CN104864391B - 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 the high-efficiency cleaning trans-utilization of coal and coal gas cleaning combustion power generation technology field, and in particular to one
Plant 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. thermal NO x, fuel type NOx, Quick-type
NOx.Under common ignition temperature, in the NOx that coal combustion is generated, NO accounts for more than 90%, NO2Account for 5%～10%.At present, fire
The control method of NOx is broadly divided into three classes in coal-fired plant's boiler：One is to carry out firing front denitrogenation using low nitrogen fuel or to fuel；Two
It is that three is to carry out denitration to coal-fired flue-gas using low NOx combustion mode.Secondly nitrogenous in coal is at most fuel oil, general in combustion gas
Without or seldom, it is clear that fuel oil, combustion gas are adopted for fuel, to the NO in reduction flue gasXGeneration be it is favourable, but power plant
The direct fuel oil of boiler, the high cost of natural gas power, can say without economy substantially.The raw coke oven gas of semi-coke enterprise by-product enters pot
The direct combustion power generation of stove also has the example of many applications, but the subject matter for existing is as traditional Coal Chemical Industry, semi-coke industry
Belong to serious production capacity surplus and belong to the backward industry being phased out, in addition semi-coke enterprise mostly is the small enterprise of decentralized, whole
The body utilization of capacity is not enough, and the raw coke oven gas quality produced also has larger undulatory property with quantity.Denitrogenation technology is only existed at present before combustion
Laboratory research stage, its difficulty is larger, and, investment intensity higher to coal selectivity is excessive, also has very apart from commercial application
Long road will be walked.Low NOx combustion mode is mainly by the excess air coefficient of control pulverized coal friring process, fuel staging combustion
Burn, reduce as far as possible using low-NOx combustor the growing amount of NOx.But for coal-burning boiler, by the way
Also the growing amount of thermal NO x can be only controlled, it is in fact very limited for the reduction of fuel type NOx, Quick-type NOx.
Simultaneously as reducing excess air coefficient and pulverized coal staging combustion, the efficiency of combustion of coal dust is had a great impact.Therefore mesh
Front most of coal-burning power plants are most widely used.The major technique of end denitration has SCR methods, SNCR methods, alkali absorption method, electronics
Beam irradiation etc..SNCR method denitration efficiencies are too low, alkali absorption method, electron beam irradiation method denitration high cost, and power plant is difficult to hold
Receive, therefore the use of most end denitration technology is exactly SCR methods.Although SCR method denitration efficiencies are higher, in actual application
In there is also the problem that cannot be overcome, the such as Layout Problem of denitrification apparatus, the position of current SCR methods denitrification apparatus is main
Have：1. high ash-laden gas section (before boiler air preheater and cleaner unit), 2. low ash-laden gas section (cleaner unit and desulfurizer
Between), 3. tail flue gas section (after cleaner unit and desulfurizer).For 1., due to reaction temperature it is higher, selectable denitration
Catalyst type is more, and flue-gas temperature can directly meet denitration reaction temperature, relative to 2., 3. for, eliminate flue gas reheat
System, so as to save investment and operating cost.But due to dust concentration it is higher, it is more serious to the erosion corrosion of catalyst,
Catalyst blockage of the micro orifice can also be caused, its life-span and activity is affected；SO in flue gas2Under the catalytic action of denitrating catalyst,
SO can be converted into3, follow-up desulfurization difficulty increase.Although for 2. dust concentration is reduced, needing to set up flue gas reheat
System, rises investment and operating cost, while there is also the SO in flue gas2SO can be converted into3Problem.Although for 3.
Not there are problems that dust is washed away to the active impact of catalyst life in flue gas, does not have the SO in flue gas yet2Can be converted into
SO3Problem, but equally face and set up flue gas reheat system, the problem for making investment and operating cost increase.Meanwhile, SCR methods
Greatest problem be used to heavy metal such as lead, chromium, cadmium, arsenic etc. of generally existing in ammonia, and coal-fired flue-gas and may all make SCR
Catalyst poisoning is inactivated, and has a strong impact on its normal life-span.
The content of the invention
It is an object of the invention to provide a kind of coal gas low nitrogen oxide burning generating multi-joint-production apparatus and method.
