CN106989610A - Heat power generating system based on coke-oven plant's heat recovery - Google Patents
Heat power generating system based on coke-oven plant's heat recovery Download PDFInfo
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- CN106989610A CN106989610A CN201710352837.6A CN201710352837A CN106989610A CN 106989610 A CN106989610 A CN 106989610A CN 201710352837 A CN201710352837 A CN 201710352837A CN 106989610 A CN106989610 A CN 106989610A
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- coke
- heat
- heat recovery
- dry
- waste
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- 238000011084 recovery Methods 0.000 title claims abstract description 98
- 239000000571 coke Substances 0.000 claims abstract description 245
- 239000007789 gas Substances 0.000 claims abstract description 139
- 238000010791 quenching Methods 0.000 claims abstract description 117
- 230000000171 quenching effect Effects 0.000 claims abstract description 117
- 239000002918 waste heat Substances 0.000 claims abstract description 90
- 239000003245 coal Substances 0.000 claims abstract description 21
- 238000004519 manufacturing process Methods 0.000 claims abstract description 18
- 239000008400 supply water Substances 0.000 claims abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 47
- 230000008676 import Effects 0.000 claims description 15
- 238000001816 cooling Methods 0.000 claims description 12
- 238000013459 approach Methods 0.000 claims description 10
- 235000014171 carbonated beverage Nutrition 0.000 claims description 8
- 229920006395 saturated elastomer Polymers 0.000 claims description 7
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 6
- 238000011049 filling Methods 0.000 claims description 6
- 239000003546 flue gas Substances 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 5
- 239000002826 coolant Substances 0.000 claims description 3
- 230000000630 rising effect Effects 0.000 claims description 3
- 238000004891 communication Methods 0.000 claims description 2
- 150000001875 compounds Chemical class 0.000 claims description 2
- 238000001704 evaporation Methods 0.000 claims 1
- 230000008020 evaporation Effects 0.000 claims 1
- 238000010025 steaming Methods 0.000 claims 1
- 238000005516 engineering process Methods 0.000 abstract description 9
- 238000010276 construction Methods 0.000 abstract description 4
- 230000005611 electricity Effects 0.000 abstract description 4
- 230000010354 integration Effects 0.000 abstract 1
- 238000000034 method Methods 0.000 description 12
- 230000008569 process Effects 0.000 description 8
- 238000004939 coking Methods 0.000 description 6
- 238000010248 power generation Methods 0.000 description 5
- 239000002912 waste gas Substances 0.000 description 5
- 238000003763 carbonization Methods 0.000 description 4
- 238000006392 deoxygenation reaction Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 239000007921 spray Substances 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 235000019504 cigarettes Nutrition 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000005553 drilling Methods 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000005457 optimization Methods 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 238000005273 aeration Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000010000 carbonizing Methods 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 230000008602 contraction Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 238000007726 management method Methods 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000011819 refractory material Substances 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/004—Systems for reclaiming waste heat
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01D—NON-POSITIVE DISPLACEMENT MACHINES OR ENGINES, e.g. STEAM TURBINES
- F01D15/00—Adaptations of machines or engines for special use; Combinations of engines with devices driven thereby
- F01D15/10—Adaptations for driving, or combinations with, electric generators
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K27/00—Plants for converting heat or fluid energy into mechanical energy, not otherwise provided for
- F01K27/02—Plants modified to use their waste heat, other than that of exhaust, e.g. engine-friction heat
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/004—Systems for reclaiming waste heat
- F27D2017/006—Systems for reclaiming waste heat using a boiler
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Environmental & Geological Engineering (AREA)
- Coke Industry (AREA)
Abstract
The invention provides a kind of heat power generating system based on coke-oven plant's heat recovery, including：Coke oven, coke dry quenching furnace, raw coke oven gas waste-heat recovery device, stack gases waste-heat recovery device and dry coke quenching residual heat boiler and high pressure, low pressure drum, high-pressure superheater, high pressure evaporator, high-pressure economizer, low-pressure superheater, low pressure evaporator and low-pressure coal saver are disposed with the dry coke quenching residual heat boiler, wherein low pressure drum is that the raw coke oven gas waste-heat recovery device and stack gases waste-heat recovery device supply water.The present invention can carry out comprehensive integration recovery to the coke sensible heat, crude-gas sensible heat and stack gases sensible heat produced in coke dry quenching furnace production technology and be generated electricity for driving steam turbine, compared with the pattern that three kinds of traditional residual heat resources are individually reclaimed, system is greatly simplified, construction cost is greatly reduced, and the overall efficiency of residual neat recovering system is obviously improved.
Description
Technical field
Field is utilized the present invention relates to coking industry waste heat of coke oven, specifically, more particularly to one kind can be to coke oven area
The thermal power generation system based on coke-oven plant's heat recovery that the waste heat that domain is produced in coking is reclaimed and recycled
System.
Background technology
Coke oven, coke oven in other words, refer under normal conditions it is a kind of with refractory material build city be used for make coal carbonization,
Equipment to produce coke, is the main Thermal Equipment of coking.In coke oven the main production of coke be using coal as raw material,
Under conditions of isolation cut-in without ball, coal is heated to 950 degrees Celsius to 1050 degrees Celsius, drying, pyrolysis, melting, bonding,
The high temperature distillation process such as solidification, contraction, finally give coke.
