CN210922310U - Ammonia still tower top ammonia steam waste heat recovery system and coking process system - Google Patents
Ammonia still tower top ammonia steam waste heat recovery system and coking process system Download PDFInfo
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- CN210922310U CN210922310U CN201921470663.4U CN201921470663U CN210922310U CN 210922310 U CN210922310 U CN 210922310U CN 201921470663 U CN201921470663 U CN 201921470663U CN 210922310 U CN210922310 U CN 210922310U
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- ammonia
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 518
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 263
- 239000002918 waste heat Substances 0.000 title claims abstract description 59
- 238000011084 recovery Methods 0.000 title claims abstract description 41
- 238000000034 method Methods 0.000 title claims abstract description 33
- 238000004939 coking Methods 0.000 title claims abstract description 25
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 claims abstract description 101
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 62
- 238000010521 absorption reaction Methods 0.000 claims abstract description 48
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 16
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 16
- 238000005057 refrigeration Methods 0.000 claims abstract description 15
- 238000001816 cooling Methods 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims description 46
- 238000010438 heat treatment Methods 0.000 claims description 22
- 239000007789 gas Substances 0.000 claims description 13
- 238000009833 condensation Methods 0.000 claims description 5
- 230000005494 condensation Effects 0.000 claims description 5
- 238000004821 distillation Methods 0.000 claims description 5
- 238000003763 carbonization Methods 0.000 claims description 4
- 239000000571 coke Substances 0.000 claims description 4
- 238000010992 reflux Methods 0.000 claims description 4
- 238000010791 quenching Methods 0.000 claims description 3
- 230000000171 quenching effect Effects 0.000 claims description 3
- 239000003507 refrigerant Substances 0.000 description 12
- 239000006096 absorbing agent Substances 0.000 description 8
- 239000000498 cooling water Substances 0.000 description 5
- 239000002699 waste material Substances 0.000 description 5
- 239000002351 wastewater Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 3
- 238000005086 pumping Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005352 clarification Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
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Abstract
The utility model discloses an ammonia still tower top of tower ammonia steam waste heat recovery system and coking process system, waste heat recovery system include ammonia still and ammonia cold ware, be provided with ammonia steam outlet on the ammonia still, this waste heat recovery system still includes lithium bromide absorption formula unit, ammonia steam outlet with the generator of lithium bromide absorption formula unit communicates, be provided with the ammonia outlet on the generator, the ammonia steam that gets into the generator is discharged through the ammonia outlet after cooling in the generator, lithium bromide absorption formula unit can operate refrigeration operating mode or heat the operating mode; and/or the ammonia water heater also comprises a heat exchanger, wherein the ammonia steam outlet is communicated with the heat exchanger, and the ammonia steam entering the heat exchanger exchanges heat in the heat exchanger to prepare hot water. The ammonia still tower top ammonia vapor waste heat recovery system can effectively improve the energy utilization rate.
Description
Technical Field
The utility model relates to a coking process technology field, more specifically say, relate to an ammonia still top of tower ammonia steam waste heat recovery system and coking process system.
Background
As shown in FIG. 1, the equipment used in the ammonia distillation process of residual ammonia water in the prior art comprises a steam reboiler 01, an ammonia distillation tower 02, a condenser 03, a gas-liquid separator 04 and an ammonia cooler 05. In the prior art, after residual ammonia water of a coking process enters an ammonia still, steam generated by a steam reboiler is heated, the generated ammonia steam enters a dephlegmator for cooling and then enters a gas-liquid separator for gas or liquid separation, the ammonia steam enters the next procedure after being cooled by an ammonia condenser, and the liquid returns to the ammonia still through a reflux pump. The wastewater at the bottom of the tower generally enters a biochemical treatment device for treatment. Wherein, ammonia steam heat at the top of the ammonia still is generally cooled by cooling water, which causes energy waste, huge energy loss and greatly reduces the energy utilization rate.