To reach above-mentioned purpose, the inventive system comprises coal dust feed arrangement and the powder being connected with coal dust feed arrangement
Coal upgrading conversion reactor, fine coal upgrading conversion reactor lower end is connected with lime-ash storage tank, the output of fine coal upgrading conversion reactor
Containing tar and ash raw gas Jing fine coal upgradings conversion reactor outlet be connected with dedusting, segregation apparatuss, by dedusting, separation
Tar in the raw gas that device is reclaimed sends into tar storage tank, and the coal gas that dedusting, segregation apparatuss are exported is Jing after desulfurizing tower desulfurization
Purification coal gas enters primary combustion zone by the burner hearth jet for gas on differing heights on boiler furnace respectively, by convection current
Heat exchanging segment jet for gas enters the rear burning-out zone of boiler, and cold air point three branch roads Jing after air preheater preheating pass through respectively
Rear burning-out zone, the combustion air nozzle for firing wind nozzle again into boiler is into primary combustion zone, afterburning wind nozzle into secondary
Combustion zone, the superheated steam and reheated steam produced by boiler overheating heat exchanger and again heat exchanger is high by superheated steam respectively
Pressure turbine, reheated steam intermediate pressure turbine drive generating set to generate electricity, the follow-up cigarettes of flue gas Jing that boiler bottom exhanst gas outlet is discharged
After gas gas wash tower udst separation again Jing air-introduced machine pressurization after be divided into three branch roads：All the way flue gas send through coal dust conveying flue gas pipeline
Enter coal dust feed arrangement, the second road flue gas sends into burner hearth by combustion air nozzle of circulating flue gas pipeline Jing boiler bottoms；The
Arrange outside three road Jing chimneys.
Fine ash controller that described dedusting, segregation apparatuss include being sequentially connected, grain catcher, oil-gas knockout tower and
Coal gas depth removing oil tower, wherein fine ash controller entrance are connected with the outlet of fine coal upgrading conversion reactor, coal gas depth removing oil
The outlet of tower is connected with the entrance of desulfurizing tower, and fine ash controller, the outlet of grain catcher lower end are turned by pipeline and fine coal upgrading
Change reactor to be connected, oil-gas knockout tower and the outlet of coal gas depth removing oil tower lower end are connected with tar storage tank.
Circulation refeed line is additionally provided with described fine coal upgrading conversion reactor, the class spiral type that refeed line is formed is circulated
Or class involute-type runner so that 70～80% in the carbonaceous particles of the mesh of particle size range 30～100 are captured and loop back powder
The reaction zone of coal upgrading conversion reactor.
Described fine coal upgrading conversion reactor is circulating fluid bed reactor, upgrading conversion dry gas yield is 3.0～
4.5Nm3/ kg dry pulverized coals, coal gas Lower heat value is 4000～8000kJ/Nm3。
There is 5～20 mutation undergauge ratio in described fine coal upgrading conversion reactor top riser, bottom gas can be made
Change the high temperature of section generation, flow up low-pressure area of the gas-solid fluid-mixing in fine coal upgrading conversion reactor top formation local at a high speed
Even negative pressuren zone, with this realize being pyrolyzed section feeding and gas-solid fluid-mixing moment carry out quickly, efficient heat transfer and mass transfer.
Described desulfurizing tower adopts the wet desulphurization of spray column, spray tower or drip bed-type, or dry method packed tower desulfurization, or
Wet desulphurization and the cascaded structure of dry method packed tower desulfurization, the H in coal gas Jing after desulfurizing tower process2S contents are less than 5.0mg/Nm3。
Described primary combustion zone excess air coefficient is 0.7～0.9；Secondary conbustion zone excess air coefficient be 0.8～
1.0；Afterwards burning-out zone excess air coefficient is 1.05～1.1.
The coal gas amount of described primary combustion zone injection accounts for the 85～95% of total amount proportion, the coal gas amount of rear burning-out zone injection
Account for the 5～15% of total amount proportion.
