CN220062618U - Coke oven flue gas and ammonia distillation waste heat utilization system - Google Patents
Coke oven flue gas and ammonia distillation waste heat utilization system Download PDFInfo
- Publication number
- CN220062618U CN220062618U CN202321255443.6U CN202321255443U CN220062618U CN 220062618 U CN220062618 U CN 220062618U CN 202321255443 U CN202321255443 U CN 202321255443U CN 220062618 U CN220062618 U CN 220062618U
- Authority
- CN
- China
- Prior art keywords
- ammonia
- pipeline
- heat
- heat exchanger
- water
- 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
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 322
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 156
- 238000004821 distillation Methods 0.000 title claims abstract description 70
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 41
- 239000003546 flue gas Substances 0.000 title claims abstract description 41
- 239000002918 waste heat Substances 0.000 title claims abstract description 33
- 239000000571 coke Substances 0.000 title claims abstract description 22
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 68
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 68
- 238000009833 condensation Methods 0.000 claims abstract description 38
- 230000005494 condensation Effects 0.000 claims abstract description 38
- 238000000746 purification Methods 0.000 claims abstract description 29
- 238000010438 heat treatment Methods 0.000 claims abstract description 19
- 230000001105 regulatory effect Effects 0.000 claims abstract description 19
- 239000002351 wastewater Substances 0.000 claims abstract description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 64
- 238000012546 transfer Methods 0.000 claims description 16
- 239000008236 heating water Substances 0.000 claims description 14
- 230000035515 penetration Effects 0.000 claims description 14
- 238000001816 cooling Methods 0.000 claims description 10
- 239000000498 cooling water Substances 0.000 claims description 7
- 238000004891 communication Methods 0.000 claims description 4
- 239000002699 waste material Substances 0.000 claims description 4
- 238000011144 upstream manufacturing Methods 0.000 claims description 2
- 239000007789 gas Substances 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 10
- 238000001704 evaporation Methods 0.000 abstract description 4
- 230000008020 evaporation Effects 0.000 abstract description 4
- 230000008569 process Effects 0.000 abstract description 4
- 230000001276 controlling effect Effects 0.000 abstract description 3
- 238000010521 absorption reaction Methods 0.000 description 12
- 238000004939 coking Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000003044 adaptive effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Abstract
The utility model provides a coke oven flue gas and ammonia evaporation waste heat utilization system, which comprises a first heat exchanger, an ammonia evaporation tower, an ammonia condensation and purification heat exchanger, a heat pump unit, a second heat exchanger, an induced draft fan and a chimney, wherein the flue gas is conveyed through a flue gas pipeline sequentially, an ammonia water circulation heating pipeline is arranged between the first heat exchanger and the ammonia evaporation tower, a circulation heat-taking pipeline is arranged between the ammonia condensation and purification heat exchanger, the heat pump unit and the second heat exchanger, and the heat release side of the heat pump unit utilizes the heat release pipeline to realize heat circulation conveying to a heat source demand end. The system recovers the waste heat of the coke oven flue gas to provide a heat source for the ammonia distillation process, reduces the ammonia distillation waste water amount and reduces the treatment load of a biochemical device; meanwhile, waste heat discharged by the ammonia distillation process is recovered for heating in winter or other low-temperature process heat; regulating and controlling ammonia distillation pressure, further concentrating and purifying the concentrated ammonia water, and improving the concentration of the ammonia water.
Description
Technical Field
The utility model relates to the technical field of waste heat recovery in coking chemical industry, in particular to a coke oven flue gas and ammonia distillation waste heat utilization system.
Background
The ammonia distillation process in the coking industry comprises two methods of directly steaming ammonia and indirectly heating ammonia. The direct steam ammonia distillation refers to direct contact heat transfer between the steam and the descending ammonia water in the ammonia distillation tower. The indirect heating ammonia distillation method is divided into three methods of conduction oil heating ammonia distillation, tubular furnace heating ammonia distillation and reboiler ammonia distillation. The indirect ammonia distillation process is more complex than the direct ammonia distillation process, but reduces the ammonia distillation wastewater quantity and the treatment load of the biochemical device.
