CN104864391A - Poly-generation apparatus and method using low nitrogen oxides in coal gas for combustion power generation - Google Patents
Poly-generation apparatus and method using low nitrogen oxides in coal gas for combustion power generation Download PDFInfo
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Abstract
The invention provides a poly-generation apparatus and method using low nitrogen oxides in coal gas for combustion power generation. According to the invention, one or more low rank coal selected from the group consisting of brown coal, long flame coal, sub-bituminous coal and soft coal are added into a fine coal upgrading conversion reactor for rapid conversion, crude coal gas produced after conversion undergoes dedusting and purifying, oil-gas separation, and desulphurization and purification; and purified coal gas is successively injected into a boiler for combustion through graded combustion nozzles. Compared with the prior art, the invention has the following advantages: a desired air excess coefficient is small, combustion temperature is lower than a typical temperature--1400 DEG C at which a great amount of thermal NOx is produced, so production of thermal NOx in the process of combustion is radically inhibited and production of fuel NOx and rapid NOx is avoided; the concentration of respirable particulates like SO2, PM2.5 and PM10 in combustion flue gas is extremely low, and ultra-low concentration discharge of SO2 and NOx can be realized; and the combustion flue gas is almost free of heavy metals like lead, chromium, cadmium, arsenic and mercury.
Description
Technical field
The present invention relates to high-efficiency cleaning trans-utilization and the coal gas clean burning technical field of power generation of coal, be specifically related to a kind of coal gas low nitrogen oxide burning generating multi-joint-production apparatus and method.
Background technology
In boiler of power plant coal combustion process, the main source of NOx has three, i.e. heating power type NOx, fuel type NOx, Quick-type NOx.Under common ignition temperature, in the NOx that coal combustion generates, NO accounts for more than 90%, NO
2account for 5% ~ 10%.At present, in coal-fired plant boiler, the control method of NOx is mainly divided three classes: one is adopt low nitrogen fuel or fire front denitrogenation to fuel; Two is adopt low NOx combustion mode, and three is carry out denitration to coal-fired flue-gas.At most nitrogenous in coal, secondly be fuel oil, in combustion gas general not containing or seldom, obviously, adopt fuel oil, combustion gas be fuel, to the NO in reduction flue gas
xgeneration be favourable, but the high cost of the direct fuel oil of boiler of power plant, natural gas power, substantially can say without economy.The raw coke oven gas of Lan Tan enterprise by-product enters the example that the direct combustion power generation of boiler also has a lot of application, but the subject matter existed is as traditional coal chemical industry, blue charcoal industry belongs to serious production capacity surplus and belongs to the backward industry of progressively eliminating, Lan Tan enterprise mostly is the small enterprise of decentralized in addition, the overall utilization of capacity is not enough, and the raw coke oven gas quality of producing and quantity also have larger fluctuation.Before combustion, denitride technology is only in the laboratory research stage at present, and its difficulty is comparatively large, to coal selective higher, investment intensity is excessive, distance commercial application is had got long long way to go.Low NOx combustion mode is mainly by the growing amount controlling the excess air coefficient of pulverized coal friring process, fuel-staged combustion, employing low-NOx combustor reduce NOx as much as possible.But for coal-burning boiler, also only can control the growing amount of thermal NO x by the way, the reduction for fuel type NOx, Quick-type NOx is in fact very limited.Meanwhile, owing to decreasing excess air coefficient and pulverized coal staging combustion, the efficiency of combustion of coal dust is had a great impact.Therefore current most of coal-burning power plant is most widely used.The major technique of end denitration has SCR method, SNCR method, alkali absorption method, electron beam irradiation method etc.SNCR method denitration efficiency is too low, alkali absorption method, electron beam irradiation method denitration high cost, and power plant is difficult to bear, and therefore uses maximum end denitration technologies to be exactly SCR