The method of the present invention is comprised the following steps：
1) by the mesh moisture content of particle diameter 30～300 less than 2.0wt% brown coal, jet coal, ub-bituminous coal, bituminous coal in one kind or
It is several by coal gas convey flue gas enter to pressurize continuous feeders add carry out in 2～3s in fine coal upgrading conversion reactor it is quick
Conversion；
2) by feed coal rapid conversion generate containing unconverted carbonaceous particles of 30～100 purposes contained in oil gas and anti-
Answer device bed to pass through circulation refeed line and return fine coal upgrading conversion reactor；
3) by step 2) described in the unconverted carbonaceous particles of the mesh of removing 30～100 and reactor bed primary purifying coal gas
Continue through fine ash controller, microparticle catcher and further remove wherein 100～300 mesh therein with compared with Large ratio surface
The fine solid particle of product, return fine coal upgrading conversion reactor as solid thermal carriers；
4) by step 2), 3) described in through 3-stage dust-removal purification containing oil gas through oil-gas knockout tower, coal gas depth
Removing oil tower carries out the oil removing purified treatment of coal gas；
5) step 4) described in through oil-gas isolation of purified process purification coal gas enter back into desulfurizing tower removing raw gas in
Hydrogen sulfide, the tar of extraction sends into tar storage tank；
6) by step 5) described in through udst separation, oil-gas separate, desulfurizing and purifying process dust content be 1.0～
5.0/Nm3Purification coal gas passes sequentially through again the burner hearth jet for gas and heat convection section coal gas spray on burner hearth on differing heights
Burnt in mouth point level Four injection boiler, cold air point three branch roads Jing after air preheater preheating, respectively by firing wind again
Nozzle, combustion air nozzle, an afterburning wind nozzle injection boiler, after coal gas injection boiler, point three combustion zones are primary combustion
Area, secondary conbustion zone, rear burning-out zone are burnt, and the combustion reference temperature of primary combustion zone coal gas is 1000～1300 DEG C；It is secondary
The combustion reference temperature of level combustion zone coal gas is 900～1100 DEG C；Afterwards the flue-gas temperature scope of burning-out zone is 800～900 DEG C, its
It is 85～95% that the coal gas amount of middle primary combustion zone injection accounts for the proportion of total amount, and the coal gas amount of rear burning-out zone injection accounts for the ratio of total amount
Weigh about as 5～15%, the flue gas produced by rear burning-out zone crosses heat exchanger, again heat exchanger, economizer, air with boiler again
Preheater carries out heat convection, and the superheated steam and reheated steam produced by boiler overheating heat exchanger and again heat exchanger leads to respectively
Crossing superheated steam high pressure turbine, reheated steam intermediate pressure turbine drives generating set to generate electricity, and boiler bottom exhanst gas outlet is discharged
Flue gas Jing follow-up flue gas ash removal tower removing dust purification after again Jing air-introduced machine pressurization after be divided into three branch roads：All the way flue gas is through coal dust
Conveying flue gas pipeline is conveyed into pressurization continuous feeders as the raw material fine coal that conveying gas exports lock hopper, continuous feeders of pressurizeing
Stable transferring raw material coal dust is to fine coal upgrading conversion reactor；Second road flue gas then enters boiler by circulating flue gas pipeline
Burner hearth；Combustion air of combustion air nozzle injection is the circulating flue gas of circulating flue gas pipeline and the gaseous mixture of air, one
Oxygen content scope is 3～21vol% in secondary combustion air, is arranged outside the 3rd road Jing chimneys.
Compared with prior art, the present invention has following technical advantage：
1) coal-based clean oil product fuel production and fuel gas generation technology have been carried out it is highly integrated, improve coal resources product
The comprehensive added value of product, realizes the efficient of coal resources, cleaning and cascade utilization；
2) raw gas enters boiler and directly burns, and required excess air factor is less, and ignition temperature is big less than thermal NO x
1400 DEG C of the representative temperature that amount is produced, because fuel is coal gas, therefore generates without fuel type NOx, Quick-type NOx；
3) raw gas has carried out dedusting, desulfurizing and purifying before burning, SO in combustion product gases2、PM2.5And PM10Deng inhalable particles
Thing concentration is extremely low, is capable of achieving SO2、NOXUltra-low concentration discharge；
4) heavy metal such as hardly leaded in combustion product gases, chromium, cadmium, arsenic, hydrargyrum.
Description of the drawings
Fig. 1 is the overall structure diagram of the present invention.
In figure：1st, 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, fine ash controller are micro- 9, grain catcher 10, oil-gas knockout tower 11, coal gas depth removing oil
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 pipeline
19th, fire again 20, combustion air nozzle 21 of wind nozzle, afterburning wind nozzle 22, primary combustion zone 23, secondary conbustion zone 24,
Burning-out zone 25, flue-gas dust removal and purification tower 26, air-introduced machine 27, chimney 28, coal dust conveying flue gas 29, gasification-pyrolysis coupling afterwards
Reactor outlet 30, lime-ash storage tank 31, tar storage tank 32, boiler flue gas outlet 33, cold air.
Specific embodiment
In order that technical scheme and advantage are more clear apparent, below in conjunction with the accompanying drawings and embodiment is to the present invention
It is described in further detail.
