CN215311359U - Flue gas waste heat comprehensive utilization system of coke oven flue gas semi-dry process technology - Google Patents
Flue gas waste heat comprehensive utilization system of coke oven flue gas semi-dry process technology Download PDFInfo
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- CN215311359U CN215311359U CN202022318810.5U CN202022318810U CN215311359U CN 215311359 U CN215311359 U CN 215311359U CN 202022318810 U CN202022318810 U CN 202022318810U CN 215311359 U CN215311359 U CN 215311359U
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Abstract
The utility model discloses a flue gas waste heat comprehensive utilization system of a coke oven flue gas semi-dry process, which comprises an ammonia wastewater heat exchange unit, wherein the ammonia wastewater heat exchange unit is used for evaporating ammonia from ammonia wastewater by using the waste heat of coking flue gas after desulfurization and denitrification; the ammonia wastewater heat exchange unit comprises an ammonia water heat exchange assembly, and the ammonia water heat exchange assembly is used for carrying out heat exchange on the coking flue gas and the ammonia wastewater. The comprehensive flue gas waste heat utilization system further comprises an MGGH heat exchange unit, the MGGH heat exchange unit comprises a flue gas cooler and a flue gas heater, the flue gas cooler is used for reducing the entering temperature of the coking flue gas in the desulfurization and dedusting process, and the flue gas heater is used for increasing the entering temperature of the coking flue gas in the denitration process. The utility model fully combines the self ammonia distillation working section of the coking plant, so that the chemical product workshop and the desulfurization and denitrification unit are organically combined and mutually beneficial, and the coking plant achieves the purposes of cost reduction and efficiency improvement.
Description
Technical Field
The utility model belongs to the technical field of flue gas treatment, and particularly relates to a flue gas waste heat comprehensive utilization system for a coke oven flue gas semi-dry process.
Background
At present, in most coking industries, in order to meet the latest emission index requirements and estimate project cost, various semi-dry process technologies are adopted to treat coke oven flue gas, and finally the emission indexes meet the environmental protection requirements. Basically, the main process routes of several semi-dry processes are relatively fixed and follow the flow of firstly desulfurizing, then dedusting and then denitrating. Some engineering projects may not be able to be further refined and configured too much due to the limitations of the re-construction site. However, the above semi-dry process has a slight deficiency in the utilization of the residual heat in terms of the treatment of the coke oven flue gas itself. Therefore, aiming at the problem of fully and reasonably utilizing the heat of the system, the existing semi-dry process route is adjusted and optimized.
SUMMERY OF THE UTILITY MODEL
Aiming at the defects of the prior art, the utility model aims to provide a flue gas waste heat comprehensive utilization system for a coke oven flue gas semi-dry process technology.
The technical scheme adopted by the utility model for solving the technical problem is as follows:
the comprehensive flue gas waste heat utilization system for the coke oven flue gas semi-dry process comprises an ammonia wastewater heat exchange unit, wherein the ammonia wastewater heat exchange unit is used for evaporating ammonia from ammonia wastewater by using the waste heat of coking flue gas after desulfurization and denitrification.
In the above-mentioned flue gas waste heat comprehensive utilization system, as an preferred embodiment, the ammonia wastewater heat exchange unit includes aqueous ammonia heat exchange assembly, aqueous ammonia heat exchange assembly be used for with the coking flue gas with ammonia wastewater carries out the heat exchange.
In the above comprehensive utilization system of flue gas waste heat, as a preferred embodiment, the ammonia water heat exchange assembly comprises a first steam-water heat exchanger and a second steam-water heat exchanger which are connected with each other; the first steam-water heat exchanger is used for carrying out heat exchange on the coking flue gas and softened water so that the softened water forms softened water steam; the second steam-water heat exchanger is used for exchanging heat between the softened water steam and the ammonia wastewater so as to increase the temperature of the ammonia wastewater.
In the above comprehensive utilization system for flue gas waste heat, as a preferred embodiment, a circulation loop of a heat exchange medium is formed between the first steam-water heat exchanger and the second steam-water heat exchanger, the heat exchange medium enters the second steam-water heat exchanger after being heated by coking flue gas in the first steam-water heat exchanger, and returns to the first steam-water heat exchanger after being cooled in the second steam-water heat exchanger as a cold source medium.
Preferably, a downcomer and an riser are arranged between the first steam-water heat exchanger and the second steam-water heat exchanger, the downcomer is used for conveying the softened water entering the shell pass of the second steam-water heat exchanger from the shell pass of the second steam-water heat exchanger to the first steam-water heat exchanger, and the riser is used for conveying the softened water vapor from the first steam-water heat exchanger to the shell pass of the second steam-water heat exchanger.
In the above comprehensive utilization system of flue gas waste heat, as an optimal implementation manner, the first steam-water heat exchanger is a heat pipe type steam generator.
In the above comprehensive utilization system of flue gas waste heat, as a preferred embodiment, the second steam-water heat exchanger is a steam-collecting heat exchanger.
In the above system for comprehensive utilization of flue gas waste heat, as an optimal implementation manner, the flue gas inlet of the first steam-water heat exchanger is connected with the flue gas outlet of the denitration reactor in the desulfurization and denitration process.
In the above-mentioned flue gas waste heat comprehensive utilization system, as an preferred embodiment, the ammonia wastewater heat exchange unit further includes an ammonia still, the ammonia wastewater flows into the ammonia water heat exchange assembly from the ammonia still, and after heat exchange, the ammonia wastewater flows back to the ammonia still for flash evaporation.
In the above system for comprehensive utilization of flue gas waste heat, as a preferred embodiment, the ammonia still and the second steam-water heat exchanger tube pass further form a circulation path of ammonia wastewater; preferably, an ammonia wastewater outlet of the ammonia still is connected with a tube pass inlet of the second steam-water heat exchanger, and a tube pass outlet of the second steam-water heat exchanger is connected with an ammonia wastewater inlet of the ammonia still.
In the above system for comprehensive utilization of waste heat of flue gas, as a preferred embodiment, a flash evaporation tank is arranged in the ammonia still and used for the ammonia wastewater to perform the flash evaporation.
In the above comprehensive utilization system for flue gas waste heat, as a preferred embodiment, the comprehensive utilization system for flue gas waste heat further comprises an MGGH heat exchange unit, the MGGH heat exchange unit comprises a flue gas cooler and a flue gas heater, the flue gas cooler is used for reducing the entry temperature of coking flue gas in the desulfurization and dedusting process, and the flue gas heater is used for increasing the entry temperature of coking flue gas in the denitration process;
preferably, a circulation loop of a heat exchange medium is formed between the flue gas cooler and the flue gas heater; the heat exchange medium enters the flue gas heater after being heated by coking flue gas in the flue gas cooler, and then part of the heat exchange medium flows into the flue gas cooler after being cooled in the flue gas heater, and part of the heat exchange medium flows back into the flue gas heater; the heat exchange medium is preferably demineralized water.
In the above system for comprehensive utilization of flue gas waste heat, as a preferred embodiment, the flue gas outlet of the flue gas cooler is connected to the flue gas inlet of the desulfurization reactor.
In the above comprehensive utilization system of flue gas waste heat, as a preferred embodiment, the flue gas inlet of the flue gas heater is connected with the flue gas outlet of the dust remover, and the flue gas outlet of the flue gas heater is connected with the flue gas inlet of the denitration reactor.
In the above comprehensive utilization system of flue gas waste heat, as a preferred embodiment, the dust remover is a bag-type dust remover.
In the above comprehensive utilization system of flue gas waste heat, as a preferred embodiment, the comprehensive utilization system of flue gas waste heat further comprises a desulfurization and denitrification unit, and the desulfurization and denitrification unit comprises the desulfurization reactor, the dust remover and the denitrification reactor which are sequentially connected along the flow direction of flue gas.
Compared with the prior art, the utility model has the following beneficial effects:
(1) the ultralow modification coking project adopting the semi-dry process not only ensures that the desulfurization reaction is carried out at the optimal reaction temperature on the basis of embedding the MGGH unit, but also reduces the specification size of the desulfurization reactor and the bag-type dust collector by about 30 percent, and can meet the temperature requirement of the subsequent denitration reaction. The utility model optimizes the one-time investment cost and the later operation and maintenance cost of the project.