method.Although SCR method denitration efficiency is higher, but in actual application, also there is the problem that cannot overcome, as the Layout Problem of denitrification apparatus, the position of current SCR method denitrification apparatus mainly contains: 1. high ash-laden gas section (boiler air preheater and deduster before), 2. low ash-laden gas section (between deduster and desulfurizer), 3. tail flue gas section (deduster and desulfurizer after).For 1., because reaction temperature is higher, selectable denitrating catalyst kind is more, and flue-gas temperature can directly meet denitration reaction temperature, relative to 2., 3. for, eliminate flue gas reheat system, thus save investment and operating cost.But because dust concentration is higher, comparatively serious to the erosion corrosion of catalyst, also catalyst blockage of the micro orifice be can cause, its life-span and activity affected; SO in flue gas
2under the catalytic action of denitrating catalyst, SO can be converted into
3, follow-up desulfurization difficulty increases.Although reduce for 2. dust concentration, need to set up flue gas reheat system, make investment and operating cost increase, also there is the SO in flue gas simultaneously
2sO can be converted into
3problem.Although wash away and affect problem for 3. there is not dust in flue gas to catalyst life activity, there is not the SO in flue gas yet
2sO can be converted into
3problem, but face equally and set up flue gas reheat system, make the problem that investment and operating cost rise.Meanwhile, the greatest problem of SCR method to use ammonia, and in coal-fired flue-gas, ubiquitous heavy metal all may make SCR catalyst poisoning and deactivation as lead, chromium, cadmium, arsenic etc., has a strong impact on its normal life-span.
Summary of the invention
The object of the present invention is to provide a kind of coal gas low nitrogen oxide burning generating multi-joint-production apparatus and method.
For achieving the above object, the fine coal upgrading conversion reactor that the inventive system comprises coal dust feed arrangement and be connected with coal dust feed arrangement, fine coal upgrading conversion reactor lower end is connected with lime-ash storage tank, the raw gas containing tar and ash content that fine coal upgrading conversion reactor exports exports and dedusting through fine coal upgrading conversion reactor, separator is connected, by dedusting, tar in the raw gas that separator reclaims sends into tar storage tank, dedusting, the purification coal gas of coal gas after desulfurizing tower desulfurization that separator exports enters primary combustion zone respectively by the burner hearth jet for gas be positioned on boiler furnace on differing heights, the rear burning-out zone of boiler is entered by heat convection section jet for gas, cold air is point three branch roads after air preheater preheating, respectively by the rear burning-out zone firing wind nozzle again and enter boiler, one time combustion air nozzle enters primary combustion zone, afterburning wind nozzle enters secondary conbustion zone, 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 is divided into three branch roads again after the udst separation of follow-up flue gas ash removal tower after air-introduced machine pressurization: a road flue gas sends into coal dust feed arrangement through coal dust supplied flue gases pipeline, second road flue gas sends into burner hearth by circulating flue gas pipeline through boiler bottom combustion air nozzle, 3rd tunnel is arranged outward through chimney.
Described dedusting, separator comprise the thin grey controller, grain catcher, oil-gas knockout tower and the coal gas degree of depth de-oiling tower that are connected successively, wherein thin grey controller entrance is connected with the outlet of fine coal upgrading conversion reactor, the outlet of coal gas degree of depth de-oiling tower is connected with the entrance of desulfurizing tower, thin grey controller, the outlet of grain catcher lower end are connected with fine coal upgrading conversion reactor by pipeline, and oil-gas knockout tower is connected with tar storage tank with the outlet of coal gas degree of depth de-oiling tower lower end.
Circulation refeed line is also provided with in described fine coal upgrading conversion reactor, the class spirality that circulation refeed line is formed or class involute-type runner, make in particle size range 30 ~ 100 object carbonaceous particles 70 ~ 80% be captured and loop back the reaction zone of fine coal upgrading conversion reactor.