Referring to Fig. 1, the inventive system comprises coal dust feed arrangement and the fine coal upgrading being connected with coal dust feed arrangement
Conversion reactor 6, the lower end of fine coal upgrading conversion reactor 6 is connected with lime-ash storage tank 30, the output of fine coal upgrading conversion reactor 6
Raw gas Jing fine coal upgradings conversion reactor 6 containing tar and ash outlet 29 is connected with dedusting, segregation apparatuss, by dedusting, divides
Tar in the raw gas reclaimed from device sends into tar storage tank 31, and dedusting, the gas exit Jing desulfurizing towers 12 of segregation apparatuss take off
Sulfur after-purification coal gas enters primary by the burner hearth jet for gas 14,15,16 on differing heights on the burner hearth of boiler 13 respectively
Combustion zone 22, by heat convection section jet for gas 17 the rear burning-out zone 24 of boiler 13, the Jing air preheaters of cold air 33 are entered
Point three branch roads after preheating, respectively by firing wind nozzle 19 again into 24, combustion air nozzle 20 of rear burning-out zone of boiler 13
Secondary conbustion zone 23 is entered into boiler bottom entrance, afterburning wind nozzle 21, boiler 13 crosses heat exchanger and reheating heat exchanger institute
The superheated steam and reheated steam of generation drives generating set by superheated steam high pressure turbine, reheated steam intermediate pressure turbine respectively
Generate electricity, the flue gas that the bottom exhanst gas outlet 32 of boiler 13 is discharged Jing air-introduced machines 26 again Jing after the udst separation of follow-up flue gas ash removal tower 25
It is divided into three branch roads after pressurization：All the way flue gas sends into coal dust feed arrangement, the second road flue gas through coal dust conveying flue gas pipeline 28
The burner hearth sent into by the combustion air nozzle 20 of 18 Jing boilers of circulating flue gas pipeline, 35 bottom one time；The outer row of 3rd road Jing chimney 27.
Wherein dedusting, segregation apparatuss include fine ash controller 8, grain catcher 9, the oil-gas knockout tower 10 being sequentially connected
With coal gas depth removing oil tower 11, the wherein entrance of fine ash controller 8 is connected with the outlet of fine coal upgrading conversion reactor 6, coal gas depth
The outlet of degree removing oil tower 11 is connected with the entrance of desulfurizing tower 12, and fine ash controller 8, the outlet of the lower end of grain catcher 9 pass through pipeline
It is connected with fine coal upgrading conversion reactor 6, oil-gas knockout tower 10 and the lower end of coal gas depth removing oil tower 11 export and tar storage tank 31
It is connected.
Coal dust feed arrangement includes that the raw material coal bunker 1, feed storage tank 2, feed hopper 3, lock hopper 4 and the pressurization that are sequentially connected are continuous
Feeder 5, the outlet of flue gas pipeline 28 is connected with the entrance of pressurization continuous feeders 5.
Circulation refeed line 7 is additionally provided with fine coal upgrading conversion reactor 6, circulation refeed line 7 is formed by internals
Class spiral type or class involute-type runner so that 70～80% in the carbonaceous particles of the mesh of particle size range 30～100 are captured
And loop back reaction zone.
Fine coal upgrading conversion reactor 6 be circulating fluid bed reactor, 5～20 mutation in its top pyrolysis section riser
Undergauge ratio, pyrolysis dry gas yield is 3.0～4.5Nm3/ kg dry pulverized coals, coal gas Lower heat value is 4000～6500kJ/Nm3。
Desulfurizing tower 12 adopts the wet desulphurization of spray column, spray tower or drip bed-type, or dry method packed tower desulfurization, or wet method
Desulfurization and the cascaded structure of dry method packed tower desulfurization, the H in coal gas Jing after desulfurizing tower process2S contents are less than 5.0mg/Nm3。
The excess air coefficient of primary combustion zone 22 is 0.7～0.9；The excess air coefficient of secondary conbustion zone 23 be 0.8～
1.0；Afterwards the excess air coefficient of burning-out zone 24 is 1.05～1.1.The coal gas amount of the injection of primary combustion zone 22 accounts for the 85 of total amount proportion
～95%, the coal gas amount of the injection of rear burning-out zone 24 accounts for the 5～15% of total amount proportion.
