CN107760339A - A kind of pyrolysis gas recycling system and method - Google Patents
A kind of pyrolysis gas recycling system and method Download PDFInfo
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- CN107760339A CN107760339A CN201711138050.6A CN201711138050A CN107760339A CN 107760339 A CN107760339 A CN 107760339A CN 201711138050 A CN201711138050 A CN 201711138050A CN 107760339 A CN107760339 A CN 107760339A
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- preheater
- pyrolysis gas
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 145
- 238000004064 recycling Methods 0.000 title claims abstract description 26
- 238000000034 method Methods 0.000 title claims description 9
- 150000003839 salts Chemical class 0.000 claims abstract description 292
- 238000011084 recovery Methods 0.000 claims abstract description 63
- 239000003245 coal Substances 0.000 claims abstract description 24
- 239000007789 gas Substances 0.000 claims description 104
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 74
- 239000003546 flue gas Substances 0.000 claims description 65
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 64
- 239000002918 waste heat Substances 0.000 claims description 61
- 238000003860 storage Methods 0.000 claims description 38
- 239000002826 coolant Substances 0.000 claims description 30
- 239000007788 liquid Substances 0.000 claims description 10
- 239000000779 smoke Substances 0.000 claims description 8
- 238000010025 steaming Methods 0.000 claims description 3
- 230000008901 benefit Effects 0.000 abstract description 13
- 238000006243 chemical reaction Methods 0.000 abstract description 5
- 238000004140 cleaning Methods 0.000 abstract description 5
- 230000007613 environmental effect Effects 0.000 abstract description 4
- 238000001816 cooling Methods 0.000 description 3
- 235000019504 cigarettes Nutrition 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- 230000001754 anti-pyretic effect Effects 0.000 description 1
- 239000002221 antipyretic Substances 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 238000003682 fluorination reaction Methods 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 150000002823 nitrates Chemical class 0.000 description 1
- 239000002296 pyrolytic carbon 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
-
- 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
- C10B27/00—Arrangements for withdrawal of the distillation gases
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/06—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being molten; Use of molten metal, e.g. zinc, as heat transfer medium
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D19/00—Regenerative heat-exchange apparatus in which the intermediate heat-transfer medium or body is moved successively into contact with each heat-exchange medium
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D21/0001—Recuperative heat exchangers
- F28D21/0003—Recuperative heat exchangers the heat being recuperated from exhaust gases
- F28D21/001—Recuperative heat exchangers the heat being recuperated from exhaust gases for thermal power plants or industrial processes
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Treating Waste Gases (AREA)
Abstract
The present invention relates to a kind of recycling system of pyrolysis gas.Pyrolysis gas carries out pyrolysis generation to coal by pyrolysis oven, and the system also includes fused salt heat exchanging device；Fused salt heat exchanging device is provided with one-level pyrolysis gas entrance, one-level pyrolysis gas outlet, one-level fused salt entrance and the outlet of one-level fused salt；One-level pyrolysis gas entrance connects the pyrolysis gas outlet of the pyrolysis oven by pipeline；Pyrolysis gas enters fused salt heat exchanging device by one-level pyrolysis gas entrance, and fused salt is sent into fused salt heat exchanging device by one-level fused salt entrance；The temperature of fused salt is less than the temperature of pyrolysis gas；Fused salt and pyrolysis gas heat exchange in fused salt heat exchanging device, the pyrolysis gas after heat exchange is discharged by one-level pyrolysis gas outlet to be utilized, and the fused salt after heat exchange is exported by one-level fused salt and discharged.Caused heat during pyrolysis of coal can fully be recycled using the system, and improve the recovery utilization rate of pyrolysis gas, realized the volume high-efficiency cleaning conversion of coal resources, there is important social benefit, economic benefit and environmental benefit.
Description
Technical field
Present invention relates generally to coal pyrolysis technical field, and in particular to a kind of pyrolysis gas recycling system and method.