In above process, the heating process in production process in coke oven produces substantial amounts of raw coke oven gas, a large amount of raw coke oven gas tools
There is considerable sensible heat, meanwhile, produce the coke obtained and all have substantial amounts of sensible heat in the flue gas obtained in production.In energy
It is aobvious to crude-gas sensible heat, coke sensible heat and stack gases under the prior art that source problem and production cost management and control increasingly sharpen
The waste heat recovery of heat turns into the emphasis problem of coking industry common concern.
In the prior art, to the above-mentioned three kinds of sensible heats referred to, corresponding mode carries out waste heat recovery：
1) coke sensible heat：After the completion of high-temperature retorting technique in process of coking as previously described, obtain temperature and taken the photograph 950
Red Jiao of the coke of family name's degree to 1050 degrees Celsius, referred to as high temperature, for the ease of transporting and storing, it is necessary to enter to described red Jiao of high temperature
Row cooling, makes its temperature be down to 250 degrees centigrades, the process is referred to as quenching.Quenching can be divided into stove puts out outside quenching and stove
Jiao, with the development of coking technology, nowadays many by the way of the outer quenching of stove, the outer quenching of stove can be divided into CDQ and wet again
Method quenching, that is, the dry coke quenching being commonly called as and coke wet quenching.
Wet method of putting out is to be conveyed directly to high temperature red Jiao to be provided with multiple spray heads at the top of quenching tower, quenching tower, from spray
A large amount of water at low temperature are sprayed in water drenching head, low temperature Water spray reaches on red Jiao of high temperature to be produced largely in cooling effect, cooling procedure
Steam, then these steam are reclaimed by other means；The process of dry coke quenching, then be to be carried with circulated inert gas as heat
Body, coke cooling chamber is inputted by circulating fan by cold recyclegas, and high-temperature coke is cooled to after 250 degrees Celsius and discharged, and
And the recyclegas warp that the gas after coke sensible heat is imported after boiler progress recovery heat, generation steam, recovery heat will be absorbed
After supercooling, dedusting, then cooling chamber is returned to by blower fan cooled down again, so circulation.
2) crude-gas sensible heat：Generally used under prior art, the pipe such as tedge, bridge tube is set at the top of carbonization chamber
Road, is pooled to carbonization chamber headroom, and import by these pipelines by the raw coke oven gas produced during carbonization chamber high-temperature retorting
It is then, using the mode of ammonia spray, raw coke oven gas of the temperature in 650 degrees Celsius to 800 degree Celsius ranges is cold in dry pipe
But to 85 degrees centigrades.In this approach, the heat of raw coke oven gas is not recycled utilization, causes the huge wave of heat
Take.
3) stack gases sensible heat：The stack gases temperature produced in being produced due to coke oven is relatively low, and temperature is generally Celsius 240
Spend in the range of 280 degrees Celsius, belong to low grade heat energy.Single waste-heat recovery device is generally set to enter low grade heat energy
Row reclaims and produces low-pressure saturated steam, but the value of the low-pressure saturated steam of production is relatively low, and to low grade heat energy
Required heat-energy recovering apparatus cost is again higher, so, the processing mode for stack gases sensible heat is typically direct discharge.
In summary, the recycling of STRENGTH ON COKE sensible heat, crude-gas sensible heat and stack gases sensible heat is all in the prior art
Using independent process, the mode individually reclaimed, heat recovery rate is relatively low, and covers reclaimer more, can undoubtedly bring and is
The increase for complexity, construction costs and the operating cost of uniting.
In view of this, a kind of new mode should be provided, to the various sensible heat heat energy produced in coke dry quenching furnace production technology
Carry out integrated recycling.
The content of the invention
In order to solve the above-mentioned technical problem the present invention makes, and the purpose is to provide one kind to give birth to coke dry quenching furnace
The coke sensible heat, crude-gas sensible heat and the stack gases sensible heat that are produced in production. art carry out the thermal power generation system of comprehensive reutilization
The various residual heat resources in coke-oven plant are planned as a whole by system, simplify the complexity in system, a variety of waste heats are entered in the most optimal way
The integrated recycling of row.