The method of the present invention is as follows：
1) by the mesh moisture content of particle diameter 30～300 less than 2.0wt% brown coal, jet coal, ub-bituminous coal, bituminous coal in one kind or
It is several that fine coal upgrading conversion reaction is added by pressurization continuous feeders 5 under 0.1～2.0MPa pressure by coal gas conveying flue gas
Rapid conversion is carried out in 2～3s in device 6；
2) by feed coal rapid conversion generate containing unconverted carbonaceous particles of 30～100 purposes contained in oil gas and anti-
Answer device bed to pass through circulation refeed line 7 and return fine coal upgrading conversion reactor 6；
3) by step 2) described in the unconverted carbonaceous particles of the mesh of removing 30～100 and reactor bed primary purifying coal gas
Continuing through fine ash controller 8, microparticle catcher 9 further expels wherein 100～300 mesh therein to have compared with Large ratio surface
The fine solid particle of product, return fine coal upgrading conversion reactor 6 as solid thermal carriers；
4) by step 2), 3) described in through 3-stage dust-removal purification containing oil gas through oil-gas knockout tower 10, coal gas depth
Degree removing oil tower 11 carries out the oil removing purified treatment of coal gas；
5) step 4) described in through oil-gas isolation of purified process purification coal gas enter back into desulfurizing tower 12 removing raw gas
In hydrogen sulfide, H in coal gas2S contents are less than 5.0mg/Nm3, dust content 1.0～5.0/Nm of scope3, tar feeding Jiao of extraction
Oil tank 31；
6) by step 5) described in through udst separation, oil-gas separate, desulfurizing and purifying process dust content be 1.0～
5.0/Nm3Purification coal gas passes sequentially through again the burner hearth jet for gas 14,15,16 and heat convection on burner hearth on differing heights
Burnt in 17 points of level Four injection boilers 13 of section jet for gas, point three branch roads Jing after air preheater preheating of cold air 33,
Respectively boiler is injected by firing 19, combustion air nozzle 20 of wind nozzle, afterburning wind nozzle 21 again, after coal gas injection boiler, point
Three main combustion zone primary combustion zones 22, secondary conbustion zone 23, rear burning-out zones 24 are burnt, primary combustion zone (22) coal
The combustion reference temperature of gas is 1000～1300 DEG C；The combustion reference temperature of secondary conbustion zone (23) coal gas is 900～1100 DEG C；
Afterwards the flue-gas temperature scope of burning-out zone (24) is 800～900 DEG C, and the coal gas amount of the wherein injection of primary combustion zone 22 accounts for the ratio of total amount
Weigh about as 85～95%, the coal gas amount of the injection of rear burning-out zone 24 accounts for the proportion of total amount and is about 5～15%, produced by rear burning-out zone 24
Flue gas again with boiler 13 cross heat exchanger, again heat exchanger, economizer, air preheater carry out heat convection, boiler 13
Cross superheated steam and reheated steam produced by heat exchanger and again heat exchanger and pass through superheated steam high pressure turbine, reheating respectively
Steam intermediate pressure turbine drives generating set to generate electricity, and the flue-gas temperature that the bottom exhanst gas outlet 32 of boiler 13 is discharged is 100～120
℃、NOXConcentration range is in 1～5mg/Nm3.After purifying by the follow-up removing dust of flue gas ash removal tower 25 again Jing after the pressurization of air-introduced machine 26
It is divided into three branch roads：All the way flue gas is defeated as the raw material fine coal that conveying gas exports lock hopper 4 through coal dust conveying flue gas pipeline 28
Pressurization continuous feeders 5 is sent into, the stable transferring raw material coal dust of pressurization continuous feeders 5 is to fine coal upgrading conversion reactor 6；The
Two road flue gases then enter the burner hearth of boiler 35 by circulating flue gas pipeline 18；Combustion air of injection of combustion air nozzle 20
For the gaseous mixture of circulating flue gas and the air of circulating flue gas pipeline 18, in a combustion air oxygen content scope be 3～
21vol%, the outer row of the 3rd road Jing chimney 27.
The 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 mutation undergauge ratio, bottom gasification section produce high temperature, flow up gas-solid fluid-mixing at a high speed in top pyrolysis section formation office
The low-pressure area in portion even negative pressuren zone, with this realize being pyrolyzed section feeding and gas-solid fluid-mixing moment carry out quickly, efficient heat transfer and
Mass transfer.
The pyrolysis dry gas yield of fine coal upgrading conversion reactor 6 is 3.0～4.5Nm3/ kg dry pulverized coals, coal gas Lower heat value
For 4000～6500kJ/Nm3。
The combustion reference temperature of the coal gas of primary combustion zone of the present invention 22 is 1000～1300 DEG C；The coal gas of secondary conbustion zone 23
Combustion reference temperature is 900～1100 DEG C；Afterwards the flue-gas temperature scope of burning-out zone 24 is 800～900 DEG C.