In summary, how to effectively improve the energy utilization rate is a problem that needs to be solved urgently by those skilled in the art.
SUMMERY OF THE UTILITY MODEL
In view of this, the utility model discloses a first aim at provides an ammonia still top of tower ammonia steam waste heat recovery system, this ammonia still top of tower ammonia steam waste heat recovery system's structural design can improve energy utilization effectively, the utility model discloses a second aim at provides a coking process systems including above-mentioned ammonia still top of tower ammonia steam waste heat recovery system.
In order to achieve the first object, the present invention provides the following technical solutions:
an ammonia still tower top ammonia vapor waste heat recovery system comprises an ammonia still and an ammonia cooler, wherein an ammonia vapor outlet is formed in the ammonia still, the ammonia still further comprises a lithium bromide absorption type unit, the ammonia vapor outlet is communicated with a generator of the lithium bromide absorption type unit, an ammonia discharge port is formed in the generator, ammonia vapor entering the generator is cooled in the generator and then discharged through the ammonia discharge port, and the lithium bromide absorption type unit can operate a refrigeration working condition or a heating working condition; and/or the presence of a gas in the gas,
the ammonia steam outlet is communicated with the heat exchanger, and the ammonia steam entering the heat exchanger exchanges heat in the heat exchanger to prepare hot water.
Preferably, the system for recovering the ammonia steam waste heat at the top of the ammonia still further comprises a gas-liquid separator, wherein the ammonia discharge port is communicated with an inlet of the gas-liquid separator, the ammonia steam entering the generator is cooled in the generator and then discharged into the gas-liquid separator through the ammonia discharge port, a liquid outlet of the gas-liquid separator is communicated with the ammonia still, and a gas outlet of the gas-liquid separator is communicated with an inlet of the ammonia cooler.
Preferably, in the system for recovering the ammonia vapor waste heat at the top of the ammonia still, a reflux pump is further arranged on a pipeline between the liquid outlet of the gas-liquid separator and the ammonia still.
Preferably, the ammonia still tower top ammonia vapor waste heat recovery system further comprises a dephlegmator, and the ammonia vapor outlet is communicated with the dephlegmator, the generator and the heat exchanger through pipelines.
Preferably, in the system for recovering the ammonia vapor waste heat at the top of the ammonia still, a valve is arranged between the ammonia vapor outlet and the dephlegmator.
Preferably, the system for recovering the ammonia vapor waste heat at the top of the ammonia still further comprises a steam reboiler, and ammonia water in the ammonia still enters the steam reboiler to be heated to form ammonia vapor and then returns to the ammonia still.
Preferably, the system for recovering the ammonia vapor waste heat at the tower top of the ammonia still further comprises a condensation pumping device, a water ring vacuum pump or an induced draft fan, wherein the condensation pumping device is communicated with the ammonia discharging port of the generator.
A coking process system comprises a coke oven carbonization chamber, a bridge pipe, a gas collecting pipe, a clarifying tank and a primary cooler, and further comprises an ammonia still tower top ammonia steam waste heat recovery system.
Preferably, in the coking process system, the ammonia vapor waste heat recovery system at the top of the ammonia still comprises a lithium bromide absorption unit, wherein the lithium bromide absorption unit is used for preparing cold water under a refrigeration working condition, and the prepared cold water is used for flowing into the primary cooler to be used for cooling the low-temperature section in the primary cooler process.
Preferably, in the coking process system, the ammonia vapor waste heat recovery system at the top of the ammonia still comprises a lithium bromide absorption unit, the lithium bromide absorption unit prepares hot water under a heating working condition, and the prepared hot water is used for heating, preheating of dry quenching deoxidized water and water replenishing of a waste heat boiler.
Preferably, the coking process system further comprises a condensation device, a water ring vacuum pump or an induced draft fan.
