CN108131656B - Ultra-clean emission cold and hot co-production system of coking plant - Google Patents
Ultra-clean emission cold and hot co-production system of coking plant Download PDFInfo
- Publication number
- CN108131656B CN108131656B CN201710558062.8A CN201710558062A CN108131656B CN 108131656 B CN108131656 B CN 108131656B CN 201710558062 A CN201710558062 A CN 201710558062A CN 108131656 B CN108131656 B CN 108131656B
- Authority
- CN
- China
- Prior art keywords
- outlet
- flue gas
- inlet
- heat
- communicated
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000004939 coking Methods 0.000 title claims abstract description 27
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 16
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 170
- 239000003546 flue gas Substances 0.000 claims abstract description 170
- 238000010521 absorption reaction Methods 0.000 claims abstract description 131
- 239000002918 waste heat Substances 0.000 claims abstract description 39
- 239000000571 coke Substances 0.000 claims description 37
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 36
- 238000010438 heat treatment Methods 0.000 claims description 26
- 239000006096 absorbing agent Substances 0.000 claims description 13
- 239000007921 spray Substances 0.000 claims description 3
- 230000008676 import Effects 0.000 claims 6
- 238000001704 evaporation Methods 0.000 claims 1
- 238000007872 degassing Methods 0.000 abstract description 2
- 238000006477 desulfuration reaction Methods 0.000 abstract 1
- 230000023556 desulfurization Effects 0.000 abstract 1
- 239000000428 dust Substances 0.000 abstract 1
- 239000000779 smoke Substances 0.000 description 17
- 230000007613 environmental effect Effects 0.000 description 8
- 238000011084 recovery Methods 0.000 description 6
- 239000007789 gas Substances 0.000 description 5
- 238000010248 power generation Methods 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 238000005057 refrigeration Methods 0.000 description 4
- 238000004891 communication Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000004134 energy conservation Methods 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000008236 heating water Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Classifications
-
- 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
- F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
- F22B1/1892—Systems therefor not provided for in F22B1/1807 - F22B1/1861
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Combustion & Propulsion (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Sorption Type Refrigeration Machines (AREA)
Abstract
The invention provides an ultra-clean emission cold and hot co-production system of a coking plant, which comprises a denitration device, a waste heat boiler, an absorption tower and a regenerator, wherein the denitration device is used for carrying out denitration treatment on flue gas, the waste heat boiler is used for recovering waste heat of the flue gas, the flue gas of the waste heat boiler provides a heat source for an absorption refrigerating unit through a heat exchanger, and the absorption tower and the regenerator are used for carrying out deep desulfurization, dust removal and degassing sol treatment on the flue gas. According to the ultra-clean emission cold and hot co-production system of the coking plant, devices such as a denitration device, a waste heat boiler, an absorption tower and a regenerator are configured, waste heat of coking furnace flue gas is deeply recycled and efficiently utilized, and flue gas is treated in a grading manner, so that ultra-clean emission of the flue gas is realized, and annual energy-saving and environment-friendly benefits are ensured.
Description
Technical Field
The invention relates to an ultra-clean emission cold and hot co-production system of a coking plant.
Background
The energy is an important material foundation for social development, and the energy problems faced by China are mainly embodied in the aspects of low energy utilization efficiency, poor economic benefit, rapid increase of energy consumption, obvious ecological environment pressure and the like.
The coke oven is a high-efficiency thermal equipment in the energy conversion device, and the net efficiency is as high as 87% -89%. The coking process is not only a perfect energy conversion process, and can generate high-quality secondary energy, but also the coke oven body equipment is improved continuously for more than one hundred years, and is perfect in the aspects of gas combustion, flue gas heat utilization, heat insulation and the like. But this does not suggest that it has no room for energy conservation.
The efficient recycling of waste heat resources generated in the coking process is a main direction and potential of energy conservation of a green coking plant with resource conservation and environmental friendliness, and is one of main ways for improving efficiency. At present, the existing energy-saving measures mainly comprise: 1. the output heat of the coke oven is fully recycled; 2. deep popularization of a dry quenching technology, and full recycling of the waste heat of red coke; 3. researching and developing recycling of waste heat of raw gas; 4. and (5) recycling waste heat of flue gas of the coke oven.
In the above measures, the waste heat recovery of the coke oven is studied from a certain aspect, and the optimal configuration of the energy sources of the coke oven plant is not studied deeply, so that the maximization and the comprehensiveness of energy conservation cannot be realized. In addition, the existing energy-saving measures are deficient in the research on environmental protection, and the existing environmental protection products often increase energy consumption and do not have the energy-saving characteristic.
Disclosure of Invention
The invention aims to overcome the defects of low energy saving efficiency and no environmental protection effect of waste heat recovery measures of a coke oven in the prior art, and provides an ultra-clean emission cold and heat cogeneration system of a coke oven plant.