Background technology
The pyrolysis of coal is one of important channel that coal cleaning efficiently utilizes, and is coal under isolation air or inert atmosphere conditions
During continuous heating to higher temperature, a series of physical change of generation and chemical reaction.The pyrolysis of coal be exactly can normal pressure, in it is low
Temperature, without under catalysts conditions from high volatile low-order coal extracting liq product, fine chemicals, high heating value gas.In
Low-temperature rapid thermal solution realizes that oil gas is extracted in pyrolysis of coal, extracts the hydrocarbon rich resource contained in coal to greatest extent, realizes coal
The high-efficiency cleaning conversion of resource, has very important social benefit, economic benefit and environmental benefit.
Coal produces the product resources such as abundant pyrolysis oil, antipyretic air and heat semicoke after pyrolysis, at present after to pyrolysis of coal
Product recycling utilize, all there is preferably processing to utilize means pyrolysis oil, pyrolytic carbon, and the utilization rate of pyrolysis gas compared with
It is low.
Therefore, in order to improve the utilization ratio of high temperature pyrolysis gas, it is necessary to propose a kind of recycling of high temperature pyrolysis gas
System.
The content of the invention
It is an object of the invention to provide a kind of pyrolysis gas recycling system and method.Returned using the pyrolysis gas of the present invention
Receiving can fully be recycled using system to caused heat during pyrolysis of coal, and improve the recycling of pyrolysis gas
Rate, the volume high-efficiency cleaning conversion of coal resources is realized, there is important social benefit, economic benefit and environmental benefit.
The invention provides a kind of pyrolysis gas recycling system, the pyrolysis gas carries out pyrolysis production by pyrolysis oven to coal
It is raw, in addition to fused salt heat exchanging device；
The fused salt heat exchanging device is provided with one-level pyrolysis gas entrance, one-level pyrolysis gas outlet, one-level fused salt entrance and one-level
Fused salt exports；The one-level pyrolysis gas entrance connects the pyrolysis gas outlet of the pyrolysis oven by pipeline；
The pyrolysis gas enters the fused salt heat exchanging device by the one-level pyrolysis gas entrance, and fused salt is melted by the one-level
Salt entrance is sent into the fused salt heat exchanging device；The temperature of the fused salt is less than the temperature of the pyrolysis gas；
The fused salt and pyrolysis gas heat exchange in the fused salt heat exchanging device, the pyrolysis gas after heat exchange is by described
The discharge of one-level pyrolysis gas outlet is utilized, and the fused salt after heat exchange is exported by the one-level fused salt and discharged.
Further, the fused salt heat exchanging device is plate type heat exchanger.
Further, in addition to steam generator, the steam generator go out provided with two level fused salt entrance, two level fused salt
Mouth, one-level steam inlet, one-level steam (vapor) outlet；The two level fused salt inlet duct connects the one-level fused salt outlet；
Enter the steam generator through the two level fused salt entrance by the fused salt of one-level fused salt outlet discharge；Institute
State one-level steam inlet and be passed through water vapour, the water vapour enters the steam generator；The temperature of the water vapour be less than into
Enter the temperature of the fused salt of the steam generator；
Fused salt and water vapour heat exchange in the steam generator into the steam generator, in the steaming
Fused salt in vapour generator after heat exchange is exported by two level fused salt discharges, the water vapour in the steam generator after heat exchange
Discharged by the one-level steam (vapor) outlet.
Further, in addition to preheater, the preheater export, in advance provided with preheater fused salt entrance, preheater fused salt
Hot device water inlet, preheater steam (vapor) outlet；The preheater fused salt inlet duct connects the two level fused salt outlet, the preheating
Device steam (vapor) outlet pipeline connects the one-level steam inlet；
Enter the preheater through the preheater fused salt entrance by the fused salt of two level fused salt outlet discharge；
Water is passed through in the preheater water inlet, the water enters the preheater, and the temperature of the water, which is less than, enters institute
State the temperature of the fused salt of preheater；The water heat exchange and produces water with entering the fused salt of the preheater in the preheater
Steam；
Fused salt in the preheater after heat exchange is exported by the preheater fused salt discharges；Produced in the preheater
Raw water vapour enters the steam generator by the preheater water out through the one-level steam inlet.