The utility model provides an ammonia still tower top of tower ammonia steam waste heat recovery system includes ammonia still, ammonia cooler and lithium bromide absorption formula unit, wherein is provided with ammonia steam outlet on the ammonia still, and ammonia steam outlet and the generator intercommunication of lithium bromide absorption formula unit on the ammonia still are provided with the ammonia exhaust mouth on the generator, and ammonia exhaust mouth and ammonia cooler intercommunication, lithium bromide absorption formula unit can move refrigeration operating mode and heat the operating mode. When the lithium bromide absorption type unit is in a refrigeration working condition, cold water can be prepared, and when the lithium bromide absorption type unit is in a heating working condition, hot water can be prepared.
The generator is provided with an ammonia inlet and an ammonia outlet, ammonia vapor enters the generator through the ammonia inlet, the ammonia vapor is used as a driving heat source to drive the lithium bromide absorption type unit to operate, and the lithium bromide absorption type unit can produce cold water under a refrigeration working condition and can also produce hot water under a heating working condition. Specifically, the lithium bromide absorption type unit can be selected to be in a refrigeration working condition or a heating working condition according to the region, the season or the actual requirement. For example, hot water is used more in winter in northern areas, heating working conditions can be selected in winter in northern areas, cold water is used more in summer in southern areas, and refrigerating working conditions can be selected in summer in southern areas. So, the ammonia steam waste heat of following ammonia still top of the tower exhaust of recycle has avoided the waste of the energy, has improved energy utilization greatly and has rateed, the cold and hot demand of fully provided customer simultaneously.
Preferably, the system for recovering the ammonia steam waste heat at the tower top of the ammonia still further comprises a gas-liquid separator, an ammonia discharge port on the generator is communicated with an inlet of the gas-liquid separator, and the ammonia steam entering the generator is cooled in the generator and then is discharged into the gas-liquid separator through the ammonia discharge port. The liquid outlet of the gas-liquid separator is communicated with the ammonia still, and the gas outlet of the gas-liquid separator is communicated with the inlet of the ammonia cooler.
In order to achieve the second purpose, the utility model also provides a coking process system, this coking process system includes above-mentioned any kind of ammonia still top of the tower ammonia steam waste heat recovery system. Because the ammonia still tower top ammonia vapor waste heat recovery system has the technical effects, the coking process system with the ammonia still tower top ammonia vapor waste heat recovery system also has corresponding technical effects.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a flow diagram of a prior art ammonia still process using residual ammonia water;
fig. 2 is a schematic view of a coking process system in a refrigeration condition according to an embodiment of the present invention;
FIG. 3 is a schematic view of the ammonia still tower top ammonia vapor waste heat recovery system provided by the embodiment of the present invention under a refrigeration condition;
fig. 4 is a schematic view of a coking process system provided by an embodiment of the present invention in a heating condition;
FIG. 5 is a schematic view of the ammonia still tower top ammonia vapor waste heat recovery system provided by the embodiment of the present invention in a heating condition;
fig. 6 is a schematic view of a coking process system in a heating condition according to another embodiment of the present invention;
fig. 7 is a schematic view of the ammonia still tower top ammonia vapor waste heat recovery system provided by another embodiment of the present invention in a heating condition.
In fig. 1:
01-steam reboiler, 02-ammonia still, 03-dephlegmator, 04-gas-liquid separator and 05-ammonia cooler;
in fig. 2-7:
1-coke oven carbonization chamber, 2-gas collecting pipe, 3-primary cooler, 4-clarifying tank, 5-residual ammonia water pump, 6-ammonia water heat exchanger, 7-waste water pump, 8-steam reboiler, 9-ammonia still, 10-reflux pump, 11-dephlegmator, 12-gas-liquid separator, 13-ammonia cooler, 14-lithium bromide absorption type machine set and 15-heat exchanger.
Detailed Description
The utility model discloses a first aim at provides an ammonia still top of tower ammonia steam waste heat recovery system, this ammonia still top of tower ammonia steam waste heat recovery system's structural design can improve energy utilization effectively, the utility model discloses a second aim at provides a coking process systems including above-mentioned ammonia still top of tower ammonia steam waste heat recovery system.
