CN104776426A - Device and method for synchronous power generation and multi-generation of coal gas and powdered coal - Google Patents
Device and method for synchronous power generation and multi-generation of coal gas and powdered coal Download PDFInfo
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- 239000003245 coal Substances 0.000 title claims abstract description 87
- 239000003034 coal gas Substances 0.000 title claims abstract description 42
- 238000000034 method Methods 0.000 title claims abstract description 13
- 238000010248 power generation Methods 0.000 title abstract 2
- 230000001360 synchronised effect Effects 0.000 title abstract 2
- 239000007789 gas Substances 0.000 claims abstract description 66
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 56
- 239000003546 flue gas Substances 0.000 claims abstract description 56
- 238000000197 pyrolysis Methods 0.000 claims abstract description 29
- 238000006243 chemical reaction Methods 0.000 claims abstract description 27
- 238000002485 combustion reaction Methods 0.000 claims abstract description 22
- 238000002156 mixing Methods 0.000 claims abstract description 22
- 239000002817 coal dust Substances 0.000 claims abstract description 21
- 238000000926 separation method Methods 0.000 claims abstract description 21
- 239000000446 fuel Substances 0.000 claims abstract description 19
- 230000005611 electricity Effects 0.000 claims abstract description 17
- 238000012545 processing Methods 0.000 claims abstract description 13
- 239000002283 diesel fuel Substances 0.000 claims abstract description 12
- 239000000843 powder Substances 0.000 claims abstract description 6
- 239000003502 gasoline Substances 0.000 claims abstract description 4
- 239000003077 lignite Substances 0.000 claims abstract description 4
- 239000011269 tar Substances 0.000 claims description 76
- 230000008878 coupling Effects 0.000 claims description 25
- 238000010168 coupling process Methods 0.000 claims description 25
- 238000005859 coupling reaction Methods 0.000 claims description 25
- 238000007670 refining Methods 0.000 claims description 15
- 239000000203 mixture Substances 0.000 claims description 14
- 238000004519 manufacturing process Methods 0.000 claims description 13
- 239000002994 raw material Substances 0.000 claims description 13
- 238000010612 desalination reaction Methods 0.000 claims description 12
- 230000005855 radiation Effects 0.000 claims description 12
- 238000012546 transfer Methods 0.000 claims description 12
- 239000002641 tar oil Substances 0.000 claims description 11
- 238000010079 rubber tapping Methods 0.000 claims description 10
- 238000003860 storage Methods 0.000 claims description 8
- 238000005984 hydrogenation reaction Methods 0.000 claims description 7
- 239000002245 particle Substances 0.000 claims description 7
- 239000000779 smoke Substances 0.000 claims description 7
- 230000001502 supplementing effect Effects 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 6
- 230000003009 desulfurizing effect Effects 0.000 claims description 5
- 239000003517 fume Substances 0.000 claims description 5
- 238000000746 purification Methods 0.000 claims description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 239000007788 liquid Substances 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 238000003303 reheating Methods 0.000 claims description 4
- 238000010521 absorption reaction Methods 0.000 claims description 3
- 239000011280 coal tar Substances 0.000 claims description 3
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 238000000605 extraction Methods 0.000 claims description 3
- 230000003134 recirculating effect Effects 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 239000000295 fuel oil Substances 0.000 claims description 2
- 238000011084 recovery Methods 0.000 claims description 2
- 229920006395 saturated elastomer Polymers 0.000 claims description 2
- 238000002309 gasification Methods 0.000 claims 1
- 238000005516 engineering process Methods 0.000 abstract description 7
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 abstract description 2
- 229910052785 arsenic Inorganic materials 0.000 abstract description 2
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 abstract description 2
- 229910052793 cadmium Inorganic materials 0.000 abstract description 2
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 abstract description 2
- 229910052804 chromium Inorganic materials 0.000 abstract description 2
- 239000011651 chromium Substances 0.000 abstract description 2
- 239000002737 fuel gas Substances 0.000 abstract description 2
- 229910001385 heavy metal Inorganic materials 0.000 abstract description 2
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 abstract description 2
- 229910052753 mercury Inorganic materials 0.000 abstract description 2
- 238000002360 preparation method Methods 0.000 abstract description 2
- 239000000470 constituent Substances 0.000 abstract 1
- 238000010494 dissociation reaction Methods 0.000 abstract 1
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- 239000012530 fluid Substances 0.000 abstract 1
- 230000001131 transforming effect Effects 0.000 abstract 1