Described fine coal upgrading conversion reactor is circulating fluid bed reactor, and it is 3.0 ~ 4.5Nm that upgrading transforms dry gas output
3/ kg dry pulverized coal, coal gas Lower heat value is 4000 ~ 8000kJ/Nm
3.
There is in described fine coal upgrading conversion reactor top riser the sudden change undergauge ratio of 5 ~ 20, the high temperature that bottom gasification section can be made to produce, the gas-solid fluid-mixing of high speed up-flow form the low-pressure area even negative pressuren zone of local on fine coal upgrading conversion reactor top, realize pyrolysis section charging and gas-solid fluid-mixing carries out fast instantaneously, efficient heat transfer and mass transfer with this.
Described desulfurizing tower adopts the wet desulphurization of spray column, spray tower or drip bed-type, or the desulfurization of dry method packed tower, or the cascaded structure of wet desulphurization and the desulfurization of dry method packed tower, H in coal gas after desulfurizing tower process
2s content is lower than 5.0mg/Nm
3.
Described primary combustion zone excess air coefficient is 0.7 ~ 0.9; Secondary conbustion zone excess air coefficient is 0.8 ~ 1.0; Rear burning-out zone excess air coefficient is 1.05 ~ 1.1.
The coal gas amount that described primary combustion zone injects accounts for 85 ~ 95% of total amount proportion, and the coal gas amount that rear burning-out zone injects accounts for 5 ~ 15% of total amount proportion.
Method of the present invention comprises the following steps:
1) particle diameter 30 ~ 300 order moisture content is added in fine coal upgrading conversion reactor inherence 2 ~ 3s lower than one or more in the brown coal of 2.0wt%, jet coal, ub-bituminous coal, bituminous coal carried out rapid conversion by coal gas supplied flue gases continuous feeders of entering to pressurize;
2) what generated by feed coal rapid conversion returns fine coal upgrading conversion reactor containing the unconverted carbonaceous particles of 30 ~ 100 object contained in oil gas and reactor beds material by circulation refeed line;
3) using step 2) described in the unconverted carbonaceous particles of removing 30 ~ 100 order and the primary purifying coal gas of reactor beds material continues through thin grey controller, microparticle catcher wherein 100 ~ 300 orders removed further wherein have compared with bigger serface, return the fine solid particle of fine coal upgrading conversion reactor as solid thermal carriers;
4) by step 2), 3) described in the oil removing purified treatment of carrying out coal gas containing oil gas through oil-gas knockout tower, coal gas degree of depth de-oiling tower through 3-stage dust-removal purification;
5) step 4) described in the purification coal gas through the process of oil-gas isolation of purified enter desulfurizing tower again and remove hydrogen sulfide in raw gas, the tar of extraction sends into tar storage tank;
6) by step 5) described in be separated through udst separation, oil-gas, the dust content of desulfurizing and purifying process is 1.0 ~ 5.0/Nm
3purification coal gas injects a boiler burn by being arranged in burner hearth jet for gas on burner hearth on differing heights and heat convection section jet for gas point level Four successively again, cold air is point three branch roads after air preheater preheating, respectively by firing wind nozzle, combustion air nozzle, an afterburning wind nozzle injection boiler again, after coal gas injects boiler, point three combustion zones and primary combustion zone, secondary conbustion zone, rear burning-out zone burn, and the combustion reference temperature of primary combustion zone coal gas is 1000 ~ 1300 DEG C, the combustion reference temperature of secondary conbustion zone coal gas is 900 ~ 1100 DEG C, the flue-gas temperature scope of rear burning-out zone is 800 ~ 900 DEG C, the proportion that the coal gas amount that wherein primary combustion zone injects accounts for total amount is 85 ~ 95%, the proportion that the coal gas amount that rear burning-out zone injects accounts for total amount is about 5 ~ 15%, the flue gas that rear burning-out zone produces again with 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 is divided into three branch roads through follow-up flue gas ash removal tower again after udst separation after air-introduced machine pressurization: the raw material fine coal that lock hopper exports as conveying gas through coal dust supplied flue gases pipeline by a road flue gas is delivered into pressurization continuous feeders, pressurization continuous feeders stablizes transferring raw material coal dust in fine coal upgrading conversion reactor, second road flue gas then enters the burner hearth of boiler by circulating flue gas pipeline, a combustion air of a combustion air nozzle injection is the gaseous mixture of circulating flue gas and air, and in a combustion air, oxygen content scope is 3 ~ 21vol%, and the 3rd tunnel is arranged outward through chimney.