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
In the description of the present invention, it is to be understood that the terms "upper", "lower", "front", "rear", "left" and "right" and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplification of description, but do not indicate or imply that the indicated position or element must have a specific orientation, be constituted in a specific orientation, and be operated, and thus, are not to be construed as limitations of the present invention. Furthermore, the terms "first" and "second" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
Referring to fig. 2-5, an embodiment of the present invention provides an ammonia still tower top ammonia vapor waste heat recovery system, which includes an ammonia still 9, an ammonia cooler 13 and a lithium bromide absorption unit 14, wherein the ammonia still 9 is provided with an ammonia vapor outlet, the ammonia vapor outlet of the ammonia still 9 is communicated with a generator of the lithium bromide absorption unit 14, the generator is provided with an ammonia discharge port, and the ammonia discharge port is communicated with an inlet of the ammonia cooler, and ammonia vapor entering the generator is cooled in the generator and then discharged to the ammonia cooler through the ammonia discharge port. The lithium bromide absorption unit 14 can operate in a cooling mode and a heating mode. When the lithium bromide absorption type unit 14 is in a refrigeration working condition, cold water can be prepared, and when the lithium bromide absorption type unit 14 is in a heating working condition, hot water can be prepared.
The generator is provided with an ammonia inlet and an ammonia outlet, ammonia vapor enters the generator through the ammonia inlet, the ammonia vapor is used as a driving heat source to drive the lithium bromide absorption type unit 14 to operate, and the lithium bromide absorption type unit 14 can produce cold water under a refrigeration working condition or hot water under a heating working condition.
Specifically, the lithium bromide absorption unit 14 may be selected to be in a cooling condition or a heating condition according to the region, the season or the actual demand. For example, hot water is used more in winter in northern areas, heating working conditions can be selected in winter in northern areas, cold water is used more in summer in southern areas, and refrigerating working conditions can be selected in summer in southern areas. So, the recovery has utilized from the ammonia still 9 top of the tower exhaust ammonia steam waste heat, has avoided the waste of the energy, has improved energy utilization greatly, fully satisfies the cold and hot demand of customer simultaneously.
It should be noted here that the lithium bromide absorption unit includes an evaporator, an absorber, a condenser, and a generator. Of course, the lithium bromide absorption unit may also include heat exchangers, pumps and other accessories.
When the operation is in a refrigeration working condition, ammonia vapor discharged from the top of the ammonia still 9 enters the generator to be used as a driving heat source, and the lithium bromide dilute solution is heated in the generator to generate refrigerant vapor. The refrigerant steam enters the condenser, is cooled by cooling water in the condenser, is condensed into liquid and then enters the evaporator in a throttling mode. The refrigerant is evaporated in the evaporator to produce cold water. The evaporated refrigerant is absorbed by the concentrated solution in the absorber. The solution (dilute solution) diluted by absorbing the refrigerant is sent to the generator by the solution pump through the heat exchanger. The concentrated solution enters an absorber after being subjected to heat exchange with the dilute solution through a heat exchanger, and absorbs refrigerant steam generated by evaporation in an evaporator. The whole cycle is completed.
When the heating working condition is operated, ammonia vapor discharged from the top of the ammonia still 9 enters the generator to be used as a driving heat source, and the lithium bromide dilute solution is heated in the generator to generate refrigerant vapor. The refrigerant steam enters the condenser, heats the hot water flowing through the heat transfer pipe of the condenser, condenses into liquid and enters the evaporator in a throttling mode. The refrigerant water absorbs the heat of the residual heat water flowing through the heat transfer pipe of the evaporator, the residual heat water flows out of the unit after the temperature of the residual heat water is reduced, and the refrigerant water is vaporized into refrigerant steam after absorbing the heat and enters the absorber. The lithium bromide solution concentrated by the generator returns to the absorber and then is sprayed to absorb the refrigerant steam from the evaporator and release heat to heat the hot water flowing through the heat transfer pipe of the absorber. After the hot water is heated by the absorber and the condenser, the hot water is conveyed to the heat using unit to complete the whole circulation.