- 239000000047 product Substances 0.000 description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 230000008901 benefit Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 239000000571 coke Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 238000005979 thermal decomposition reaction Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 238000010795 Steam Flooding Methods 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000002802 bituminous coal Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910017464 nitrogen compound Inorganic materials 0.000 description 1
- 150000002830 nitrogen compounds Chemical class 0.000 description 1
- -1 nuclear energy Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- 238000007348 radical reaction Methods 0.000 description 1
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- 238000012216 screening Methods 0.000 description 1
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- 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
- Y02E20/14—Combined heat and power generation [CHP]
-
- 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 invention relates to a device and a method for synchronous power generation and multi-generation of coal gas and powdered coal. High-volatile constituent faulty coal lignite, jet coal, non-caking coal, weakly caking coal, bottle coal are taken as feed coal, and enter a gasification-thermal dissociation coupled reactor by pressurizing a feeder so as to be subjected to high-efficiency and rapid pyrolysis reaction. the tar recovered from crude gas is pyrolyzed, the pyrolyzed tar is purified, then the purified tar is subjected to deep processing and transforming, finally, the tar is transformed into clean fuels such as liquefied gas, gasoline and diesel oil, the coal gas and bunker coal powder obtained by separation are subjected to blending combustion in a pulverized fuel boiler or a circulating fluid bed boiler, and thus steam is generated to drive a steam turbine so as to generate electricity. According to the invention, the preparation of coal-based clean fuels and fuel gas electricity generation technology are highly integrated; the coal gas and the coal dust are subjected to blending combustion in the boiler, so that the quantity of flue gas is deeply reduced; the concentration of PM2.5 and PM10 in flue gas is extremely low, the light-concentration emission of SO2, NOX, and heavy metals such as lead, chromium, cadmium, arsenic, mercury is realized, and the multi-generation of coal base energy source and gradient high efficiency utilization are realized.
Description
Technical field
The present invention relates to high-efficiency cleaning trans-utilization and the coal poly-generation technical field of coal, be specifically related to a kind of coal extract coal tar and produce clean fuel, by-product raw gas enter boiler of power plant and fine coal according to special ratios carry out mixing the coal gas of burning and fine coal work in coordination with generate electricity, multi-joint-production apparatus and method.
Background technology
According to the world energy sources statistical yearbooks in 2013 that BP company announces, within 2013, world's primary energy structure of consumer demand Crude Oil, natural gas, coal, nuclear energy, water power, regenerative resource mean ratio are 32.9:23.7:30.1:4.4:6.7:2.2, and the corresponding ratio of China is then 17.8:5.1:67.5:0.9:7.2:1.5.The energy consumption structure of China based on coal is the first cause directly causing China's environmental pollution, is also to cause the overall efficiency of energy utilization of China low, one of major reason that economic benefit is not good enough.In recent years, although the proportion of coal in China shared by whole primary energy consumption structure is declining year by year, but the energy consumption structure of China's main body changes not quite substantially, and coal remains the major consumers energy of China, and the status of its main body consuming energy can not be changed in nearly 50 years.Therefore, need to improve coal utilization efficiency by some measures, such as promote that coal deep processing, decreasing pollution thing discharge, promote clean coal technology etc., this is also promote the healthy and stable development of coal industry, improves the inevitable approach of China's Energy situation.
The NOx generated in coal combustion process has three kinds of modes: 1. thermal NO x, and it is that nitrogen in air is at high temperature oxidized and the NOx generated; 2. fuel type NOx, it is that the nitrogen compound contained in fuel carries out thermal decomposition in combustion, is then oxidized and the NOx generated; 3. Quick-type, the NOx that hydrocarbon radical reaction when it is burning in air in nitrogen and fuel generates.Under common ignition temperature, in the NOx that coal combustion generates, NO accounts for more than 90%, NO
2account for 5% ~ 10%.
Wherein thermal NO
xgeneration mainly more than 1400 DEG C time, the nitrogen in air at high temperature, thermal NO
xcan 20% be reached, wherein fuel type NO
xaccount for NO
x75% ~ 90% of total amount.As the important component part of denitration technology, by its know-why, two large classes can be divided into: the first kind reduces ignition temperature in boiler to reduce thermal NO
xgeneration; Equations of The Second Kind is that the reproducibility atmosphere in construction coal powder ignition region is to reduce fuel type NO
xgeneration.