In either method, the ammonia distillation process requires a large amount of primary energy to be consumed while a large amount of waste heat is exhausted. Taking 140 ten thousand tons of coke produced in a year as an example, the ammonia distillation process consumes 20 tons of steam per hour and 17 ten thousand tons of steam per year, and most of the heat is discharged to the atmosphere. The primary energy consumption of ammonia distillation is reduced, and the waste heat of the ammonia distillation is recycled, so that the production cost can be obviously reduced; simultaneously controlling the ammonia distillation pressure and increasing the concentration of ammonia water can obviously improve economic benefits, and is very necessary and urgently needed in the coking industry at present.
The waste heat of the coke oven flue gas is huge, and even if the waste heat boiler is adopted for recycling, the temperature of the discharged flue gas can still reach 220-260 ℃, so that the waste heat boiler is a good ammonia evaporation heat source. The Chinese patent with publication number of CN102602960B provides a method and equipment for distilling ammonia by utilizing waste heat of flue gas of a coke oven, and the waste heat of the flue gas is recovered by a heat exchanger to heat ammonia water of an ammonia distillation tower to 95 ℃ and return the ammonia water to the ammonia distillation tower, so that the heat exchange efficiency is high once, but the technology is only suitable for a negative pressure ammonia distillation process, and the application range is small. The Chinese patent with publication number of CN102502703B provides an ammonia distillation method by using waste heat of flue gas of a coke oven, which can be applied to an ammonia distillation process at normal pressure by one-time heat exchange, but the technology can not control the ammonia distillation pressure, can not control and improve the concentration of the produced ammonia water, and can not recycle the waste heat of the ammonia distillation process, and the ammonia distillation heat is still white and discharged.
Disclosure of Invention
The utility model aims to overcome the defects in the prior art and provide a coke oven flue gas and ammonia distillation waste heat utilization system. The system recovers the waste heat of the coke oven flue gas to provide a heat source for the ammonia distillation process, reduces the ammonia distillation waste water amount and reduces the treatment load of a biochemical device; meanwhile, waste heat discharged by the ammonia distillation process is recovered for heating in winter or other low-temperature process heat; regulating and controlling ammonia distillation pressure, and further concentrating and purifying the concentrated ammonia water to improve the concentration of the ammonia water; the purposes of waste heat recovery, cost reduction and synergy are realized.
The technical scheme adopted for solving the technical problems is as follows: the utility model provides a coke oven flue gas and evaporate ammonia waste heat utilization system, includes first heat exchanger, ammonia still, ammonia condensation purification heat exchanger, heat pump set, second heat exchanger, draught fan, chimney, first heat exchanger, draught fan and chimney loop through the flue gas pipeline and realize flue gas transportation, be provided with aqueous ammonia circulation heating pipeline between first heat exchanger and the ammonia still, a surplus aqueous ammonia transfer line is used for surplus aqueous ammonia to the transport in the ammonia still, ammonia still with be provided with steam transfer line and comdenstion water transfer line between the ammonia condensation purification heat exchanger, ammonia condensation purification heat exchanger realizes the output of strong aqueous ammonia through a strong aqueous ammonia transfer line, be provided with circulation between ammonia condensation purification heat exchanger, heat pump set and the second heat exchanger and get the heat pipe way, a cooling water circulation pipeline realizes the cooling tower with circulation gets the link up of heat pipe way, the exothermic side of heat pump set utilizes exothermic pipeline to realize to the heat circulation transport of heat source demand end, the ammonia still realizes to the waste ammonia of second heat exchanger is carried through waste water transfer line, the second heat exchanger utilizes the waste water that discharges the pipeline to realize with the waste water that link up.
Preferably, the flue gas pipeline comprises a first pipeline, a second pipeline and a third pipeline, wherein the first pipeline is used for conveying coke oven flue gas to a flue gas inlet of the first heat exchanger, the second pipeline is used for realizing the communication between the first heat exchanger and the induced draft fan, and the third pipeline is used for realizing the communication between the induced draft fan and the chimney.