To achieve these goals, the invention provides a kind of thermal power generation system based on coke-oven plant's heat recovery
System, it is characterised in that including coke oven, coke dry quenching furnace, dry coke quenching residual heat boiler, raw coke oven gas waste-heat recovery device, stack gases waste heat
Retracting device, high pressure drum, low pressure drum, forced circulation pump, steam turbine and generator, wherein,
The coke export of the coke oven is connected with the coke inlet of the coke dry quenching furnace, the high-temperature coke produced in the coke oven
It is sent in the coke dry quenching furnace and cools down；
The exhanst gas outlet of the coke oven is connected with the stack gases waste-heat recovery device, the flue produced in the coke oven
Waste gas, is discharged in the stack gases waste-heat recovery device；
The raw coke oven gas waste-heat recovery device is connected by tedge with the coke oven, the raw coke oven gas produced in the coke oven
It is discharged in the raw coke oven gas waste-heat recovery device and is cooled down；
The low pressure drum is connected by down-comer with the import of forced circulation pump, the outlet difference of the forced circulation pump
It is connected with the water inlet of the raw coke oven gas waste-heat recovery device and the stack gases waste-heat recovery device, respectively described waste coal
Gas waste-heat recovery device and the stack gases waste-heat recovery device supply water；
The stack gases waste-heat recovery device, the raw coke oven gas waste-heat recovery device pass through the low pressure drum and institute
State dry coke quenching residual heat boiler to be connected, the vapour that the stack gases waste-heat recovery device and the raw coke oven gas waste-heat recovery device are produced
Aqueous mixtures carry out feeding dry coke quenching residual heat boiler after steam-water separation in the drum and overheated；
The gas approach of the dry coke quenching residual heat boiler is connected with the recyclegas outlet in the coke dry quenching furnace, described dry to put out
The exhanst gas outlet of coke waste heat boiler is connected with the recyclegas import in the coke dry quenching furnace, forms circulation loop, the dry coke quenching
Waste heat boiler is reclaimed to the sensible heat of the recyclegas；Superheater, evaporator are provided with the dry coke quenching residual heat boiler
And economizer, the air intake of the steam turbine is connected with the venthole of the superheater, the steam turbine and the generator
It is connected, wherein,
During the system operation production, the high-temperature coke of the coke oven output is pushed into the coke dry quenching furnace
The dry cooling medium put out in cooling, the coke dry quenching furnace of row is recyclegas, after the recyclegas absorption heat, dry is put out from described
The recyclegas outlet of stove is discharged, and enters the gas approach of the dry coke quenching residual heat boiler by pipeline, by the overheat
Cool, discharged from the exhanst gas outlet of the dry coke quenching residual heat boiler, then pass through pipe after device, evaporator and economizer heat exchange
Road returns to the recyclegas import of the coke dry quenching furnace, so circulation；
The low pressure drum is respectively the raw coke oven gas waste-heat recovery device and the stack gases by forced circulation pump
Waste-heat recovery device provides feedwater, and, the vapour of the raw coke oven gas waste-heat recovery device and the stack gases waste-heat recovery device
Aqueous mixtures are exported, and all the rising mouth of pipe with the low pressure drum is connected, and are constituted two-way and are forced steam/water circulating；
The saturated vapor that the high pressure drum and the low pressure drum are isolated respectively enters the superheater overheat, and warp
Steam after overheat, enters from the air intake of the steam turbine, drives the steam turbine to do work and drives the generator to send out
Electricity.
Preferably, in the dry coke quenching residual heat boiler, the superheater includes high-pressure superheater and low-pressure superheater, institute
Stating evaporator includes high pressure evaporator and low pressure evaporator, and the economizer includes high-pressure economizer and low-pressure coal saver.
It is high-pressure superheater, high pressure evaporator, high-pressure economizer, low it is further preferred that in the dry coke quenching residual heat boiler
Pressure superheater, low pressure evaporator, low-pressure coal saver are set gradually according to flue gas flow direction.
Still further preferably, the air intake of the high-pressure superheater is connected with the venthole of the high pressure drum, described
The venthole of high-pressure superheater is connected with the main air intake of the steam turbine；The water inlet and venthole of the high pressure evaporator point
Do not connected by down-comer and tedge with the high pressure drum, form high pressure carbonated drink natural convection loop；The high pressure saves coal
The water inlet of device is connected with the delivery port of the low pressure drum, and feed pump is provided with connecting pipeline, the high-pressure economizer
Delivery port is connected with the water inlet of the high pressure drum.
Preferably, the air intake of the low-pressure superheater is connected with the low pressure drum, and the low-pressure superheater goes out vapour
Mouth is connected with the filling mouth of the steam turbine；The water inlet and venthole of the low pressure evaporator pass through down-comer and rising respectively
Pipe is connected with the low pressure drum, forms low pressure vapor natural convection loop.
Preferably, condenser, the air intake of the condenser and the steamer are provided with the steam drain of the steam turbine
The steam drain connection of machine, the water inlet of the delivery port of the condenser successively with condensate pump, the low-pressure coal saver is connected.
Preferably, oxygen-eliminating device, the water inlet of the oxygen-eliminating device and the low-pressure coal saver are provided with the low pressure drum
Delivery port connection.
Preferably, the system also includes the first deduster and the second deduster, and first deduster is arranged on described
On the pipeline that the recyclegas outlet of coke dry quenching furnace is connected with the gas approach of the dry coke quenching residual heat boiler, second deduster
It is described on the pipeline for being arranged on the exhanst gas outlet of the dry coke quenching residual heat boiler and the recyclegas inlet communication of the coke dry quenching furnace
Circulating fan is additionally provided between second deduster and the recyclegas import of the coke dry quenching furnace.