Existing pulverized-coal fired boiler or fluidized-bed combustion boiler are mixed and burnt electricity generation system is carry out mixing burning with the raw coke oven gas of the blast furnace gas of steel mill, coke-stove gas or coke-oven plant and coal substantially, reduce burner hearth pulverized coal friring temperature by mixing burning system, form combustion zone reducing atmosphere, suppress fuel type and thermal NO to the full extent
xgrowing amount.But coal-fired power generator set, coal-based clean liquid fuel production technology all do not combine by existing burning system of mixing, really do not realize the step efficiency utilization of coal-based energy multi-connection product and coal resources.
Summary of the invention
The object of the present invention is to provide one to realize coal resources are efficient, step, comprehensive utilization, thus coal-fired power generator set, coal-based clean liquid fuel production technology are combined, realize coal-based energy multi-connection produce and coal gas and the fine coal of step efficiency utilization of coal resources work in coordination with generate electricity, multi-joint-production apparatus and method.
For achieving the above object, coal gas of the present invention and fine coal are worked in coordination with and are generated electricity, multi-joint-production apparatus comprises coal dust feed arrangement and gasification-pyrolysis coupling reactor of being connected with coal dust feed arrangement and boiler, the raw gas containing tar and ash content that gasification-pyrolysis coupling reactor exports and dedusting, separator is connected, by dedusting, tar in the raw gas that separator reclaims is sent into follow-up tar oil treatment device and is obtained naphtha and diesel oil, containing the raw gas of tar and ash content through dedusting, be divided into two branch roads to enter in boiler after separator to burn, the coal gas of a branch road is entered in boiler by the burner nozzle on boiler furnace top and carries out blending burning with bunker coal, the coal gas of another branch road enters boiler by the burner nozzle of boiler heat convection section, with the preheated air entering boiler heat convection section through supplementing combustion air nozzle, second-time burning is carried out in the Gas phase Smoke mixing of flake hearth-tapping after radiation heat transfer, and with in boiler cross heat exchanger, heat exchanger again, economizer, air preheater carries out heat convection, the superheated steam that boiler overheating heat exchanger and reheating heat exchanger produce and reheated steam are respectively by superheated steam high pressure turbine, reheated steam intermediate pressure turbine drives generating set generating, the flue gas that boiler bottom exhanst gas outlet is discharged sends into follow-up flue gas processing device,
Cold air divides and is also divided into two branch roads after boiler air preheater preheating, one tunnel enters boiler furnace through boiler bottom preheated air entrance, another road through supplementing combustion air nozzle and the flue gas of flake hearth-tapping after radiation heat transfer, enter the coal gas of boiler through the burner nozzle of heat convection section and mix mutually and carry out second-time burning.
Described dedusting, separator comprises the elementary deduster be connected successively, degree of depth deduster, oil-gas knockout tower and degree of depth oil-gas knockout tower, wherein elementary deduster entrance is connected with the outlet of gasification-pyrolysis coupling reactor, the outlet of degree of depth oil-gas knockout tower divide two-way respectively with the burner nozzle on boiler furnace top, the burner nozzle of boiler heat convection section is connected, elementary deduster is connected with gasification-pyrolysis coupling reactor by pipeline with the outlet of degree of depth deduster lower end, oil-gas knockout tower is connected with follow-up tar oil treatment device by the road with the lower end outlet of degree of depth oil-gas knockout tower.
Described gasification-pyrolysis coupling reactor is the gasification-pyrolysis integrated recirculating fluidized bed pyrolytic reaction device using the solid circle particle of circulating ratio scope 5 ~ 100 as heat carrier.
Described boiler is coal-powder boiler or the CFBB of coal-burning power plant
It is the super critical boiler of 2020t/h that described boiler adopts nominal output to be the subcritical boiler of 35 ~ 1025t/h or nominal output, regulates exerting oneself of boiler by the ratio adjusted within the scope of 0% ~ 70wt% shared by blending gas.
Described follow-up flue gas processing device comprises the gas wash tower, fume desulfurizing tower and the denitrating flue gas tower that are connected successively, flue gas after udst separation is divided into two branch roads after air-introduced machine pressurization: a road flue gas is connected through the suction line of circulating flue gas pipeline with pressurization continuous feeders, and another road flue gas is then arranged outward by chimney.
Described follow-up tar oil treatment device comprises end to end tar storage tank, tar surge tank, tar desalination tower feed pump, tar desalination tower, tar udst separation tower feed pump, tar udst separation tower, tar pre-hydrotreating reaction tower feed pump, tar pre-hydrotreating reaction tower, hydrogenation of tar refining reaction tower and tar refining product rectification tower successively, and rectifying product enters Naphtha tank and diesel oil tank by tar refining product rectification top of tower and outlet at bottom respectively.