Compared with prior art, the present invention has following technical advantage:
1) coal-based clean oil product fuel production and fuel gas generation technology carried out highly integrated, improve the comprehensive added value of coal resources product, achieve the efficient, clean of coal resources and cascade utilization;
2) raw gas enters boiler and directly burns, and required excess air factor is less, the representative temperature 1400 DEG C that ignition temperature produces in a large number lower than thermal NO x, because fuel is coal gas, therefore generates without fuel type NOx, Quick-type NOx;
3) raw gas has carried out burn front dedusting, desulfurizing and purifying, SO in combustion product gases
2, PM
2.5and PM
10extremely low Deng inspirable particle concentration, can SO be realized
2, NO
xultra-low concentration discharge;
4) leaded, the heavy metal such as chromium, cadmium, arsenic, mercury hardly in combustion product gases.
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, power feed device 6, fine coal upgrading conversion reactor 7, circulation refeed line 8, thin grey controller micro-9, grain catcher 10, oil-gas knockout tower 11, coal gas degree of depth de-oiling tower 12, desulfurizing tower, 13, boiler 14-16, burner hearth jet for gas 17, stream heat exchanging segment jet for gas 18, circulating flue gas 19, fire wind nozzle 20 again, a combustion air nozzle 21, afterburning wind nozzle 22, primary combustion zone 23, secondary conbustion zone 24, rear burning-out zone 25, flue-gas dust removal and purification tower 26, air-introduced machine 27, chimney 28, coal dust supplied flue gases 29, gasification-pyrolysis coupling reactor outlet 30, lime-ash storage tank 31, tar storage tank 32, boiler flue gas outlet 33, 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 described in further detail.
See Fig. 1, the fine coal upgrading conversion reactor 6 that the inventive system comprises coal dust feed arrangement and be connected with coal dust feed arrangement, fine coal upgrading conversion reactor 6 lower end is connected with lime-ash storage tank 30, the raw gas containing tar and ash content that fine coal upgrading conversion reactor 6 exports exports 29 and dedusting through fine coal upgrading conversion reactor 6, separator is connected, by dedusting, tar in the raw gas that separator reclaims sends into tar storage tank 31, dedusting, the gas exit of separator through desulfurizing tower 12 desulfurization after-purification coal gas respectively by the burner hearth jet for gas 14 be positioned on boiler 13 burner hearth on differing heights, 15, 16 enter primary combustion zone 22, the rear burning-out zone 24 of boiler 13 is entered by heat convection section jet for gas 17, cold air 33 is point three branch roads after air preheater preheating, respectively by the rear burning-out zone 24 firing wind nozzle 19 again and enter boiler 13, one time combustion air nozzle 20 enters boiler bottom entrance, afterburning wind nozzle 21 enters secondary conbustion zone 23, the superheated steam that boiler 13 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 13, exhanst gas outlet 32 is discharged is divided into three branch roads again after the udst separation of follow-up flue gas ash removal tower 25 after air-introduced machine 26 pressurizes: a road flue gas sends into coal dust feed arrangement through coal dust supplied flue gases pipeline 28, second road flue gas is by the burner hearth of circulating flue gas pipeline 18 combustion air nozzle 20 feeding bottom boiler 35, 3rd tunnel is through the outer row of chimney 27.
