CN107903924A - A kind of uplink heat accumulating type fine coal fast pyrogenation reaction system and method - Google Patents
A kind of uplink heat accumulating type fine coal fast pyrogenation reaction system and method Download PDFInfo
- Publication number
- CN107903924A CN107903924A CN201711166196.1A CN201711166196A CN107903924A CN 107903924 A CN107903924 A CN 107903924A CN 201711166196 A CN201711166196 A CN 201711166196A CN 107903924 A CN107903924 A CN 107903924A
- Authority
- CN
- China
- Prior art keywords
- gas
- pyrolysis
- semicoke
- uplink
- condenser
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000003245 coal Substances 0.000 title claims abstract description 53
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 35
- 238000000034 method Methods 0.000 title claims abstract description 26
- 238000000197 pyrolysis Methods 0.000 claims abstract description 167
- 238000005338 heat storage Methods 0.000 claims abstract description 55
- 230000008676 import Effects 0.000 claims abstract description 23
- 238000009825 accumulation Methods 0.000 claims abstract description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 45
- 239000000047 product Substances 0.000 claims description 32
- 239000002817 coal dust Substances 0.000 claims description 27
- 238000001556 precipitation Methods 0.000 claims description 24
- 239000004519 grease Substances 0.000 claims description 17
- 239000012263 liquid product Substances 0.000 claims description 16
- 238000010438 heat treatment Methods 0.000 claims description 14
- 238000009826 distribution Methods 0.000 claims description 13
- 238000002485 combustion reaction Methods 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 8
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 239000007787 solid Substances 0.000 claims description 7
- 238000003860 storage Methods 0.000 claims description 7
- 238000004064 recycling Methods 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 239000000843 powder Substances 0.000 claims description 4
- 230000009471 action Effects 0.000 claims description 3
- 230000008569 process Effects 0.000 abstract description 9
- 239000007789 gas Substances 0.000 description 137
- 239000011269 tar Substances 0.000 description 44
- 239000000428 dust Substances 0.000 description 15
- 238000000926 separation method Methods 0.000 description 15
- 239000002245 particle Substances 0.000 description 10
- 238000004458 analytical method Methods 0.000 description 7
- 238000005979 thermal decomposition reaction Methods 0.000 description 7
- 239000012265 solid product Substances 0.000 description 6
- 239000000969 carrier Substances 0.000 description 5
- 239000003077 lignite Substances 0.000 description 5
- 238000012546 transfer Methods 0.000 description 5
- 229910052573 porcelain Inorganic materials 0.000 description 4
- 239000007921 spray Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- 230000026676 system process Effects 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000005299 abrasion Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 230000005855 radiation Effects 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 206010068052 Mosaicism Diseases 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 210000000038 chest Anatomy 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000000921 elemental analysis Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000012634 fragment Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 210000003765 sex chromosome Anatomy 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
Abstract
The present invention relates to a kind of uplink heat accumulating type fine coal fast pyrogenation reaction system and method.System includes uplink heat storage type pyrolysis stove, cyclone separator, semicoke condenser and oil-gas condenser, uplink heat storage type pyrolysis stove includes furnace body and radiant tube, the top of furnace body is equipped with product exit, the bottom of furnace body is equipped with gas feed and reaction-ure feeding mouth, radiant tube is arranged in the furnace body, and radiant tube is one group of heat accumulation type radiant tube being vertically intervally arranged；The product inlet of cyclone separator is connected with the product exit of uplink heat storage type pyrolysis stove；The semicoke import of semicoke condenser is connected with the semicoke outlet of cyclone separator；The oil and gas import of oil-gas condenser is connected with the oil gas vent of cyclone separator.The present invention realizes effective control of pyrolytic reaction depth and reaction process, improves conversion ratio, improves target product yield；Technological process is simple, temperature control is accurate, temperature adjustment is convenient, reduces the failure rate of system, improves the thermal efficiency of system, reduces tar dustiness.
Description
Technical field
The present invention relates to pulverized coal pyrolysis technical field, more particularly to a kind of uplink heat accumulating type fine coal fast pyrogenation reaction system
And method.
Background technology
Coal is one of conventional resource that proved reserves are the abundantest in the world, as coal production maximum in the world and
Country of consumption, the energy resource structure feature in China are rich coal, oil-poor, few gas.It is the urgent of national product that the clean and effective of coal, which utilizes,
Demand.At this stage, the coal resources in China mainly have several Land use systems such as burning, gasification, liquefaction, pyrolysis.Coal directly fires
Burning can produce heat, and efficiency is than relatively low, and emission would seriously pollute the environment；Coal Gasification, liquefaction process generally require full
The reaction condition of the harshness such as sufficient high temperature, high pressure, oxygen-enriched, this cost requirement to reactor performance and technical process are higher.Phase
Than in these types of Land use systems, pyrolysis of coal converts coal into solid-state, liquid and gaseous product, there are obvious advantage and prospect.
At present, from the point of view of mode of heating, domestic and international existing pyrolytic process uses porcelain ball and thermal decomposition product semicoke conduct more
Coal gas after solid thermal carriers, or product char Gasification is as mode of heatings such as gas heat carriers.But these mode of heatings are related to
The processes such as heating, separation to heat carrier, can cause system process to be grown, system failure rate is higher.
Moreover, finding that porcelain ball is heated to more than 600 DEG C and recycled repeatedly in experiment, abrasion sex chromosome mosaicism can be produced；It is glutinous
Knot property coal can be attached in pyrolytic process on porcelain ball, and only non-caking coal and Iight sticky coal can be used for the technique, usually
Tar yield is not high.