The invention solves the technical problems by the following technical proposal:
the invention provides an ultra-clean emission cold and hot co-production system of a coking plant, which comprises:
the denitration device is provided with a denitration flue gas inlet and a denitration flue gas outlet, and flue gas enters the denitration device from the denitration flue gas inlet and is discharged from the denitration flue gas outlet;
the waste heat boiler is provided with a boiler smoke inlet, a boiler smoke outlet, a boiler cold source inlet and a boiler cold source outlet, wherein the boiler smoke inlet and the boiler smoke outlet are communicated through a boiler smoke pipeline, the boiler cold source inlet and the boiler cold source outlet are communicated through a boiler cold source pipeline, smoke in the boiler smoke pipeline exchanges heat with working media in the boiler cold source pipeline, and the boiler smoke inlet is communicated with a denitration smoke outlet;
the absorption tower is provided with an absorption tower smoke inlet, an absorption tower smoke outlet, an absorption tower solution inlet and an absorption tower solution outlet, wherein the absorption tower smoke inlet is communicated with the boiler smoke outlet, the absorption tower smoke inlet is positioned at the lower part of the absorption tower and discharges the smoke into the absorption tower, the absorption tower smoke outlet is positioned at the upper part of the absorption tower and discharges the smoke to the outside, the absorption tower solution inlet is positioned at the upper part of the absorption tower and sprays the moisture absorption solution into the absorption tower, and the absorption tower solution outlet is positioned at the lower part of the absorption tower and discharges the moisture absorption solution;
the regenerator is provided with a regenerator solution inlet, a regenerator solution outlet and a secondary steam outlet, wherein the regenerator solution inlet is communicated with the absorption tower solution outlet, the regenerator solution outlet is communicated with the absorption tower solution inlet, and the secondary steam outlet discharges the secondary steam heated and evaporated by the moisture absorption solution.
Preferably, the ultra-clean emission combined heat and power generation system of the coking plant further comprises at least one heat exchanger, and the boiler flue gas outlet and/or the secondary steam outlet are/is communicated with at least one heat exchanger and exchange heat.
Preferably, the absorption tower is further provided with an absorption tower cold source inlet and an absorption tower cold source outlet, the absorption tower cold source inlet and the absorption tower cold source outlet are communicated through an absorption tower cold source pipeline, and the working medium in the absorption tower cold source pipeline exchanges heat with the working medium in the absorption tower.
Preferably, the cold source outlet of the absorption tower is communicated with at least one heat exchanger and exchanges heat.
Preferably, the regenerator is further provided with a regenerator heat source inlet and a regenerator heat source outlet, the regenerator heat source inlet is communicated with the regenerator heat source outlet through a regenerator heat source pipeline, the working medium in the regenerator heat source pipeline exchanges heat with the working medium in the regenerator, and the regenerator heat source inlet is communicated with the boiler heat source outlet.
Preferably, the regenerator heat source outlet is in communication with and in heat exchange with at least one heat exchanger.
Preferably, the ultra-clean emission combined heat and power generation system of the coking plant further comprises an absorption refrigerating unit, wherein the absorption refrigerating unit is communicated with at least one heat exchanger and exchanges heat.
Preferably, the ultra-clean emission combined heat and power generation system of the coking plant further comprises:
the first heat exchanger is positioned between the boiler flue gas outlet and the absorber tower flue gas inlet, the first heat exchanger is provided with a first flue gas inlet, a first flue gas outlet, a first cold source inlet and a first cold source outlet, the first flue gas inlet and the first flue gas outlet are communicated through a first flue gas pipeline, the first cold source inlet and the first cold source outlet are communicated through a first cold source pipeline, flue gas in the first flue gas pipeline is subjected to heat exchange with working media in the first cold source pipeline, the boiler flue gas outlet is communicated with the first flue gas inlet, and the first flue gas outlet is communicated with the absorber tower flue gas inlet;
the second heat exchanger is provided with a second cold source inlet, a second cold source outlet, a second heat source inlet and a second heat source outlet, the second cold source inlet and the second heat source outlet are communicated through a second cold source pipeline, the second heat source inlet and the second heat source outlet are communicated through a second heat source pipeline, a working medium in the second heat source pipeline exchanges heat with a working medium in the second heat source pipeline, the second heat source inlet is communicated with the secondary steam outlet, the second heat source outlet is communicated with an external pipeline, and the second cold source inlet, the second cold source outlet and the first cold source outlet are mutually communicated;
the third heat exchanger is provided with a third cold source inlet, a third cold source outlet, a third heat source inlet and a third heat source outlet, the third cold source inlet and the third heat source outlet are communicated through a third cold source pipeline, the third heat source inlet and the third heat source outlet are communicated through a third heat source pipeline, a working medium in the third heat source pipeline exchanges heat with a working medium in the third heat source pipeline, the third heat source inlet is communicated with the secondary steam outlet, the third heat source outlet is communicated with the second heat source outlet, and the third cold source inlet and the third heat source outlet are both communicated with the external pipeline.
Preferably, the absorption tower is further provided with an absorption tower cold source inlet and an absorption tower cold source outlet, the absorption tower cold source inlet and the absorption tower cold source outlet are communicated through an absorption tower cold source pipeline, and the working medium of the absorption tower cold source pipeline exchanges heat with the working medium in the absorption tower;
the regenerator is also provided with a regenerator heat source inlet and a regenerator heat source outlet, the regenerator heat source inlet is communicated with the regenerator heat source outlet through a regenerator heat source pipeline, working media in the regenerator heat source pipeline are subjected to heat exchange with working media in the regenerator, and the regenerator heat source inlet is communicated with the boiler cold source outlet;
the ultra-clean emission cold and heat co-production system of the coking plant further comprises a fourth heat exchanger, wherein the fourth heat exchanger is provided with a fourth cold source inlet, a fourth cold source outlet, a fourth heat source inlet and a fourth heat source outlet, the fourth cold source inlet and the fourth heat source outlet are communicated through a fourth cold source pipeline, the fourth heat source inlet and the fourth heat source outlet are communicated through a fourth heat source pipeline, a working medium in the fourth heat source pipeline is in heat exchange with a working medium in the fourth heat source pipeline, the fourth heat source inlet is communicated with a heat source outlet of the regenerator, the fourth heat source outlet is communicated with an external pipeline, the fourth cold source inlet is communicated with a cold source outlet of the absorption tower, and the fourth heat source outlet is communicated with a third cold source inlet.