(2) The utility model fully combines the self ammonia distillation working section of the coking plant, so that the chemical product workshop and the desulfurization and denitrification unit are organically combined and mutually beneficial, and the coking plant achieves the purposes of cost reduction and efficiency improvement.
Drawings
FIG. 1 is a structural diagram of a flue gas waste heat comprehensive utilization system of a coke oven flue gas semi-dry process.
Wherein, 1 is the flue gas cooler, 2 is the flue gas heater, 3 is the desulfurization reactor, 4 is the sack cleaner, 5 is the denitration reactor, 6 is heat pipe formula steam generator, 7 is collection vapour formula heat exchanger, 8 is the soft water pump, 9 is the downcomer, 10 is the tedge, 11 is the ammonia still, 12 is the flash tank, 13 is the draught fan, 14 is owner's demineralized water unit, 15 is coking raw flue gas inlet port, 16 is the flowmeter, 17 is the moisturizing valve, 18 is the softened water tank, 19 is the level gauge, 20 is the overflow pipe way, 21 is the softened water return line, 22 is the softened water circulation main pipe way, 23 is the softened water circulating pump, 24 is the manometer, 25 is pressure transmitter, 26 is the waste ammonia water frequency conversion circulating pump, 28 is the moisturizing pipeline of collection vapour formula heat exchanger.
Detailed Description
In order to highlight the objects, technical solutions and advantages of the present invention, the present invention is further illustrated by the following examples, which are presented by way of illustration of the present invention and are not intended to limit the present invention. The technical solution of the present invention is not limited to the specific embodiments listed below, and includes any combination of the specific embodiments.
Referring to fig. 1, the utility model provides a flue gas waste heat comprehensive utilization system of a coke oven flue gas semi-dry process, which comprises an MGGH heat exchange unit, wherein the MGGH heat exchange unit comprises a flue gas cooler 1 and a flue gas heater 2, and the flue gas cooler 1 is positioned in front of a desulfurization reactor 3 in a coking semi-dry process and used for reducing the temperature of coking flue gas entering the desulfurization reactor 3; specifically, the flue gas outlet of the flue gas cooler 1 is connected to the flue gas inlet of the desulfurization reactor 3, the coke oven raw flue gas extracted from the coke oven side and the coke side flows into the flue gas cooler 1 from the coking raw flue gas inlet 15, and after cooling by the flue gas cooler 1, the temperature of the coke oven flue gas is reduced from about 250 ℃ to about 120 ℃ for example, so that the temperature of the cooled coke oven flue gas is kept above the acid dew point, thereby preventing the desulfurization reactor 3 from being corroded by acid, and the amount of flue gas entering the desulfurization reactor 3 can be reduced after the temperature of the coke oven flue gas is reduced, thereby optimizing the design of the desulfurization reactor (for example, reducing the size of the desulfurization reactor). After the temperature of the coke oven flue gas is reduced, when the desulfurization reaction is carried out in the desulfurization reactor 3, the evaporation of water in the hydrated lime desulfurization agent is slowed down, and the adsorption mass transfer efficiency of the neutralization reaction can be enhanced.
Preferably, the coke oven flue gas flows into the bag-type dust remover 4 for dust removal after the desulfurization reaction is carried out in the desulfurization reactor 3, and the temperature of the coke oven flue gas entering the desulfurization reactor 3 is reduced by the flue gas cooler 1, so that the temperature of the coke oven flue gas entering the bag-type dust remover 4 is reduced; in order to ensure that the semi-dry process requires that the design filtering air speed of the bag-type dust remover is lower than 0.7m/min, so that the cost of the bag-type dust remover accounts for about 30% of the cost of the whole bag-type dust remover, the working condition temperature of the bag is reduced, and the specification material and the quantity of the bag can be greatly reduced (for example, after the temperature of coke oven smoke is reduced, the quantity of the coke oven smoke entering the bag-type dust remover converted to the working condition is reduced, and when the filtering air speed of the bag-type dust remover is fixed, the area of the bag can be reduced, so that the required quantity of the bag can be reduced), and the one-time investment cost of a bag-type dust removing part and the corresponding maintenance cost in the later period are optimized.
After the temperature reduction, desulfurization and dust removal reach the standard, in order to fully utilize the heat of the original flue gas of the coke oven, the coke oven flue gas flows into a flue gas heater 2 of an MGGH heat exchange unit from a bag-type dust collector 4, the flue gas heater 2 heats the coke oven flue gas, then the coke oven flue gas enters a denitration reactor 5 for denitration reaction, and the arrangement of the flue gas heater 2 improves the temperature of the coke oven flue gas entering the denitration reactor, so that the load and the synchronization rate of a heat supplementing system can be reduced, and the effects of energy conservation and consumption reduction are achieved. The flue gas cooler 1 and the flue gas heater 2 form a set of closed MGGH circulating heat exchange system, a circulating loop of a heat exchange medium is formed between the flue gas cooler 1 and the flue gas heater 2, and the heat exchange medium is preferably softened water; the heat exchange medium enters the flue gas heater 2 as a heat source medium of the flue gas heater 2 after being heated by coking flue gas in the flue gas cooler 1, then part of the heat exchange medium flows into the flue gas cooler 1 through a softened water circulation main pipeline 22 after being cooled by the flue gas heater 2, and part of the heat exchange medium flows back into the flue gas heater 2 through a softened water return pipeline 21; under the condition of need, the softened water of the heat exchange medium cooled by the flue gas heater 2 can also completely flow back to the flue gas cooler 1 for cooling the original coking flue gas; the softened water return pipeline 21 is a pipeline indicated by an upward arrow in the attached drawing 1), the softened water circulation main pipeline 22 is a pipeline indicated by a downward arrow in the attached drawing 1, the softened water return pipeline 21 controls the actual amount of softened water entering the flue gas heater 2 through a valve, so as to control the heat exchange amount of the circulation system and the temperature of flue gas at the outlet of the flue gas cooler, and thus the temperature requirement of the desulfurization reaction is met; the main softened water circulation pipeline 22 is used for transferring heat of the flue gas cooler and the reheater through water medium;
preferably, the softened water from the flue gas heater 2 is fed into the softened water return line 21 and the main softened water circulation line 22 by the softened water circulation pump 23, respectively, wherein the softened water circulation pump 23 comprises a stand-by softened water circulation pump for powering the heat transfer medium of the flue gas cooler and the heater.
Preferably, the comprehensive utilization system for the flue gas waste heat further comprises a desulfurization and denitrification unit, wherein the desulfurization and denitrification unit comprises a desulfurization reactor 3 (wherein the desulfurization is preferably carried out by adopting a sodium bicarbonate process, and the desulfurizing agent is NaHCO)3) A bag-type dust collector 4 and a denitration reactor 5 (wherein, the denitration is preferably carried out by adopting a medium-low temperature SCR process, and the denitration agent is ammonia water with the concentration of 20%).
As a preferred implementation mode, the comprehensive utilization system for the waste heat of the flue gas further comprises an ammonia wastewater heat exchange unit, the coking flue gas flowing out of the desulfurization and denitrification process enters the ammonia wastewater heat exchange unit, the waste heat of the coking flue gas is used in the ammonia distillation process of the ammonia distillation wastewater, the ammonia wastewater can be ammonia distillation wastewater of an ammonia distillation section of a coke-oven plant, the arrangement can enable the chemical product workshop and the desulfurization and denitrification to be organically combined and mutually beneficial, and the coke-oven plant achieves the purposes of cost reduction and efficiency improvement.
Preferably, the ammonia wastewater heat exchange unit comprises an ammonia water heat exchange assembly, the ammonia water heat exchange assembly comprises a first steam-water heat exchanger and a second steam-water heat exchanger which are connected, the first steam-water heat exchanger is preferably a heat pipe type steam generator 6, and the second steam-water heat exchanger is preferably a steam collecting type heat exchanger 7; the heat pipe type steam generator 6 is used for carrying out heat exchange on the coking flue gas and softened water so that the softened water is gasified to form softened water vapor; the steam-collecting heat exchanger 7 is used for exchanging heat between the softened water vapor and the ammonia wastewater, so that the temperature of the ammonia wastewater is increased. Preferably, a down pipe 9 and an up pipe 10 are arranged between the heat pipe type steam generator 6 and the steam collecting type heat exchanger 7, the down pipe 9 is used for conveying softened water on the shell side of the steam collecting type heat exchanger 7 from the shell side of the steam collecting type heat exchanger 7 to the steam generator 6, the up pipe 10 is used for conveying softened water vapor formed in the heat pipe type steam generator 6 from the heat pipe type steam generator 6 to the shell side of the steam collecting type heat exchanger 7, wherein cooling water (softened water) is introduced into the steam collecting type heat exchanger 7 at the beginning, phase change circulation is always carried out after the cooling water (softened water), and frequent water supplement is not carried out; however, if the liquid level of the downcomer 9 drops due to leakage, overflow and drip, the water can be supplemented in a linkage manner.
Preferably, the ammonia wastewater heat exchange unit further comprises an ammonia still 11, and the ammonia still 11 and a second steam-water heat exchanger, namely a steam-collecting heat exchanger 7, form a circulation passage of ammonia wastewater; preferably, the ammonia wastewater outlet of the ammonia still 11 is connected with the tube pass inlet of the steam-collecting heat exchanger 7, and the tube pass outlet of the steam-collecting heat exchanger 7 is connected with the ammonia wastewater inlet of the ammonia still 11. Preferably, a flash evaporation tank 12 is arranged in the ammonia still 11 for flash evaporation of the ammonia wastewater entering the ammonia still 11.
Preferably, a pressure transmitter 25 for judging the resistance condition of the heat exchangers, a waste ammonia water variable-frequency circulating pump 27 for adjusting the flow rate of waste ammonia water and a pressure gauge 24 are arranged on a pipeline between the steam-collecting heat exchangers 7 and 11.
Specifically, softened water (preferably, industrial softened water, which may cause scaling of pipes in the system, etc.) first enters the softened water tank 18 from the main softened water unit 14 (wherein a flow meter 16 for medium consumption statistics and a water supply valve 17 for low-level interlock water supply of the softened water tank 18 are provided on a pipe between the main softened water unit 14 and the softened water tank 18, and a level gauge 19 and an overflow pipe 20 for softened water tank level display and interlock alarm are provided on the softened water tank 18), then enters the steam-collecting heat exchanger 7 (steam-collecting tube heat exchanger) shell side through the water supply pipe 28 of the steam-collecting heat exchanger and the soft water pump 8, then enters the heat pipe steam generator 6 from the shell side of the steam-collecting tube heat exchanger 7 through the downcomer 9, and in the heat pipe steam generator 6, the softened water exchanges heat with coking flue gas (about 200 degrees celsius) entering the heat pipe steam generator 6 from the heat pipe denitration reactor 5, softened water absorbs heat and becomes saturated water, the saturated water continuously absorbs heat and is converted into saturated vapor, and then the saturated vapor enters the shell side of the steam-collecting heat exchanger 7 through the ascending pipe 10; the (steam) ammonia wastewater flows into a tube pass of a steam-collecting heat exchanger 7 from a wastewater outlet of an ammonia still 11, the ammonia wastewater and saturated steam exchange heat in the steam-collecting heat exchanger 7 (the ammonia wastewater exchanges heat with shell pass steam in the tube pass of the steam-collecting heat exchanger), the ammonia wastewater rises to 15-20 ℃, and is sent to an ammonia still 11 of a chemical production section through an ammonia wastewater circulating pump for flash evaporation, the cooled saturated water enters a heat pipe steam generator 6 again through a descending pipe 9 to generate steam with the temperature of, for example, 0.3MPa and 140 ℃, and the steam-water closed circulation is carried out between the heat pipe steam generator 6 and the steam-collecting heat exchanger 7 in sequence in a reciprocating manner, so that the ammonia wastewater in the ammonia still 11 is flashed, and finally the coking flue gas is discharged through a draught fan 13.
The foregoing embodiments illustrate the principles, principal features and advantages of the utility model, and it will be understood by those skilled in the art that the utility model is not limited to the foregoing embodiments, which are merely illustrative of the principles of the utility model, and that various changes and modifications may be made therein without departing from the scope of the principles of the utility model.