Claims (9)
1. a kind of coal gas low nitrogen oxide burning generating multi-joint-production apparatus, it is characterised in that：Including coal dust feed arrangement and with
Connected fine coal upgrading conversion reactor (6) of coal dust feed arrangement, fine coal upgrading conversion reactor (6) lower end is connected with lime-ash storage
Tank (30), raw gas Jing fine coal upgrading conversion reactor (6) containing tar and ash of fine coal upgrading conversion reactor (6) output
Outlet (29) is connected with dedusting, segregation apparatuss, and the tar in the raw gas reclaimed by dedusting, segregation apparatuss sends into tar storage tank
(31), purification coal gas of the coal gas of dedusting, segregation apparatuss output Jing after desulfurizing tower (12) desulfurization is respectively by positioned at boiler (13)
Burner hearth jet for gas (14,15,16) on burner hearth on differing heights into primary combustion zone (22), by heat convection section coal gas
Nozzle (17) into boiler (13) rear burning-out zone (24), cold air (33) point three branch roads Jing after air preheater preheating, point
Tong Guo not again fire wind nozzle (19) and enter primary combustion into the rear burning-out zone (24) of boiler (13), a combustion air nozzle (20)
, into secondary conbustion zone (23), boiler (13) crosses heat exchanger and the again mistake produced by heat exchanger for area, afterburning wind nozzle (21)
Vapourss and reheated steam drive generating set to generate electricity by superheated steam high pressure turbine, reheated steam intermediate pressure turbine respectively, pot
The flue gas that stove (13) bottom exhanst gas outlet (32) is discharged Jing air-introduced machines again Jing after the udst separation of follow-up flue gas ash removal tower (25)
(26) it is divided into three branch roads after pressurizeing：All the way flue gas through coal dust conveying flue gas pipeline (28) send into coal dust feed arrangement, second
Road flue gas sends into burner hearth by the combustion air nozzle (20) of circulating flue gas pipeline (18) Jing boilers (35) bottom one time；3rd road Jing cigarettes
Chimney (27) is arranged outward.
2. coal gas low nitrogen oxide burning generating multi-joint-production apparatus according to claim 1, it is characterised in that：Described removes
Dirt, segregation apparatuss include fine ash controller (8), grain catcher (9), oil-gas knockout tower (10) and the coal gas depth being sequentially connected
Degree removing oil tower (11), wherein fine ash controller (8) entrance is connected with the outlet of fine coal upgrading conversion reactor (6), coal gas depth
The outlet of removing oil tower (11) is connected with the entrance of desulfurizing tower (12), and fine ash controller (8), the outlet of grain catcher (9) lower end are logical
Cross pipeline to be connected with fine coal upgrading conversion reactor (6), oil-gas knockout tower (10) and coal gas depth removing oil tower (11) lower end export
It is connected with tar storage tank (31).
3. coal gas low nitrogen oxide burning generating multi-joint-production apparatus according to claim 1, it is characterised in that：Described powder
Circulation refeed line (7) is additionally provided with coal upgrading conversion reactor (6), the class spiral type or class of refeed line (7) formation is circulated gradually
The type that bursts at the seams runner so that 70～80% in the carbonaceous particles of the mesh of particle size range 30～100 are captured and loop back fine coal upgrading
The reaction zone of conversion reactor (6).
4. coal gas low nitrogen oxide burning generating multi-joint-production apparatus according to claim 1, it is characterised in that：Described powder
Coal upgrading conversion reactor (6) is circulating fluid bed reactor, and upgrading conversion dry gas yield is 3.0～4.5Nm3/ kg dry coals
Powder, coal gas Lower heat value is 4000～8000kJ/Nm3。
5. coal gas low nitrogen oxide burning generating multi-joint-production apparatus according to claim 1, it is characterised in that：Described powder
There is in the riser of coal upgrading conversion reactor (6) top 5～20 mutation undergauge ratio, make high temperature that bottom gasification section produces,
Gas-solid fluid-mixing is flowed up at a high speed forms the low-pressure area even negative pressuren zone of local on fine coal upgrading conversion reactor (6) top, it is real
Now be pyrolyzed section feeding and gas-solid fluid-mixing moment carry out quickly, efficient heat transfer and mass transfer.