Understood as described above with practice, the thermal power generation of the present invention based on coke-oven plant's heat recovery
System, is integrated back to the coke sensible heat, crude-gas sensible heat and stack gases sensible heat produced in coke dry quenching furnace production technology
Receive and utilize, respectively by dry coke quenching residual heat boiler, raw coke oven gas waste-heat recovery device, stack gases waste-heat recovery device to more than three kinds
Thermal resource is reclaimed, and the progress of waste heat recovery therrmodynamic system is highly integrated, and according to heat source characteristic, by a whole set of boiler circuit
High pressure, low pressure two systems are designed to, the optimization design of therrmodynamic system is fully carried out based on the second law of thermodynamics, passes through flue gas
Heat quality is matched with carbonated drink grade, realizes the step Optimum utilization of smoke heat energy, and coke oven region residual heat resources
The limit is reclaimed.The present invention only sets a steam turbine to digest high pressure, the steam resource of two grades of low pressure, greatly reduces
The cost of investment of coke oven region afterheat generating system, and diffusing for low-pressure steam resource is avoided, realize the maximum of resource
Change and utilize.Present invention optimizes dry coke quenching residual neat recovering system, coke oven coke oven uprising tube raw coke oven gas residual neat recovering system and coke oven cigarette
The pattern that road waste gas afterheat recovery system is independently arranged, is returned to dry coke quenching residual neat recovering system, coke oven coke oven uprising tube raw coke oven gas waste heat
Receipts system, the therrmodynamic system of stack gases residual neat recovering system carry out height coupling, enormously simplify boiler circuit so that a whole set of
Heat power generating system is more succinct, and project occupation of land area and construction totle drilling cost are greatly reduced.Because three kinds of residual heat resources are
Produced simultaneously with coke oven production technology, therefore the present invention has good exploitativeness and actual application value.
Brief description of the drawings
Fig. 1 is schematic diagram, shows the heat power generating system of the present invention based on coke-oven plant's heat recovery
Structure；
Fig. 2 is schematic diagram, is shown in the heat power generating system recycled based on coke-oven plant's residual heat resources shown in Fig. 1
Dry coke quenching residual heat boiler in structure.
Embodiment
The heat power generating system of the present invention based on coke-oven plant's heat recovery described below with reference to the accompanying drawings
Embodiment.One of ordinary skill in the art will recognize, without departing from the spirit and scope of the present invention, can
To be modified with a variety of modes to described embodiment.Therefore, accompanying drawing and description are inherently illustrative,
It is not intended to limit the scope of the claims.In addition, in this manual, accompanying drawing is drawn not in scale, and it is identical
Reference represent identical part.
Fig. 1 is schematic diagram, shows the heat power generating system of the present invention based on coke-oven plant's heat recovery
Attachment structure.As shown in figure 1, the heat power generating system of the present invention based on coke-oven plant's heat recovery include coke oven 1,
Coke dry quenching furnace 2, dry coke quenching residual heat boiler 4, raw coke oven gas waste-heat recovery device 7, stack gases waste-heat recovery device 8, high pressure drum 16,
Low pressure drum 14, forced circulation pump 17, steam turbine 9 and generator 10, wherein, the coke export of coke oven 1 and Jiao of coke dry quenching furnace 2
Charcoal entrance is connected, and the high-temperature coke of output, which is sent in coke dry quenching furnace 2, in coke oven 1 is cooled down (as shown by arrows in FIG.), coke oven 1
Exhanst gas outlet be connected with stack gases waste-heat recovery device 8, coke oven 1 produce stack gases, be discharged to stack gases waste heat
In retracting device 8.Raw coke oven gas waste-heat recovery device 7 is connected by tedge with coke oven 1, and the raw coke oven gas produced in coke oven 1 is arranged
Cooled down into raw coke oven gas waste-heat recovery device.In this embodiment of the invention, in raw coke oven gas waste-heat recovery device 7, coke oven 1 is given birth to
The raw coke oven gas produced during production contains substantial amounts of sensible heat, and raw coke oven gas is entered more than raw coke oven gas from the top of coke oven 1 by tedge
In heat reclamation device 7, heat is released in raw coke oven gas waste-heat recovery device 7.Meanwhile, coke oven flue waste gas is arranged from the bottom of coke oven 1
Go out, heat is released into stack gases waste-heat recovery device 8, and in stack gases waste-heat recovery device 8.
Gas approach 41 on dry coke quenching residual heat boiler 4 is connected by pipeline with the recyclegas outlet 21 in coke dry quenching furnace 2,
Exhanst gas outlet 42 thereon is connected by pipeline with the recyclegas import 22 of coke dry quenching furnace 2, forms a circulation loop, i.e. dry
Putting out is used in stove 2 after the red burnt inert gas absorption heat of cooling down high-temperature, is discharged into by pipeline in dry coke quenching residual heat boiler 4, and
It is cooled in dry coke quenching residual heat boiler 4, finally discharges dry coke quenching residual heat boiler 4, and is returned in coke dry quenching furnace 2, it is lazy as circulating
Property gas is continuing with, and is circulated with this.In addition, recyclegas outlet 21 and the flue gas of dry coke quenching residual heat boiler 4 of coke dry quenching furnace 2
The first deduster 3, the exhanst gas outlet 42 of dry coke quenching residual heat boiler 4 and following for coke dry quenching furnace 2 are provided with the pipeline that import 41 is connected
It is provided between the second deduster 5, and the second deduster 5 and coke dry quenching furnace 2 and is additionally provided with the pipeline that ring gas feed 22 is connected
Circulating fan 6.
The water inlet of the raw coke oven gas waste-heat recovery device 7 and stack gases waste-heat recovery device 8 with low pressure drum 14
The decline mouth of pipe be connected, be provided with forced circulation pump 17 on connecting line, the low pressure drum 14 passes through 17 points of forced circulation pump
Not Wei raw coke oven gas waste-heat recovery device 7 and stack gases waste-heat recovery device 8 supply water.