Claims (10)
1. The comprehensive flue gas waste heat utilization system for the coke oven flue gas semi-dry process is characterized by comprising an ammonia wastewater heat exchange unit, wherein the ammonia wastewater heat exchange unit is used for evaporating ammonia from ammonia wastewater by using the waste heat of coking flue gas after desulfurization and denitrification.
2. The comprehensive utilization system of the flue gas waste heat according to claim 1, wherein the ammonia wastewater heat exchange unit comprises an ammonia water heat exchange assembly, and the ammonia water heat exchange assembly is used for carrying out heat exchange on the coking flue gas and the ammonia wastewater.
3. The comprehensive utilization system of the flue gas waste heat according to claim 2, wherein the ammonia water heat exchange assembly comprises a first steam-water heat exchanger and a second steam-water heat exchanger which are connected with each other; the first steam-water heat exchanger is used for carrying out heat exchange on the coking flue gas and softened water so that the softened water forms softened water steam; the second steam-water heat exchanger is used for exchanging heat between the softened water steam and the ammonia wastewater so as to increase the temperature of the ammonia wastewater.
4. The system for comprehensively utilizing the waste heat of the flue gas as claimed in claim 3, wherein a circulation loop of a heat exchange medium is formed between the first steam-water heat exchanger and the second steam-water heat exchanger, the heat exchange medium enters the second steam-water heat exchanger after being heated by the coking flue gas in the first steam-water heat exchanger, and the heat exchange medium returns to the first steam-water heat exchanger after being cooled in the second steam-water heat exchanger to serve as a cold source medium.
5. The comprehensive utilization system of the flue gas waste heat according to claim 3, wherein a downcomer and an upcomer are arranged between the first steam-water heat exchanger and the second steam-water heat exchanger, the downcomer is used for conveying the softened water entering the shell side of the second steam-water heat exchanger from the shell side of the second steam-water heat exchanger to the first steam-water heat exchanger, and the upcomer is used for conveying the softened water vapor from the first steam-water heat exchanger to the shell side of the second steam-water heat exchanger.
6. The comprehensive utilization system of the flue gas waste heat according to claim 3, wherein the first steam-water heat exchanger is a heat pipe type steam generator; the second steam-water heat exchanger is a steam-collecting heat exchanger; and the flue gas inlet of the first steam-water heat exchanger is connected with the flue gas outlet of the denitration reactor in the desulfurization and denitration process.
7. The system for comprehensively utilizing the waste heat of the flue gas as claimed in claim 3, wherein the ammonia wastewater heat exchange unit further comprises an ammonia still, the ammonia wastewater flows into the ammonia water heat exchange assembly from the ammonia still, and after heat exchange, the ammonia wastewater flows back to the ammonia still for flash evaporation; the ammonia still and the second steam-water heat exchanger tube pass form a circulation passage of ammonia wastewater; and an ammonia wastewater outlet of the ammonia still is connected with a tube pass inlet of the second steam-water heat exchanger, and a tube pass outlet of the second steam-water heat exchanger is connected with an ammonia wastewater inlet of the ammonia still.
8. The comprehensive utilization system of flue gas waste heat according to any one of claims 1 to 7, further comprising an MGGH heat exchange unit, wherein the MGGH heat exchange unit comprises a flue gas cooler and a flue gas heater; and a circulation loop of a heat exchange medium is formed between the flue gas cooler and the flue gas heater.
9. The system for comprehensively utilizing the waste heat of the flue gas as claimed in claim 8, wherein the flue gas outlet of the flue gas cooler is connected with the flue gas inlet of the desulfurization reactor; and the flue gas inlet of the flue gas heater is connected with the flue gas outlet of the dust remover, and the flue gas outlet of the flue gas heater is connected with the flue gas inlet of the denitration reactor.
10. The system for comprehensively utilizing the waste heat of the flue gas as claimed in claim 9, further comprising a desulfurization and denitrification unit, wherein the desulfurization and denitrification unit comprises the desulfurization reactor, the dust remover and the denitrification reactor which are sequentially connected along the flow direction of the flue gas.
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