In another embodiment, the ammonia still tower top ammonia vapor waste heat recovery system comprises an ammonia still 9, an ammonia cooler 13, a lithium bromide absorption unit 14 and a heat exchanger 15, wherein an ammonia vapor outlet is communicated with both the heat exchanger 15 and a generator, and when ammonia vapor enters the heat exchanger 15, the ammonia vapor entering the heat exchanger 15 exchanges heat in the heat exchanger 15 to prepare hot water. Namely, the ammonia vapor enters the heat exchanger 15 and then exchanges heat with water, so as to achieve the purpose of preparing hot water. Therefore, the waste heat of the ammonia steam discharged from the top of the ammonia still 9 is recycled, the waste of energy is avoided, and the energy utilization rate is greatly improved. When ammonia vapor enters the generator, it is the same as in the first embodiment described above and will not be described again.
As shown in FIG. 4, in another embodiment of the present invention, the ammonia still tower top ammonia vapor waste heat recovery system includes an ammonia still 9, an ammonia cooler 13 and a heat exchanger 15, the ammonia vapor outlet is communicated with the heat exchanger 15, and the ammonia vapor entering the heat exchanger 15 exchanges heat in the heat exchanger 15 to produce hot water. Namely, the ammonia vapor enters the heat exchanger 15 and then exchanges heat with water, so as to achieve the purpose of preparing hot water. Therefore, the waste heat of the ammonia steam discharged from the top of the ammonia still 9 is recycled, the waste of energy is avoided, and the energy utilization rate is greatly improved.
Preferably, the system for recovering the ammonia steam waste heat at the tower top of the ammonia still further comprises a gas-liquid separator 12, an ammonia discharge port on the generator is communicated with an inlet of the gas-liquid separator 12, and the ammonia steam entering the generator is cooled in the generator and then discharged into the gas-liquid separator 12 through the ammonia discharge port. The liquid outlet of the gas-liquid separator 12 is communicated with the ammonia still 9, and the gas outlet of the gas-liquid separator 12 is communicated with the inlet of the ammonia cooler 13, but the gas-liquid separator 12 is not necessarily provided, and is not limited herein.
In the above embodiment, the ammonia vapor waste heat recovery system at the top of the ammonia still further includes a dephlegmator 11, and the ammonia vapor outlet is communicated with the dephlegmator 11, the generator and the heat exchanger. The outlet of the condenser 11 communicates with the inlet of the gas-liquid separator 12. Thus, the ammonia vapor can be selectively introduced into the dephlegmator 11, the generator or the heat exchanger 15, and when cold water or warm water is required to be produced, the ammonia vapor can be selectively introduced into the generator. When high temperature hot water is required, ammonia vapor may optionally be introduced into heat exchanger 15. Or when the lithium bromide absorption type unit 14 has a fault, the ammonia vapor can enter the dephlegmator 11, and the ammonia vapor exchanges heat with cooling water in the dephlegmator 11 and then flows into the gas-liquid separator 12.
Further, for the convenience of control, a valve is provided between the ammonia vapor outlet and the dephlegmator 11, and the valve is closed when the lithium bromide absorption unit 14 or the heat exchanger 15 is operating normally. The valve is opened when the lithium bromide absorption unit 14 fails or does not need to refrigerate or heat.
Preferably, the ammonia still tower top ammonia vapor waste heat recovery system further comprises a vapor reboiler 8, and the ammonia water in the ammonia still 9 enters the vapor reboiler 8 to be heated to form ammonia vapor and then returns to the ammonia still 9. The ammonia water in the ammonia still 9 is heated by the steam reboiler 8 to generate more ammonia steam.
In order to smoothly return the ammonia water in the gas-liquid separator 12 to the ammonia still 9, a return pump 10 may be provided in a pipe between the liquid outlet of the gas-liquid separator 12 and the ammonia still 9.