Raw coke oven gas waste-heat recovery device 7 is connected by low pressure drum 14 with dry coke quenching residual heat boiler 4, and its carbonated drink produced is mixed
Compound carries out sending into dry coke quenching residual heat boiler 4 after steam-water separation in low pressure drum 14.Equally, stack gases waste-heat recovery device
8 are connected also by low pressure drum 14 with dry coke quenching residual heat boiler 4, and its steam water interface produced is also carried out in low pressure drum 14
Dry coke quenching residual heat boiler 4 is sent into after steam-water separation.
Superheater, evaporator and economizer, the main steam import 91 of steam turbine 9 are provided with dry coke quenching residual heat boiler 4
It is connected with the venthole of the superheater, the steam turbine 9 is connected with generator 10.
It is additionally provided with low pressure drum 14 at oxygen-eliminating device 13, the steam drain 93 of steam turbine 9 and is provided with condenser 11, condenser
11 air intake 111 is connected with the steam drain 93 of steam turbine 9, and the delivery port 112 of condenser 11 passes through condensate pump 12 and province's coal
The water inlet connection of device, the water inlet of oxygen-eliminating device 13 is connected with the delivery port of economizer.
During the system operation production, the high-temperature coke of the output of coke oven 1, which is pushed into coke dry quenching furnace 2, carries out dry put out
Cooling medium in cooling, coke dry quenching furnace 2 is recyclegas, and recyclegas is absorbed after heat, is exported from the recyclegas of coke dry quenching furnace 2
21 discharge, and enter the gas approach of dry coke quenching residual heat boiler 4 by pipeline, by the superheater, evaporator and province's coal
Cool, and discharged from the exhanst gas outlet 42 of dry coke quenching residual heat boiler 4 after device heat exchange, then coke dry quenching furnace 2 is returned to by pipeline
Recyclegas import 22, so circulation；The low-pressure section for the steam water interface that evaporator in dry coke quenching residual heat boiler 4 is produced
Into low pressure drum 14, low pressure drum 14 is respectively raw coke oven gas waste-heat recovery device 7 and stack gases by forced circulation pump 17
Waste-heat recovery device 8 supplies water, the steam water interface that raw coke oven gas waste-heat recovery device 7 and stack gases waste-heat recovery device 8 are produced
Low pressure drum 14 is returned again, and the saturated vapor that low pressure drum 14 and high pressure drum 16 are produced respectively enters dry coke quenching residual heat boiler 4
Overheated, the superheated steam that dry coke quenching residual heat boiler 4 is exported enters steam turbine 9, drive steam turbine 9 to do work and generate electricity.
Fig. 2 is schematic diagram, is shown dry in the heat power generating system based on coke-oven plant's heat recovery shown in Fig. 1
Structure in quenching waste heat boiler.In this embodiment of the invention, according to from its gas approach 41 in dry coke quenching residual heat boiler 4
To the direction of exhanst gas outlet 42, high-pressure superheater 43, high pressure evaporator 44, high-pressure economizer 45, low area overheat are disposed with
Device 46, low pressure evaporator 47 and low-pressure coal saver 48.
The attachment structure in dry coke quenching residual heat boiler in the embodiment of the present invention is detailed below.Referring to Fig. 1 and figure
2, the air intake 432 of high-pressure superheater 43 is connected with the venthole 161 of high pressure drum 16, the venthole 431 of high-pressure superheater 43
Connected with the main steam import 91 of steam turbine 9；The water inlet 442 and venthole 441 of high pressure evaporator 44 pass through down-comer respectively
Connected with tedge with high pressure drum 16, form high pressure carbonated drink Natural Circulation；The water inlet 452 and low pressure cooker of high-pressure economizer 45
Feed pump 15, delivery port 451 and the high pressure drum 16 of high-pressure economizer 45 are provided with the delivery port connection of cylinder 14, connecting pipeline
Water inlet 162 connect.The air intake 462 of low-pressure superheater 46 is connected with low pressure drum 14, the venthole of low-pressure superheater 46
461 connect with the filling mouth 92 of steam turbine 9；The water inlet 472 and venthole 471 of low pressure evaporator 47 respectively by down-comer and
Tedge is connected with low pressure drum 14, forms low pressure vapor natural convection loop.In addition, the delivery port 481 of low-pressure coal saver 48
Connected with the water inlet of oxygen-eliminating device 13, the water inlet 482 of low-pressure coal saver 48 passes through the water outlet of condensate pump 12 and condenser 11
Mouth 112 is connected.
In actual production process, the red coke feeding coke dry quenching furnace 2 of high temperature released from the carbonizing chamber of coke oven 1 passes through circulating air
Body is cooled down, and arranged the high temperature circulation gas come after absorption heat in coke dry quenching furnace 2 separates coarse granule by the first deduster 3
After coke powder, heat exchange is carried out into dry coke quenching residual heat boiler 4, is that dry coke quenching residual heat boiler 4 provides thermal source；Dry coke quenching residual heat boiler
The low-temperature circulating gas discharged after 4 absorbing and cooling temperatures passes through blower fan 6 after the further separate fine particles coke powder of the second deduster 5
Pressurization is then returned to the bottom air inlet mouthful of coke dry quenching furnace 2, is continued on for cooling down red Jiao of high temperature to be cooled in coke dry quenching furnace, is formed one
Circulating cooling process.
The raw coke oven gas waste-heat recovery device 7 entered from the raw coke oven gas of the top of coke oven 1 discharge at the top of coke oven, raw coke oven gas waste heat is returned
Receiving apparatus 7 absorbs the sensible heat of raw coke oven gas, and raw gas temperature is reduced into 500 DEG C or so from 800 DEG C or so.