During using semicoke as heat carrier, since a large amount of burnt tiny fragments of stone, coal, etc. fine graineds are brought into tar, solid particulate matter in tar
Content is up to 40%-50%, and the processing and utilization to tar bring difficulty；Using can be because of tar and particle during caking coal
Aggegation and cause failure；The semicoke of coal and heat is mixed using mechanical agitation, abrasion is more serious, and equipment amplification, which exists, asks
Topic.
Using gas as heat carrier, be related to heating, separate, cause system process to be grown, system failure rate compared with
It is high；Using combustible gas as heat carrier, combustible gas in warm if there is leakage phenomenon, may be with the heating of heating chamber
Media contact, brings security risk.
In short, the solid thermal carriers such as semicoke, porcelain ball have seriously affected the air heats such as the disposal ability of pyrolysis furnace apparatus, coal gas
There is also larger security risk for carrier preheating.
In addition, the pyrolysis oven used at present, majority is fixed bed, or has the function of downflow fluidized bed, and pulverized coal pyrolysis is not
Abundant or volatility product twice decomposition is serious, causes conversion ratio and target product yield too low.It would therefore be highly desirable to research and develop a kind of new
Type pyrolytic process.
The content of the invention
In view of the above-mentioned problems, the present invention is intended to provide a kind of uplink heat accumulating type fine coal fast pyrogenation reaction system and method,
To simplify system process, the failure rate of system is reduced so that system temperature control is accurate, temperature adjustment is convenient, to pyrolytic reaction depth
It control effectively with reaction process, improves converting rate, improve target product yield, improves the thermal efficiency of system.
The present invention provides a kind of uplink heat accumulating type fine coal fast pyrogenation reaction system, and the system comprises uplink heat-accumulation type hot
Solution stove, cyclone separator, semicoke condenser and oil-gas condenser, the uplink heat storage type pyrolysis stove include furnace body and radiant tube,
The top of the furnace body is equipped with product exit, and the bottom of the furnace body is equipped with gas feed and reaction-ure feeding mouth, the reaction
Position of the thing feed inlet on the vertical direction of the furnace body is higher than the gas feed；The radiant tube is arranged on the furnace body
Interior, above the reaction-ure feeding mouth, the radiant tube is one group of heat accumulation type radiant tube being vertically intervally arranged；
The product inlet of the cyclone separator is connected with the product exit of the uplink heat storage type pyrolysis stove；The semicoke condenser
Semicoke import is connected with the semicoke outlet of the cyclone separator；The oil and gas import of the oil-gas condenser and the cyclonic separation
The oil gas vent of device is connected.
Above-mentioned system, the uplink heat storage type pyrolysis stove further include gas distribution grid, and the gas distribution grid is arranged at
In the furnace body, below the reaction-ure feeding mouth, the gas feed connection is distributed on the gas distribution grid
One group of air inlet.
Above-mentioned system, the radiant tube both ends are both provided with burner, the burner respectively with outside the furnace body
Storage heater be connected, the burner and the storage heater correspond.
Above-mentioned system, the system also includes semicoke collector, electric precipitation decontaminating separator, tar well, pyrolysis
Gas condenser, oil water separator, pyrolysis water collector and pyrolysis gas collector；The semicoke collector and the semicoke condenser
Condensation semicoke outlet be connected；The gas-liquid import of the electric precipitation decontaminating separator and the gas liquid outlet phase of the oil-gas condenser
Even；The tar import of the tar well is connected with the tar outlet of the electric precipitation decontaminating separator；The pyrolysis air cooling
The oil-containing water pyrolysis gas import of condenser is connected with the oil-containing water pyrolysis gas outlet of the electric precipitation decontaminating separator；The grease point
Grease import from device is connected with the grease outlet of the pyrolysis gas condenser；The pyrolysis water collector and the water-oil separating
The pyrolysis water out of device is connected；The pyrolysis gas collector is connected with the pyrolysis gas outlet of the pyrolysis gas condenser.
Above-mentioned system, is equipped with heat exchanger in the semicoke condenser, for recycling the heat of semicoke, the heat exchanger
Pyrolysis gas import is connected with the pyrolysis gas collector, and the pyrolysis gas outlet of the heat exchanger is connected with powder coal charge device.
Above-mentioned system, the bottom of the uplink heat storage type pyrolysis stove are equipped with gas compressor, for being stored to the uplink
Hot type pyrolysis oven conveying hoisting gas；The gas access of the gas compressor is connected with the pyrolysis gas outlet of the heat exchanger.
The present invention also provides a kind of method being pyrolyzed using above-mentioned uplink heat accumulating type fine coal fast pyrogenation reaction system,
Including：
Coal dust is sent into the uplink heat storage type pyrolysis stove from the reaction-ure feeding mouth of the uplink heat storage type pyrolysis stove
In furnace body；
Lift gas is sent into the uplink by the gas feed from the bottom of the uplink heat storage type pyrolysis stove to store
In the furnace body of hot type pyrolysis oven；
The coal dust is set to be transported under the action of the lift gas along the lower to upper part of the uplink heat storage type pyrolysis stove
It is dynamic；
The coal dust is heated by the radiant tube and pyrolytic reaction occurs, generation gaseous state, liquid product and solid semicoke；
The product of pyrolytic reaction generation is discharged from the top of the uplink heat storage type pyrolysis stove；
Semicoke, gaseous state and liquid product are isolated by the cyclone separator；
Semicoke is collected by the semicoke condenser；
The gaseous state and liquid product are condensed by the oil-gas condenser.