Coal gas of the present invention and fine coal is collaborative to generate electricity, Poly-generation method, comprises the following steps:
1) feed coal of one or more compositions in coal brown coal inferior for high volatile, jet coal, non-caking coal, weakly caking coal, bottle coal, gangue is dried to moisture content and is 1.0 ~ 2.0wt% and is crushed to particle diameter to be 50 ~ 500 μm of raw material coal dusts;
2) by step 2) raw material coal dust be delivered into pressurization continuous feeders by circulating flue gas, in the charging of 0.1 ~ 2.0MPa continous-stable, raw material coal dust enters gasification-pyrolysis coupling reactor by continuous pressure feeder, in 450 ~ 1100 DEG C, carry out rapid conversion under 0.1 ~ 1.5MPa condition, the tar obtained after the raw gas that feed coal conversion generates enters dedusting, separator sends into the tar component in follow-up tar oil treatment device recovery raw gas;
3) step 2) described in raw gas in tar component work in coordination with technique reclaim by absorption, condensation separation and extraction;
4) step 3) crude coal tar that reclaims is after the purification pretreatment of necessity, carry out deep processing conversion again, it is finally converted into the clean fuel oil product of comprehensive liquid fuel more than the yield 85wt% formed primarily of liquefied gas, gasoline, diesel oil;
5) after dedusting, separator process, the purification coal gas of gained is divided into two branch roads to be entered in boiler by burner nozzle according to the ratio of 0 ~ 70wt% burning, the coal gas of one of them branch road enters burner hearth by the burner being positioned at boiler furnace top, carry out mixing burning with bunker coal, the flue-gas temperature produced is 1200 ~ 1400 DEG C and produces saturated vapors by the radiation heat transfer face laid in burner hearth, coal gas and bunker coal mix the oxygen-enriched combusting or air burning that burning mode can be oxygen content 30 ~ 70vol%; The coal gas of another branch road enters boiler by the burner nozzle of boiler heat convection section, mix with supplementary combustion air, the flake hearth-tapping Gas phase Smoke after radiation heat transfer and carry out second-time burning, the flue-gas temperature that burning produces is 850 ~ 1000 DEG C, and the high-temperature flue gas that this partial combustion produces carries out heat convection with heat exchanger, again heat exchanger, economizer, air preheater excessively in boiler again.50 ~ 70wt% heating power type and 30 ~ 50wt% fuel type NO can be cut down under the blending combusted proportion of 1200 ~ 1400 DEG C, 850 ~ 1000 DEG C
xgeneration;
6) flue gas after heat convection is again after follow-up flue gas processing device purified treatment, one tunnel enters chimney of electric plant through air-introduced machine and arranges outward, coal dust of leading up to conveying feed channel as conveying gas coal dust is sent into step 2) described in continuous pressure dispenser.
It is described that to enter the coal gas Lower heat value that gasification-pyrolysis coupling reactor that boiler and coal dust carry out mixing burning produces be 4000 ~ 8000kJ/Nm
3.
Compared with direct coal-fired power generator set, the present invention has obvious technical advantage, can produce following beneficial effect:
1) coal-based clean preparation of fuel and fuel gas generation technology carried out highly integrated;
2) the efficient, clean of coal resources and cascade utilization is achieved;
3), compared with directly burning with coal, coal gas and coal dust enter boiler and mix and mix burning, significantly can cut down smoke yields;
4) pyrolysis coal gas enters PM in the flue gas that boiler combustion produces
2.5and PM
10extremely low Deng inspirable particle concentration, can SO be realized
2, NO
xand the low concentration discharge of the heavy metal such as lead, chromium, cadmium, arsenic, mercury.
The tar that the present invention reclaims after purification pretreatment, then carries out deep processing conversion, and it is finally converted into the clean fuels such as liquefied gas, gasoline, diesel oil; In boiler coal gas and bunker coal mix burning, the heating power type of 50 ~ 70% and the fuel type NO of 30 ~ 50% can be cut down
xgenerate.
Accompanying drawing explanation
Fig. 1 is overall structure schematic diagram of the present invention.