The stack gases waste heat that the low temperature flue waste gas come out from the flue of coke oven 1 is introduced into the setting of the bottom side of coke oven 1 is returned
Receiving apparatus 8, stack gases waste-heat recovery device 8 absorbs the sensible heat of flue waste vapour, and stack gases temperature is reduced to from 280 DEG C or so
160 DEG C or so.Recyclegas is cooled to 150 DEG C or so by dry coke quenching residual heat boiler 4 from 900 DEG C or so.
The superheated steam that the high-pressure superheater 43 of dry coke quenching residual heat boiler 4 is discharged is dry to put out as main steam red switch steam turbine 9
The superheated steam that the low-pressure superheater 46 of coke waste heat boiler 4 is discharged enters steam turbine 9 as filling, and main steam and filling are driven jointly
Dynamic steam turbine 9 rotates and drives generator 10 to generate electricity.
The steam discharge of the low pressure (LP) cylinder of steam turbine 9 enters condenser 11, and condensate is condensed into condenser 11.In condenser 11
Condensate is pressurizeed by condensate pump 12, is then sent to the low-pressure coal saver 48 of dry coke quenching residual heat boiler 4；Condensate is saved in low pressure
Feeding oxygen-eliminating device 13 carries out deoxygenation after being preheated in coal device 48, and the water after deoxygenation falls into the low pressure stage pot for being arranged on the lower section of oxygen-eliminating device 13
Cylinder 14.Deaerating type of cycles is used passes through down-comer and tedge between deoxygenation pattern, i.e. low pressure drum 14 and low pressure evaporator 47
Natural Circulation process is formed, low pressure drum 14 is again between raw coke oven gas waste-heat recovery device 7 and stack gases waste-heat recovery device 8
Pass through the formation two-way forced circulation process of forced circulation pump 17, raw coke oven gas waste-heat recovery device 7, stack gases waste-heat recovery device
8 and the steam water interface that produces of low pressure evaporator 47 steam-water separation is carried out in the low pressure drum 14, the saturated vapor of generation enters
Enter oxygen-eliminating device 13, thermal de-aeration is carried out to the condensate of low-pressure coal saver 48.The saturation separated of low pressure drum 14 is steamed
Vapour, removes the part that deoxygenation autophage falls, residual steam is overheated into low-pressure superheater 46, subsequently into steam turbine 9
Filling mouth 92.
The delivery port of low pressure drum 14 is connected with the water inlet 452 of high-pressure economizer 45, the water outlet of low pressure drum by
Water pump 15 is delivered to after pressurizeing to be heated in high-pressure economizer 45, then enters high pressure by the water inlet 162 of high pressure drum 16
Drum 16, high pressure drum 16 is connected by the water inlet 442 and venthole 441 of down-comer and tedge and high pressure evaporator 44 respectively
It is logical, high pressure carbonated drink Natural Circulation is formed, the saturated vapor that high pressure drum 16 is isolated is overheated into high-pressure superheater 43, so
Enter the main steam import 91 of steam turbine 9 afterwards.
Understood as described above with practice, the thermal power generation of the present invention based on coke-oven plant's heat recovery
System, is integrated back to the coke sensible heat, crude-gas sensible heat and stack gases sensible heat produced in coke dry quenching furnace production technology
Receive and utilize, respectively by dry coke quenching residual heat boiler, raw coke oven gas waste-heat recovery device, stack gases waste-heat recovery device to more than three kinds
Thermal resource is reclaimed, and the progress of waste heat recovery therrmodynamic system is highly integrated, and according to heat source characteristic, by a whole set of boiler circuit
High pressure, low pressure two systems are designed to, the optimization design of therrmodynamic system is fully carried out based on the second law of thermodynamics, passes through flue gas
Heat quality is matched with carbonated drink grade, realizes the step Optimum utilization of smoke heat energy, and coke oven region residual heat resources
The limit is reclaimed.The present invention only sets a steam turbine to digest high pressure, the steam resource of two grades of low pressure, greatly reduces
The cost of investment of coke oven region afterheat generating system, and diffusing for low-pressure steam resource is avoided, realize the maximum of resource
Change and utilize.Present invention optimizes dry coke quenching residual neat recovering system, coke oven coke oven uprising tube raw coke oven gas residual neat recovering system and coke oven cigarette
The pattern that road waste gas afterheat recovery system is independently arranged, is returned to dry coke quenching residual neat recovering system, coke oven coke oven uprising tube raw coke oven gas waste heat
Receipts system, the therrmodynamic system of stack gases residual neat recovering system carry out height coupling, enormously simplify boiler circuit so that a whole set of
Heat power generating system is more succinct, and project occupation of land area and construction totle drilling cost are greatly reduced.Because three kinds of residual heat resources are
Produced simultaneously with coke oven production technology, therefore the present invention has good exploitativeness and actual application value.
In summary, coke sensible heat, crude-gas sensible heat and the stack gases of the invention to being produced in coke oven production technology
Sensible heat carries out the heat power generating system of comprehensive reutilization, and the various residual heat resources in coke-oven plant are planned as a whole, and simplifies in system
A variety of waste heats are carried out integrated recycling by complexity in the most optimal way.
Described in an illustrative manner above with reference to accompanying drawing and be based on coke-oven plant's heat recovery according to of the present invention
Heat power generating system.It will be understood by those skilled in the art, however, that for the invention described above proposed based on more than coke-oven plant
The heat power generating system that recuperation of heat is utilized, can also make various improvement on the basis of present invention is not departed from.Therefore, originally
The protection domain of invention should be determined by the content of appended claims.
Claims (8)
1. a kind of heat power generating system based on coke-oven plant's heat recovery, it is characterised in that including coke oven, coke dry quenching furnace, do
Quenching waste heat boiler, raw coke oven gas waste-heat recovery device, stack gases waste-heat recovery device, high pressure drum, low pressure drum, pressure are followed
Ring pump, steam turbine and generator, wherein,
The coke export of the coke oven is connected with the coke inlet of the coke dry quenching furnace, and the high-temperature coke produced in the coke oven is sent
Cooled down into the coke dry quenching furnace；
The exhanst gas outlet of the coke oven is connected with the stack gases waste-heat recovery device, and the flue produced in the coke oven gives up
Gas, is discharged in the stack gases waste-heat recovery device；
The raw coke oven gas waste-heat recovery device is connected by tedge with the coke oven, and the raw coke oven gas produced in the coke oven is arranged
Cooled down into the raw coke oven gas waste-heat recovery device；
The low pressure drum is connected by down-comer with the import of forced circulation pump, the outlet of the forced circulation pump respectively with institute
The water inlet that raw coke oven gas waste-heat recovery device is stated with the stack gases waste-heat recovery device is connected, more than respectively described raw coke oven gas
Heat reclamation device and the stack gases waste-heat recovery device supply water；
The stack gases waste-heat recovery device, the raw coke oven gas waste-heat recovery device are done by the low pressure drum with described
Quenching waste heat boiler is connected, and the steam water interface that raw coke oven gas waste-heat recovery device and the raw coke oven gas waste-heat recovery device are produced exists
Feeding dry coke quenching residual heat boiler after steam-water separation is carried out in the drum to be overheated；
The gas approach of the dry coke quenching residual heat boiler is connected with the recyclegas outlet in the coke dry quenching furnace, more than the dry coke quenching
The exhanst gas outlet of heat boiler is connected with the recyclegas import in the coke dry quenching furnace, forms circulation loop, the dry coke quenching waste heat
Boiler is reclaimed to the sensible heat of the recyclegas；
Superheater, evaporator and economizer, the air intake of the steam turbine and institute are provided with the dry coke quenching residual heat boiler
The venthole for stating superheater is connected, and the steam turbine is connected with the generator, wherein,
During the system operation production, the high-temperature coke of the coke oven output, which is pushed into the coke dry quenching furnace, to be done
It is recyclegas to put out the cooling medium in cooling, the coke dry quenching furnace, and the recyclegas is absorbed after heat, from the coke dry quenching furnace
Recyclegas outlet is discharged, and enters the gas approach of the dry coke quenching residual heat boiler by pipeline, by the superheater, steaming
Cool, discharged from the exhanst gas outlet of the dry coke quenching residual heat boiler, then sent by pipeline after hair device and economizer heat exchange
The recyclegas import of the coke dry quenching furnace is back to, so circulation；
The low pressure drum is respectively the raw coke oven gas waste-heat recovery device and the stack gases waste heat by forced circulation pump
Retracting device provides water inlet, and, the carbonated drink of the raw coke oven gas waste-heat recovery device and the stack gases waste-heat recovery device is mixed
Compound is exported, and all the rising mouth of pipe with the low pressure drum is connected, and is constituted two-way and is forced steam/water circulating；
The saturated vapor that the high pressure drum and the low pressure drum are isolated respectively enters the superheater overheat, and passes through
Steam after heat, enters from the air intake of the steam turbine, drives the steam turbine to do work and drives the electrical power generators.
2. the heat power generating system as claimed in claim 1 based on coke-oven plant's heat recovery, it is characterised in that described dry
In quenching waste heat boiler, the superheater includes high-pressure superheater and low-pressure superheater, and the evaporator includes high-pressure evaporation
Device and low pressure evaporator, the economizer include high-pressure economizer and low-pressure coal saver.
3. the heat power generating system as claimed in claim 2 based on coke-oven plant's heat recovery, it is characterised in that described dry
In quenching waste heat boiler, high-pressure superheater, high pressure evaporator, high-pressure economizer, low-pressure superheater, low pressure evaporator, low pressure are saved
Coal device is set gradually according to flue gas flow direction.
4. the heat power generating system as claimed in claim 3 based on coke-oven plant's heat recovery, it is characterised in that the high pressure
The air intake of superheater is connected with the venthole of the high pressure drum, the venthole of the high-pressure superheater and the steam turbine
Main air intake connection；The water inlet and venthole of the high pressure evaporator pass through down-comer and tedge and the pressure cooker respectively
Cylinder connection, forms high pressure carbonated drink natural convection loop；The delivery port of the water inlet of the high-pressure economizer and the low pressure drum
Feed pump is provided with connection, connecting pipeline, the delivery port of the high-pressure economizer is connected with the water inlet of the high pressure drum.