Further, in addition to flue gas waste heat recovery apparatus；The flue gas waste heat recovery apparatus be provided with cooling medium entrance,
Cooling medium exports and waste-heat recovery device exhanst gas outlet, waste-heat recovery device smoke inlet；
The exhanst gas outlet pipeline of the pyrolysis oven connects the waste-heat recovery device smoke inlet；Caused by the pyrolysis oven
Flue gas is passed through the waste-heat recovery device by the flue gas waste heat recovery apparatus smoke inlet, and cooling medium is by the cooling medium
Entrance is sent into the flue gas waste heat recovery apparatus；The temperature for being passed through the flue gas of the flue gas waste heat recovery apparatus is higher than the cooling
The temperature of medium, the flue gas of the flue gas waste heat recovery apparatus is passed through with the cooling medium in the flue gas waste heat recovery apparatus
Interior heat exchange；
Flue gas in the flue gas waste heat recovery apparatus after heat exchange is arranged by the exhanst gas outlet of the waste-heat recovery device
Go out to utilize；Cooling medium in the flue gas waste heat recovery apparatus after heat exchange is exported by the cooling medium discharges.
Further, the cooling medium is water；The cooling medium outlet conduit connects the preheater water inlet,
Water in the waste-heat recovery device after heat exchange is passed through in the preheater through cooling medium outlet.
Further, in addition to fused salt storage tank, the fused salt storage tank connects the one-level fused salt entrance by pipeline, described
Fused salt storage tank is used to store fused salt；
The pipeline is provided with pump for liquid salts, and the fused salt in the fused salt storage tank is delivered to the fused salt heat exchanging by the pump for liquid salts
Device.
Further, the fused salt storage tank is provided with fused salt storage tank fused salt entrance and fused salt storage tank fused salt exports, the fused salt
Storage tank fused salt outlet conduit connects the one-level fused salt entrance, and the fused salt storage tank fused salt inlet duct connects the preheater and melted
Salt exports, and the fused salt that discharge is exported by the preheater fused salt is sent into the fused salt storage tank through the fused salt storage tank fused salt entrance.
The present invention also provide it is a kind of using above-mentioned pyrolysis gas recycling system to pyrolysis gas recoverying and utilizing method, bag
Include：
Step S1, pyrolysis gas caused by the pyrolysis oven is passed through the fused salt heat exchanging device, filled in the fused salt heat exchanging
Fused salt is passed through in putting；
Step S2, the pyrolysis gas and fused salt for being passed through the fused salt heat exchanging device carry out hot friendship in the fused salt heat exchanging device
Change；
Step S3, the pyrolysis gas after being exchanged heat in the fused salt heat exchanging device discharges profit by the one-level pyrolysis gas outlet
With；Fused salt after being exchanged heat in the fused salt heat exchanging device is exported by the one-level fused salt discharges.
Further, including：
Step S4, the fused salt discharged by the fused salt heat exchanging device is passed through the steam generator；Simultaneously in the steaming
Water vapour is passed through in vapour generator；The fused salt for being passed through the steam generator and the water vapour for being passed through the steam generator are carried out
Heat exchange；Water vapour in the steam generator after heat exchange is discharged by the one-level steam (vapor) outlet；
Step S5, the fused salt after the heat exchange in the steam generator is passed through the preheater；
Meanwhile water is passed through in the preheater, the water being passed through in the preheater is molten in the preheater with being passed through
Salt carries out heat exchange in the preheater and produces water vapour；
Step S6, the fused salt after the heat exchange in the preheater is passed through the fused salt storage tank, the water vapour is led to
Enter the steam generator；
Step S7.1, the fused salt in the fused salt storage tank is pumped into the fused salt heat exchanging device by the fused salt；
Step S7.2, flue gas caused by the pyrolysis oven is passed through the flue gas waste heat recovery apparatus, while in the cigarette
Water is passed through in gas waste-heat recovery device, the flue gas of the flue gas waste heat recovery apparatus is passed through and is passed through the flue gas waste heat recovery dress
The water put carries out heat exchange in the flue gas waste heat recovery apparatus；
Flue gas discharge in the flue gas waste heat recovery apparatus after heat exchange utilizes；In the flue gas waste heat recovery apparatus
Water after interior heat exchange is passed through the steam generator.