Above-mentioned method, the fire box temperature of the uplink heat storage type pyrolysis stove is 450-950 DEG C, furnace pressure 0.2-
0.4Mpa；For the temperature control of the radiant tube at 500-1000 DEG C, the temperature difference on the single radiant tube is not higher than 30 DEG C.
Above-mentioned method, when producing tar, the fire box temperature of the furnace body is 500-700 DEG C；When medium-heat-value coal in production
During gas, the fire box temperature of the furnace body is 700-900 DEG C.
Above-mentioned method, after being exchanged heat by being passed through pyrolysis gas into the heat exchanger of the semicoke condenser, makes heating
Pyrolysis gas be sent into the bottom of the uplink heat storage type pyrolysis stove as lift gas, and by the uplink heat storage type pyrolysis furnace bottom
The coal dust in portion is fed through the inside of the uplink heat storage type pyrolysis stove.
The uplink heat accumulating type fine coal fast pyrogenation reaction technology of the present invention, by controlling lift gas flow, regulates and controls particle
Speed and particle residence time, so as to fulfill effective control for pyrolytic reaction depth and reaction process, improve conversion ratio,
Improve target product yield；The present invention uses more heat accumulation type radiant tubes, and heat source is provided for the coal dust in pyrolysis oven, without heat
Carrier and mechanical rotation device, technological process is simple, system temperature control is accurate, temperature adjustment is convenient, without gas and solid thermal carriers
Heating, separation process, reduce the failure rate of system, can combine convection current, heat transfer and radiant heat transfer control, improve system
The thermal efficiency, reduce tar dustiness.
Brief description of the drawings
Fig. 1 is uplink heat accumulating type fine coal fast pyrogenation reaction system schematic diagram of the embodiment of the present invention；
Fig. 2 is uplink heat accumulating type fine coal fast pyrogenation furnace structure schematic diagram of the embodiment of the present invention.
Embodiment
Below in conjunction with drawings and examples, the embodiment of the present invention is described in more details, so as to energy
The advantages of enough more fully understanding the solution of the present invention and various aspects.However, specific embodiments described below and implementation
Example is for illustrative purposes only, rather than limitation of the present invention.
As shown in Figure 1, the present invention provides a kind of uplink heat accumulating type fine coal fast pyrogenation reaction system, the system is mainly wrapped
Include uplink heat storage type pyrolysis stove 4, cyclone separator 6, semicoke condenser 8 and oil-gas condenser 11.
As shown in Fig. 2, the uplink heat storage type pyrolysis stove 4 includes furnace body 45 and radiant tube 46, the top of the furnace body 45
Equipped with product exit 47, the bottom of the furnace body 45 is equipped with gas feed 41 and reaction-ure feeding mouth 44, the reaction-ure feeding
44 position on the vertical direction of the furnace body of mouth is higher than the gas feed 41；The radiant tube 46 is arranged on the furnace body 45
Interior, above the reaction-ure feeding mouth 44, the radiant tube 46 is one group of heat accumulating type spoke being vertically intervally arranged
Penetrate pipe.
As shown in Figure 1, the product exit of the product inlet of the cyclone separator 6 and the uplink heat storage type pyrolysis stove 4
It is connected；The semicoke import of the semicoke condenser 8 is connected with the semicoke outlet of the cyclone separator 6；The oil-gas condenser
11 oil and gas import is connected with the oil gas vent of the cyclone separator 6.
To ensure that the reactant of pyrolysis furnace bottom there are enough momentum, and uniformly moved upwards along burner hearth, uplink heat accumulating type
Pyrolysis oven 4 further includes gas distribution grid 42.The gas distribution grid is arranged in the furnace body 45, positioned at the reaction-ure feeding
The lower section of mouth 44, the gas feed 41 connect one group of air inlet 43 being distributed on the gas distribution grid 42.
In said system, 46 both ends of radiant tube are both provided with burner, burner respectively with the storage heater phase outside furnace body
Even, the burner is corresponded with the storage heater.More heat accumulation type radiant tubes are the pyrolytic reaction in pyrolysis oven reactor
Heat source is provided.
Above-mentioned system, the system may also include semicoke collector 9, electric precipitation decontaminating separator 12, tar well
14th, gas condenser 16, oil water separator 18, pyrolysis water collector 20 and pyrolysis gas collector 22 are pyrolyzed；The semicoke collector 9
It is connected with the condensation semicoke outlet of the semicoke condenser 8；The gas-liquid import of the electric precipitation decontaminating separator 12 and the oil
The gas liquid outlet of gas condenser 11 is connected；The tar import of the tar well 14 and the electric precipitation decontaminating separator 12
Tar outlet is connected；The pyrolysis oil-containing water pyrolysis gas import of gas condenser 16 and containing for the electric precipitation decontaminating separator 12
Grease pyrolysis gas outlet is connected；The grease import of the oil water separator 18 and the grease of the pyrolysis gas condenser 16 export phase
Even；The pyrolysis water collector 20 is connected with the pyrolysis water out of the oil water separator 18；The pyrolysis gas collector 22 with
The pyrolysis gas outlet of the pyrolysis gas condenser 16 is connected.