Further, the ammonia water circulation heating pipeline comprises a fourth pipeline, a fifth pipeline and a first water pump, the fourth pipeline is used for realizing the through of an ammonia outlet of the ammonia still and an ammonia inlet of the first heat exchanger, the fifth pipeline is used for realizing the through of an ammonia outlet of the first heat exchanger and a steam inlet of the ammonia still, the first water pump is arranged on the fourth pipeline, a first bypass pipeline is arranged between the fourth pipeline and the fifth pipeline, the joint of the first bypass pipeline and the fourth pipeline is positioned at the downstream of the first water pump, and a first electric control regulating valve is arranged on the first bypass pipeline.
Further, the residual ammonia water conveying pipeline comprises a sixth pipeline and a seventh pipeline, the sixth pipeline is used for conveying residual ammonia water into the separator in the ammonia distillation tower, and the seventh pipeline is used for conveying residual ammonia water in the separator into a residual ammonia water inlet of the ammonia distillation tower; the steam delivery pipeline is used for realizing the penetration of a steam port of the ammonia still and a steam inlet of the ammonia condensing and purifying heat exchanger, and the condensed water delivery pipeline is used for realizing the penetration of a condensed water outlet of the ammonia condensing and purifying heat exchanger and a condensed water inlet of the ammonia still.
Further, the circulating heat-collecting pipeline comprises an eleventh pipeline, a twelfth pipeline and a second water pump, the eleventh pipeline is communicated with an inlet of the heat absorption side of the ammonia condensing and purifying heat exchanger, the twelfth pipeline is communicated with an outlet of the heat absorption side of the ammonia condensing and purifying heat exchanger, the second water pump is arranged on the twelfth pipeline, a second bypass pipeline is arranged between the pipeline in the heat absorption side of the ammonia condensing and purifying heat exchanger and the twelfth pipeline, a second electric control regulating valve is arranged on the second bypass pipeline, the twelfth pipeline is communicated with an outlet of the heat absorption side of the second heat exchanger, the joint of the fourteenth pipeline and the twelfth pipeline is located at the upstream of the second water pump, the fifteenth pipeline is communicated with an inlet of the heat absorption side of the second heat exchanger, the cooling water circulating pipeline comprises a sixteenth pipeline and a seventeenth pipeline, a water outlet of the sixteenth pipeline is communicated with an outlet of the cooling tower is communicated with the seventeenth pipeline, and the seventeenth pipeline is communicated with a seventeenth pipeline is arranged on the seventeenth pipeline, and the seventeenth pipeline is communicated with a third switch is arranged on the seventeenth pipeline.
Further, the heat release pipeline comprises a heating water inlet pipe and a heating water outlet pipe, the heating water inlet pipe is used for realizing the penetration of a water outlet of a heat source demand end and a water inlet of a heat release side of the heat pump unit, the heating water outlet pipe is used for realizing the penetration of a water inlet of the heat source demand end and a water outlet of the heat release side of the heat pump unit, a third water pump is arranged on the concentrated ammonia water conveying pipeline, and a fourth water pump is arranged on the waste water conveying pipeline.
Further, the first heat exchanger is a plate heat exchanger, the second heat exchanger is a spiral plate heat exchanger, the ammonia condensing and purifying heat exchanger is a two-stage condensing heat exchanger, the first water pump is a variable frequency pump, and the heat source demand end is a heating hot end.
The beneficial effects of the utility model are as follows: the utility model has simple structure and convenient processing and manufacturing; the system recovers the waste heat of the coke oven flue gas to provide a heat source for the ammonia distillation process, reduces the ammonia distillation waste water amount and reduces the treatment load of a biochemical device; meanwhile, the ammonia condensation purification heat exchanger and the second heat exchanger are utilized to realize the recovery of waste heat discharged by an ammonia distillation process, and the recovered waste heat is used for heating a heating end in winter or other low-temperature process heat, so that the utilization rate of waste heat is improved; the first electric control regulating valve and the first water pump are utilized to realize the automatic adaptive regulation of the flow of the ammonia water entering the first heat exchanger, then realize the ammonia distillation pressure regulation in the ammonia distillation tower, and the second electric control regulating valve is utilized to realize the flow regulation of the cooling water in the ammonia condensation purification heat exchange device, so that the sectional condensation concentration purification of the ammonia water is realized, and the concentration of the ammonia water is improved.