Using the pyrolysis gas recycling system of the present invention profit can be fully reclaimed to caused heat during pyrolysis of coal
With, and the recovery utilization rate of pyrolysis gas is improved, the volume high-efficiency cleaning conversion of coal resources is realized, there is important society's effect
Benefit, economic benefit and environmental benefit.
Brief description of the drawings
Fig. 1 is the schematic diagram of pyrolysis gas recycling system of the present invention；
Description of reference numerals：
10- pyrolysis ovens；
101- radiant tubes；
20- fused salt heat exchanging devices；
30- steam generators；
40- preheaters；
50- fused salt storage tanks；
60- pump for liquid salts；
70- flue gas waste heat recovery apparatus.
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 its various aspects.However, specific embodiments described below and reality
Example is applied to be for illustrative purposes only, rather than limitation of the present invention.
As shown in figure 1, the pyrolysis gas recycling system of the present invention, pyrolysis gas carry out pyrolysis production by pyrolysis oven 10 to coal
Raw, pyrolysis gas recycling system also includes fused salt heat exchanging device 20.Fused salt heat exchanging device 20 is provided with one-level pyrolysis gas entrance, one
Level pyrolysis gas outlet, one-level fused salt entrance and the outlet of one-level fused salt；One-level pyrolysis gas entrance connects pyrolysis oven 10 by pipeline
Pyrolysis gas outlet.Pyrolysis gas enters fused salt heat exchanging device 20 by one-level pyrolysis gas entrance, and fused salt is sent into by one-level fused salt entrance
Fused salt heat exchanging device 20.The temperature for the fused salt being passed through in fused salt heat exchanging device 20 is less than the pyrolysis gas into fused salt heat exchanging device 20
Temperature.
Fused salt and the pyrolysis gas heat exchange in fused salt heat exchanging device 20 being passed through in fused salt heat exchanging device 20, after heat exchange
Pyrolysis gas is discharged by one-level pyrolysis gas outlet and utilized, and the fused salt after heat exchange is exported by one-level fused salt and discharged.
Fused salt heat exchanging device 20 can use plate type heat exchanger, pipe heat exchanger or plate type heat exchanger and pipe heat exchanger
Both are used in combination.Fused salt type can use Nitrates, carbonate, chlorination salt or fluorination salt etc., pass through regulation and control
Into the fused salt type and fused salt amount in fused salt heat exchanging device 20, it can be controlled, obtained with the pyrolysis gas temperature after heat exchanging
Need the pyrolysis gas of temperature.Meanwhile exchanged heat using fused salt heat exchanging device 20 with pyrolysis gas, avoid steam and pyrolysis gas
(high temperature) existing possibility in same heat exchanger, greatly improve the security of system.
Either using plate type heat exchanger still using pipe heat exchanger as fused salt heat exchanging device 20, its equipment profile
The appearance and size of heat transmission equipment of the size than using water as heat transferring medium is small, and floor space is equally also small, and heat exchange efficiency is high,
The expense for investing operation is low.
In the wherein embodiment of the present invention, pyrolysis gas recycling system is additionally provided with steam generator 30, preheater
40th, fused salt storage tank 50, pump for liquid salts 60, flue gas waste heat recovery apparatus 70.
Steam generator 30 is provided with two level fused salt entrance, the outlet of two level fused salt, one-level steam inlet and one-level steam (vapor) outlet.
Two level fused salt entrance is exported with one-level fused salt and connected by pipeline, and the fused salt in fused salt heat exchanging device 20 after heat exchange leads to
Cross connecting pipe and enter steam generator 30.Vapor is passed through into steam generator 30 from one-level steam inlet, this vapor
Temperature be less than into steam generator 30 fused salt temperature.Vapor and fused salt into steam generator 30 are sent out in steam
Enter type heat exchange in raw device, the fused salt after heat exchange is exported by two level fused salt and discharged, and the vapor after heat exchange is by one-level steam
Outlet discharge.