Wherein dedusting, separator comprise the thin grey controller 8, grain catcher 9, oil-gas knockout tower 10 and the coal gas degree of depth de-oiling tower 11 that are connected successively, wherein thin grey controller 8 entrance is connected with the outlet of fine coal upgrading conversion reactor 6, the outlet of coal gas degree of depth de-oiling tower 11 is connected with the entrance of desulfurizing tower 12, thin grey controller 8, the outlet of grain catcher 9 lower end are connected with fine coal upgrading conversion reactor 6 by pipeline, and oil-gas knockout tower 10 is connected with tar storage tank 31 with the outlet of coal gas degree of depth de-oiling tower 11 lower end.
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, and the outlet of flue gas pipeline 28 is connected with the entrance of pressurization continuous feeders 5.
Circulation refeed line 7 is also provided with in fine coal upgrading conversion reactor 6, the class spirality that circulation refeed line 7 is formed by internals or class involute-type runner, make in particle size range 30 ~ 100 object carbonaceous particles 70 ~ 80% be captured and loop back reaction zone.
Fine coal upgrading conversion reactor 6 is circulating fluid bed reactor, in its top pyrolysis section riser 5 ~ 20 sudden change undergauge ratio, pyrolysis dry gas output is 3.0 ~ 4.5Nm
3/ kg dry pulverized coal, coal gas Lower heat value is 4000 ~ 6500kJ/Nm
3.
Desulfurizing tower 12 adopts the wet desulphurization of spray column, spray tower or drip bed-type, or the desulfurization of dry method packed tower, or the cascaded structure of wet desulphurization and the desulfurization of dry method packed tower, H in coal gas after desulfurizing tower process
2s content is lower than 5.0mg/Nm
3.
Primary combustion zone 22 excess air coefficient is 0.7 ~ 0.9; Secondary conbustion zone 23 excess air coefficient is 0.8 ~ 1.0; Rear burning-out zone 24 excess air coefficient is 1.05 ~ 1.1.The coal gas amount that primary combustion zone 22 injects accounts for 85 ~ 95% of total amount proportion, and the coal gas amount that rear burning-out zone 24 injects accounts for 5 ~ 15% of total amount proportion.
Method of the present invention is as follows:
1) particle diameter 30 ~ 300 order moisture content to be added in fine coal upgrading conversion reactor 6 by pressurization continuous feeders 5 by coal gas supplied flue gases lower than one or more in the brown coal of 2.0wt%, jet coal, ub-bituminous coal, bituminous coal under 0.1 ~ 2.0MPa pressure in 2 ~ 3s, carry out rapid conversion;
2) what generated by feed coal rapid conversion returns fine coal upgrading conversion reactor 6 containing the unconverted carbonaceous particles of 30 ~ 100 object contained in oil gas and reactor beds material by circulation refeed line 7;
3) using step 2) described in the unconverted carbonaceous particles of removing 30 ~ 100 order and the primary purifying coal gas of reactor beds material continue through thin grey controller 8, microparticle catcher 9 further expulsion wherein 100 ~ 300 orders wherein have compared with bigger serface, return the fine solid particle of fine coal upgrading conversion reactor 6 as solid thermal carriers;
4) by step 2), 3) described in the oil removing purified treatment of carrying out coal gas containing oil gas through oil-gas knockout tower 10, coal gas degree of depth de-oiling tower 11 through 3-stage dust-removal purification;
5) step 4) described in the purification coal gas through the process of oil-gas isolation of purified enter desulfurizing tower 12 again and remove hydrogen sulfide in raw gas, H in coal gas