Drawings
In order to more clearly illustrate the embodiments of the utility model or the technical solutions of the prior art, the drawings which are used in the description of the embodiments or the prior art will be briefly described, it being obvious that the drawings in the description below are some preferred embodiments of the utility model and that other drawings can be obtained from these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of the system principle of the present utility model;
in the figure: a first heat exchanger, a 2 ammonia distillation tower, a 21 separator, a 3 ammonia condensing and purifying heat exchanger, a 4 heat pump unit, a 5 second heat exchanger, a 6 induced draft fan, a 7 chimney, a 101 first pipeline, a 102 second pipeline, a 103 third pipeline, a 104 fourth pipeline, a 105 fifth pipeline, a 106 sixth pipeline, a 107 seventh pipeline, a 108 steam conveying pipeline, a 109 condensate conveying pipeline, a 110 concentrated ammonia water conveying pipeline, a 111 eleventh pipeline, a 112 twelfth pipeline, a 113 second bypass pipeline, a 114 fourteenth pipeline, a 115 fifteenth pipeline, a 116 sixteenth pipeline, a 117 seventeenth pipeline, a 118 waste water conveying pipeline, a 119 waste ammonia discharging pipeline, a 120 heating water inlet pipe, a 121 heating water outlet pipe, a 201 first bypass pipeline, a 301 first electric control regulating valve, a 302 second electric control regulating valve, a 303 third switching valve, a 304 fourth switching valve, a 401 first water pump, a 402 second water pump, a 403 third water pump and a 404 fourth water pump.
Detailed Description
The technical solutions of the embodiments of the present utility model will be clearly and completely described below with reference to specific embodiments and fig. 1, and it is apparent that the described embodiments are only some of the preferred embodiments of the present utility model, but not all embodiments. Similar modifications can be made by those skilled in the art without departing from the spirit of the utility model, and therefore the utility model is not to be limited by the specific embodiments disclosed below.
The utility model provides a coke oven flue gas and ammonia distillation waste heat utilization system (shown in figure 1), which comprises a first heat exchanger 1, an ammonia distillation tower 2, an ammonia condensation purification heat exchanger 3, a heat pump unit 4, a second heat exchanger 5, an induced draft fan 6 and a chimney 7, wherein the first heat exchanger 1, the induced draft fan 2 and the chimney 7 sequentially realize flue gas conveying through flue gas pipelines, and when coke oven flue gas circulates from the first heat exchanger 1, the first heat exchanger 1 is utilized to realize heat absorption of the coke oven flue gas, so that the waste heat utilization of the flue gas is realized; an ammonia water circulation heating pipeline is arranged between the first heat exchanger 1 and the ammonia distillation tower 2, the heat absorbed by the first heat exchanger 1 is used for heating the ammonia water mixed liquid flowing out of the ammonia distillation tower 2 to change the ammonia water mixed liquid into high-temperature high-pressure steam, a residual ammonia water conveying pipeline is used for conveying the residual ammonia water into the ammonia distillation tower 2, the high-temperature high-pressure steam generated in the first heat exchanger 1 enters the ammonia distillation tower 2 and then heats the residual ammonia water flowing into the ammonia distillation tower 2 to generate steam, the subsequent purification and concentration of the ammonia water are facilitated, a steam conveying pipeline 108 and a condensed water conveying pipeline 109 are arranged between the ammonia distillation tower 2 and the ammonia condensation purification heat exchanger 3, the ammonia water in a steam state and the water are condensed and separated by the ammonia condensation purification heat exchanger 3, the ammonia condensation purification heat exchanger 3 is convenient to realize the output of the concentrated ammonia water through a concentrated ammonia water conveying pipeline 110, and a third water pump 403 is arranged on the concentrated ammonia water conveying pipeline 110 to provide conveying power; the concentrated ammonia water can be conveyed into a concentrated ammonia water tank, a circulating heat-taking pipeline is arranged among the ammonia condensation purification heat exchanger 3, the heat pump unit 4 and the second heat exchanger 5, the circulating heat-taking pipeline absorbs heat in the ammonia condensation purification heat exchanger 3 and the second heat exchanger 5 and transmits the heat to the heat pump unit 4, the heat release side of the heat pump unit 4 utilizes the heat release pipeline to realize heat circulation conveying to a heat source demand end, so that waste heat utilization is realized, a cooling water circulation pipeline realizes the through connection of a cooling tower and the circulating heat-taking pipeline, and in practical application, when the heat absorbed by the circulating heat-taking pipeline is not needed any more, the cooling water circulation pipeline can be utilized to convey the heat into the cooling tower, so that heat release is realized; the ammonia still 2 realizes the waste ammonia delivery to the second heat exchanger 5 through a waste water delivery pipeline 118, a fourth water pump 118 is arranged on the waste water delivery pipeline 118, and the waste water discharge power is realized by the fourth water pump 118; the second heat exchanger 5 is communicated with a wastewater tank by a wastewater discharge pipeline 119.