In figure: 1, raw material coal bunker 2, feed storage tank 3, feed hopper 4, lock hopper 5, pressurization continuous feeders 6, gasification-pyrolysis coupling reactor 7, elementary deduster 8, degree of depth deduster 9, oil-gas knockout tower 10, degree of depth oil-gas knockout tower 11, boiler 12, flue gas ash removal tower 13, fume desulfurizing tower 14, denitrating flue gas tower 15, chimney 16, tar storage tank 17, tar desalination tower 18, tar udst separation tower 19, tar pre-hydrotreating reaction tower 20, hydrogenation of tar refining reaction tower 21, tar desalination tower feed pump 22, tar udst separation tower feed pump 23, tar pre-hydrotreating reaction tower feed pump 24, tar refining product rectification tower 25, tar surge tank 26, Naphtha tank 27, diesel oil tank 28, gasification-pyrolysis coupling reactor feed nozzle 29, boiler feed nozzle 30, gasification-pyrolysis coupling reactor outlet 31, boiler furnace burner nozzle (31) 32, the burner nozzle 33 of boiler heat convection section, supplement combustion air nozzle 34, boiler flue gas outlet 35, circulating flue gas pipeline 36, rectifying tower top outlet 37, rectifying column bottom outlet 38, tar refining product rectification tower entrance 39, boiler bottom preheated air entrance 40, cold air.
Detailed description of the invention
In order to make technical scheme of the present invention and advantage clearly distinct, below in conjunction with drawings and Examples, the present invention is further elaborated.
See Fig. 1, the inventive system comprises coal dust feed arrangement and gasification-pyrolysis coupling reactor 6 of being connected with coal dust feed arrangement and boiler 11, the raw gas containing tar and ash content that gasification-pyrolysis coupling reactor 6 exports and dedusting, separator is connected, by dedusting, tar in the raw gas that separator reclaims is sent into follow-up tar oil treatment device and is obtained naphtha and diesel oil, containing the raw gas of tar and ash content through dedusting, be divided into two branch roads to enter in boiler 11 after separator to burn, the coal gas of a branch road is entered in boiler 11 by the burner nozzle 31 on boiler furnace top and carries out blending burning with bunker coal, the coal gas of another branch road enters boiler 11 by the burner nozzle 32 of boiler heat convection section, with the preheated air entering boiler 11 heat convection section through supplementing combustion air nozzle 33, second-time burning is carried out in the Gas phase Smoke mixing of flake hearth-tapping after radiation heat transfer, and with in boiler 11 cross heat exchanger, heat exchanger again, economizer, air preheater carries out heat convection, the superheated steam that boiler 11 mistake heat exchanger and reheating heat exchanger produce and reheated steam are respectively by superheated steam high pressure turbine, reheated steam intermediate pressure turbine drives generating set generating, the flue gas that bottom boiler 11, exhanst gas outlet 34 is discharged is discharged after follow-up flue gas processing device,
Cold air 40 divides and is also divided into two branch roads after boiler air preheater preheating, one tunnel enters boiler 11 burner hearth through boiler 11 bottom heating air intake 39, another road through supplementing combustion air nozzle 33 and the flue gas of flake hearth-tapping after radiation heat transfer, enter the coal gas of boiler 11 through the burner nozzle 33 of heat convection section and mix mutually and carry out second-time burning.
Described dedusting, separator comprises the elementary deduster 7 be connected successively, degree of depth deduster 8, oil-gas knockout tower 9 and degree of depth oil-gas knockout tower 10, wherein elementary deduster 7 entrance is connected with the outlet of gasification-pyrolysis coupling reactor 6, the outlet of degree of depth oil-gas knockout tower 10 divide two-way respectively with the burner nozzle 31 on boiler furnace top, the burner nozzle 32 of boiler heat convection section is connected, elementary deduster 7 is connected with gasification-pyrolysis coupling reactor 6 by pipeline with the outlet of degree of depth deduster 8 lower end, oil-gas knockout tower 9 is connected with follow-up tar oil treatment device by the road with the lower end outlet of degree of depth oil-gas knockout tower 10.
Described coal dust feed arrangement comprises the raw material coal bunker 1, feed storage tank 2, feed hopper 3, lock hopper 4 and the pressurization continuous feeders 5 that are connected successively.
Described follow-up flue gas processing device comprises the gas wash tower 12, fume desulfurizing tower 13 and the denitrating flue gas tower 14 that are connected successively, flue gas after udst separation is divided into two branch roads after air-introduced machine 23 pressurizes: a road flue gas is connected through the suction line of circulating flue gas pipeline 35 with pressurization continuous feeders 5, and another road flue gas is then by the outer row of chimney 15.