Preheater 40 is provided with preheater fused salt entrance, the outlet of preheater fused salt, preheater water inlet and preheater steam and gone out
Mouthful.Preheater fused salt entrance is connected by pipeline and the outlet of two level fused salt, and the fused salt discharged from the outlet of two level fused salt is through this pipeline
Into preheater 40.Preheater steam (vapor) outlet is connected by pipeline with one-level steam inlet, from preheater water inlet to preheater
Water is passed through in 40, the temperature of water is less than the temperature into the fused salt of preheater 40.Fused salt and water into preheater 40 are preheating
Heat exchange is carried out in device 40, and produces vapor.Fused salt after heat exchange is exported by preheater fused salt discharges, in preheater 40
Caused vapor then enters steam generator 30 by the pipeline of preheater steam (vapor) outlet.
Fused salt storage tank 50 is provided with fused salt storage tank fused salt entrance and fused salt storage tank fused salt exports.Fused salt storage tank fused salt entrance with it is pre-
Hot device fused salt outlet is connected by pipeline, and the fused salt discharged from preheater 40 enters fused salt storage tank 50 by this pipeline.Fused salt
The outlet of storage tank fused salt is connected with one-level fused salt entrance by pipeline, and pump for liquid salts 60, pump for liquid salts 60 are additionally provided with this connecting pipe
Fused salt in fused salt storage tank 50 is pumped to fused salt heat exchanging device 20.
Flue gas waste heat recovery apparatus 70 is provided with cooling medium entrance, cooling medium outlet, waste-heat recovery device exhanst gas outlet
With waste-heat recovery device smoke inlet.The exhanst gas outlet of pyrolysis oven 10 is connected with waste-heat recovery device smoke inlet pipelines, pyrolysis
Stove 10 is during pyrolysis of coal because flue gas caused by burning by this connecting pipe enters waste-heat recovery device 70.It is situated between by cooling
Matter entrance is passed through cooling medium into flue gas waste heat recovery apparatus 70, and the temperature of cooling medium, which is less than, enters flue gas waste heat recovery dress
The temperature of 70 flue gas is put, cooling medium carries out heat exchange with flue gas in flue gas waste heat recovery apparatus.Flue gas after heat exchange
Discharged by waste-heat recovery device exhanst gas outlet, the cooling medium after heat exchange is exported by cooling medium and discharged.
When using water as cooling medium in flue gas waste heat recovery apparatus 70, cooling medium outlet by pipeline with advance
Hot device water inlet is connected, and the water in flue gas waste heat recovery apparatus 70 after heat exchange is directly entered in preheater 40 and preheater 40
Fused salt carry out heat exchange.
In a kind of pyrolytic process of fine coal, using the present invention pyrolysis gas recycling system, by 10mm after drying with
Under coal dust be sent into pyrolysis oven 10 by feed screw, pyrolysis gas caused by pyrolysis, which is partly into radiant tube 101, to burn,
For the heat supply of pyrolysis oven 10, make pulverized coal pyrolysis, pyrolysis temperature is 700 DEG C -950 DEG C.Pyrolysis gas temperature caused by pyrolysis be 650 DEG C-
900℃。
650 DEG C -900 DEG C of pyrolysis gas enters in fused salt heat exchanging device 20 carries out heat exchange with fused salt, is pyrolyzed after heat exchange
The temperature of gas is reduced to 150 DEG C -600 DEG C, is discharged by one-level pyrolysis gas outlet, is sent into pyrolysis gas gas holder and recycles.Pass through
The fused salt of variety classes varying number is sent into fused salt heat exchanging device 20, the pyrolysis gas temperature of pyrolysis gas gas holder is sent into after heat exchange
Height is different.
After fused salt exchanges heat in fused salt heat exchanging device 20 with 650 DEG C -900 DEG C of pyrolysis gas, temperature of molten salt is increased to 500
℃-890℃.500 DEG C -890 DEG C of fused salt is exported by one-level fused salt and discharged, and enters steam generator 30 through two level fused salt entrance.