On the basis of the embodiment, the specific implementation mode of the flue gas pipeline comprises a first pipeline 101, a second pipeline 102 and a third pipeline 103, wherein the first pipeline 101 is used for conveying coke oven flue gas to a flue gas inlet of the first heat exchanger 1, the second pipeline 102 is used for realizing the through between the first heat exchanger 1 and the induced draft fan 6, the third pipeline 103 is used for realizing the through between the induced draft fan 6 and the chimney 7, and in practical application, the induced draft fan 6 is used for providing circulating power for the flue gas, so that high-temperature flue gas continuously flows into the first heat exchanger 1, continuous absorption and utilization of flue gas waste heat are realized, and the flue gas after heat exchange is directly discharged from the chimney.
Based on the above embodiment, the specific implementation manner of the ammonia water circulation heating pipeline is as follows: the ammonia water circulation heating pipeline comprises a fourth pipeline 104, a fifth pipeline 105 and a first water pump 401, the fourth pipeline 104 is used for realizing the through of an ammonia outlet of the ammonia distillation tower 2 and an ammonia inlet of the first heat exchanger 1, the fifth pipeline 105 is used for realizing the through of an ammonia outlet of the first heat exchanger 1 and a steam inlet of the ammonia distillation tower 2, the first water pump 401 is arranged on the fourth pipeline 104, the first water pump 401 is used for realizing the circulation of the ammonia water in the ammonia distillation tower 2 to enter the first heat exchanger 1 and be heated to generate steam, a first bypass pipeline 201 is arranged between the fourth pipeline 104 and the fifth pipeline 105, the joint of the first bypass pipeline 201 and the fourth pipeline 104 is positioned at the downstream of the first water pump 401, a first electric control regulating valve 301 is arranged on the first bypass pipeline 201, in the practical application process, the first water pump 401 is a variable frequency water pump, the automatic regulating capacity of the first electric control regulating valve 301 and the first water pump 401 is used for realizing the automatic regulating capacity of the first water pump 401, and the automatic regulating capacity of the first water pump 401 is used for realizing the automatic regulating capacity of the ammonia water pump 2, and the safety regulation of the ammonia water 2 in the ammonia distillation tower 2 is realized.
Based on the above embodiment, the specific implementation manner of the residual ammonia water conveying pipeline is as follows: the residual ammonia water conveying pipeline comprises a sixth pipeline 106 and a seventh pipeline 107, the sixth pipeline 106 is used for conveying residual ammonia water into a separator 21 in the ammonia distillation tower 2, the separator 21 achieves preliminary heat exchange between steam in the ammonia distillation tower 2 and the residual ammonia water, and then achieves preheating of the residual ammonia water, the seventh pipeline 107 is used for conveying the residual ammonia water in the separator 21 into a residual ammonia water inlet of the ammonia distillation tower 2, and when the residual ammonia water enters the ammonia distillation tower 2 from the residual ammonia water inlet of the ammonia distillation tower 2, the residual ammonia water is heated by high-temperature and high-pressure steam in the ammonia distillation tower 2, so that the residual ammonia water generates steam; the steam delivery pipeline 108 is used for realizing the penetration of the steam port of the ammonia distillation tower 2 and the steam inlet of the ammonia condensation purification heat exchanger 3, after the steam in the steam delivery pipeline 108 enters the ammonia condensation purification heat exchanger 3, cooling condensation is carried out, and the condensation temperature of the steam and the ammonia steam is different, so that the condensation purification of ammonia water can be realized, and the ammonia condensation purification heat exchanger 3 can be further improved in condensation concentration purity of the ammonia water, wherein the ammonia condensation purification heat exchanger 3 is provided with a two-stage condensation heat exchanger, namely, the ammonia condensation purification heat exchanger is formed by two conventional condensation heat exchangers, the first condensation heat exchanger is used for mainly condensing the steam, the second condensation heat exchanger is used for further condensing the steam and the ammonia water steam, so that the purity of strong water can be improved, and the condensation delivery pipeline 109 is used for realizing the penetration of the condensation water outlet of the ammonia condensation purification heat exchanger 3 and the condensation water inlet of the ammonia distillation tower 2, so that the water resource of the ammonia distillation tower 2 is saved.