Uplink heat storage type pyrolysis stove 4 is used to coal dust 1 being pyrolyzed, generation gaseous state, liquid and solid product and dust 5.Whirlwind
Separator 6 is used to pyrogenous origin product isolating semicoke 7 and gaseous state and liquid product 10.Semicoke condenser 8 is used to divide
Separate out the semicoke 7 come to condense, easy to the recycling of follow-up semicoke collector 9.
Gaseous state and liquid product 10 are separated through electric precipitation decontaminating separator 12 again after the condensation of oil-gas condenser 11, are obtained
To tar 13 and the pyrolysis gas 15 of oil-containing water.Isolated tar 13 is delivered to tar well 14 and carries out tar recycling, point
From obtained oil-containing water pyrolysis gas 15 further be delivered to pyrolysis gas condenser 16 condensed, obtain grease 17 and pyrolysis gas
21.Grease 17 is delivered to oil water separator 18 and is separated, and further obtains pyrolysis water 19 and tar 13.Tar 13 can be delivered to
Tar well 14 carries out tar recycling.Pyrolysis water 19 is further delivered to pyrolysis water collector 20 and is recycled.Pyrolysis gas 21
Pyrolysis gas collector 22 is delivered to be recycled.
Above-mentioned system, is equipped with heat exchanger in the semicoke condenser 8, for recycling the heat of semicoke, the heat exchanger
Pyrolysis gas import be connected with the pyrolysis gas collector 22, the pyrolysis gas outlet of the heat exchanger is connected with powder coal charge device 3.
Coal bunker 2 can be also set before feeder 3.
Above-mentioned system, the bottom of the uplink heat storage type pyrolysis stove are equipped with gas compressor 23, for the uplink
4 conveying hoisting gas 24 of heat storage type pyrolysis stove；The gas access of the gas compressor 23 and the pyrolysis gas of the heat exchanger go out
Mouth is connected.
Fine coal is pyrolyzed using said system, technique is as described below.
After dry coal dust 1 is crushed to 90% particle less than below 6mm, it is fitted into coal bunker 2, is sprayed into through feeder 3
4 bottom of uplink heat storage type pyrolysis stove.Row powder fan is installed in feeder 3, it, which is acted on, is pyrolyzed using 200-300 DEG C after preheating
Coal dust 1 in coal bunker 2 is sprayed into the top of uplink heat storage type pyrolysis stove 4 by gas 24.
4 fire box temperature of uplink heat storage type pyrolysis stove is 450-950 DEG C, the fire box temperature of uplink heat storage type pyrolysis stove 4 according to
Target pyrolysis gas quality or coal inlet amount specifically determine.Preferable temperature is 500-900 DEG C, if for the purpose of producing tar, stove
Bore temperature is arranged on 500-700 DEG C；If based on calorific value of gas in production, fire box temperature is arranged on 700-900 DEG C.
Furnace pressure is 0.2-0.4Mpa.Fire box temperature is provided by more radiant tubes, and radiant tube temperature control is in 500-
1000 DEG C, the temperature difference on single heat accumulation type radiant tube is not higher than 30 DEG C.Coal dust 1 in uplink heat storage type pyrolysis stove 4 is being lifted
Under the action of gas 24, while from the bottom of uplink heat storage type pyrolysis stove 4 to top movements, the fast pyrogenation in 2-10s, produces
A large amount of gaseous state, liquid and solid products and a small amount of dust 5.Product and dust 5 are discharged from the top of uplink heat storage type pyrolysis stove 4.
Gaseous state and liquid product are pyrolysis gas and water and tar, solid product are semicoke.
Wherein, the heat-accumulation combustion process of above-mentioned heat accumulation type radiant tube is as follows：Heat accumulation type radiant tube is set respectively at tube body both ends
Burner is equipped with, is entered to after fuel gas and the configured regenerative chamber preheating outside pyrolysis oven of temperature gas and is arranged on radiant tube A
Combustion reaction occurs for the burner of port, and the flame that one end burner combustion produces forms temperature when spraying along radiant tube direction
Gradient, i.e., along radiant tube A ends to the opposite side B ends of the radiant tube, temperature downward trend in gradient.After the completion of A end burnings, A ends
The flue gas that burning produces enters to B ends regenerative chamber, pre-heating fuel and combustion air, and the fuel and combustion air after preheating enter to radiation
Pipe B end burner, temperature gradient is also formed when the flame that other end burner combustion produces is spraying.Same radiant tube both ends
Burner alternating reversing combustion.
When the burner at both ends alternately burns, two temperature gradients formed are superimposed so that whole heat accumulating type
Radiant tube bulk temperature is evenly distributed.To ensure that pyrolysis oven internal-response material is heated evenly, on single heat accumulation type radiant tube
Temperature difference is not higher than 30 DEG C.In pyrolysis oven inside reactor, more heat accumulation type radiant tubes are vertically intervally arranged, and ensure each
Regional temperature is evenly distributed.Wherein, A ends can be the either port of radiant tube, and B ends are another corresponding to same radiant tube A ends
One end.
It is fed through from the product and dust 5 of the discharge of the top of uplink heat storage type pyrolysis stove 4 in high temperature cyclone separator 6, semicoke 7
Separated from gas, semicoke collector 9 is entered to by semicoke condenser 8, as solid product.Superfine dust is with cigarette
Gas is discharged.