When the ammonia vapor is negative pressure ammonia vapor or the micro-positive pressure ammonia vapor does not flow sufficiently, the lithium bromide absorption type unit can also add a condensation device or a water ring vacuum pump or an induced draft fan at the outlet of the generator to ensure the heat exchange effect of the generator. Since ammonia vapor itself is corrosive, corresponding measures for corrosion protection are also to be taken into account.
The working process of the ammonia still 9, the gas-liquid separator 12 and the ammonia cooler 13 is that the ammonia steam generated after the residual ammonia water enters the ammonia still 9 is cooled in the generator or the heat exchanger 15 and then enters the gas-liquid separator 12 for gas-liquid separation, and then the ammonia steam enters the next process after being cooled by the ammonia condenser. The liquid is refluxed to the ammonia still 9. The wastewater at the bottom of the tower is pumped out by a wastewater pump 7 and then enters a biochemical treatment device for treatment. In the above, the residual ammonia water is refluxed to the ammonia still 9 by the residual ammonia water pump 5.
In addition, the residual ammonia water exchanges heat with the wastewater flowing out of the ammonia still 9 in the ammonia water heat exchanger 6 before entering the ammonia still 9, so as to further improve the capacity utilization rate.
Based on ammonia still tower top ammonia steam waste heat recovery system that provides in the above-mentioned embodiment, the utility model also provides a coking process system, this coking process system include coke oven carbonization chamber 1, bridge pipe, gas collecting pipe 2, clarification tank 4, primary cooler 3 and above-mentioned embodiment arbitrary ammonia still tower top ammonia steam waste heat recovery system. Because the coking process system adopts the ammonia still tower top ammonia vapor waste heat recovery system in the embodiment, please refer to the embodiment for the beneficial effect of the coking process system.
In order to further improve the energy utilization rate, the ammonia vapor waste heat recovery system at the top of the ammonia still comprises a lithium bromide absorption type unit 14, cold water is prepared when the lithium bromide absorption type unit 14 is in a refrigeration working condition, and the prepared cold water can be used for flowing into the primary cooler 3 to be used for cooling the low-temperature section in the process of the primary cooler 3.
The ammonia still tower top ammonia steam waste heat recovery system comprises a lithium bromide absorption type unit 14, when the lithium bromide absorption type unit 14 is in a heating working condition, hot water is prepared, and the prepared hot water can be used for heating, dry quenching deaerated water preheating and waste heat boiler water replenishing. Of course, the hot water produced may also be used as process hot water, and is not limited herein.
In addition, the residual heat water can adopt large system process cooling water, for example, the cooling water of the primary cooler 3 enters the evaporator of the lithium bromide absorption type unit 14, and the absorber and the condenser of the lithium bromide absorption type unit 14 prepare hot water, so that the device has two functions.
It should be noted here that the cold water and the hot water produced by the lithium bromide absorption unit 14 can be used for any purpose, and are not limited to the above-described purpose.
The embodiments in the present description are described in a progressive manner, each embodiment focuses on differences from other embodiments, and the same and similar parts among the embodiments are referred to each other.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (10)
1. The ammonia still tower top ammonia steam waste heat recovery system comprises an ammonia still (9) and an ammonia cooler (13), wherein an ammonia steam outlet is formed in the ammonia still (9), and the system is characterized by further comprising a lithium bromide absorption type unit (14), the ammonia steam outlet is communicated with a generator of the lithium bromide absorption type unit (14), an ammonia discharge port is formed in the generator, ammonia steam entering the generator is cooled in the generator and then is discharged through the ammonia discharge port, and the lithium bromide absorption type unit (14) can operate in a refrigeration working condition or a heating working condition; and/or the presence of a gas in the gas,
the ammonia water heater further comprises a heat exchanger (15), the ammonia steam outlet is communicated with the heat exchanger (15), and ammonia steam entering the heat exchanger (15) exchanges heat in the heat exchanger (15) to prepare hot water.