6. coal gas low nitrogen oxide burning generating multi-joint-production apparatus according to claim 1, it is characterised in that：Described is de-
Sulfur tower (12) using spray column, spray tower or drip bed-type wet desulphurization, or dry method packed tower desulfurization, or wet desulphurization with it is dry
The cascaded structure of method packed tower desulfurization, the H in coal gas Jing after desulfurizing tower process2S contents are less than 5.0mg/Nm3。
7. coal gas low nitrogen oxide burning generating multi-joint-production apparatus according to claim 1, it is characterised in that：Described is first
Level combustion zone (22) excess air coefficient is 0.7～0.9；Secondary conbustion zone (23) excess air coefficient is 0.8～1.0；After-burning
To the greatest extent area (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 characterised in that：Described is first
The coal gas amount of level combustion zone (22) injection accounts for the 85～95% of total amount proportion, and the coal gas amount of rear burning-out zone (24) injection accounts for total amount ratio
The 5～15% of weight.
9. a kind of coal gas low nitrogen oxide burning generating Poly-generation method of device as claimed in claim 1, it is characterised in that bag
Include following steps：
1) one or more in brown coal, jet coal, ub-bituminous coal, the bituminous coal by the mesh moisture content of particle diameter 30～300 less than 2.0wt%
Flue gas is conveyed by coal gas to enter to carry out in 2～3s in continuous feeders of pressurizeing (5) addition fine coal upgrading conversion reactor (6) soon
Speed conversion；
2) by the generation of feed coal rapid conversion containing the unconverted carbonaceous particles of 30～100 purposes and reactor contained in oil gas
Bed returns fine coal upgrading conversion reactor (6) by circulation refeed line (7)；
3) by step 2) described in the unconverted carbonaceous particles of the mesh of removing 30～100 and reactor bed primary purifying coal gas continue
Wherein 100～300 mesh therein are further removed by fine ash controller (8), microparticle catcher (9) to have compared with Large ratio surface
Fine solid particle of long-pending, return fine coal upgrading conversion reactor (6) as solid thermal carriers；
4) by step 2), 3) described in through 3-stage dust-removal purification containing oil gas through oil-gas knockout tower (10), coal gas depth
Removing oil tower (11) carries out the oil removing purified treatment of coal gas；
5) step 4) described in through oil-gas isolation of purified process purification coal gas enter back into desulfurizing tower (12) removing raw gas in
Hydrogen sulfide, the tar of extraction sends into tar storage tank (31)；
6) by step 5) described in through udst separation, oil-gas separate, desulfurizing and purifying process dust content be 1.0～5.0/Nm3
Purification coal gas passes sequentially through again burner hearth jet for gas (14,15,16) and the heat convection section coal on burner hearth on differing heights
Burnt in gas jets (17) point level Four injection boiler (13), cold air (33) divides three Jing after air preheater preheating
Road, injects boiler, coal gas injection by firing wind nozzle (19), combustion air nozzle (20), afterburning wind nozzle (21) again respectively
After boiler, points of three combustion zones are that primary combustion zone (22), secondary conbustion zone (23), rear burning-out zone (24) are burnt, primary
The combustion reference temperature of 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；Afterwards the flue-gas temperature scope of burning-out zone (24) is 800～900 DEG C, wherein the coal of primary combustion zone (22) injection
It is 85～95% that tolerance accounts for the proportion of total amount, and it is 5～15% that the coal gas amount that rear burning-out zone (24) is injected accounts for the proportion of total amount, after-burning
Flue gas to the greatest extent produced by area (24) again with boiler (13) cross heat exchanger, again heat exchanger, economizer, air preheater are carried out
Heat convection, the heat exchanger excessively of boiler 13 and the again superheated steam and reheated steam produced by heat exchanger are respectively by overheated steaming
Vapour high pressure turbine, reheated steam intermediate pressure turbine drive generating set to generate electricity, what boiler (13) bottom exhanst gas outlet (32) was discharged
Flue gas Jing follow-up flue gas ash removal tower (25) removing dust purification after again Jing air-introduced machine (26) pressurization after be divided into three branch roads：Flue gas all the way
Through coal dust conveying flue gas pipeline (28) the raw material fine coal that lock hopper (4) is exported is conveyed into pressurization continuous feeders as conveying gas
(5) the stable transferring raw material coal dust of continuous feeders (5) of, pressurizeing is to fine coal upgrading conversion reactor (6)；Second road flue gas then leads to
Circulating flue gas pipeline (18) is crossed into the burner hearth of boiler (35)；Combustion air of combustion air nozzle (20) injection is circulation
The circulating flue gas of flue gas pipeline (18) and the gaseous mixture of air, oxygen content scope is 3～21vol% in a combustion air, the
Arrange outward on three roads Jing chimneys (27).