Based on the above embodiment, the specific implementation manner of the circulating heat-taking pipeline is as follows: the circulating heat-taking pipeline comprises an eleventh pipeline 111, a twelfth pipeline 112 and a second water pump 402, wherein the eleventh pipeline 111 realizes the through connection of an outlet of the heat release side of the heat pump unit 4 and an inlet of the heat absorption side of the ammonia condensing and purifying heat exchanger 3, the twelfth pipeline 112 realizes the through connection of an outlet of the heat absorption side of the ammonia condensing and purifying heat exchanger 3 and an inlet of the heat pump unit 4, the second water pump 402 is arranged on the twelfth pipeline 112, a first second bypass pipeline 113 is arranged between a pipeline in the heat absorption side of the ammonia condensing and purifying heat exchanger 3 and the twelfth pipeline 112, a first second electronic control regulating valve 302 is arranged on the second bypass pipeline 113, the automatic regulating capability of the second electronic control regulating valve 302 is utilized, the flow regulation of heat exchange medium of a pipeline in the heat absorption side of the ammonia condensing and purifying heat exchanger 3 is realized, the operation control of the ammonia condensing and purifying work of the ammonia condensing and the heat exchanger 3 in a stage is conveniently realized, the fourteenth pipeline 112 realizes the through connection of the twelfth pipeline 112 and an outlet of the heat absorption side of the second heat exchanger 5, the seventeenth pipeline 114 is connected with the eleventh pipeline 114, the seventeenth pipeline 116 is arranged on the seventeenth pipeline 116, the seventeenth pipeline 117 is connected with the seventeenth pipeline 116, the seventeenth pipeline 116 is connected with the seventeenth pipeline 116, the seventeenth pipeline 117 is arranged on the cooling pipeline 116, the seventeenth pipeline 117 is connected with the seventeenth pipeline 116, and the pipeline 117 is arranged on the cooling pipeline 116, further, the heat release pipeline includes a heating water inlet pipe 120 and a heating water outlet pipe 121, the heating water inlet pipe 120 realizes the penetration of the water outlet of the heat source demand end and the water inlet of the heat release side of the heat pump unit 4, and the heating water outlet pipe 121 realizes the penetration of the water inlet of the heat source demand end and the water outlet of the heat release side of the heat pump unit 4. In practical application, when the heat source demand end needs to collect heat, the third switch valve 303 and the fourth switch valve 304 are closed, and meanwhile, the heat pump unit 4 is in a working state, so that the heat pump unit 4 uses the heat provided by the ammonia condensation purification heat exchanger 3 and the second heat exchanger 5 to perform heat conversion, so as to realize heat supply to the heat source demand end, when the heat source demand end does not need to collect heat, the third switch valve 303 and the fourth switch valve 304 are opened, and meanwhile, the heat pump unit 4 is in a closing state, so as to realize heat discharge in the ammonia condensation purification heat exchanger 3 and the second heat exchanger 5 by using the cooling tower.
In practical application, the first heat exchanger 1 is a plate heat exchanger, and the second heat exchanger 5 is a spiral plate heat exchanger.
Other than the technical features described in the specification, all are known to those skilled in the art.
While the preferred embodiments and examples of the present utility model have been described in detail with reference to the accompanying drawings, the present utility model is not limited to the embodiments and examples, and it will be apparent to those skilled in the art that various modifications and variations can be made without departing from the spirit of the present utility model, and the scope of the utility model is also defined by the appended claims.