2s content is lower than 5.0mg/Nm
3, dust content scope 1.0 ~ 5.0/Nm
3, the tar of extraction sends into tar storage tank 31;
6) by step 5) described in be separated through udst separation, oil-gas, the dust content of desulfurizing and purifying process is 1.0 ~ 5.0/Nm
3purification coal gas injects boilers 13 burn by being arranged in burner hearth jet for gas 14,15,16 on burner hearth on differing heights and heat convection section jet for gas 17 points of level Four successively again, cold air 33 is point three branch roads after air preheater preheating, respectively by firing wind nozzle 19, combustion air nozzle 20 again, afterburning wind nozzle 21 injects boiler, after coal gas injects boiler, points of three main combustion zone primary combustion zone 22, secondary conbustion zone 23, rear burning-out zones 24 burn, and the combustion reference temperature of primary combustion zone (22) coal gas is 1000 ~ 1300 DEG C, the combustion reference temperature of secondary conbustion zone (23) coal gas is 900 ~ 1100 DEG C, the flue-gas temperature scope of rear burning-out zone (24) is 800 ~ 900 DEG C, the proportion that the coal gas amount that wherein primary combustion zone 22 injects accounts for total amount is about 85 ~ 95%, the proportion that the coal gas amount that rear burning-out zone 24 injects accounts for total amount is about 5 ~ 15%, the flue gas that rear burning-out zone 24 produces again with boiler 13 cross heat exchanger, heat exchanger again, economizer, air preheater carries out heat convection, the superheated steam that boiler 13 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 temperature that bottom boiler 13, exhanst gas outlet 32 is discharged is 100 ~ 120 DEG C, NO
xconcentration range is at 1 ~ 5mg/Nm
3.After udst separation, be divided into three branch roads by follow-up flue gas ash removal tower 25 again after air-introduced machine 26 pressurizes: a road flue gas is delivered into pressurization continuous feeders 5 through coal dust supplied flue gases pipeline 28 as the raw material fine coal that lock hopper 4 exports by conveying gas, pressurization continuous feeders 5 stablizes transferring raw material coal dust in fine coal upgrading conversion reactor 6; Second road flue gas then enters the burner hearth of boiler 35 by circulating flue gas pipeline 18; A combustion air of combustion air nozzle 20 injection is the gaseous mixture of circulating flue gas (18) and air, and in a combustion air, oxygen content scope is 3 ~ 21vol%, and the 3rd tunnel is through the outer row of chimney 27.
Fine coal upgrading conversion reactor 6 of the present invention is circulating fluid bed reactor, based in the pyrolysis section riser of top 5 ~ 20 sudden change undergauge ratio, the high temperature that bottom gasification section produces, the gas-solid fluid-mixing of high speed up-flow form the low-pressure area even negative pressuren zone of local at top pyrolysis section, realize pyrolysis section charging and gas-solid fluid-mixing carries out fast instantaneously, efficient heat transfer and mass transfer with this.
Fine coal upgrading conversion reactor 6 pyrolysis dry gas output is 3.0 ~ 4.5Nm
3/ kg dry pulverized coal, coal gas Lower heat value is 4000 ~ 6500kJ/Nm
3.
The combustion reference temperature of primary combustion zone 22 coal gas of the present invention is 1000 ~ 1300 DEG C; The combustion reference temperature of secondary conbustion zone 23 coal gas is 900 ~ 1100 DEG C; The flue-gas temperature scope of rear burning-out zone 24 is 800 ~ 900 DEG C.