5. the heat power generating system as claimed in claim 3 based on coke-oven plant's heat recovery, it is characterised in that described low
The air intake of pressure superheater is connected with the low pressure drum, the filling mouth of the venthole of the low-pressure superheater and the steam turbine
Connection；The water inlet and venthole of the low pressure evaporator are connected by down-comer and tedge with the low pressure drum respectively,
Form low pressure vapor natural convection loop.
6. the heat power generating system as claimed in claim 5 based on coke-oven plant's heat recovery, it is characterised in that the vapour
Condenser is provided with the steam drain of turbine, the air intake of the condenser is connected with the steam drain of the steam turbine, it is described solidifying
Water inlet of the delivery port of vapour device successively with condensate pump, the low-pressure coal saver is connected.
7. the heat power generating system as claimed in claim 5 based on coke-oven plant's heat recovery, it is characterised in that described low
Oxygen-eliminating device is provided with pressure drum, the water inlet of the oxygen-eliminating device is connected with the delivery port of the low-pressure coal saver.
8. the heat power generating system as claimed in claim 1 based on coke-oven plant's heat recovery, it is characterised in that the system
System also include the first deduster and the second deduster, first deduster be arranged on the coke dry quenching furnace recyclegas outlet with
On the pipeline of the gas approach connection of the dry coke quenching residual heat boiler, second deduster is arranged on the dry coke quenching waste heat pot
On the pipeline of the exhanst gas outlet of stove and the recyclegas inlet communication of the coke dry quenching furnace, second deduster and the coke dry quenching furnace
Recyclegas import between be additionally provided with circulating fan.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108917411A (en) * | 2018-04-17 | 2018-11-30 | 安徽华铂再生资源科技有限公司 | A kind of method of lead skim recycling and UTILIZATION OF VESIDUAL HEAT IN in lead smelting process |
| CN109707472A (en) * | 2019-02-28 | 2019-05-03 | 东北大学 | A kind of distributed energy resource system using dry coke quenching waste heat |
| CN110206606A (en) * | 2018-12-18 | 2019-09-06 | 西安华江环保科技股份有限公司 | A kind of dry coke quenching with filling heat generating system again |
| CN110240949A (en) * | 2019-07-02 | 2019-09-17 | 武汉方特工业设备技术有限公司 | A kind of raw coke oven gas waste heat recycling system and method |
| CN111139090A (en) * | 2019-12-27 | 2020-05-12 | 中冶焦耐(大连)工程技术有限公司 | Ultralow-load operation method of dry quenching system |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101216166A (en) * | 2007-12-28 | 2008-07-09 | 杭州锅炉集团股份有限公司 | Double pressure dry-extinguishing coke waste heat boiler |
| CN101655019A (en) * | 2009-04-13 | 2010-02-24 | 浙江西子联合工程有限公司 | Dry quenching dual pressure high-temperature and high-pressure residual heat power generation system |
| CN103242865A (en) * | 2013-05-10 | 2013-08-14 | 中国船舶重工集团公司第七�三研究所 | Device and method for generating electricity by utilizing waste heat of raw coke oven gas |
| CN103952162A (en) * | 2014-04-16 | 2014-07-30 | 上海交通大学 | Coke oven sensile heat recovery process |
| CN206875997U (en) * | 2017-05-18 | 2018-01-12 | 中冶华天南京工程技术有限公司 | Heat power generating system based on coke-oven plant's heat recovery |
-
2017
- 2017-05-18 CN CN201710352837.6A patent/CN106989610A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101216166A (en) * | 2007-12-28 | 2008-07-09 | 杭州锅炉集团股份有限公司 | Double pressure dry-extinguishing coke waste heat boiler |
| CN101655019A (en) * | 2009-04-13 | 2010-02-24 | 浙江西子联合工程有限公司 | Dry quenching dual pressure high-temperature and high-pressure residual heat power generation system |
| CN103242865A (en) * | 2013-05-10 | 2013-08-14 | 中国船舶重工集团公司第七�三研究所 | Device and method for generating electricity by utilizing waste heat of raw coke oven gas |
| CN103952162A (en) * | 2014-04-16 | 2014-07-30 | 上海交通大学 | Coke oven sensile heat recovery process |
| CN206875997U (en) * | 2017-05-18 | 2018-01-12 | 中冶华天南京工程技术有限公司 | Heat power generating system based on coke-oven plant's heat recovery |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108917411A (en) * | 2018-04-17 | 2018-11-30 | 安徽华铂再生资源科技有限公司 | A kind of method of lead skim recycling and UTILIZATION OF VESIDUAL HEAT IN in lead smelting process |
| CN110206606A (en) * | 2018-12-18 | 2019-09-06 | 西安华江环保科技股份有限公司 | A kind of dry coke quenching with filling heat generating system again |
| CN109707472A (en) * | 2019-02-28 | 2019-05-03 | 东北大学 | A kind of distributed energy resource system using dry coke quenching waste heat |
| CN109707472B (en) * | 2019-02-28 | 2021-10-22 | 东北大学 | Distributed energy system utilizing dry quenching waste heat |
| CN110240949A (en) * | 2019-07-02 | 2019-09-17 | 武汉方特工业设备技术有限公司 | A kind of raw coke oven gas waste heat recycling system and method |
| CN111139090A (en) * | 2019-12-27 | 2020-05-12 | 中冶焦耐(大连)工程技术有限公司 | Ultralow-load operation method of dry quenching system |
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Application publication date: 20170728 |