Described follow-up tar oil treatment device comprises end to end tar storage tank 16, tar surge tank 25, tar desalination tower feed pump 21, tar desalination tower 17, tar udst separation tower feed pump 22, tar udst separation tower 18, tar pre-hydrotreating reaction tower feed pump 23, tar pre-hydrotreating reaction tower 19, hydrogenation of tar refining reaction tower 20 and tar refining product rectification tower 24 successively, and rectifying product enters Naphtha tank 26 and diesel oil tank 27 by tar refining product rectification tower 24 top and outlet at bottom 36,37 respectively.
Described gasification-pyrolysis coupling reactor 6 is the gasification-thermal decomposition integrated recirculating fluidized bed pyrolytic reaction devices using the solid circle particle of circulating ratio scope 5 ~ 100 as heat carrier.
Described boiler is coal-powder boiler or CFBB.
It is the super critical boiler of 2020t/h that described boiler 11 adopts nominal output to be the subcritical boiler of 35 ~ 1025t/h or nominal output, regulates exerting oneself of boiler 11 by the ratio adjusted within the scope of 10% ~ 70wt% shared by blending gas.
Its process is as follows: first by coal inferior for high volatile as brown coal, jet coal, bituminous coal, the feed coal of one or more compositions in coke is through pulverizing, screening, the moisture content of drying gained is 1.0 ~ 2.0wt%, the powder that particle size range is 50 ~ 400 μm adds in raw material coal bunker 1, and the fine coal in raw material coal bunker 1 is successively through feed storage tank 2, feed hopper 3, lock hopper 4 enter under the conveying of circulating flue gas pressurization continuous feeders 5, pressurization continuous feeders 5 under 0.1 ~ 2.0MPa pressure, respectively by feed nozzle 28, 29 are delivered to gasification-pyrolysis coupling reactor 6 by stable for raw material coal dust, boiler 11, gasification-pyrolysis coupling reactor 6 exports the raw gas containing tar and ash content of 30 outputs successively through follow-up elementary deduster 7, degree of depth deduster 8, oil-gas knockout tower 9, degree of depth oil-gas knockout tower 10 removes dedusting, be divided into two branch roads to enter in boiler 11 after removing tar to burn: a branch road is entered in boiler 11 by the burner nozzle 31 on boiler furnace top and carries out blending burning with bunker coal, and the flue-gas temperature that multifuel combustion produces is 1200 ~ 1400 DEG C, the coal gas of another one branch road enters boiler 11 by the burner nozzle 32 of boiler heat convection section, with through supplementing, combustion air nozzle 33 enters the preheated air of boiler 11 heat convection section, flake hearth-tapping Gas phase Smoke of temperature range 750 ~ 800 DEG C after radiation heat transfer mix and carries out second-time burning, the flue gas of the temperature range that second-time burning produces 850 ~ 1000 DEG C carries out heat convection with mistake heat exchanger, the again heat exchanger in boiler 11, economizer, air preheater again.The superheated steam that boiler 11 mistake heat exchanger and reheating heat exchanger produce and reheated steam drive generating set generating respectively by superheated steam high pressure turbine, reheated steam intermediate pressure turbine.
The flue gas of 100 ~ 120 DEG C that bottom boiler 11, exhanst gas outlet 34 is discharged is divided into two branch roads through follow-up flue gas ash removal tower 12, fume desulfurizing tower 13, denitrating flue gas tower 14 again after udst separation after air-introduced machine 23 pressurizes: a road flue gas is delivered into pressurization continuous feeders 5 through circulating flue gas pipeline 35 as the raw material fine coal that lock hopper 4 exports by conveying gas, and pressurization continuous feeders 5 stablizes transferring raw material coal dust in gasification-pyrolysis coupling reactor 6, boiler 11; Another road flue gas is then by the outer row of chimney 15.
Cold air 40 divides and is also divided into two branch roads after boiler air preheater preheating, one tunnel enters boiler 11 burner hearth through boiler 11 bottom heating air intake 39, and another Lu Zejing entrance 33 as a supplement flue gas of combustion air nozzle and flake hearth-tapping temperature range 800 ~ 900 DEG C after radiation heat transfer, the coal gas that enters boiler 11 through the burner nozzle 32 of heat convection section mixes mutually and carries out second-time burning.