Claims (7)
1. The utility model provides a coke oven flue gas and evaporate ammonia waste heat utilization system, its characterized in that includes first heat exchanger, ammonia still, ammonia condensation purification heat exchanger, heat pump set, second heat exchanger, draught fan, chimney, first heat exchanger, draught fan and chimney loop through the flue gas pipeline and realize flue gas transportation, be provided with aqueous ammonia circulation heating pipeline between first heat exchanger and the ammonia still, a surplus aqueous ammonia transfer line is used for surplus aqueous ammonia to the transport in the ammonia still, ammonia still with be provided with steam transfer line and comdenstion water transfer line between the ammonia condensation purification heat exchanger, ammonia condensation purification heat exchanger realizes the output of strong aqueous ammonia through a strong aqueous ammonia transfer line, be provided with circulation between ammonia condensation purification heat exchanger, heat pump set and the second heat exchanger and get through with circulation heat transfer line, a cooling water circulation pipeline realizes the cooling tower with circulation heat transfer line's heat release side of heat pump set utilizes the exothermic pipeline to realize to the heat circulation transfer of heat source demand end, the ammonia still realizes to the ammonia transfer of waste heat transfer line through waste water transfer line, the second heat exchanger realizes with waste water tank that discharges.
2. The system of claim 1, wherein the flue gas pipeline comprises a first pipeline, a second pipeline and a third pipeline, the first pipeline is used for conveying the coke oven flue gas to the flue gas inlet of the first heat exchanger, the second pipeline is used for realizing the communication between the first heat exchanger and the induced draft fan, and the third pipeline is used for realizing the communication between the induced draft fan and the chimney.
3. The coke oven flue gas and ammonia distillation waste heat utilization system according to claim 2, wherein the ammonia water circulation heating pipeline comprises a fourth pipeline, a fifth pipeline and a first water pump, the fourth pipeline is used for realizing the penetration of an ammonia outlet of the ammonia distillation tower and an ammonia inlet of the first heat exchanger, the fifth pipeline is used for realizing the penetration of an ammonia outlet of the first heat exchanger and a steam inlet of the ammonia distillation tower, the first water pump is arranged on the fourth pipeline, a first bypass pipeline is arranged between the fourth pipeline and the fifth pipeline, a joint of the first bypass pipeline and the fourth pipeline is positioned at the downstream of the first water pump, and a first electric control regulating valve is arranged on the first bypass pipeline.
4. A coke oven gas and ammonia distillation waste heat utilization system as claimed in claim 3, wherein the residual ammonia water conveying pipeline comprises a sixth pipeline and a seventh pipeline, wherein the sixth pipeline is used for conveying residual ammonia water into a separator in the ammonia distillation tower, and the seventh pipeline is used for conveying residual ammonia water in the separator into a residual ammonia water inlet of the ammonia distillation tower; the steam delivery pipeline is used for realizing the penetration of a steam port of the ammonia still and a steam inlet of the ammonia condensing and purifying heat exchanger, and the condensed water delivery pipeline is used for realizing the penetration of a condensed water outlet of the ammonia condensing and purifying heat exchanger and a condensed water inlet of the ammonia still.
5. The system according to claim 4, wherein the circulating heat-extracting pipe comprises an eleventh pipe, a twelfth pipe and a second water pump, the eleventh pipe is used for realizing that an outlet of a heat releasing side of the heat pump unit is communicated with an inlet of a heat absorbing side of the ammonia condensing and purifying heat exchanger, the twelfth pipe is used for realizing that an outlet of the heat absorbing side of the ammonia condensing and purifying heat exchanger is communicated with an inlet of the heat pump unit, the second water pump is arranged on the twelfth pipe, a second bypass pipe is arranged between a pipe in a heat absorbing side of the ammonia condensing and purifying heat exchanger and the twelfth pipe, a second electric control regulating valve is arranged on the second bypass pipe, a fourteenth pipe is used for realizing that the twelfth pipe is communicated with an outlet of the heat absorbing side of the second heat exchanger, a fifteenth pipe is positioned at the upstream of the second water pump, the fifteenth pipe is used for realizing that the eleventh pipe is communicated with an inlet of the side of the second heat exchanger, the cooling water circulating pipe comprises a sixteenth pipe and a seventeenth pipe, a sixteenth valve is arranged on the seventeenth pipe is used for realizing that the seventeenth pipe is communicated with the cooling pipe, and the seventeenth pipe is arranged on the seventeenth pipe.