Preferably, the ultra-clean emission cold and hot co-production system of the coking plant further comprises an absorption refrigerating unit, the absorption refrigerating unit is provided with a refrigerating unit heat source inlet, a refrigerating unit heat source outlet, a refrigerating unit chilled water inlet and a refrigerating unit chilled water outlet, the refrigerating unit heat source inlet and the refrigerating unit heat source outlet are communicated through a refrigerating unit heat source pipeline, the refrigerating unit chilled water inlet and the refrigerating unit chilled water outlet are communicated through a chilled water pipeline, chilled water in the chilled water pipeline is in heat exchange with working media in the refrigerating unit heat source pipeline, the refrigerating unit chilled water inlet and the refrigerating unit chilled water outlet are connected with an external pipeline, the refrigerating unit heat source inlet is communicated with a first cold source outlet, and the refrigerating unit heat source outlet is communicated with the first cold source inlet.
Preferably, the ultra-clean emission cold and hot co-production system of the coking plant further comprises a denitration device, wherein the denitration device is provided with a denitration flue gas inlet and a denitration flue gas outlet, the denitration flue gas outlet is communicated with the boiler flue gas inlet, and flue gas enters the denitration device from the denitration flue gas inlet and is discharged from the denitration flue gas outlet.
Preferably, the ultra-clean emission cold and hot co-production system of the coking plant further comprises a heater, wherein the heater comprises a coke oven flue gas inlet, a coke oven flue gas outlet, a heating source inlet and a heating source outlet, the coke oven flue gas inlet and the coke oven flue gas outlet are communicated through a coke oven flue gas pipeline, the heating source inlet and the heating source outlet are communicated through a heating source pipeline, flue gas in the coke oven flue gas pipeline is subjected to heat exchange with working media in the heating source pipeline, and the coke oven flue gas outlet is communicated with the denitration flue gas inlet.
On the basis of conforming to the common knowledge in the field, the above preferred conditions can be arbitrarily combined to obtain the preferred examples of the invention.
The invention has the positive progress effects that:
the ultra-clean emission cold and hot co-production system of the coking plant is provided with devices such as a waste heat boiler, an absorption tower, a regenerator and the like, so that the waste heat of the flue gas of the coking furnace is deeply recovered and efficiently utilized, the ultra-clean emission cold and hot co-production system of the coking plant also has the environmental benefit of ultra-clean emission of the flue gas, and the annual energy-saving and environmental benefits are ensured.
Drawings
FIG. 1 is a schematic diagram of the ultra-clean emission cogeneration system of the coke plant of the invention.
Description of the reference numerals
Waste heat boiler 1
Boiler flue gas inlet 11
Boiler flue gas outlet 12
Boiler cold source inlet 13
Boiler cold source outlet 14
Absorption tower 2
Absorption tower flue gas inlet 21
Absorber flue gas outlet 22
Absorption tower solution inlet 23
Absorption tower solution outlet 24
Absorption tower cold source inlet 25
Absorption tower cold source outlet 26
Regenerator 3
Regenerator solution inlet 31
Regenerator solution outlet 32
Secondary steam outlet 33
Regenerator heat source inlet 34
Regenerator heat source outlet 35
Absorption refrigerating unit 4
Heat source inlet 41 of refrigerating unit
Heat source outlet 42 of refrigerating unit
Chilled water inlet 43 of a refrigeration unit
First heat exchanger 5 of chilled water outlet 44 of refrigerating unit
First flue gas inlet 51
First flue gas outlet 52
First cold source inlet 53
First cold source outlet 54
Second heat exchanger 6
Second cold source inlet 61
Second cold source outlet 62
Second heat source inlet 63
Second heat source outlet 64
Third heat exchanger 7
Third cold source inlet 71
Third cold source outlet 72
Third heat source inlet 73
Third heat source outlet 74
Fourth heat exchanger 8
Fourth cold source inlet 81
Fourth cold source outlet 82
Fourth heat source inlet 83
Fourth heat source outlet 84
Denitration device 9
Denitration flue gas inlet 91
Denitration flue gas outlet 92
Heater 10
Coke oven flue gas inlet 101
Coke oven flue gas outlet 102
Heating source inlet 103
Heating source outlet 104
Detailed Description
The invention is further illustrated by means of the following examples, which are not intended to limit the scope of the invention.