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| CN107541297B (en) * | 2017-09-06 | 2018-08-14 | 恒盛能源股份有限公司 | A kind of dustless environment protecting coal fired power generation method |
| CN109404950A (en) * | 2018-09-27 | 2019-03-01 | 哈尔滨工业大学 | A kind of boiler flue gas treatment system of high efficiency, low cost |
| CN110129100B (en) * | 2019-05-28 | 2023-12-22 | 彭万旺 | Efficient combustion system and method |
| CN111156535B (en) * | 2020-01-20 | 2024-04-26 | 山西平朔煤矸石发电有限责任公司 | Double fluidized bed pyrolysis combustion waste heat utilization system and method |
| CN114963160A (en) * | 2022-05-17 | 2022-08-30 | 哈尔滨工业大学 | FW type W flame boiler device and method for coupling combustion of gasification crude synthesis gas and coal |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE920485T1 (en) * | 1995-11-28 | 1999-09-16 | Foster Wheeler Energia Oy | METHOD AND DEVICE FOR THE USE OF FUEL OR WASTE MATERIAL IN ENERGY PRODUCTION |
| CN1693428A (en) * | 2005-04-21 | 2005-11-09 | 上海交通大学 | Gas heating and electric combined supply application system using shale |
| CN101108986A (en) * | 2007-08-21 | 2008-01-23 | 陕西秦能天脊科技有限公司 | Gray melting poly-fluid bed powder coal gasification method |
| CN101761920A (en) * | 2009-12-16 | 2010-06-30 | 上海理工大学 | Method and device for burning low NOx by utilizing reburning of pulverized coal pyrolysis gas |
| CN101865451A (en) * | 2010-05-24 | 2010-10-20 | 叶力平 | Biomass high-temperature flue gas gasification combination coal burning boiler and low-pollution combustion method thereof |
| CN102373089A (en) * | 2010-08-18 | 2012-03-14 | 中国科学院过程工程研究所 | Coal gasification method |
| CN103820170A (en) * | 2014-02-21 | 2014-05-28 | 陕西延长石油（集团）有限责任公司碳氢高效利用技术研究中心 | Apparatus for converting tar component and carbonaceous particles in raw gas, and method thereof |
| CN204058390U (en) * | 2014-03-28 | 2014-12-31 | 上海锅炉厂有限公司 | Solid fuel classification gasification-burning double bed polygenerations systeme |
| CN104403697A (en) * | 2014-11-26 | 2015-03-11 | 陕西延长石油（集团）有限责任公司 | Flue gas emission pollutant control process device for coal-fired boiler in power plant and control method |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6892654B2 (en) * | 2002-04-18 | 2005-05-17 | Eastman Chemical Company | Coal gasification feed injector shield with oxidation-resistant insert |
-
2015
- 2015-03-31 CN CN201510150148.8A patent/CN104864391B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE920485T1 (en) * | 1995-11-28 | 1999-09-16 | Foster Wheeler Energia Oy | METHOD AND DEVICE FOR THE USE OF FUEL OR WASTE MATERIAL IN ENERGY PRODUCTION |
| CN1693428A (en) * | 2005-04-21 | 2005-11-09 | 上海交通大学 | Gas heating and electric combined supply application system using shale |
| CN101108986A (en) * | 2007-08-21 | 2008-01-23 | 陕西秦能天脊科技有限公司 | Gray melting poly-fluid bed powder coal gasification method |
| CN101761920A (en) * | 2009-12-16 | 2010-06-30 | 上海理工大学 | Method and device for burning low NOx by utilizing reburning of pulverized coal pyrolysis gas |
| CN101865451A (en) * | 2010-05-24 | 2010-10-20 | 叶力平 | Biomass high-temperature flue gas gasification combination coal burning boiler and low-pollution combustion method thereof |
| CN102373089A (en) * | 2010-08-18 | 2012-03-14 | 中国科学院过程工程研究所 | Coal gasification method |
| CN103820170A (en) * | 2014-02-21 | 2014-05-28 | 陕西延长石油（集团）有限责任公司碳氢高效利用技术研究中心 | Apparatus for converting tar component and carbonaceous particles in raw gas, and method thereof |
| CN204058390U (en) * | 2014-03-28 | 2014-12-31 | 上海锅炉厂有限公司 | Solid fuel classification gasification-burning double bed polygenerations systeme |
| CN104403697A (en) * | 2014-11-26 | 2015-03-11 | 陕西延长石油（集团）有限责任公司 | Flue gas emission pollutant control process device for coal-fired boiler in power plant and control method |
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