Oil-gas knockout tower 9, degree of depth oil-gas knockout tower 10 is by absorption, condensation separation, tar in the raw gas that the modes such as chemical extraction reclaim is successively through tar storage tank 16, after the pressurization of tar desalination tower feed pump 21, tar desalination tower 17 is entered after tar surge tank 25, tar after desalination enters in tar udst separation tower 18 and carries out udst separation further after the pressurization of tar udst separation tower feed pump 22, through desalination, tar after udst separation enters tar pre-hydrotreating reaction tower 19 after the pressurization of tar pre-hydrotreating reaction tower feed pump 23, carry out pre-hydrocracking reaction, oil product after pre-hydrogenation lighting enters in hydrogenation of tar refining reaction tower 20 again and carries out deep hydrofinishing.Deep hydrogenation product enters the separation carrying out different boiling range product in tar refining product rectification tower 24 through entrance 38.Rectifying product is entered in Naphtha tank 26, diesel oil tank 27 by tar refining product rectification tower 24 top and outlet at bottom 36,37 respectively.
Claims (9)
1. a coal gas and fine coal are worked in coordination with and are generated electricity, multi-joint-production apparatus, it is characterized in that: the gasification comprising coal dust feed arrangement and be connected with coal dust feed arrangement-pyrolysis coupling reactor (6) and boiler (11), the raw gas containing tar and ash content that gasification-pyrolysis coupling reactor (6) exports and dedusting, separator is connected, by dedusting, tar in the raw gas that separator reclaims is sent into follow-up tar oil treatment device and is obtained naphtha and diesel oil, containing the raw gas of tar and ash content through dedusting, two branch roads are divided into enter burning in boiler (11) after separator, the coal gas of a branch road is entered in boiler (11) by the burner nozzle (31) on boiler furnace top and carries out blending burning with bunker coal, the coal gas of another branch road enters boiler (11) by the burner nozzle (32) of boiler heat convection section, with the preheated air entering boiler (11) heat convection section through supplementing combustion air nozzle (33), second-time burning is carried out in the Gas phase Smoke mixing of flake hearth-tapping after radiation heat transfer, and with in boiler (11) cross heat exchanger, heat exchanger again, economizer, air preheater carries out heat convection, the superheated steam that boiler (11) mistake heat exchanger and reheating heat exchanger produce and reheated steam are respectively by superheated steam high pressure turbine, reheated steam intermediate pressure turbine drives generating set generating, the flue gas that boiler (11) bottom exhanst gas outlet (34) is discharged sends into follow-up flue gas processing device,
Cold air (40) divides and is also divided into two branch roads after boiler air preheater preheating, one tunnel enters boiler (11) burner hearth through boiler (11) bottom heating air intake (39), another road through supplementing combustion air nozzle (33) and the flue gas of flake hearth-tapping after radiation heat transfer, enter the coal gas of boiler (11) through the burner nozzle (33) of heat convection section and mix mutually and carry out second-time burning.
2. coal gas according to claim 1 and fine coal are worked in coordination with and are generated electricity, multi-joint-production apparatus, it is characterized in that: described dedusting, separator comprises the elementary deduster (7) be connected successively, degree of depth deduster (8), oil-gas knockout tower (9) and degree of depth oil-gas knockout tower (10), wherein elementary deduster (7) entrance is connected with the outlet of gasification-pyrolysis coupling reactor (6), the outlet of degree of depth oil-gas knockout tower (10) divide two-way respectively with the burner nozzle (31) on boiler furnace top, the burner nozzle (32) of boiler heat convection section is connected, elementary deduster (7) is connected with gasification-pyrolysis coupling reactor (6) by pipeline with the outlet of degree of depth deduster (8) lower end, oil-gas knockout tower (9) is connected with follow-up tar oil treatment device by the road with the lower end outlet of degree of depth oil-gas knockout tower (10).
3. coal gas according to claim 1 and fine coal collaboratively to generate electricity, multi-joint-production apparatus, it is characterized in that: described gasification-pyrolysis coupling reactor (6) is the gasification-pyrolysis integrated recirculating fluidized bed pyrolytic reaction device using the solid circle particle of circulating ratio scope 5 ~ 100 as heat carrier.
4. coal gas according to claim 1 and fine coal collaboratively to generate electricity, multi-joint-production apparatus, it is characterized in that: the coal-powder boiler that described boiler (11) is existing coal-burning power plant or CFBB.
5. coal gas according to claim 1 and fine coal collaboratively to generate electricity, multi-joint-production apparatus, it is characterized in that: it is the super critical boiler of 2020t/h that described boiler (11) adopts nominal output to be the subcritical boiler of 35 ~ 1025t/h or nominal output, regulates exerting oneself of boiler (11) by the ratio adjusted within the scope of 0% ~ 70wt% shared by blending gas.