500 DEG C -890 DEG C of fused salt carries out heat exchange in steam generator 30 with vapor, and after heat exchange, temperature of molten salt is reduced to
130℃-300℃。
130 DEG C -300 DEG C of fused salt is exported by two level fused salt, and preheated device fused salt entrance enters preheater 40, in preheater
Heat exchange occurs with being passed through the water of preheater 40 in 40, the fused salt after heat exchange further reduces, and the fused salt after cooling passes through pre-
Hot device fused salt outlet enters fused salt storage tank 50.Fused salt in fused salt storage tank 50 is fed again into fused salt in the presence of pump for liquid salts 60
Heat-exchanger rig 20.It is using the method and step of above-mentioned pyrolysis gas recycling system progress pyrolysis gas recycling：
Step S1, pyrolysis gas caused by pyrolysis oven 10 is passed through fused salt heat exchanging device 20, led in fused salt heat exchanging device 20
Enter fused salt；
Step S2, the pyrolysis gas and fused salt for being passed through fused salt heat exchanging device 20 carry out heat exchange in fused salt heat exchanging device 20；
Step S3, the pyrolysis gas after being exchanged heat in fused salt heat exchanging device 20 is discharged by one-level pyrolysis gas outlet to be utilized；Molten
Fused salt after being exchanged heat in salt heat-exchanger rig 20 is exported by one-level fused salt discharges；
Step S4, the fused salt discharged by fused salt heat exchanging device 20 is passed through steam generator 30；Simultaneously in steam generator
Water vapour is passed through in 30；The fused salt for being passed through steam generator 30 and the water vapour for being passed through steam generator 30 carry out heat exchange；
Water vapour in steam generator 30 after heat exchange is discharged by one-level steam (vapor) outlet；
Step S5, the fused salt after the heat exchange in steam generator 30 is passed through preheater 40；
Meanwhile water is passed through in preheater 40, the water being passed through in preheater 40 is with the fused salt that is passed through in preheater 40 pre-
Heat exchange is carried out in hot device 40 and produces water vapour；
Step S6, the fused salt after the heat exchange in preheater 40 is passed through fused salt storage tank 50, water vapour is passed through steam hair
Raw device；
Step S7.1, the fused salt in fused salt storage tank 50 is sent into fused salt heat exchanging device 20 by pump for liquid salts 60；
Step S7.2, flue gas caused by pyrolysis oven 10 is passed through flue gas waste heat recovery apparatus 70, while returned in fume afterheat
Water is passed through in receiving apparatus 70, the flue gas of flue gas waste heat recovery apparatus 70 is passed through and is passed through the water of flue gas waste heat recovery apparatus 70 in cigarette
Heat exchange is carried out in gas waste-heat recovery device 70；
Flue gas discharge in flue gas waste heat recovery apparatus 70 after heat exchange utilizes；It is hot in flue gas waste heat recovery apparatus 70
Water after exchange is passed through steam generator.
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 recycling system of pyrolysis gas, the pyrolysis gas carries out pyrolysis generation by pyrolysis oven to coal, it is characterised in that
Also include fused salt heat exchanging device；
The fused salt heat exchanging device is provided with one-level pyrolysis gas entrance, one-level pyrolysis gas outlet, one-level fused salt entrance and one-level fused salt
Outlet；The one-level pyrolysis gas entrance connects the pyrolysis gas outlet of the pyrolysis oven by pipeline；
The pyrolysis gas enters the fused salt heat exchanging device by the one-level pyrolysis gas entrance, and fused salt is entered by the one-level fused salt
Mouth is sent into the fused salt heat exchanging device；The temperature of the fused salt is less than the temperature of the pyrolysis gas；
The fused salt and pyrolysis gas heat exchange in the fused salt heat exchanging device, the pyrolysis gas after heat exchange is by the one-level
Pyrolysis gas outlet discharge is utilized, and the fused salt after heat exchange is exported by the one-level fused salt and discharged.
2. pyrolysis gas recycling system according to claim 1, it is characterised in that the fused salt heat exchanging device is board-like
Heat exchanger.
