s or so in the residence time of pyrolysis section 3, with containing a large amount of hydrogen
The reaction of synthesis gas direct contact heat transfer, and synthesis pressure is higher (4MPa), realize hydrogenation fast pyrogenation, therefore the present apparatus
Tar yield significantly improves, and light oil proportion greatly increases；Again, the present apparatus combines sufficiently profit by gasification furnace and pyrolysis oven
With gasification synthesis gas and the sensible heat of pyrolysis char, while the combination of two sections of different traffic directions, substantially reduce high-temperature semi-coke
With the fed distance of high-temperature synthesis gas and overall device highly, it is achieved thereby that integrated apparatus；Finally, in the present apparatus
The devices such as internal cyclone 4-4, built-in coil pipe or comb cooler 4-6 are additionally provided with, so as to greatly reduce out the gas of the present apparatus
Dustiness and semicoke temperature, be follow-up phase gas in tar separation and semicoke conveying reduce difficulty.Present apparatus pin
The fine coal high pressure pyrolytic gasification one using the gasification of air upflow bed and the pyrolysis of descending pyrolysis oven proposed to the deficiency of current techniques
Body makeup is put, and can reach requirement of the processing particle diameter less than 50um or so fine coal, device tool fully profit by such scheme
With high-temperature synthesis gas and pyrolysis char sensible heat, unit capacity is big, and tar yield is high, and light oil content is high, and device is highly low, tar
The advantages that content amount is small, and integrated multi-connection production designs.
In another specific embodiment, the gasification section 1 is arranged on the high-pressure gasified thermal decomposition integrated makeup of the fine coal and put
Left bottom opening position.
In another specific embodiment, gasification section 1 and the pyrolysis section 3 of the gasification of high-pressure pulverized coal thermal decomposition integrated use
It is arranged in juxtaposition, gasification section 1 uses air upflow bed, and pyrolysis section 3 uses descending air flow bed operative combination；It is effectively reducing equipment
The fed distance of high-temperature gasification gas and high-temperature semi-coke is substantially reduced while height, reduces the manufacture of high-temperature pipe and valve
Difficulty.
In another specific embodiment, the Quench section 2 is arranged at the top position of the gasification section 1.
In another specific embodiment, the pyrolysis section 3 at the right positions of the Quench section 2 with gasification section 1 simultaneously
Row arrangement.
In another specific embodiment, the refrigerated separation section 4 is arranged on the lower position of the pyrolysis section 3, and
Refrigerated separation section, which realizes the separation of semicoke, dedusting, is cooled in same shell section completes, and avoids the conveying of HTHP semicoke
Problem, while reduce the investment of housing.
In another specific embodiment, the semicoke recycling section 5 is arranged on the lower position of the refrigerated separation section 4
Place.
In another specific embodiment, internal cyclone 4-4 is arranged to refractory metal or ceramic material.
In another specific embodiment, coil pipe or comb the cooler 4-6 is entered by the cooling water in pipe to semicoke
Cooling is in the ranks connect, semicoke is cooled to 300 DEG C.
In another specific embodiment, the steam jet 1-3 and the raw coal burner 1-4 are from top to bottom set successively
Put in the bottom of the gasification piece housing 1-1.
In another specific embodiment, the lime-ash outlet 1-5 is arranged on the bottom of the gasification piece housing 1-1.
The high-pressure gasified thermal decomposition integrated makeup of fine coal of the present invention is put, in its another embodiment：Using a diameter of 4
Rice, the integrated apparatus that a height of 16 meters of gasification furnace and a diameter of 2 meters a height of 20 meters of pyrolysis sections 3 are arranged side by side 4MPa,
28t/h semicoke and 12t/h raw coal are gasified at 1300 DEG C, 90000Nm can be obtained3/ h high-temperature synthesis gas, lead to
Cross and 90000Nm3/ h 300 DEG C of low temperature synthesis gas, which carry out Quench mixing, can obtain 180000Nm3/ h 800 DEG C of synthesis gas.Should
Synthesis gas and 40t/h drying brown coal are pyrolyzed when being blended in 500 DEG C, and the semicoke that can obtain 28t/h enters gasification furnace, together
When obtain 7500Nm3/ h pyrolysis gas, 2.4t/h tar.Whole device uses the dry pulverized coal of 50 μm or so of mean particle diameter
Charging, handle lignite.
Although above with general explanation and specific embodiment, the present invention is described in detail, at this
On the basis of invention, it can be made some modifications or improvements, this will be apparent to those skilled in the art.Therefore,
These modifications or improvements without departing from theon the basis of the spirit of the present invention, belong to the scope of protection of present invention.