6. coal gas according to claim 2 and fine coal collaboratively to generate electricity, multi-joint-production apparatus, it is characterized in that: described follow-up flue gas processing device comprises the gas wash tower (12), fume desulfurizing tower (13) and the denitrating flue gas tower (14) that are connected successively, flue gas after udst separation is divided into two branch roads after air-introduced machine (23) pressurization: a road flue gas is connected through the suction line of circulating flue gas pipeline (35) with pressurization continuous feeders (5), and another road flue gas is then arranged outward by chimney (15).
7. coal gas according to claim 2 and fine coal are worked in coordination with and are generated electricity, multi-joint-production apparatus, it is characterized in that: described follow-up tar oil treatment device comprises end to end tar storage tank (16) successively, tar surge tank (25), tar desalination tower feed pump (21), tar desalination tower (17), tar udst separation tower feed pump 22, tar udst separation tower (18), tar pre-hydrotreating reaction tower feed pump (23), tar pre-hydrotreating reaction tower (19), hydrogenation of tar refining reaction tower (20) and tar refining product rectification tower (24), rectifying product is respectively by tar refining product rectification tower (24) top and outlet at bottom (36, 37) Naphtha tank (26) and diesel oil tank (27) is entered.
8. as claimed in claim 1 the coal gas of device and fine coal collaboratively to generate electricity, a Poly-generation method, it is characterized in that comprising the following steps:
1) feed coal of one or more compositions in coal brown coal inferior for high volatile, jet coal, non-caking coal, weakly caking coal, bottle coal, gangue is dried to moisture content and is 1.0 ~ 2.0wt% and is crushed to particle diameter to be 50 ~ 500 μm of raw material coal dusts;
2) by step 2) raw material coal dust by circulating flue gas be delivered into pressurization continuous feeders (5), in the charging of 0.1 ~ 2.0MPa continous-stable, raw material coal dust enters gasification-pyrolysis coupling reactor (6) by continuous pressure feeder (5), in 450 ~ 1100 DEG C, carry out rapid conversion under 0.1 ~ 1.5MPa condition, the tar obtained after the raw gas that feed coal conversion generates enters dedusting, separator sends into the tar component in follow-up tar oil treatment device recovery raw gas;
3) step 2) described in raw gas in tar component work in coordination with technique reclaim by absorption, condensation separation and extraction;
4) step 3) crude coal tar that reclaims is after the purification pretreatment of necessity, carry out deep processing conversion again, it is finally converted into the clean fuel oil product of comprehensive liquid fuel more than the yield 85wt% formed primarily of liquefied gas, gasoline, diesel oil;
5) after dedusting, separator process, the purification coal gas of gained is divided into two branch roads to be entered in boiler by burner nozzle according to the ratio of 0 ~ 70wt% burning, the coal gas of one of them branch road enters burner hearth by the burner being positioned at boiler furnace top, carry out mixing burning with bunker coal, the flue-gas temperature produced is 1200 ~ 1400 DEG C and produces saturated vapors by the radiation heat transfer face laid in burner hearth, coal gas and bunker coal mix the oxygen-enriched combusting or air burning that burning mode can be oxygen content 30 ~ 70vol%; The coal gas of another branch road enters boiler by the burner nozzle of boiler heat convection section, mix with supplementary combustion air, the flake hearth-tapping Gas phase Smoke after radiation heat transfer and carry out second-time burning, the flue-gas temperature that burning produces is 850 ~ 1000 DEG C, and the high-temperature flue gas that this partial combustion produces carries out heat convection with heat exchanger, again heat exchanger, economizer, air preheater excessively in boiler again.50 ~ 70wt% heating power type and 30 ~ 50wt% fuel type NO can be cut down under the blending combusted proportion of 1200 ~ 1400 DEG C, 850 ~ 1000 DEG C
xgeneration;
6) flue gas after heat convection is again after follow-up flue gas processing device purified treatment, one tunnel enters chimney of electric plant through air-introduced machine and arranges outward, coal dust of leading up to conveying feed channel as conveying gas coal dust is sent into step 2) described in continuous pressure dispenser.
9. coal gas according to claim 8 and fine coal collaboratively to generate electricity, Poly-generation method, it is characterized in that: entering the coal gas Lower heat value that gasification-pyrolysis coupling reactor (6) produces that boiler and coal dust carry out mixing burning is 4000 ~ 8000kJ/Nm
3.
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