3. pyrolysis gas recycling system according to claim 1, it is characterised in that also including steam generator,
The steam generator is provided with two level fused salt entrance, the outlet of two level fused salt, one-level steam inlet, one-level steam (vapor) outlet；Institute
State two level fused salt inlet duct and connect the one-level fused salt outlet；
Enter the steam generator through the two level fused salt entrance by the fused salt of one-level fused salt outlet discharge；Described one
Level steam inlet is passed through water vapour, and the water vapour enters the steam generator；The temperature of the water vapour is less than and enters institute
State the temperature of the fused salt of steam generator；
Fused salt and water vapour heat exchange in the steam generator into the steam generator, send out in the steam
Fused salt in raw device after heat exchange is exported by two level fused salt discharges, and the water vapour in the steam generator after heat exchange is by institute
State the discharge of one-level steam (vapor) outlet.
4. pyrolysis gas recycling system according to claim 3, it is characterised in that also including preheater,
The preheater is provided with preheater fused salt entrance, the outlet of preheater fused salt, preheater water inlet, preheater steam (vapor) outlet；
The preheater fused salt inlet duct connects the two level fused salt outlet, and the preheater steam (vapor) outlet pipeline connects the one-level
Steam inlet；
Enter the preheater through the preheater fused salt entrance by the fused salt of two level fused salt outlet discharge；
Water is passed through in the preheater water inlet, the water enters the preheater, and the temperature of the water is less than into described pre-
The temperature of the fused salt of hot device；The water with enter the preheater fused salt in the preheater heat exchange and produce water steaming
Vapour；
Fused salt in the preheater after heat exchange is exported by the preheater fused salt discharges；Caused by the preheater
Water vapour enters the steam generator by the preheater water out through the one-level steam inlet.
5. pyrolysis gas recycling system according to claim 4, it is characterised in that also filled including flue gas waste heat recovery
Put；The flue gas waste heat recovery apparatus is provided with cooling medium entrance, cooling medium outlet and waste-heat recovery device exhanst gas outlet, remaining
Heat reclamation device smoke inlet；
The exhanst gas outlet pipeline of the pyrolysis oven connects the waste-heat recovery device smoke inlet；Flue gas caused by the pyrolysis oven
The waste-heat recovery device is passed through by the flue gas waste heat recovery apparatus smoke inlet, cooling medium is by the cooling medium entrance
It is sent into the flue gas waste heat recovery apparatus；The temperature for being passed through the flue gas of the flue gas waste heat recovery apparatus is higher than the cooling medium
Temperature, it is hot in the flue gas waste heat recovery apparatus to be passed through the flue gas of the flue gas waste heat recovery apparatus and the cooling medium
Exchange；
Flue gas in the flue gas waste heat recovery apparatus after heat exchange discharges profit by the exhanst gas outlet of the waste-heat recovery device
With；Cooling medium in the flue gas waste heat recovery apparatus after heat exchange is exported by the cooling medium discharges.
6. pyrolysis gas recycling system according to claim 5, it is characterised in that the cooling medium is water；
The cooling medium outlet conduit connects the preheater water inlet, the water in the waste-heat recovery device after heat exchange
It is passed through through cooling medium outlet in the preheater.
7. pyrolysis gas recycling system according to claim 1, it is characterised in that described molten also including fused salt storage tank
Salt storage tank connects the one-level fused salt entrance by pipeline, and the fused salt storage tank is used to store fused salt；
The pipeline is provided with pump for liquid salts, and the fused salt in the fused salt storage tank is delivered to the fused salt heat exchanging and filled by the pump for liquid salts
Put.
8. pyrolysis gas recycling system according to claim 7, it is characterised in that the fused salt storage tank is stored up provided with fused salt
Tank fused salt entrance and the outlet of fused salt storage tank fused salt, the fused salt storage tank fused salt outlet conduit connect the one-level fused salt entrance, institute
State fused salt storage tank fused salt inlet duct and connect the preheater fused salt outlet, the fused salt that discharge is exported by the preheater fused salt passes through
The fused salt storage tank fused salt entrance is sent into the fused salt storage tank.