Heat exchanger, such as heat exchange coil are added in semicoke condenser 8, recycles the heat of semicoke.Pyrolysis is passed through in heat exchange coil
Gas 21, pyrolysis gas 21 exchange heat with semicoke, and the 200-300 DEG C of pyrolysis gas 24 (also known as " lift gas ") after preheating, a part is passed through
Gas compressor 23, by 24 gas-phase transport of pyrolysis gas to the bottom of uplink heat storage type pyrolysis stove 4, and is used for uplink heat-accumulation type hot
The coal dust of 4 bottom of solution stove is fed through inside uplink heat storage type pyrolysis stove 4, in the radiation of radiant tube, conduction, convection current heat transfer effect
Under, pyrolytic reaction occurs；200-300 DEG C of gas 24 after part preheating is fed through feeder 3, is fed for coal dust.
The speed that gas 24 sprays into is 5-10m/s.Gas sprays into speed and is controlled by gas compressor 23, the speed of coal dust 1
Speed depending on lift gas 24.
300-700 DEG C of pyrolysis oil gas (gaseous state and liquid product) 10 is come out from high temperature cyclone separator 6 and is fed through oil gas
Condenser 11, by pyrolysis oil gas condensation to 70-90 DEG C.Gas mixture is pyrolyzed from oil-gas condenser 11 to purify by electric precipitation
Separator 12 is separated.The tar 13 separated from 12 lower part of electric precipitation decontaminating separator is fed through in tar well 14
As liquid form product.
The pyrolysis gas 15 for the oil-containing water separated from 12 top of electric precipitation decontaminating separator passes through pyrolysis gas condenser 16,
Condensed pyrolysis gas 21 and grease 17 are fed through pyrolysis 20 He of water collector from 16 upper and lower part of pyrolysis gas condenser respectively
In oil water separator 18.Tar 13 of the grease 17 further after the separation of oil water separator 18 is fed through in tar well 14,
Pyrolysis water 19 after separation is fed through in pyrolysis water collector 20.Meanwhile through non-purified complete in electric precipitation decontaminating separator 12
Oil gas circulation be again introduced into oil-gas condenser 11, carry out dust separation, obtain tar 13 and pyrolysis gas 21.
The uplink heat accumulating type fine coal fast pyrogenation reaction system of the present invention, by controlling lift gas flow, regulates and controls particle
Speed and particle residence time, so as to fulfill effective control for pyrolytic reaction depth and reaction process, improve conversion ratio, carry
High target product yield；
The present invention uses more heat accumulation type radiant tubes, heat source is provided for the coal dust in pyrolysis oven, without heat carrier and machinery
Tumbler, technological process is simple, system temperature control is accurate, temperature adjustment is convenient, and heating without gas and solid thermal carriers, separated
Journey, reduces the failure rate of system.
The present invention can combine convection current, heat transfer and radiant heat transfer control, improve the thermal efficiency of system.
The present invention reduces tar dustiness compared with semicoke is as heat carrier.
The technique of the present invention is strong to coal adaptability, no matter equal for non-caking coal, Iight sticky coal, strong caking coal
It is suitable for.
Embodiment one
A kind of uplink heat accumulating type jet coal low-temperature rapid thermal solution reaction system, as shown in Figure 1.By it is dried containing
The jet coal of 8.64% moisture is crushed to below 6mm, and coal particle size distribution is as shown in table 1, the Industrial Analysis of coal dust and element point
Analysis is as shown in table 2 and table 3.Coal dust is fitted into coal bunker 2,4 bottom of uplink heat storage type pyrolysis stove is sprayed into through feeder 3.With pyrolysis
Coal dust 1 is fed through top by the gas of generation by 4 bottom of uplink heat storage type pyrolysis stove, is taken respectively at a temperature of different heating twice
Coal dust inlet amount is 100kg/ (m2﹒ s) carry out thermal decomposition test.Gas sprays into speed and is controlled by gas compressor 23, the speed of gas
Spend for 5m/s.The radiant tube surface temperature for being pyrolyzed uplink heat storage type pyrolysis stove 4 twice is respectively 600 DEG C and 500 DEG C, is pyrolyzed twice
Fire box temperature is respectively 500 DEG C and 450 DEG C, and the temperature difference on single heat accumulation type radiant tube is no more than 30 DEG C.Burner hearth is pyrolyzed twice
Pressure be respectively 0.3Mpa and 0.2Mpa.Coal dust 1 in uplink heat storage type pyrolysis stove 4 under lift gas effect, while from
Burner hearth bottom is to top movements, the fast pyrogenation in 5s, generates product and dust.Wherein, contain in first time thermal decomposition product
12.33% tar, 10.51% pyrolysis water, 12.51% pyrolysis gas and 64.65% semicoke.Contain in second of thermal decomposition product
12.55% tar, 11.36% pyrolysis water, 10.55% pyrolysis gas and 65.54% semicoke.Product and dust are from uplink heat-accumulation type hot
The discharge of the top of stove 4 is solved, and is fed through in 500 DEG C of cyclone separator 6.Semicoke is separated from the gas of cyclone separator 6,
It is fed through through the semicoke condenser 8 that excess temperature is 25 DEG C in semicoke collector 9, as solid product.In cyclonic separation gaseous state and
Liquid product removes dust, after impurity by electric precipitation decontaminating separator 12, and tar is from 12 lower part of electric precipitation decontaminating separator
Separate out to be fed through tar well 14.The gaseous state and liquid product separated from 12 top of electric precipitation decontaminating separator are through 25
DEG C pyrolysis gas condenser 16 condenses, and condensed pyrolysis gas and grease are fed through pyrolysis water from condenser upper and lower part respectively and receive
In storage 20 and oil water separator 18.Tar of the grease further after the separation of oil water separator 18 is fed through tar well 14
In, the pyrolysis water after separation is fed through in pyrolysis water collector 20.Meanwhile through non-purified complete in electric precipitation decontaminating separator 12
Oil gas circulation be again introduced into oil-gas condenser 11, carry out dust separation, obtain tar and pyrolysis gas.
1 jet coal particle diameter distribution of table
2 long flame proximate analysis of coal (%) of table
3 long flame ultimate analysis of coal (%) of table
M hereinadRepresent moisture；AadRepresent ash content；VadRepresent volatile matter；CadRepresent fixed carbon content；HadRepresent hydrogen
Content；OadRepresent oxygen content；NadRepresent nitrogen content；SadRepresent sulfur content.
Embodiment two
A kind of uplink heat accumulating type lignite medium temperature fast pyrogenation reaction system, as shown in Figure 1.By it is dried containing
The lignite of 15.10% or so moisture is crushed to below 6mm, and coal particle size distribution is as shown in table 4, the Industrial Analysis of coal dust and element
Analysis is as shown in table 5 and table 6.Coal dust is fitted into coal bunker 2,4 bottom of uplink heat storage type pyrolysis stove is sprayed into through feeder 3.With heat
Solve the gas produced and coal dust 1 is fed through top by 4 bottom of uplink heat storage type pyrolysis stove, at a temperature of different heating twice respectively
It is 100kg/ (m to take coal dust inlet amount2﹒ s) carry out thermal decomposition test.Gas sprays into speed and is controlled by gas compressor 23, gas
Speed is 7m/s.It is respectively 900 DEG C, 1000 DEG C to be pyrolyzed uplink heat storage type pyrolysis furnace radiating pipe surface temperature twice, is pyrolyzed twice
Fire box temperature is respectively 700 DEG C and 950 DEG C, and the temperature difference on single heat accumulation type radiant tube is no more than 30 DEG C.Burner hearth is pyrolyzed twice
Pressure be respectively 0.3Mpa and 0.4Mpa.Coal dust 1 is under lift gas effect in uplink heat storage type pyrolysis stove 4, while from stove
Thorax bottom is to top movements, the fast pyrogenation in 7s, generates product and dust.Wherein, 1.20% is contained in first time thermal decomposition product
Tar, 7.52% pyrolysis water, 38.71% pyrolysis gas and 52.27% semicoke.In second of thermal decomposition product containing 0.86% tar,
6.11% pyrolysis water, 41.85% pyrolysis gas and 51.18% semicoke.Product and dust are discharged from uplink heat storage type pyrolysis furnace roof portion,
And it is fed through in 800 DEG C of cyclone separator 6.Semicoke is separated from the gas of cyclone separator 6, is 25 DEG C through excess temperature
Semicoke condenser 8 be fed through in semicoke collector 9, as solid product.Gaseous state and liquid product are by electricity in cyclonic separation
After dust separation separator 12 removes dust, impurity, tar is separated from 12 lower part of electric precipitation decontaminating separator and is fed through Jiao
Oil interceptor 14.The gaseous state and liquid product separated from 12 top of electric precipitation decontaminating separator are through 25 DEG C of pyrolysis gas condensers
16 condensations, condensed pyrolysis gas and grease are fed through pyrolysis water collector 20 and grease point from condenser upper and lower part respectively
From in device 18.Tar of the grease further after the separation of oil water separator 18 is fed through in tar well 14, the heat after separation
Xie Shui is fed through in pyrolysis water collector 20.Meanwhile through non-purified complete oil gas circulation in electric precipitation decontaminating separator 12 again
It is secondary to enter in oil-gas condenser 11, dust separation is carried out, obtains tar and pyrolysis gas.
4 lignite particle diameter distribution of table
5 lignite Industrial Analysis (%) of table
6 lignite elemental analysis (%) of table
Finally it should be noted that：Obviously, above-described embodiment is only intended to clearly illustrate example of the present invention, and simultaneously
The non-restriction to embodiment.For those of ordinary skill in the field, can also do on the basis of the above description
Go out other various forms of changes or variation.There is no necessity and possibility to exhaust all the enbodiments.And thus drawn
Among the obvious changes or variations that Shen goes out is still in protection scope of the present invention.
Claims (10)
1. a kind of uplink heat accumulating type fine coal fast pyrogenation reaction system, it is characterised in that the system comprises uplink heat-accumulation type hot
Stove, cyclone separator, semicoke condenser and oil-gas condenser are solved, wherein,
The uplink heat storage type pyrolysis stove includes furnace body and radiant tube, and the top of the furnace body is equipped with product exit, the furnace body
Bottom be equipped with gas feed and reaction-ure feeding mouth, position of the reaction-ure feeding mouth on the vertical direction of the furnace body
Higher than the gas feed；
The radiant tube is arranged in the furnace body, and above the reaction-ure feeding mouth, the radiant tube is for one group along vertically
The heat accumulation type radiant tube that direction is intervally arranged；
The product inlet of the cyclone separator is connected with the product exit of the uplink heat storage type pyrolysis stove；The semicoke condensation
The semicoke import of device is connected with the semicoke outlet of the cyclone separator；The oil and gas import of the oil-gas condenser and the whirlwind
The oil gas vent of separator is connected.
2. system according to claim 1, it is characterised in that the uplink heat storage type pyrolysis stove further includes gas distribution
Plate, the gas distribution grid are arranged in the furnace body, and below the reaction-ure feeding mouth, the gas feed connection is equal
One group of air inlet being distributed on the gas distribution grid.
3. system according to claim 1, it is characterised in that the radiant tube both ends are both provided with burner, the combustion
Burner is connected with the storage heater outside the furnace body respectively, and the burner is corresponded with the storage heater.
4. system according to claim 1, it is characterised in that the system also includes semicoke collector, electric precipitation to purify
Separator, tar well, pyrolysis gas condenser, oil water separator, pyrolysis water collector and pyrolysis gas collector；The semicoke
Collector is connected with the condensation semicoke outlet of the semicoke condenser；The gas-liquid import of the electric precipitation decontaminating separator with it is described
The gas liquid outlet of oil-gas condenser is connected；The tar import of the tar well and the tar of the electric precipitation decontaminating separator
Outlet is connected；The oil-containing water pyrolysis gas import of the pyrolysis gas condenser and the oil-containing aquathermolysis of the electric precipitation decontaminating separator
Gas outlet is connected；The grease import of the oil water separator is connected with the grease outlet of the pyrolysis gas condenser；The pyrolysis
Water collector is connected with the pyrolysis water out of the oil water separator；The pyrolysis gas collector and the pyrolysis gas condenser
Pyrolysis gas outlet is connected.
5. system according to claim 4, it is characterised in that heat exchanger is equipped with the semicoke condenser, for recycling
The heat of semicoke, the pyrolysis gas import of the heat exchanger are connected with the pyrolysis gas collector, and the pyrolysis gas of the heat exchanger goes out
Mouth is connected with powder coal charge device.
6. system according to claim 5, it is characterised in that the bottom of the uplink heat storage type pyrolysis stove is equipped with gas pressure
Contracting machine, for the uplink heat storage type pyrolysis stove conveying hoisting gas；The gas access of the gas compressor is changed with described
The pyrolysis gas outlet of hot device is connected.
7. it is pyrolyzed a kind of using any one of claim 1 to the 6 uplink heat accumulating type fine coal fast pyrogenation reaction system
Method, it is characterised in that the described method includes：
Coal dust is sent into the furnace body of the uplink heat storage type pyrolysis stove from the reaction-ure feeding mouth of the uplink heat storage type pyrolysis stove
It is interior；
Lift gas is sent into the uplink heat accumulating type from the bottom of the uplink heat storage type pyrolysis stove by the gas feed
In the furnace body of pyrolysis oven；
The coal dust is set to be moved under the action of the lift gas along the lower to upper part of the uplink heat storage type pyrolysis stove；
The coal dust is heated by the radiant tube and pyrolytic reaction occurs, generation gaseous state, liquid product and solid semicoke；
The product of pyrolytic reaction generation is discharged from the top of the uplink heat storage type pyrolysis stove；
Semicoke, gaseous state and liquid product are isolated by the cyclone separator；
Semicoke is collected by the semicoke condenser；
The gaseous state and liquid product are condensed by the oil-gas condenser.
8. the method according to the description of claim 7 is characterized in that the fire box temperature of the uplink heat storage type pyrolysis stove is 450-
950 DEG C, furnace pressure 0.2-0.4Mpa；The temperature control of the radiant tube is at 500-1000 DEG C, on the single radiant tube
Temperature difference be not higher than 30 DEG C.
9. according to the method described in claim 8, it is characterized in that, when producing tar, the fire box temperature of the furnace body is
500-700℃；When calorific value of gas in production, the fire box temperature of the furnace body is 700-900 DEG C.
10. the method according to the description of claim 7 is characterized in that by being passed through into the heat exchanger of the semicoke condenser
After pyrolysis gas is exchanged heat, the pyrolysis gas of heating is set to be sent into the bottom of the uplink heat storage type pyrolysis stove as lift gas, and
The coal dust of the uplink heat storage type pyrolysis furnace bottom is fed through to the inside of the uplink heat storage type pyrolysis stove.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711166196.1A CN107903924A (en) | 2017-11-21 | 2017-11-21 | A kind of uplink heat accumulating type fine coal fast pyrogenation reaction system and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711166196.1A CN107903924A (en) | 2017-11-21 | 2017-11-21 | A kind of uplink heat accumulating type fine coal fast pyrogenation reaction system and method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107903924A true CN107903924A (en) | 2018-04-13 |
Family
ID=61846669
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711166196.1A Pending CN107903924A (en) | 2017-11-21 | 2017-11-21 | A kind of uplink heat accumulating type fine coal fast pyrogenation reaction system and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107903924A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109355073A (en) * | 2018-11-02 | 2019-02-19 | 武汉博立达农业科技发展有限公司 | Biomass and coal copyrolysis reactor |
| CN109355074A (en) * | 2018-11-02 | 2019-02-19 | 武汉博立达农业科技发展有限公司 | Biomass and coal copyrolysis reactor |
| WO2019210755A1 (en) * | 2018-05-03 | 2019-11-07 | 大连爱为能源有限公司 | Process for solid heat carrier cyclic dry distillation of high ash oil slurry |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102766475A (en) * | 2012-07-05 | 2012-11-07 | 北京神雾环境能源科技集团股份有限公司 | Method and system for performing drying and dry distillation on fluidized bed pulverized coal based on overheating steam medium |
| CN103045275A (en) * | 2011-10-17 | 2013-04-17 | 中国科学院工程热物理研究所 | Self-heating pyrolysis method |
| CN203925629U (en) * | 2014-05-13 | 2014-11-05 | 昆明理工大学 | Distributed living beings and organic Rankine circulation cogeneration, the hot polygenerations systeme of charcoal |
| CN106367119A (en) * | 2016-10-26 | 2017-02-01 | 南京大学 | Pyrolysis and biomass gas catalytic reforming reactor and application thereof |
| CN107227392A (en) * | 2017-07-25 | 2017-10-03 | 神雾科技集团股份有限公司 | Miberal powder also original system |
| CN207659386U (en) * | 2017-11-21 | 2018-07-27 | 北京神雾电力科技有限公司 | A kind of uplink heat accumulating type fine coal fast pyrogenation reaction system |
-
2017
- 2017-11-21 CN CN201711166196.1A patent/CN107903924A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103045275A (en) * | 2011-10-17 | 2013-04-17 | 中国科学院工程热物理研究所 | Self-heating pyrolysis method |
| CN102766475A (en) * | 2012-07-05 | 2012-11-07 | 北京神雾环境能源科技集团股份有限公司 | Method and system for performing drying and dry distillation on fluidized bed pulverized coal based on overheating steam medium |
| CN203925629U (en) * | 2014-05-13 | 2014-11-05 | 昆明理工大学 | Distributed living beings and organic Rankine circulation cogeneration, the hot polygenerations systeme of charcoal |
| CN106367119A (en) * | 2016-10-26 | 2017-02-01 | 南京大学 | Pyrolysis and biomass gas catalytic reforming reactor and application thereof |
| CN107227392A (en) * | 2017-07-25 | 2017-10-03 | 神雾科技集团股份有限公司 | Miberal powder also original system |
| CN207659386U (en) * | 2017-11-21 | 2018-07-27 | 北京神雾电力科技有限公司 | A kind of uplink heat accumulating type fine coal fast pyrogenation reaction system |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2019210755A1 (en) * | 2018-05-03 | 2019-11-07 | 大连爱为能源有限公司 | Process for solid heat carrier cyclic dry distillation of high ash oil slurry |
| CN109355073A (en) * | 2018-11-02 | 2019-02-19 | 武汉博立达农业科技发展有限公司 | Biomass and coal copyrolysis reactor |
| CN109355074A (en) * | 2018-11-02 | 2019-02-19 | 武汉博立达农业科技发展有限公司 | Biomass and coal copyrolysis reactor |
| CN109355073B (en) * | 2018-11-02 | 2023-12-01 | 武汉兰多生物科技有限公司 | Biomass and coal co-pyrolysis reactor |
| CN109355074B (en) * | 2018-11-02 | 2023-12-01 | 武汉兰多生物科技有限公司 | Biomass and coal co-pyrolysis reactor |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101544901A (en) | Method and device for preparing biological oil by biomass cracking | |
| CN102358841B (en) | Multistage pulverized coal multiple-tube rotary low temperature dry distillation technology and system | |
| CN102358840B (en) | Single-stage fine coal multi-pipe rotary low-temperature destructive distillation technology and system | |
| CN102212399A (en) | Thermal pyrolysis combination method and device | |
| CN102533296B (en) | Oil shale rotary kiln dry distillation and circulating fluidized bed combustion process | |
| CN102643703B (en) | Novel external heating type lignite pyrolysis quality increasing system and process | |
| CN101289621B (en) | Process for preparing carbocoal, coke tar and coal gas by treating bovey coal by suspending pyrogenation device | |
| CN104073263B (en) | Heat accumulating type rotating bed low-temperature carbonization system and technique | |
| CN102329628A (en) | Large-size low-temperature destructive distillation system for low-order lignite | |
| CN107903924A (en) | A kind of uplink heat accumulating type fine coal fast pyrogenation reaction system and method | |
| CN201343520Y (en) | Flash dry distillation technology device of oil shale | |
| CN101289622B (en) | Process for upgrading of bovey coal by solid thermal-loading suspending pyrogenation device of bovey coal | |
| CN103980920B (en) | A kind of inferior fuel pyrolytic process | |
| CN104232127A (en) | Internal and external heating combination type compound destructive distillation method for granular coals | |
| CN105273763A (en) | Heat pipe heating type biomass and coal segmented collaborative pyrolysis system | |
| CN207659386U (en) | A kind of uplink heat accumulating type fine coal fast pyrogenation reaction system | |
| CN102766476A (en) | Multi-layer upright tower type duff dust and oil shale distillation plant with stirring function and process | |
| CN105907413B (en) | The low temperature distillation technique of low order fine coal | |
| CN205803398U (en) | A kind of low order fine coal hydrogenation pressurization fast low temperature destructive distillation device | |
| CN102492445A (en) | Multi-pipe revolving low-temperature dry distillation technology of fine coal | |
| CN105861008B (en) | Pyrolysis of coal reactor-pulverized-coal fired boiler combined system and the method for handling coal using it | |
| CN106010610A (en) | Low-order pulverized coal hydrogenated and pressurized fast low-temperature carbonization process and device | |
| CN105754624A (en) | Low-order powdered coal pyrolysis system and method | |
| CN205635481U (en) | Low order fine coal pyrolysis system | |
| CN206278922U (en) | The system that a kind of sludge prepares activated carbon |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20180413 |