Claims (9)
1. a coal gas low nitrogen oxide burning generating multi-joint-production apparatus, it is characterized in that: the fine coal upgrading conversion reactor (6) comprising coal dust feed arrangement and be connected with coal dust feed arrangement, fine coal upgrading conversion reactor (6) lower end is connected with lime-ash storage tank (30), the raw gas containing tar and ash content that fine coal upgrading conversion reactor (6) exports exports (29) and dedusting through fine coal upgrading conversion reactor (6), separator is connected, by dedusting, tar in the raw gas that separator reclaims sends into tar storage tank (31), dedusting, the purification coal gas of the coal gas that separator exports after desulfurizing tower (12) desulfurization is respectively by the burner hearth jet for gas (14 be positioned on boiler (13) burner hearth on differing heights, 15, 16) primary combustion zone (22) is entered, the rear burning-out zone (24) of boiler (13) is entered by heat convection section jet for gas (17), cold air (33) is point three branch roads after air preheater preheating, respectively by the rear burning-out zone (24) firing wind nozzle (19) again and enter boiler (13), one time combustion air nozzle (20) enters primary combustion zone, afterburning wind nozzle (21) enters secondary conbustion zone (23), the superheated steam that boiler (13) 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 (13) bottom exhanst gas outlet (32) is discharged is divided into three branch roads again after the udst separation of follow-up flue gas ash removal tower (25) after air-introduced machine (26) pressurization: a road flue gas sends into coal dust feed arrangement through coal dust supplied flue gases pipeline (28), second road flue gas sends into burner hearth by circulating flue gas pipeline (18) through boiler (35) one time, bottom combustion air nozzle (20), 3rd tunnel is arranged outward through chimney (27).
2. coal gas low nitrogen oxide burning generating multi-joint-production apparatus according to claim 1, it is characterized in that: described dedusting, separator comprises the thin grey controller (8) be connected successively, grain catcher (9), oil-gas knockout tower (10) and coal gas degree of depth de-oiling tower (11), wherein thin grey controller (8) entrance is connected with the outlet of fine coal upgrading conversion reactor (6), the outlet of coal gas degree of depth de-oiling tower (11) is connected with the entrance of desulfurizing tower (12), thin grey controller (8), the outlet of grain catcher (9) lower end is connected with fine coal upgrading conversion reactor (6) by pipeline, oil-gas knockout tower (10) is connected with tar storage tank (31) with the outlet of coal gas degree of depth de-oiling tower (11) lower end.
3. coal gas low nitrogen oxide burning generating multi-joint-production apparatus according to claim 1, it is characterized in that: in described fine coal upgrading conversion reactor (6), be also provided with circulation refeed line (7), the class spirality that circulation refeed line (7) is formed or class involute-type runner, make in particle size range 30 ~ 100 object carbonaceous particles 70 ~ 80% be captured and loop back the reaction zone of fine coal upgrading conversion reactor (6).
4. coal gas low nitrogen oxide burning generating multi-joint-production apparatus according to claim 1, it is characterized in that: described fine coal upgrading conversion reactor (6) is circulating fluid bed reactor, it is 3.0 ~ 4.5Nm that upgrading transforms dry gas output
3/ kg dry pulverized coal, coal gas Lower heat value is 4000 ~ 8000kJ/Nm
3.
5. coal gas low nitrogen oxide burning generating multi-joint-production apparatus according to claim 1, it is characterized in that: there is in described fine coal upgrading conversion reactor (6) top riser the sudden change undergauge ratio of 5 ~ 20, the high temperature that bottom gasification section is produced, the gas-solid fluid-mixing of high speed up-flow form the low-pressure area even negative pressuren zone of local on fine coal upgrading conversion reactor (6) top, realize pyrolysis section charging and gas-solid fluid-mixing carries out fast instantaneously, efficient heat transfer and mass transfer.
6. coal gas low nitrogen oxide burning generating multi-joint-production apparatus according to claim 1, it is characterized in that: described desulfurizing tower (12) adopts the wet desulphurization of spray column, spray tower or drip bed-type, or the desulfurization of dry method packed tower, or the cascaded structure of wet desulphurization and the desulfurization of dry method packed tower, H in coal gas after desulfurizing tower process
2s content is lower than 5.0mg/Nm
3.
7. coal gas low nitrogen oxide burning generating multi-joint-production apparatus according to claim 1, is characterized in that: described primary combustion zone (22) excess air coefficient is 0.7 ~ 0.9; Secondary conbustion zone (23) excess air coefficient is 0.8 ~ 1.0; Rear burning-out zone (24) excess air coefficient is 1.05 ~ 1.1.