Claims (10)
1. a kind of high-pressure gasified thermal decomposition integrated makeup of fine coal is put, including is sequentially connected the gas for the gasification furnace for forming closed cycle structure
Change section (1), Quench section (2), pyrolysis section (3), refrigerated separation section (4) and semicoke recycling section (5)；Characterized in that,
The gasification section (1) includes gasification piece housing (1-1), gasification section refractory matter (1-2), steam jet (1-3), raw coal and burnt
Mouth (1-4) and lime-ash outlet (1-5)；The gasification section refractory matter (1-2) is arranged on the inside of the gasification piece housing (1-1),
The steam jet (1-3), the raw coal burner (1-4) and lime-ash outlet (1-5) are separately positioned on the gasification section
On housing (1-1)；
The Quench section (2) includes the Quench piece housing (2-1) of the pressure-bearing positioned at outside and positioned at the Quench piece housing (2-1)
The internal Quench section refractory matter (2-2) for being used to bear high temperature, and at least two Quench gas jets for cooling down high-temperature gas
(2-3)；The Quench gas jets (2-3) are arranged on the Quench piece housing (2-1)；
The pyrolysis section (3) includes pyrolysis piece housing (3-1), pyrolysis section refractory matter (3-2), one section of raw coal burner (3-3), pyrolysis
Section inner member (3-4) and two sections of hydrogen nozzles (3-5)；The pyrolysis section refractory matter (3-2) is arranged on the pyrolysis piece housing (3-
1) in, one section of raw coal burner (3-3), the pyrolysis section inner member (3-4) and two sections of hydrogen nozzles (3-5) are by up to
Under be successively set on pyrolysis piece housing (3-1)；
Refrigerated separation section (4) includes pressure-bearing shell (4-2), and refrigerated separation section refractory matter is provided with the pressure-bearing shell (4-2)
(4-3), the top perforate of the pressure-bearing shell (4-2) are connected with the inner cylinder (4-1) of pyrolysis section (3) bottom, the pressure-bearing shell
Body (4-2) is internal to be divided into two chambers by dividing plate (4-5), and the chamber top is provided with least two and pyrolysis section (3)
The internal cyclone (4-4) that inner cylinder (4-1) is connected；The gas vent of internal cyclone (4-4) is arranged on described in top at chamber, and gas converges
Discharged after collection by the gas vent (4-10) of pyrolysis gas and synthesis gas；The dipleg of internal cyclone (4-4) passes through the dividing plate
(4-5) is stretched into the bed of material of chamber described in bottom；It is laid with the bed of material described in bottom as semicoke cooling in chamber
Coil pipe or comb cooler (4-6), to be cooled down indirectly to semicoke by the cooling water in pipe, with according to semicoke discharge valve
The requirement of (4-8) cools semicoke, and chamber described in bottom is connected with pine by loosening gas entrance (4-7) and loosening gas outlet (4-9)
Take offence；
The semicoke recycling section (5) includes semicoke sending cans (5-2), and it is defeated to be provided with semicoke on the semicoke sending cans (5-2)
Pipe (5-5) is sent, the top of the semicoke sending cans (5-2) is provided with semicoke entrance (5-1), the semicoke sending cans (5-2)
Middle part is provided with conveying gas entrance (5-3), and the bottom of the semicoke sending cans (5-2) is provided with the emergent discharge port (5-4) of semicoke.
2. the high-pressure gasified thermal decomposition integrated makeup of fine coal as claimed in claim 1 is put, it is characterised in that the gasification of high-pressure pulverized coal
For the gasification section (1) of thermal decomposition integrated with pyrolysis section (3) using being arranged in juxtaposition, gasification section (1) uses air upflow bed, pyrolysis section
(3) descending air flow bed operative combination is used.
3. the high-pressure gasified thermal decomposition integrated makeup of fine coal as claimed in claim 2 is put, it is characterised in that the Quench section (2) sets
Put at the top position of the gasification section (1).
4. the high-pressure gasified thermal decomposition integrated makeup of fine coal as claimed in claim 3 is put, it is characterised in that the pyrolysis section (3) exists
It is arranged in juxtaposition at the right positions of the Quench section (2) with gasification section (1).
5. the high-pressure gasified thermal decomposition integrated makeup of fine coal as claimed in claim 4 is put, it is characterised in that the refrigerated separation section
(4) it is arranged on the lower position of the pyrolysis section (3).
6. the high-pressure gasified thermal decomposition integrated makeup of fine coal as claimed in claim 5 is put, it is characterised in that the semicoke recycles section
(5) it is arranged on the lower position of the refrigerated separation section (4).
7. the high-pressure gasified thermal decomposition integrated makeup of fine coal as claimed in claim 6 is put, it is characterised in that internal cyclone (4-4) is set
For refractory metal or ceramic material.
8. the high-pressure gasified thermal decomposition integrated makeup of fine coal as claimed in claim 7 is put, it is characterised in that the coil pipe or comb are cold
But device (4-6) is cooled down indirectly by the cooling water in pipe to semicoke, and semicoke is cooled into 300 DEG C.
9. the high-pressure gasified thermal decomposition integrated makeup of fine coal as claimed in claim 8 is put, it is characterised in that the steam jet
(1-3) and the raw coal burner (1-4) are from top to bottom successively set on the bottom of the gasification piece housing (1-1).
10. the high-pressure gasified thermal decomposition integrated makeup of fine coal as claimed in claim 9 is put, it is characterised in that the lime-ash exports (1-
5) it is arranged on the bottom of the gasification piece housing (1-1).
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| CN110591745A (en) * | 2019-10-14 | 2019-12-20 | 西北大学 | Pyrolysis-gasification integrated device and process |
| CN112080322A (en) * | 2020-09-16 | 2020-12-15 | 新奥科技发展有限公司 | Pulverized coal grading gasification system and method |
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| CN110591745A (en) * | 2019-10-14 | 2019-12-20 | 西北大学 | Pyrolysis-gasification integrated device and process |
| CN110591745B (en) * | 2019-10-14 | 2024-04-26 | 西北大学 | Pyrolysis-gasification integrated device and process |
| CN112080322A (en) * | 2020-09-16 | 2020-12-15 | 新奥科技发展有限公司 | Pulverized coal grading gasification system and method |
| CN115584285A (en) * | 2022-12-05 | 2023-01-10 | 浙江百能科技有限公司 | Cyclone gasification furnace and pyrolysis gasification system and process based on cyclone gasification furnace |
| CN115584285B (en) * | 2022-12-05 | 2023-04-11 | 浙江百能科技有限公司 | Pyrolysis gasification system and process based on cyclone furnace |
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