2. The system for recovering the waste heat of the ammonia steam at the tower top of the ammonia still as claimed in claim 1, further comprising a gas-liquid separator (12), wherein the ammonia discharge port is communicated with an inlet of the gas-liquid separator (12), the ammonia steam entering the generator is cooled in the generator and then is discharged into the gas-liquid separator (12) through the ammonia discharge port, a liquid outlet of the gas-liquid separator (12) is communicated with the ammonia still (9), and a gas outlet of the gas-liquid separator (12) is communicated with an inlet of the ammonia cooler (13).
3. The ammonia still tower top ammonia vapor waste heat recovery system according to claim 2, characterized in that a reflux pump (10) is further arranged on a pipeline between the liquid outlet of the gas-liquid separator (12) and the ammonia still tower (9).
4. The system for recovering the waste heat of the ammonia steam at the tower top of the ammonia still as claimed in claim 1, further comprising a dephlegmator (11), wherein the ammonia steam outlet is communicated with the dephlegmator (11), the generator and the heat exchanger (15) through pipelines.
5. The system for recovering the waste heat of the ammonia steam at the tower top of the ammonia still as claimed in claim 4, wherein a valve is arranged between the ammonia steam outlet and the dephlegmator (11).
6. The system for recovering the waste heat of the ammonia distillation tower top ammonia steam as defined in claim 1, further comprising a steam reboiler (8), wherein the ammonia water in the ammonia distillation tower (9) enters the steam reboiler (8) to be heated to form ammonia steam, and then returns to the ammonia distillation tower (9).
7. The system for recovering the ammonia vapor waste heat at the tower top of the ammonia still as claimed in claim 1, further comprising a condensation device, a water ring vacuum pump or an induced draft fan which is communicated with the ammonia discharge port of the generator.
8. A coking process system, comprising a coke oven carbonization chamber (1), a bridge pipe, a gas collecting pipe (2), a clarifying tank (4) and a primary cooler (3), and further comprising the ammonia still tower top ammonia steam waste heat recovery system according to any one of claims 1 to 7.
9. The coking process system according to claim 8, wherein the ammonia still tower overhead ammonia vapor waste heat recovery system comprises a lithium bromide absorption unit (14), the lithium bromide absorption unit (14) is used for preparing cold water when in a refrigeration condition, and the prepared cold water is used for flowing into the primary cooler (3) for cooling a low temperature section in the primary cooler (3) process.
10. The coking process system of claim 8, wherein the ammonia still tower top ammonia vapor waste heat recovery system comprises a lithium bromide absorption unit (14), the lithium bromide absorption unit (14) produces hot water when in a heating working condition, and the produced hot water is used for heating, dry quenching deoxidization water preheating and waste heat boiler water replenishing.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921470663.4U CN210922310U (en) | 2019-09-05 | 2019-09-05 | Ammonia still tower top ammonia steam waste heat recovery system and coking process system |
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|---|---|---|---|
| CN201921470663.4U CN210922310U (en) | 2019-09-05 | 2019-09-05 | Ammonia still tower top ammonia steam waste heat recovery system and coking process system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110440626A (en) * | 2019-09-05 | 2019-11-12 | 荏原冷热系统（中国）有限公司 | Ammonia steam waste heat recovery system and coking process system at the top of the ammonia distillation tower |
| CN112939129A (en) * | 2021-02-02 | 2021-06-11 | 韶关凯鸿纳米材料有限公司 | Waste heat recovery device and use method |
-
2019
- 2019-09-05 CN CN201921470663.4U patent/CN210922310U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110440626A (en) * | 2019-09-05 | 2019-11-12 | 荏原冷热系统（中国）有限公司 | Ammonia steam waste heat recovery system and coking process system at the top of the ammonia distillation tower |
| CN112939129A (en) * | 2021-02-02 | 2021-06-11 | 韶关凯鸿纳米材料有限公司 | Waste heat recovery device and use method |
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