9. a kind of pyrolysis gas recoverying and utilizing method, it is characterised in that recycled using any pyrolysis gas of claim 1-8
System, including：
Step S1, pyrolysis gas caused by the pyrolysis oven is passed through the fused salt heat exchanging device, in the fused salt heat exchanging device
It is passed through fused salt；
Step S2, the pyrolysis gas and fused salt for being passed through the fused salt heat exchanging device carry out heat exchange in the fused salt heat exchanging device；
Step S3, the pyrolysis gas after being exchanged heat in the fused salt heat exchanging device is discharged by the one-level pyrolysis gas outlet to be utilized；
Fused salt after being exchanged heat in the fused salt heat exchanging device is exported by the one-level fused salt discharges.
10. the pyrolysis gas recoverying and utilizing method according to right will go 9, it is characterised in that including：
Step S4, the fused salt discharged by the fused salt heat exchanging device is passed through the steam generator；Sent out simultaneously in the steam
Water vapour is passed through in raw device；The fused salt for being passed through the steam generator and the water vapour for being passed through the steam generator carry out hot friendship
Change；Water vapour in the steam generator after heat exchange is discharged by the one-level steam (vapor) outlet；
Step S5, the fused salt after the heat exchange in the steam generator is passed through the preheater；
Meanwhile water is passed through in the preheater, the water being passed through in the preheater exists with the fused salt being passed through in the preheater
Heat exchange is carried out in the preheater and produces water vapour；
Step S6, the fused salt after the heat exchange in the preheater is passed through the fused salt storage tank, the water vapour is passed through institute
State steam generator；
Step S7.1, the fused salt in the fused salt storage tank is pumped into the fused salt heat exchanging device by the fused salt；
Step S7.2, flue gas caused by the pyrolysis oven is passed through the flue gas waste heat recovery apparatus, while more than the flue gas
Water is passed through in heat reclamation device, the flue gas of the flue gas waste heat recovery apparatus is passed through and is passed through the flue gas waste heat recovery apparatus
Water carries out heat exchange in the flue gas waste heat recovery apparatus；
Flue gas discharge in the flue gas waste heat recovery apparatus after heat exchange utilizes；It is hot in the flue gas waste heat recovery apparatus
Water after exchange is passed through the steam generator.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114853611A (en) * | 2022-05-16 | 2022-08-05 | 华中科技大学 | Method for treating biomass pyrolysis gas |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102643703A (en) * | 2012-05-08 | 2012-08-22 | 山东天力干燥股份有限公司 | Novel external heating type lignite pyrolysis quality increasing system and process |
| CN204509191U (en) * | 2015-02-04 | 2015-07-29 | 昆明普利惠节能技术有限公司 | Take high-temperature molten salt as the new Type Coke Oven ascending tube crude-gas residual neat recovering system of medium |
| US20180100647A1 (en) * | 2015-04-21 | 2018-04-12 | General Electric Technology Gmbh | Molten salt once-through steam generator |
| CN207811665U (en) * | 2017-11-16 | 2018-09-04 | 北京神雾电力科技有限公司 | A kind of pyrolysis gas recycling system |
-
2017
- 2017-11-16 CN CN201711138050.6A patent/CN107760339A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102643703A (en) * | 2012-05-08 | 2012-08-22 | 山东天力干燥股份有限公司 | Novel external heating type lignite pyrolysis quality increasing system and process |
| CN204509191U (en) * | 2015-02-04 | 2015-07-29 | 昆明普利惠节能技术有限公司 | Take high-temperature molten salt as the new Type Coke Oven ascending tube crude-gas residual neat recovering system of medium |
| US20180100647A1 (en) * | 2015-04-21 | 2018-04-12 | General Electric Technology Gmbh | Molten salt once-through steam generator |
| CN207811665U (en) * | 2017-11-16 | 2018-09-04 | 北京神雾电力科技有限公司 | A kind of pyrolysis gas recycling system |
Non-Patent Citations (1)
| Title |
|---|
| 陈昆柏, 河南科学技术出版社 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114853611A (en) * | 2022-05-16 | 2022-08-05 | 华中科技大学 | Method for treating biomass pyrolysis gas |
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