6. The system according to claim 5, wherein the heat release pipeline comprises a heating water inlet pipe and a heating water outlet pipe, the heating water inlet pipe is used for realizing the penetration of a water outlet of a heat source demand end and a water inlet of a heat release side of the heat pump unit, the heating water outlet pipe is used for realizing the penetration of a water inlet of a heat source demand end and a water outlet of a heat release side of the heat pump unit, a third water pump is arranged on the concentrated ammonia water conveying pipeline, and a fourth water pump is arranged on the waste ammonia conveying pipeline.
7. The system of claim 6, wherein the first heat exchanger is a plate heat exchanger, the second heat exchanger is a spiral plate heat exchanger, the ammonia condensing and purifying heat exchanger is a two-stage condensing heat exchanger, the first water pump is a variable frequency pump, and the heat source demand end is a heating hot end.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321255443.6U CN220062618U (en) | 2023-05-20 | 2023-05-20 | Coke oven flue gas and ammonia distillation waste heat utilization system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321255443.6U CN220062618U (en) | 2023-05-20 | 2023-05-20 | Coke oven flue gas and ammonia distillation waste heat utilization system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220062618U true CN220062618U (en) | 2023-11-21 |
Family
ID=88755597
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321255443.6U Active CN220062618U (en) | 2023-05-20 | 2023-05-20 | Coke oven flue gas and ammonia distillation waste heat utilization system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220062618U (en) |
-
2023
- 2023-05-20 CN CN202321255443.6U patent/CN220062618U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US11821637B2 (en) | Energy-saving system using electric heat pump to deeply recover flue gas waste heat from heat power plant for district heating | |
| CN102734787B (en) | Concurrent recycling system for boiler smoke afterheat | |
| CN106766342B (en) | System for recovering ammonia steam waste heat at top of ammonia still tower by using lithium bromide absorption heat pump | |
| CN110124343B (en) | Working medium heat pump rectification process | |
| CN106369866A (en) | Waste steam directly absorbed type double-effect lithium bromide heat pump system and working method thereof | |
| CN220062618U (en) | Coke oven flue gas and ammonia distillation waste heat utilization system | |
| CN112520804A (en) | High salt waste water flash evaporation concentration system of coupling solar energy collection | |
| CN202692016U (en) | Flue gas waste heat recovery system for concurrent boiler | |
| CN113526591B (en) | Energy-saving desulfurization waste water concentration and drying zero discharge system | |
| CN111517400B (en) | Low-grade heat source coupling multi-effect flash evaporation concentration evaporation system | |
| CN112284145B (en) | Waste heat utilization device and method for metallurgical cooling tower | |
| CN113371772A (en) | Concentration desulfurization wastewater system with flue gas waste heat recovery function | |
| CN210356070U (en) | Working medium heat pump rectification system | |
| CN210688281U (en) | Flue gas treatment system | |
| CN210118815U (en) | Sewage heat recovery heating device | |
| CN1548853A (en) | Method for utilizing fully waste water residual-heat and system thereof | |
| CN206478896U (en) | A kind of circulating-water in thermal power plant afterheat utilizing system heated for high-salt wastewater | |
| CN106186132A (en) | Low cost power plant zeroth order value waste water evaporation and concentration processing system and method | |
| CN206478721U (en) | A kind of Circulating Cooling Water of Power Plant condensation waste heat utilizes system | |
| CN220034106U (en) | Energy-saving waste water evaporator | |
| CN218379973U (en) | Industrial silicon low-temperature waste flue gas recycling system | |
| CN220564348U (en) | Hot waste water economizer system | |
| CN216346214U (en) | Circulating water waste heat recovery utilizes system of thermal power plant | |
| CN102537918B (en) | Waste heat recovery device for smoke pipe of steam boiler | |
| CN218510934U (en) | Drainage waste heat recovery system of low-pressure cylinder cutting cylinder heat supply unit |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |