CN207659386U - A kind of uplink heat accumulating type fine coal fast pyrogenation reaction system - Google Patents
A kind of uplink heat accumulating type fine coal fast pyrogenation reaction system Download PDFInfo
- Publication number
- CN207659386U CN207659386U CN201721562422.3U CN201721562422U CN207659386U CN 207659386 U CN207659386 U CN 207659386U CN 201721562422 U CN201721562422 U CN 201721562422U CN 207659386 U CN207659386 U CN 207659386U
- Authority
- CN
- China
- Prior art keywords
- gas
- pyrolysis
- semicoke
- oil
- 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.)
- Expired - Fee Related
Links
Abstract
The utility model is related to a kind of uplink heat accumulating type fine coal fast pyrogenation reaction systems.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 set 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 outlet of the semicoke of cyclone separator；The oil and gas import of oil-gas condenser is connected with the oil gas vent of cyclone separator.The utility model 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 utility model is related to pulverized coal pyrolysis technical fields more particularly to a kind of uplink heat accumulating type fine coal fast pyrogenation to react
System.
Background technology
Coal is one of the conventional resource that proved reserves are the abundantest in the world, as maximum coal production 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 will produce heat, and efficiency is 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 is higher to the cost requirement of reactor performance and technical process.Phase
Than in these types of Land use systems, pyrolysis of coal converts coal into solid-state, liquid and gaseous product, there are apparent advantage and foreground.
Currently, from the point of view of mode of heating, domestic and international existing pyrolytic process mostly uses porcelain ball and thermal decomposition product semicoke conduct
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 long, system failure rate is higher.
Moreover, finding that porcelain ball is heated to 600 DEG C or more and recycled repeatedly in experiment, abrasion sex chromosome mosaicism will produce；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.
When 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 when caking coal
It is aggregated and causes 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, separation etc., cause system process long, 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 room
Media contact brings security risk.
In short, the solid thermal carriers such as semicoke, porcelain ball have seriously affected the processing capacity of pyrolysis furnace apparatus, the air heats such as coal gas
There is also larger security risks for carrier preheating.
In addition, pyrolysis oven used at present, majority is fixed bed, or has the function of downflow fluidized bed, and pulverized coal pyrolysis is not
Fully or the second decomposition of volatility product 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.
Utility model content
In view of the above-mentioned problems, the utility model is intended to provide a kind of uplink heat accumulating type fine coal fast pyrogenation reaction system, with
Simplify system process, reduce the failure rate of system so that system temperature control is accurate, temperature adjustment is convenient, to pyrolytic reaction depth and
Reaction process control effectively, and improves converting rate, improves target product yield, improves the thermal efficiency of system.
The utility model provides a kind of uplink heat accumulating type fine coal fast pyrogenation reaction system, and the system comprises uplink accumulation of heats
Formula pyrolysis oven, cyclone separator, semicoke condenser and oil-gas condenser, the uplink heat storage type pyrolysis stove includes furnace body and radiation
The top of pipe, 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, described anti-
Position of the object feed inlet on the vertical direction of the furnace body is answered to be higher than the gas feed；The radiant tube is set to the furnace body
It is interior, it is located 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 outlet of the semicoke 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 includes gas distribution grid, and the gas distribution grid is set to
In the furnace body, it is located at 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, the heat for recycling 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.
The bottom of above-mentioned system, the uplink heat storage type pyrolysis stove is 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 uplink heat accumulating type fine coal fast pyrogenation reaction technology of the utility model, by controlling lift gas flow, regulation and control
Particle speed and particle residence time improve and turn to realize effective control for pyrolytic reaction depth and reaction process
Rate improves target product yield；The utility model uses more heat accumulation type radiant tubes, and heat is provided for the coal dust in pyrolysis oven
Source, without heat carrier and mechanical rotation device, technological process is simple, system temperature control is accurate, temperature adjustment is convenient, is not necessarily to gas and solid
Heating, the separation process of heat carrier, reduce the failure rate of system, can be carried in conjunction with convection current, heat transfer and radiant heat transfer control
The high thermal efficiency of system, reduces tar dustiness.
Description of the drawings
Fig. 1 is the utility model embodiment uplink heat accumulating type fine coal fast pyrogenation reaction system schematic diagram；
Fig. 2 is the utility model embodiment uplink heat accumulating type fine coal fast pyrogenation furnace structure schematic diagram.
Specific implementation mode
Below in conjunction with drawings and examples, specific embodiment of the present utility model is described in more details, with
Just the advantages of better understood when the embodiment of the utility model and various aspects.However, specific implementations described below side
Formula and embodiment are for illustrative purposes only, rather than limitations of the present invention.
As shown in Figure 1, the utility model provides a kind of uplink heat accumulating type fine coal fast pyrogenation reaction system, the system master
To 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
Position of the mouth 44 on the vertical direction of the furnace body is higher than the gas feed 41；The radiant tube 46 is set to the furnace body 45
It is interior, it is located at 44 top of the reaction-ure feeding mouth, 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 outlet of the semicoke 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 set in the furnace body 45, is located at the reaction-ure feeding
44 lower section of mouth, the gas feed 41 are connected to one group of air inlet 43 being distributed on the gas distribution grid 42.
In above 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
14, 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 outlet of the condensation semicoke 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 generates gaseous state, liquid and solid product and dust 5 for coal dust 1 to be pyrolyzed.Whirlwind
Separator 6 is used to pyrogenous origin product isolating semicoke 7 and gaseous state and liquid product 10.Semicoke condenser 8 will be for that will divide
It separates out the semicoke 7 come to condense, is convenient for the recycling of follow-up semicoke collector 9.
Gaseous state and liquid product 10 are detached through electric precipitation decontaminating separator 12 again after the condensation of oil-gas condenser 11, are obtained
To the pyrolysis gas 15 of tar 13 and oil-containing water.Isolated tar 13 is delivered to tar well 14 and carries out tar recycling, point
Pyrolysis gas 15 from obtained oil-containing water is further delivered to pyrolysis gas condenser 16 and is condensed, and obtains grease 17 and pyrolysis gas
21.Grease 17 is delivered to oil water separator 18 and is detached, and further obtains pyrolysis water 19 and tar 13.Tar 13 can transport 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, the heat for recycling semicoke, the heat exchanger in the semicoke condenser 8
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.
The bottom of above-mentioned system, the uplink heat storage type pyrolysis stove is equipped with gas compressor 23, is used 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 above system, technique is as described below.
Dry coal dust 1 is crushed to 90% less than after 6mm particles below, 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, effect is using 200-300 DEG C of pyrolysis after preheating in feeder 3
Coal dust 1 in coal bunker 2 is sprayed into 4 top of uplink heat storage type pyrolysis stove 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 at 500-700 DEG C；If based on calorific value of gas in production, fire box temperature is arranged at 700-900 DEG C.
Furnace pressure is 0.2-0.4Mpa.Fire box temperature is provided by more radiant tubes, and radiant tube temperature is controlled 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 promoted
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 generates
A large amount of gaseous states, liquid and solid product and a small amount of dust 5.Product and dust 5 are discharged from 4 top of uplink heat storage type pyrolysis stove.
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
It is equipped with burner, fuel gas and temperature gas enter to setting in radiant tube A after being set the preheating of the regenerative chamber outside pyrolysis oven
Combustion reaction occurs for the burner of port, and the flame that one end burner combustion generates forms temperature when spraying along radiant tube direction
Gradient, i.e., along the ends radiant tube A to the other side ends B of the radiant tube, temperature downward trend in gradient.After the completion of A end burnings, the ends A
The flue gas that burning generates enters to the ends B regenerative chamber, pre-heating fuel and combustion air, and the fuel and combustion air after preheating enter to radiation
Pipe B end burner also forms temperature gradient in the flame that other end burner combustion generates when spraying.Same radiant tube both ends
Burner replace reversing combustion.
When the burner at both ends alternately burns, it is formed by two temperature gradient superpositions so that entire 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, the ends A can be the either port of radiant tube, and the ends B are another corresponding to the ends same radiant tube A
One end.
The product and dust 5 being discharged from 4 top of uplink heat storage type pyrolysis stove are fed through in high temperature cyclone separator 6, semicoke 7
It is 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, recycle 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 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 detached.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 cycle be again introduced into oil-gas condenser 11, be dusted purification, obtain tar 13 and pyrolysis gas 21.
The uplink heat accumulating type fine coal fast pyrogenation reaction system of the utility model, by controlling lift gas flow, regulation and control
Particle speed and particle residence time improve conversion to realize effective control for pyrolytic reaction depth and reaction process
Rate improves target product yield；
The utility model use more heat accumulation type radiant tubes, provide heat source for the coal dust in pyrolysis oven, without heat carrier with
Mechanical rotation device, technological process is simple, system temperature control is accurate, temperature adjustment is convenient, is not necessarily to the heating of gas and solid thermal carriers, divides
From process, the failure rate of system is reduced.
The utility model is controlled in combination with convection current, heat transfer and radiant heat transfer, improves the thermal efficiency of system.
The utility model reduces tar dustiness compared with semicoke is as heat carrier.
The technique of the utility model is strong to coal adaptability, no matter for non-caking coal, Iight sticky coal, strong cohesiveness
Coal 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 containing after drying
The jet coal of 8.64% moisture is crushed to 6mm hereinafter, coal particle size distribution is as shown in table 1, and the Industrial Analysis of coal dust and element divide
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
Degree is 5m/s.The radiant tube surface temperature of pyrolysis uplink heat storage type pyrolysis stove 4 is respectively 600 DEG C and 500 DEG C twice, 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.It is pyrolyzed burner hearth 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
4 top discharge of stove is solved, and is fed through in 500 DEG C of cyclone separator 6.Semicoke is separated from the gas of cyclone separator 6,
The semicoke condenser 8 for being 25 DEG C through excess temperature is fed through 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
It separates 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 cycle be again introduced into oil-gas condenser 11, be dusted purification, 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 containing after drying
The lignite of 15.10% or so moisture is crushed to 6mm hereinafter, coal particle size is distributed 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
It solves the gas generated 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.Pyrolysis uplink heat storage type pyrolysis furnace radiating pipe surface temperature is respectively 900 DEG C, 1000 DEG C 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.It is pyrolyzed burner hearth 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 coke
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 again through non-purified complete oil gas cycle in electric precipitation decontaminating separator 12
It is secondary to enter in oil-gas condenser 11, it is dusted purification, 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 the utility model example,
And it does not limit the embodiments.For those of ordinary skill in the art, may be used also on the basis of the above description
To make other variations or changes in different ways.There is no necessity and possibility to exhaust all the enbodiments.And thus
Among changes and variations that derived from are still in the scope of protection of the utility model.
Claims (6)
1. a kind of uplink heat accumulating type fine coal fast pyrogenation reaction system, which is characterized in that the system comprises uplink heat-accumulation type hots
Solve stove, cyclone separator, semicoke condenser and oil-gas condenser, 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 set in the furnace body, is located above the reaction-ure feeding mouth, and the radiant tube is one group along vertical
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 outlet of the semicoke 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, which is characterized in that the uplink heat storage type pyrolysis stove further includes gas distribution
Plate, the gas distribution grid are set in the furnace body, are located at below the reaction-ure feeding mouth, and the gas feed connection is equal
One group of air inlet being distributed on the gas distribution grid.
3. system according to claim 1, which is characterized 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, which is characterized in that the system also includes semicoke collector, electric precipitations 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 outlet of the condensation semicoke 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 of the tar import of the tar well and the electric precipitation decontaminating separator
Outlet is connected；The oil-containing aquathermolysis of the import of oil-containing water pyrolysis gas and the electric precipitation decontaminating separator of the pyrolysis gas condenser
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, which is characterized in that heat exchanger is equipped in 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, which is characterized in that the bottom of the uplink heat storage type pyrolysis stove is equipped with gas pressure
Contracting machine is used 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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721562422.3U CN207659386U (en) | 2017-11-21 | 2017-11-21 | A kind of uplink heat accumulating type fine coal fast pyrogenation reaction system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721562422.3U CN207659386U (en) | 2017-11-21 | 2017-11-21 | A kind of uplink heat accumulating type fine coal fast pyrogenation reaction system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN207659386U true CN207659386U (en) | 2018-07-27 |
Family
ID=62946120
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201721562422.3U Expired - Fee Related CN207659386U (en) | 2017-11-21 | 2017-11-21 | A kind of uplink heat accumulating type fine coal fast pyrogenation reaction system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN207659386U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107903924A (en) * | 2017-11-21 | 2018-04-13 | 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 and method |
| CN113214853A (en) * | 2021-04-01 | 2021-08-06 | 陕西煤业化工集团神木天元化工有限公司 | Low-rank pulverized coal rotary pyrolysis method with oil residue circulation |
-
2017
- 2017-11-21 CN CN201721562422.3U patent/CN207659386U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107903924A (en) * | 2017-11-21 | 2018-04-13 | 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 and method |
| CN113214853A (en) * | 2021-04-01 | 2021-08-06 | 陕西煤业化工集团神木天元化工有限公司 | Low-rank pulverized coal rotary pyrolysis method with oil residue circulation |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102358841B (en) | Multistage pulverized coal multiple-tube rotary low temperature dry distillation technology and system | |
| CN101544901A (en) | Method and device for preparing biological oil by biomass cracking | |
| CN102358840B (en) | Single-stage fine coal multi-pipe rotary low-temperature destructive distillation technology and system | |
| CN101289621B (en) | Process for preparing carbocoal, coke tar and coal gas by treating bovey coal by suspending pyrogenation device | |
| CN102643703B (en) | Novel external heating type lignite pyrolysis quality increasing system and process | |
| CN104762097A (en) | Rotary furnace low-order powdered coal pyrolysis upgrading method with coal gas circulation | |
| 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 | |
| CN104789244A (en) | Gas-circulating method for pyrolysis production of anthracite in coal powder rotary furnace | |
| CN201343520Y (en) | Flash dry distillation technology device of oil shale | |
| CN107903924A (en) | A kind of uplink heat accumulating type fine coal fast pyrogenation reaction system and method | |
| CN207659386U (en) | A kind of uplink heat accumulating type fine coal fast pyrogenation reaction system | |
| 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 | |
| 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 | |
| CN105907413B (en) | The low temperature distillation technique of low order fine coal | |
| CN106010610A (en) | Low-order pulverized coal hydrogenated and pressurized fast low-temperature carbonization process and device | |
| CN205590620U (en) | Low temperature pyrolysis system of low order fine coal | |
| CN206278922U (en) | The system that a kind of sludge prepares activated carbon | |
| CN205328940U (en) | System for pyrolysis coal | |
| CN207659385U (en) | A kind of uplink heat storage type pyrolysis stove | |
| CN103695013A (en) | System and method for pyrolysis of carbon-containing solid fuel | |
| CN208949207U (en) | A kind of fluidized-bed gasification furnace of fractional combustion |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20180727 Termination date: 20201121 |