The ultra-clean emission combined heat and power generation system of the coking plant provided by the invention comprises a waste heat boiler 1, an absorption tower 2 and a regenerator 3, wherein the waste heat boiler 1 is provided with a boiler flue gas inlet 11, a boiler flue gas outlet 12, a boiler cold source inlet 13 and a boiler cold source outlet 14, the boiler flue gas inlet 11 and the boiler flue gas outlet 12 are communicated through a boiler flue gas pipeline, the boiler cold source inlet 13 and the boiler cold source outlet 14 are communicated through a boiler cold source pipeline, and flue gas in the boiler flue gas pipeline exchanges heat with working media in the boiler cold source pipeline; the absorption tower 2 is provided with an absorption tower flue gas inlet 21, an absorption tower flue gas outlet 22, an absorption tower solution inlet 23 and an absorption tower solution outlet 24, wherein the absorption tower flue gas inlet 21 is communicated with the boiler flue gas outlet 12, the absorption tower flue gas inlet 21 is positioned at the lower part of the absorption tower 2 and discharges flue gas into the inside of the absorption tower 2, the absorption tower flue gas outlet 22 is positioned at the upper part of the absorption tower 2 and discharges flue gas to the outside, the absorption tower solution inlet 23 is positioned at the upper part of the absorption tower 2 and sprays moisture absorption solution into the absorption tower 2, and the absorption tower solution outlet 24 is positioned at the lower part of the absorption tower 2 and discharges moisture absorption solution; the regenerator 3 has a regenerator solution inlet 31, a regenerator solution outlet 32, and a secondary steam outlet 33, the regenerator solution inlet 31 communicates with the absorber solution outlet 24, the regenerator solution outlet 32 communicates with the absorber solution inlet 23, and the secondary steam outlet 33 discharges the secondary steam vaporized by heating the hygroscopic solution.
After the waste heat of the flue gas of the coking furnace is recovered by the waste heat boiler 1, the flue gas enters the absorption tower 2, and the waste heat of the flue gas is transmitted to working media in a boiler cold source pipeline, such as winter heating water, annual boiler water, domestic water, production water and the like. The flue gas enters the absorption tower 2 from the absorption tower flue gas inlet 21, runs from bottom to top, and performs countercurrent heat and mass transfer with the hygroscopic solution entering from the absorption tower solution inlet 23 and falling from the upper part, and the hygroscopic solution plays roles of deep dedusting and degassing sol. The flue gas is discharged out of the system through the flue gas outlet 22 of the absorption tower, and at the moment, the waste heat of the discharged flue gas is recovered and deeply purified through the hygroscopic solution, so that the waste heat recovery is realized while the ultra-clean discharge is realized. After passing through the flue gas, the hygroscopic solution absorbs water vapor in the flue gas, the concentrated solution is diluted into a dilute solution, and flows into the regenerator 3 from the absorber solution outlet 24 and the regenerator solution inlet 31. The dilute solution is heated in the regenerator 3 and evaporates the secondary steam, the dilute solution is changed into concentrated solution again, and enters the absorption tower 2 from the regenerator solution outlet 32 and the absorption tower solution inlet 23, so that the circulation of the hygroscopic solution is realized.
The waste heat boiler 1 adopts a finned tube-heat pipe type waste heat boiler with a combination of a finned tube and a heat pipe, namely, the heat exchange (primary heat exchange) is performed by the finned tube above the dew point temperature, and the heat pipe (secondary heat exchange) is performed at a position where dew point corrosion temperature is easy to occur, so that the reasonable heat exchange design and wall temperature design can improve the heat exchange coefficient, and meanwhile, the problem of low-temperature dew point corrosion is solved.
Before the flue gas enters the waste heat boiler 1, denitration treatment is needed, so that a denitration device 9 is further arranged before the waste heat boiler 1, and the flue gas firstly passes through the denitration device 9 for denitration and then enters the waste heat boiler 1. Specifically, the denitration device 9 has a denitration flue gas inlet 91 and a denitration flue gas outlet 92, the denitration flue gas outlet 92 communicates with the boiler flue gas inlet 11, and flue gas enters the denitration device 9 from the denitration flue gas inlet 91 and is discharged from the denitration flue gas outlet 92.
The flue gas needs to reach higher temperature when carrying out denitration treatment, in order to guarantee denitration effect, before the flue gas gets into denitrification facility 9, need heat in heater 10 first. Specifically, the heater 10 includes a coke oven flue gas inlet 101, a coke oven flue gas outlet 102, a heating source inlet 103, and a heating source outlet 104, the coke oven flue gas inlet 101 and the coke oven flue gas outlet 102 are communicated through a coke oven flue gas pipeline, the heating source inlet 103 and the heating source outlet 104 are communicated through a heating source pipeline, flue gas in the coke oven flue gas pipeline exchanges heat with working medium in the heating source pipeline, and the coke oven flue gas outlet 102 is communicated with a denitration flue gas inlet 91. For energy saving and comprehensive utilization, the waste heat of the raw gas of the coking furnace can be utilized to heat the flue gas, namely, the raw gas of the coking furnace enters the heating source pipeline from the heating source inlet 103 and is discharged from the heating source outlet 104, and the raw gas in the heating source pipeline exchanges heat with the flue gas in the flue gas pipeline of the coke oven to raise the temperature of the flue gas. The heater 10 may be a plate-fin heat exchanger, a heat pipe heat exchanger, a plate heat exchanger, or the like.
The system can be provided with a plurality of heat exchangers at various positions according to actual requirements, for example, a heat exchanger can be arranged between the boiler flue gas outlet 12 and the absorption tower flue gas inlet 21, for example, one or more heat exchangers can be arranged at the secondary steam outlet 33. The heat exchanger can be a plate-fin heat exchanger, a heat pipe heat exchanger, a plate heat exchanger and the like.