8. coal gas low nitrogen oxide burning generating multi-joint-production apparatus according to claim 1, it is characterized in that: the coal gas amount that described primary combustion zone (22) injects accounts for 85 ~ 95% of total amount proportion, and the coal gas amount that rear burning-out zone (24) injects accounts for 5 ~ 15% of total amount proportion.
9. a coal gas low nitrogen oxide burning generating Poly-generation method for device as claimed in claim 1, is characterized in that comprising the following steps:
1) particle diameter 30 ~ 300 order moisture content is added in the inherent 2 ~ 3s of fine coal upgrading conversion reactor (6) lower than one or more in the brown coal of 2.0wt%, jet coal, ub-bituminous coal, bituminous coal carried out rapid conversion by coal gas supplied flue gases continuous feeders (5) of entering to pressurize;
2) what generated by feed coal rapid conversion returns fine coal upgrading conversion reactor (6) containing the unconverted carbonaceous particles of 30 ~ 100 object contained in oil gas and reactor beds material by circulation refeed line (7);
3) using step 2) described in the unconverted carbonaceous particles of removing 30 ~ 100 order and the primary purifying coal gas of reactor beds material continue through thin grey controller (8), microparticle catcher (9) further wherein 100 ~ 300 orders removed wherein have comparatively bigger serface, return the fine solid particle of fine coal upgrading conversion reactor (6) as solid thermal carriers;
4) by step 2), 3) described in the oil removing purified treatment of carrying out coal gas containing oil gas through oil-gas knockout tower (10), coal gas degree of depth de-oiling tower (11) through 3-stage dust-removal purification;
5) step 4) described in the purification coal gas through the process of oil-gas isolation of purified enter desulfurizing tower (12) again and remove hydrogen sulfide in raw gas, the tar of extraction sends into tar storage tank (31);
6) by step 5) described in be separated through udst separation, oil-gas, the dust content of desulfurizing and purifying process is 1.0 ~ 5.0/Nm
3purification coal gas is more successively by being positioned at the burner hearth jet for gas (14 on burner hearth on differing heights, 15, 16) and heat convection section jet for gas (17) point level Four inject boiler (13) and burn, cold air (33) is point three branch roads after air preheater preheating, respectively by firing wind nozzle (19) again, a combustion air nozzle (20), afterburning wind nozzle (21) injects boiler, after coal gas injects boiler, divide three combustion zones and primary combustion zone (22), secondary conbustion zone (23), rear burning-out zone (24) burns, the combustion reference temperature of primary combustion zone (22) coal gas is 1000 ~ 1300 DEG C, the combustion reference temperature of secondary conbustion zone (23) coal gas is 900 ~ 1100 DEG C, the flue-gas temperature scope of rear burning-out zone (24) is 800 ~ 900 DEG C, the proportion that the coal gas amount that wherein primary combustion zone (22) injects accounts for total amount is 85 ~ 95%, the proportion that the coal gas amount that rear burning-out zone (24) injects accounts for total amount is about 5 ~ 15%, the flue gas that rear burning-out zone (24) produces again with boiler (13) cross heat exchanger, heat exchanger again, economizer, air preheater carries out heat convection, the superheated steam that boiler 13 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 (13) bottom exhanst gas outlet (32) is discharged is divided into three branch roads through follow-up flue gas ash removal tower (25) again after udst separation after air-introduced machine (26) pressurization: the raw material fine coal that lock hopper (4) exports is delivered into pressurization continuous feeders (5) through coal dust supplied flue gases pipeline (28) as conveying gas by a road flue gas, pressurization continuous feeders (5) stablizes transferring raw material coal dust in fine coal upgrading conversion reactor (6), second road flue gas then enters the burner hearth of boiler (35) by circulating flue gas pipeline (18), the combustion air that combustion air nozzle (20) is injected is circulating flue gas (18) and the gaseous mixture of air, and in a combustion air, oxygen content scope is 3 ~ 21vol%, and the 3rd tunnel is arranged outward through chimney (27).
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