The flue gas entering the absorption tower 2 only releases sensible heat, and in fact, the latent heat of vaporization in the flue gas can be recovered, and in order to further improve the recovery rate of waste heat, a heat exchange facility can be arranged in the absorption tower 2, so that the latent heat of the flue gas can be recovered. Specifically, the absorption tower 2 further has an absorption tower cold source inlet 25 and an absorption tower cold source outlet 26, the absorption tower cold source inlet 25 and the absorption tower cold source outlet 26 are communicated through an absorption tower cold source pipeline, and the working medium in the absorption tower cold source pipeline exchanges heat with the working medium in the absorption tower 2. Besides the heat exchange facilities arranged in the absorption tower 2, the cold source outlet 26 of the absorption tower can be communicated with one or more heat exchangers and can exchange heat, so that the comprehensive recovery of waste heat is realized.
Simultaneously, the hygroscopic solution enters the regenerator 3, and a heat exchange facility is also arranged in the regenerator 3, so that the steam generated after heat exchange of the waste heat boiler 1 enters the regenerator 3 and exchanges heat with the solution in the regenerator 3. Specifically, the regenerator 3 further has a regenerator heat source inlet 34 and a regenerator heat source outlet 35, the regenerator heat source inlet 34 and the regenerator heat source outlet 35 are communicated through a regenerator heat source pipeline, the working medium in the regenerator heat source pipeline exchanges heat with the working medium in the regenerator 3, and the regenerator heat source inlet 34 is communicated with the boiler cold source outlet 14. Besides the heat exchange facilities arranged in the regenerator 3, the regenerator heat source outlet 35 can be communicated with one or more heat exchangers and can exchange heat, so that the comprehensive recovery of waste heat is realized.
The steam generated by the waste heat boiler 1 has higher grade and can be directly used as a regeneration heat source of the regenerator 3, so that the energy utilization rate can be further improved by communicating the regenerator heat source inlet 34 with the boiler cold source outlet 14.
The cold source of the heat exchanger can be used for heating water in winter, boiler water in whole year, domestic water, production water and the like after being heated. Besides, the heat exchanger can be communicated with the absorption refrigerating unit 4, and is mainly used for meeting the summer refrigerating requirement of a factory.
One specific scheme of the combination of the heat exchangers is as follows:
the ultra-clean emission combined heat and cold production system of the coking plant comprises a first heat exchanger 5, a second heat exchanger 6 and a third heat exchanger 7, wherein the first heat exchanger 5 is positioned between a boiler flue gas outlet 12 and an absorber flue gas inlet 21, the first heat exchanger 5 is provided with a first flue gas inlet 51, a first flue gas outlet 52, a first cold source inlet 53 and a first cold source outlet 54, the first flue gas inlet 51 and the first flue gas outlet 52 are communicated through a first flue gas pipeline, the first cold source inlet 53 and the first cold source outlet 54 are communicated through a first cold source pipeline, flue gas in the first flue gas pipeline is subjected to heat exchange with working media in the first cold source pipeline, the boiler flue gas outlet 12 is communicated with the first flue gas inlet 51, and the first flue gas outlet 52 is communicated with the absorber flue gas inlet 21;
the second heat exchanger 6 is provided with a second cold source inlet 61, a second cold source outlet 62, a second heat source inlet 63 and a second heat source outlet 64, the second cold source inlet 61 and the second cold source outlet 62 are communicated through a second cold source pipeline, the second heat source inlet 63 and the second heat source outlet 64 are communicated through a second heat source pipeline, a working medium in the second cold source pipeline is in heat exchange with a working medium in the second heat source pipeline, the second heat source inlet 63 is communicated with the secondary steam outlet 33, the second heat source outlet 64 is communicated with an external pipeline, and the second cold source inlet 61, the second cold source outlet 62 and the first cold source outlet 54 are mutually communicated;
the third heat exchanger 7 is provided with a third cold source inlet 71, a third cold source outlet 72, a third heat source inlet 73 and a third heat source outlet 74, the third cold source inlet 71 and the third cold source outlet 72 are communicated through a third cold source pipeline, the third heat source inlet 73 and the third heat source outlet 74 are communicated through a third heat source pipeline, a working medium in the third cold source pipeline is in heat exchange with a working medium in the third heat source pipeline, the third heat source inlet 73 is communicated with the secondary steam outlet 33, the third heat source outlet 74 is communicated with the second heat source outlet 64, and the third cold source inlet 71 and the third cold source outlet 72 are both communicated with an external pipeline.
Through the first heat exchanger 5, the second heat exchanger 6 and the third heat exchanger 7, the waste heat at the positions of the boiler flue gas outlet 12 and the secondary steam outlet 33 is comprehensively recovered, and the heat exchangers are mutually communicated, so that each heat exchanger is provided with a bypass, and the safety of the system is improved.
The fourth heat exchanger 8 is used for recovering heat in the absorber 2 and the regenerator 3, the fourth heat exchanger 8 is provided with a fourth cold source inlet 81, a fourth cold source outlet 82, a fourth heat source inlet 83 and a fourth heat source outlet 84, the fourth cold source inlet 81 and the fourth cold source outlet 82 are communicated through a fourth cold source pipeline, the fourth heat source inlet 83 and the fourth heat source outlet 84 are communicated through a fourth heat source pipeline, a working medium in the fourth heat source pipeline is in heat exchange with a working medium in the fourth heat source pipeline, the fourth heat source inlet 83 is communicated with the regenerator heat source outlet 35, the fourth heat source outlet 84 is communicated with an external pipeline, the fourth cold source inlet 81 is communicated with the absorber cold source outlet 26, and the fourth cold source outlet 82 is communicated with the third cold source inlet 71.
Through the first heat exchanger 5, the second heat exchanger 6, the third heat exchanger 7 and the fourth heat exchanger 8, the waste heat of the coke oven flue gas is efficiently recycled, other waste heat in the coke oven is fully utilized, no energy is input, the ultra-low emission environmental protection benefit of the flue gas is realized, and the annual energy-saving environmental protection benefit is ensured.
The absorption refrigeration unit 4 is communicated with one or more heat exchangers, so that the cooling requirement of the factory in summer can be met. One specific solution for the absorption refrigeration unit 4 is as follows: the absorption refrigerating unit 4 is provided with a refrigerating unit heat source inlet 41, a refrigerating unit heat source outlet 42, a refrigerating unit chilled water inlet 43 and a refrigerating unit chilled water outlet 44, the refrigerating unit heat source inlet 41 and the refrigerating unit heat source outlet 42 are communicated through refrigerating unit heat source pipelines, the refrigerating unit chilled water inlet 43 and the refrigerating unit chilled water outlet 44 are communicated through chilled water pipelines, chilled water in the chilled water pipelines exchanges heat with working media in the refrigerating unit heat source pipelines, the refrigerating unit chilled water inlet 43 and the refrigerating unit chilled water outlet 44 are connected with an external pipeline, the refrigerating unit heat source inlet 41 is communicated with a first cold source outlet 54, and the refrigerating unit heat source outlet 42 is communicated with a first cold source inlet 53. The absorption refrigeration unit 4 is not limited to being in communication with the first heat exchanger 5 and the second heat exchanger 6, and may be in communication with other heat exchangers.
The present invention is not limited to the above-described embodiments, and any changes in shape or structure thereof are within the scope of the present invention. The scope of the present invention is defined by the appended claims, and those skilled in the art can make various changes or modifications to these embodiments without departing from the principle and spirit of the present invention, but these changes and modifications fall within the scope of the present invention.
Claims (2)
1. A coke plant ultra-clean emission cogeneration system, comprising:
a denitration device (9), wherein the denitration device (9) is provided with a denitration flue gas inlet (91) and a denitration flue gas outlet (92), and flue gas enters the denitration device (9) from the denitration flue gas inlet (91) and is discharged from the denitration flue gas outlet (92);
the waste heat boiler (1), the waste heat boiler (1) is provided with a boiler flue gas inlet (11), a boiler flue gas outlet (12), a boiler cold source inlet (13) and a boiler cold source outlet (14), the boiler flue gas inlet (11) and the boiler flue gas outlet (12) are communicated through a boiler flue gas pipeline, the boiler cold source inlet (13) and the boiler cold source outlet (14) are communicated through a boiler cold source pipeline, flue gas in the boiler flue gas pipeline exchanges heat with working media in the boiler cold source pipeline, and the boiler flue gas inlet (11) is communicated with a denitration flue gas outlet (92);
an absorption tower (2), wherein the absorption tower (2) is provided with an absorption tower flue gas inlet (21), an absorption tower flue gas outlet (22), an absorption tower solution inlet (23) and an absorption tower solution outlet (24), the absorption tower flue gas inlet (21) is communicated with the boiler flue gas outlet (12), the absorption tower flue gas inlet (21) is positioned at the lower part of the absorption tower (2) and discharges the flue gas into the absorption tower (2), the absorption tower flue gas outlet (22) is positioned at the upper part of the absorption tower (2) and discharges the flue gas to the outside, the absorption tower solution inlet (23) is positioned at the upper part of the absorption tower (2) and sprays a moisture absorption solution into the absorption tower (2), and the absorption tower solution outlet (24) is positioned at the lower part of the absorption tower (2) and discharges the moisture absorption solution;
a regenerator (3), wherein the regenerator (3) is provided with a regenerator solution inlet (31), a regenerator solution outlet (32) and a secondary steam outlet (33), the regenerator solution inlet (31) is communicated with the absorption tower solution outlet (24), the regenerator solution outlet (32) is communicated with the absorption tower solution inlet (23), and the secondary steam outlet (33) discharges secondary steam which is obtained by heating and evaporating the moisture absorption solution;
the boiler comprises a first heat exchanger (5), wherein the first heat exchanger (5) is positioned between a boiler flue gas outlet (12) and an absorber flue gas inlet (21), the first heat exchanger (5) is provided with a first flue gas inlet (51), a first flue gas outlet (52), a first cold source inlet (53) and a first cold source outlet (54), the first flue gas inlet (51) and the first flue gas outlet (52) are communicated through a first flue gas pipeline, the first cold source inlet (53) and the first cold source outlet (54) are communicated through a first cold source pipeline, flue gas in the first flue gas pipeline is subjected to heat exchange with working media in the first cold source pipeline, the boiler flue gas outlet (12) is communicated with the first flue gas inlet (51), and the first flue gas outlet (52) is communicated with the absorber flue gas inlet (21);
the absorption refrigerating unit (4), the absorption refrigerating unit (4) is provided with a refrigerating unit heat source inlet (41), a refrigerating unit heat source outlet (42), a refrigerating unit chilled water inlet (43) and a refrigerating unit chilled water outlet (44), the refrigerating unit heat source inlet (41) and the refrigerating unit heat source outlet (42) are communicated through a refrigerating unit heat source pipeline, the refrigerating unit chilled water inlet (43) and the refrigerating unit chilled water outlet (44) are communicated through a chilled water pipeline, chilled water in the chilled water pipeline is in heat exchange with working media in the refrigerating unit heat source pipeline, the refrigerating unit chilled water inlet (43) and the refrigerating unit chilled water outlet (44) are connected with an external pipeline, the refrigerating unit heat source inlet (41) is communicated with the first cold source outlet (54), and the refrigerating unit heat source outlet (42) is communicated with the first cold source inlet (53);
the second heat exchanger (6), the second heat exchanger (6) has second cold source import (61), second cold source export (62), second heat source import (63), second heat source export (64), link together through the second cold source pipeline between second cold source import (61), second cold source export (62), link together through the second heat source pipeline between second heat source import (63), second heat source export (64), working medium in the second cold source pipeline carries out heat exchange with working medium in the second heat source pipeline, second heat source import (63) are linked together with secondary steam export (33), second heat source export (64) are linked together with outside pipeline, link together between second cold source import (61), second cold source export (62), first cold source export (54);
the third heat exchanger (7), the third heat exchanger (7) has a third cold source inlet (71), a third cold source outlet (72), a third heat source inlet (73) and a third heat source outlet (74), the third cold source inlet (71) and the third cold source outlet (72) are communicated through a third cold source pipeline, the third heat source inlet (73) and the third heat source outlet (74) are communicated through a third heat source pipeline, a working medium in the third cold source pipeline is in heat exchange with a working medium in the third heat source pipeline, the third heat source inlet (73) is communicated with the secondary steam outlet (33), the third heat source outlet (74) is communicated with the second heat source outlet (64), and the third cold source inlet (71) and the third cold source outlet (72) are both communicated with the external pipeline;
the fourth heat exchanger (8), the fourth heat exchanger (8) has a fourth cold source inlet (81), a fourth cold source outlet (82), a fourth heat source inlet (83) and a fourth heat source outlet (84), the fourth cold source inlet (81) and the fourth cold source outlet (82) are communicated through a fourth cold source pipeline, the fourth heat source inlet (83) and the fourth heat source outlet (84) are communicated through a fourth heat source pipeline, the working medium in the fourth cold source pipeline is in heat exchange with the working medium in the fourth heat source pipeline, the fourth heat source inlet (83) is communicated with the regenerator heat source outlet (35), the fourth heat source outlet (84) is communicated with the external pipeline, the fourth cold source inlet (81) is communicated with the absorber heat source outlet (26), and the fourth cold source outlet (82) is communicated with the third cold source inlet (71);
the absorption tower (2) is also provided with an absorption tower cold source inlet (25) and an absorption tower cold source outlet (26), the absorption tower cold source inlet (25) and the absorption tower cold source outlet (26) are communicated through an absorption tower cold source pipeline, and the working medium of the absorption tower cold source pipeline exchanges heat with the working medium in the absorption tower (2);
the regenerator (3) is further provided with a regenerator heat source inlet (34) and a regenerator heat source outlet (35), the regenerator heat source inlet (34) is communicated with the regenerator heat source outlet (35) through a regenerator heat source pipeline, working media in the regenerator heat source pipeline are in heat exchange with working media in the regenerator (3), and the regenerator heat source inlet (34) is communicated with the boiler cold source outlet (14).
2. The ultra-clean emission cogeneration system of a coking plant of claim 1, wherein: the ultra-clean emission cold and hot co-production system of the coking plant further comprises a heater (10), wherein the heater (10) comprises a coke oven flue gas inlet (101), a coke oven flue gas outlet (102), a heating source inlet (103) and a heating source outlet (104), the coke oven flue gas inlet (101) and the coke oven flue gas outlet (102) are communicated through a coke oven flue gas pipeline, the heating source inlet (103) and the heating source outlet (104) are communicated through a heating source pipeline, flue gas in the coke oven flue gas pipeline is subjected to heat exchange with working media in the heating source pipeline, and the coke oven flue gas outlet (102) is communicated with a denitration flue gas inlet (91).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710558062.8A CN108131656B (en) | 2017-07-10 | 2017-07-10 | Ultra-clean emission cold and hot co-production system of coking plant |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710558062.8A CN108131656B (en) | 2017-07-10 | 2017-07-10 | Ultra-clean emission cold and hot co-production system of coking plant |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108131656A CN108131656A (en) | 2018-06-08 |
| CN108131656B true CN108131656B (en) | 2024-03-15 |
Family
ID=62388446
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710558062.8A Active CN108131656B (en) | 2017-07-10 | 2017-07-10 | Ultra-clean emission cold and hot co-production system of coking plant |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108131656B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112378116B (en) * | 2020-11-11 | 2022-02-01 | 昊姆（上海）节能科技有限公司 | Open heat pump device driven by high-temperature flue gas and application thereof |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101922821A (en) * | 2009-06-10 | 2010-12-22 | 中国科学院工程热物理研究所 | Method for simultaneously recovering water and latent heat in high-humidity flue gas and heat pump device |
| CN204027066U (en) * | 2014-07-22 | 2014-12-17 | 中冶南方工程技术有限公司 | Utilize the absorption system of silicon steel annealing furnace waste heat flue gas |
| CN105771638A (en) * | 2016-05-06 | 2016-07-20 | 济南大学 | Desulfurization and denitrification method and device for hot sparing of coke oven chimney by using coke oven flue gas |
| CN105833688A (en) * | 2016-05-06 | 2016-08-10 | 山东岱荣节能环保科技有限公司 | Energy-saving clean emission device for coke oven underground flue gas |
| CN205495310U (en) * | 2016-03-11 | 2016-08-24 | 西安华江环保科技股份有限公司 | Coke oven flue desulphurization of exhaust gas deNOx systems |
| CN106247371A (en) * | 2014-08-28 | 2016-12-21 | 国电龙源电力技术工程有限责任公司 | A kind of coal steam-electric plant smoke comprehensive waste-heat utilizing device |
| CN207019036U (en) * | 2017-07-10 | 2018-02-16 | 昊姆（上海）节能科技有限公司 | The ultra-clean cold-heat combined system of discharge in coke-oven plant |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN204987896U (en) * | 2015-06-17 | 2016-01-20 | 中冶南方工程技术有限公司 | Steam -driven blower station waste heat of boiler flue gas utilizes system |
| CN205412650U (en) * | 2016-03-18 | 2016-08-03 | 上海碳索能源环境服务有限公司 | Purifier is retrieved to latent heat |
-
2017
- 2017-07-10 CN CN201710558062.8A patent/CN108131656B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101922821A (en) * | 2009-06-10 | 2010-12-22 | 中国科学院工程热物理研究所 | Method for simultaneously recovering water and latent heat in high-humidity flue gas and heat pump device |
| CN204027066U (en) * | 2014-07-22 | 2014-12-17 | 中冶南方工程技术有限公司 | Utilize the absorption system of silicon steel annealing furnace waste heat flue gas |
| CN106247371A (en) * | 2014-08-28 | 2016-12-21 | 国电龙源电力技术工程有限责任公司 | A kind of coal steam-electric plant smoke comprehensive waste-heat utilizing device |
| CN205495310U (en) * | 2016-03-11 | 2016-08-24 | 西安华江环保科技股份有限公司 | Coke oven flue desulphurization of exhaust gas deNOx systems |
| CN105771638A (en) * | 2016-05-06 | 2016-07-20 | 济南大学 | Desulfurization and denitrification method and device for hot sparing of coke oven chimney by using coke oven flue gas |
| CN105833688A (en) * | 2016-05-06 | 2016-08-10 | 山东岱荣节能环保科技有限公司 | Energy-saving clean emission device for coke oven underground flue gas |
| CN207019036U (en) * | 2017-07-10 | 2018-02-16 | 昊姆（上海）节能科技有限公司 | The ultra-clean cold-heat combined system of discharge in coke-oven plant |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108131656A (en) | 2018-06-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2020191564A1 (en) | Energy-saving system for adopting electric heat pump to deeply recycle smoke waste heat of thermal power plant for centralized heating | |
| CN106979530B (en) | Energy-saving and water-saving system for wet desulfurization system | |
| CN202675910U (en) | Waste heat recovery device for superconducting heat pipe of industrial kiln furnace | |
| CN103244214A (en) | Smoke condensation heat recovery combined heat and power supply system based on organic Rankine cycle | |
| CN102506588B (en) | Cement kiln waste heat comprehensive utilization power generation system and method | |
| CN201569208U (en) | Residual heat reclamation device in petroleum industry | |
| CN212440669U (en) | Wet and hot flue gas waste heat recovery and utilization system | |
| CN205245217U (en) | System is utilized to steam turbine exhaust steam waste heat coupling waste heat of boiler flue gas degree of depth | |
| CN108131656B (en) | Ultra-clean emission cold and hot co-production system of coking plant | |
| CN203489246U (en) | Boiler smoke waste-heat application system | |
| CN203238215U (en) | Power generation device utilizing coke oven raw gas afterheat | |
| CN210373507U (en) | White smoke plume eliminating device of coal-fired power plant | |
| CN202924954U (en) | Waste heat recycling system for coke oven gas primary cooler | |
| CN111336487A (en) | Coke oven raw gas and waste gas waste heat recycling system | |
| CN204005923U (en) | A kind of boiler waste heat recovery system | |
| CN102522157A (en) | System and method for comprehensively utilizing waste heat in enameled wire production process | |
| CN102911679B (en) | Coke oven gas primary cooler waste heat recycling system | |
| CN206310790U (en) | A kind of magnetic suspension and suction-type lithium bromide bimodulus operation heating combined equipment | |
| CN202947122U (en) | Combined waste heat recovery system of phase change heat exchanger and low-pressure economizer | |
| CN110857843A (en) | Coke oven waste heat Stirling power generation system | |
| CN207019036U (en) | The ultra-clean cold-heat combined system of discharge in coke-oven plant | |
| CN201229117Y (en) | Waste-heat recovery device for roller kiln | |
| CN103363539A (en) | Comprehensive flue waste heat utilization device | |
| CN210367571U (en) | Deep recovery system for heat energy of coke oven crude gas | |
| CN203375525U (en) | Comprehensive utilization device of flue waste heat |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |