CN220939159U - Ammonia water recovery system - Google Patents
Ammonia water recovery system Download PDFInfo
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- CN220939159U CN220939159U CN202322302977.6U CN202322302977U CN220939159U CN 220939159 U CN220939159 U CN 220939159U CN 202322302977 U CN202322302977 U CN 202322302977U CN 220939159 U CN220939159 U CN 220939159U
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- 235000011114 ammonium hydroxide Nutrition 0.000 title claims abstract description 120
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 title claims abstract description 113
- 238000011084 recovery Methods 0.000 title claims abstract description 27
- 238000010521 absorption reaction Methods 0.000 claims abstract description 85
- 239000000463 material Substances 0.000 claims abstract description 39
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 37
- 239000007788 liquid Substances 0.000 claims abstract description 21
- 239000012535 impurity Substances 0.000 claims abstract description 20
- 239000010815 organic waste Substances 0.000 claims abstract description 20
- 239000002912 waste gas Substances 0.000 claims abstract description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 144
- 239000002994 raw material Substances 0.000 claims description 20
- 239000002699 waste material Substances 0.000 claims description 15
- 229910021529 ammonia Inorganic materials 0.000 claims description 12
- 238000004821 distillation Methods 0.000 claims description 9
- 238000000034 method Methods 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 5
- 238000004064 recycling Methods 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 25
- 238000007710 freezing Methods 0.000 description 12
- 230000008014 freezing Effects 0.000 description 12
- 239000012153 distilled water Substances 0.000 description 5
- 239000007791 liquid phase Substances 0.000 description 5
- 239000012071 phase Substances 0.000 description 5
- 239000002351 wastewater Substances 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000011144 upstream manufacturing Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- 230000003139 buffering effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000009615 deamination Effects 0.000 description 1
- 238000006481 deamination reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 238000004381 surface treatment Methods 0.000 description 1
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- Sorption Type Refrigeration Machines (AREA)
Abstract
The utility model discloses an ammonia water recovery system, in particular to the technical field of ammonia water recovery, and the technical scheme is characterized by comprising a rectifying device, a condensing device and a multistage absorption device which are sequentially connected through pipelines; the rectification device is used for separating organic waste and impurities in the ammonia water and converting liquid ammonia water into ammonia water steam; the condensing device is used for condensing the ammonia water vapor into liquid and separating organic waste materials and impurities in the liquid again; the multistage absorption device is used for recovering ammonia water, purifying residual waste gas and separating organic waste materials and impurities in the ammonia water. The utility model improves the problems of low treatment efficiency and high energy consumption in the ammonia water recovery device, can efficiently treat the ammonia water, improves the recovery rate of the ammonia water, recovers valuable ammonia water resources, effectively purifies waste gas and can meet the requirements of actual production.
Description
Technical Field
The utility model belongs to the technical field of ammonia water recovery, and particularly relates to an ammonia water recovery system.
Background
Ammonia is an important industrial chemical and is widely applied to the fields of fertilizer production, pharmacy, metal surface treatment and the like. However, a large amount of waste water and waste gas are generated in the production and use processes of the ammonia water, and organic waste materials and impurities are contained in the waste water, and the direct discharge of the waste ammonia water not only causes pollution to the environment, but also causes great threat to human health, so that the waste ammonia water is of great significance in effective treatment.
Currently existing ammonia water treatment technologies such as absorption method, evaporation method, membrane separation method and the like. However, the recycling of ammonia water in these modes has low treatment efficiency, high energy consumption and low purity of the obtained ammonia water, and is difficult to meet the requirements of actual production.
Disclosure of utility model
In order to improve the recovery treatment efficiency of ammonia water, the application provides an ammonia water recovery system which can effectively improve the recovery efficiency of ammonia water and reduce the emission of waste gas.
The application provides an ammonia water recovery system which adopts the following technical scheme:
An ammonia water recovery system comprises a rectifying device, a condensing device and a multistage absorption device which are sequentially connected through pipelines;
The rectification device is used for separating organic waste and impurities in the ammonia water and converting the liquid ammonia water into ammonia water steam;
The condensing device is used for condensing the ammonia water vapor into liquid and separating organic waste materials and impurities in the liquid again;
The multistage absorption device is used for recovering ammonia water, purifying residual waste gas and separating organic waste materials and impurities in the ammonia water.
By adopting the technical scheme, the rectification device is used for separating organic waste and impurities in the ammonia water and converting the liquid ammonia water into ammonia water steam; the condensing device is used for condensing the ammonia water vapor into liquid and separating organic waste materials and impurities in the liquid again; the multistage absorption device is used for recovering ammonia water, purifying residual waste gas and separating organic waste materials and impurities in the ammonia water. Through the combination of key steps such as rectifying device, condensing equipment and multistage alternating temperature absorbing device, can separate organic waste material and impurity in the aqueous ammonia effectively to with aqueous ammonia steam rapid condensation liquid, guaranteed the quality of retrieving aqueous ammonia can high-efficient processing aqueous ammonia waste material, improve the aqueous ammonia rate of recovery.
In a specific embodiment, the rectification device comprises a rectification column, the rectification column is connected with a raw material pump through a pipeline, a discharge pump is arranged at the bottom of the rectification column, and the rectification column is connected with a heater through a pipeline.
By adopting the technical scheme, the waste liquid is heated by the steam in the rectifying tower, the gas-phase material mainly comprising ammonia gradually rises and is enriched in the rectifying tower, and the waste leaves the rectifying tower from the bottom and is discharged from the rectifying tower by the discharge pump.
In a specific embodiment, the rectification apparatus further comprises a first heat exchanger and a second heat exchanger for heat exchanging the waste material discharged from the rectification column and the raw material to be treated entering the rectification column, the raw material pump being connected to the first heat exchanger, the first heat exchanger being connected to the second heat exchanger, the second heat exchanger being connected to the rectification column, the discharge pump being connected to the first heat exchanger.
Through adopting foretell technical scheme, make from the waste material of discharge in the rectifying column and the raw materials that want to get into waiting to handle in the rectifying column carry out the heat exchange, make the waste material that will discharge the rectifying column cool down, the raw materials that want to get into the rectifying column carries out preliminary preheating simultaneously, be favorable to improving the utilization efficiency of energy.
In a specific implementation, the condensing device comprises a mixer, the mixer is connected with a process distillation water tank through a pipeline, the mixer is sequentially connected with a first-stage condenser, a second-stage condenser, a recooler and a buffer tank I, the buffer tank I is connected with a first discharging pump and a first ammonia water pump, and the condensing device further comprises a circulating water device for assisting the first-stage condenser and the second-stage condenser in cooling and a low-temperature water device for assisting the liquid-phase material in continuously cooling.
By adopting the technical scheme, the materials coming out of the top of the tower react with distilled water in the process distilled water tank in the mixer, so that high-concentration pure ammonia water can be obtained, and the pure ammonia water can be used as an upstream process of an ammonia water product. The circulating water flows through the primary condenser and the secondary condenser to cool the materials passing through the primary condenser and the secondary condenser, and then flows through the recooler through the low-temperature water to further cool the materials, so that the materials are condensed; the condensed liquid phase material enters a buffer tank for further treatment, and qualified ammonia water is recovered by a first ammonia water pump.
In a specific embodiment, the circulating water device comprises a circulating water feed pump, a circulating water return pump and a circulating water tank, wherein the circulating water feed pump is communicated with the circulating water tank, the circulating water feed pump is communicated with the secondary condenser through a water pipe, the secondary condenser is communicated with the primary condenser through a water pipe, the primary condenser is communicated with the circulating water return pump through a water pipe, and the circulating water return pump is communicated with the circulating water tank.
By adopting the technical scheme, circulating water flows through the primary condenser and the secondary condenser, so that the material in the primary condenser and the secondary condenser is facilitated to be cooled.
In a specific embodiment, the low temperature water device comprises a chilled water supply pump, a chilled water return pump, and a chilled water tank, wherein the chilled water supply pump and the chilled water return pump are both connected to the sub-cooler via a pipeline, the chilled water supply pump and the chilled water return pump are both connected to the buffer tank I via a pipeline, the chilled water supply pump is connected to the chilled water tank, and the chilled water return pump is connected to the chilled water tank.
By adopting the technical scheme, the low-temperature water flows through the recooler, so that the auxiliary liquid-phase material is continuously cooled, and the material in the auxiliary buffer tank I is effectively cooled through the low-temperature water flowing through the buffer tank I.
In a specific embodiment, the multistage absorption device comprises a primary balance tank, wherein the primary balance tank is communicated with a primary absorption tank through a pipeline, and the primary absorption tank is connected with the buffer tank I; the first-stage absorption tank is connected with a second-stage balance tank, the second-stage balance tank is connected with a second-stage absorption tank, the second-stage absorption tank is connected with a first-stage absorption tank, the first-stage absorption tank is connected with a second buffer tank, and the second buffer tank is connected with a second discharging pump and a second ammonia pump.
By adopting the technical scheme, the liquefied gas enters the first-stage absorption tank through the first-stage balance tank, most of tail gas is absorbed by water in the absorption tank, a small amount of unabsorbed tail gas enters the second-stage absorption tank through the second-stage balance tank, and after the tail gas passes through the multi-stage absorption device, ammonia in the tail gas is absorbed to obtain an ammonia water product meeting the standard, and the ammonia water product is recovered through the first ammonia water pump.
In a specific embodiment, the primary absorption tank and the secondary absorption tank are provided with temperature sensors.
By adopting the technical scheme, the gas in different liquefaction temperature ranges can be separated by arranging the temperature sensor.
In a specific implementation manner, the frozen water supply pump is communicated with the secondary absorption tank through a water pipe, the secondary absorption tank is communicated with the primary absorption tank through a water pipe, the primary absorption tank is communicated with the buffer tank II through a water pipe, and the buffer tank II is communicated with the frozen water return pump through a water pipe.
By adopting the technical scheme, the auxiliary primary absorption tank and the auxiliary secondary absorption tank are beneficial to effectively cooling materials in the primary absorption tank and the auxiliary secondary absorption tank.
In summary, the present application includes at least one of the following beneficial technical effects:
1. The rectification device is used for separating organic waste and impurities in the ammonia water and converting the liquid ammonia water into ammonia water steam; the condensing device is used for condensing the ammonia water vapor into liquid and separating organic waste materials and impurities in the liquid again; the multistage absorption device is used for recovering ammonia water, purifying residual waste gas and separating organic waste materials and impurities in the ammonia water. The ammonia water raw material liquid is organically combined through the key steps of a rectifying device, a condensing device, a multistage absorption device and the like, so that organic waste and impurities of the ammonia water raw material liquid can be effectively separated, ammonia water vapor is rapidly condensed into liquid, the quality of recovered ammonia water is ensured, the ammonia water waste can be efficiently treated, and the recovery rate of ammonia water is improved.
2. After the ammonia water raw material liquid passes through the rectifying device and the condensing device, a small amount of non-condensable gas passes through the multistage absorption device, a small amount of non-condensable gas firstly enters the first-stage absorption tank through the first-stage balance tank, most of tail gas is absorbed by water in the absorption tank, a small amount of unabsorbed tail gas enters the second-stage absorption tank through the second-stage balance tank, after the tail gas passes through the multistage absorption device, ammonia in the tail gas is absorbed to obtain an ammonia water product meeting the standard, and the ammonia water product is recovered through the second ammonia water pump, so that the recovery rate of the ammonia water is improved.
Drawings
FIG. 1 is a schematic diagram of an ammonia recovery system according to an embodiment of the present application.
Fig. 2 is a schematic diagram of a rectifying apparatus according to an embodiment of the present application.
Fig. 3 is a schematic diagram of a condensing unit and a multistage absorption unit according to an embodiment of the present application.
Reference numerals illustrate: 1. a rectifying device; 2. a condensing device; 3. a multistage absorption device; 11. a heater; 111. a steam buffer tank; 12. a rectifying tower; 13. a raw material tank; 131. a raw material pump; 14. a discharge pump; 15. a first heat exchanger; 16. a second heat exchanger; 21. a mixer; 22. a process distillation water tank; 221. a distillation water valve; 23. a first-stage condenser; 24. a second-stage condenser; 25. a recooler; 26. buffer tank I; 261. a first bottom valve; 27. a first discharge pump; 28. an ammonia water storage tank I; 281. a first ammonia water pump; 291. a circulating water feed pump; 292. a circulating water return pump; 29. a circulation water tank; 30. a freezing water tank; 301. a chilled water supply pump; 302. freezing a water return pump; 31. a primary balance groove; 32. a primary absorption tank; 33. a first temperature sensor; 333. a second temperature sensor; 34. a secondary balance groove; 35. a secondary absorption tank; 36. buffer tank II; 361. a second bottom valve; 362. a blow-off valve; 37. a second discharge pump; 38. ammonia water storage tank II; 381. and a second ammonia pump.
Detailed Description
The application is described in further detail below with reference to fig. 1-3.
The embodiment of the application discloses an ammonia water recovery system.
Referring to fig. 1 and 2, an ammonia water recovery system includes a rectifying device 1, a condensing device 2 and a multistage absorption device 3 connected in sequence through a pipeline; the rectifying device 1 comprises a raw material tank 13, a raw material pump 131 and a rectifying tower 12 which are sequentially connected through pipelines, a discharging pump 14 is connected to the bottom of the rectifying tower 12, the rectifying device 1 further comprises a heater 11, the heater 11 is connected with a steam buffer tank 111, and the steam buffer tank 111 is communicated with the rectifying tower 12 through pipelines. The raw material pump 131 sends the waste liquid to be treated in the raw material tank 13 into the rectifying tower 12, the steam generated by the heater 11 is sent into the rectifying tower 12 through the steam buffer tank 111 to treat the waste liquid, in the rectifying tower 2, the gas phase materials mainly containing ammonia gradually rise and are enriched in the tower, the gas phase materials flow out from the tower top to the condensing device 2, and the organic waste material generated after the waste liquid treatment is discharged out of the rectifying device 1 through the discharge pump 14.
In order to be effective and energy-saving, the raw material pump 131 and the rectifying tower 12 are sequentially communicated with the first heat exchanger 15 and the second heat exchanger 16 through pipelines, the discharge pump 14 is communicated with the first heat exchanger 15 through pipelines, and waste water after deamination and waste liquid to be treated entering the rectifying tower 12 are subjected to heat exchange in the first heat exchanger 15 and the second heat exchanger 16, so that the waste material to be discharged out of the rectifying tower 12 is cooled, and meanwhile, raw materials to enter the rectifying tower 12 are subjected to preliminary preheating, thereby being beneficial to improving the energy utilization efficiency.
Referring to fig. 1 and 3, the material coming out of the top of the rectifying tower 12 enters a condensing device 2, the condensing device 2 comprises a mixer 21 communicated with the rectifying tower 12, the mixer 21 is connected with a distillation water valve 221 through a pipeline, the distillation water valve 221 is communicated with a process distillation water tank 22, the mixer 21 is sequentially connected with a primary condenser 23, a secondary condenser 24, a recooler 25 and a buffer tank one 26, the buffer tank one 26 is connected with a bottom valve one 261, the bottom valve one 261 is connected with a first discharge pump 27 and a first ammonia water pump 281, and the first ammonia water pump 281 is communicated with an ammonia water storage tank one 28. The materials firstly enter the mixer 21, the process distilled water enters the mixer 21 through the distilled water valve 221, part of ammonia in the materials can react with the process distilled water quickly to generate ammonia water products, ammonia water and gaseous ammonia in the mixer 21 are condensed gradually through the primary condenser 23, the secondary condenser 24 and the recooler 25, then liquid ammonia water enters the buffer tank I26, the liquid ammonia water is separated and buffered in the buffer tank I26, the materials in the buffer tank I26 flow out from the bottom valve I261 in a partitioning way, organic impurities are discharged through the first discharge pump 27, and the ammonia water is enriched and recycled into the ammonia water storage tank I28 through the first ammonia water pump 281. Therefore, high-concentration pure ammonia water which is more than or equal to 20% (wt) can be obtained, and the pure ammonia water can be used as an upstream process of an ammonia water product.
The condensing device 2 further comprises a circulating water device, the circulating water device comprises a circulating water tank 29, the circulating water tank 29 is communicated with a circulating water feed pump 291 and a circulating water return pump 292, the circulating water feed pump 291 is communicated with the secondary condenser 24 through a water pipe, the secondary condenser 24 sends circulating water to the primary condenser 23 through the water pipe, and the primary condenser 23 is communicated with the circulating water return pump 292 through the water pipe. The water in the circulating water tank 29 is sent to the primary condenser 23 and the secondary condenser 24 through the circulating water feed pump 291, so as to help the materials in the primary condenser 23 and the secondary condenser 24 to be cooled, and the circulating water pump 292 is used for sending the water used at the primary condenser 23 and the secondary condenser 24 to the circulating water tank 29.
The condensing unit 2 further comprises a low-temperature water device, the low-temperature water device comprises a freezing water tank 30, the freezing water tank 30 is communicated with a freezing water supply pump 301 and a freezing water return pump 302, the freezing water supply pump 301 and the freezing water return pump 302 are connected to the recooler 25 through pipelines, the freezing water supply pump 301 sends water in the freezing water tank 30 to the recooler 25 so as to assist the liquid-phase materials in the recooler 25 to continue cooling, and the freezing water return pump 302 sends water used at the recooler 25 to the freezing water tank 30. The frozen water supply pump 301 and the frozen water return pump 302 are connected to the first buffer tank 26 through pipelines, the frozen water supply pump 301 sends water in the frozen water tank 30 to the first buffer tank 26 to assist in cooling and separating materials in the first buffer tank 26, and the frozen water return pump 302 sends water used at the first buffer tank 26 to the frozen water tank 30.
Referring to fig. 1 and 3, the multistage absorption device 3 includes a primary balance tank 31 which is simultaneously communicated with a recooler 25 and a buffer tank one 26, the primary balance tank 31 is communicated with a primary absorption tank 32 through a pipeline, and a temperature sensor one 33 is provided on the primary absorption tank 32 to facilitate a worker to adjust a temperature parameter of the primary absorption tank 32 through a measured temperature. The first-stage absorption tank 32 is connected with a second buffer tank 36, the second buffer tank 36 is connected with a second discharge pump 37 and a second ammonia water pump 381, the second ammonia water pump 381 is communicated with a second ammonia water storage tank 38, and the top end of the second buffer tank 36 is provided with a vent valve 362. Non-liquefied non-condensable gas firstly enters the first-stage balance tank 31 and then enters the first-stage absorption tank 32, most of the gas is absorbed by water in the first-stage absorption tank 32, the water absorbed with the gas enters the buffer tank II 36 for buffering, ammonia water in the buffer tank II 36 is sent into the ammonia water storage tank II 38 through the second ammonia water pump 381, organic waste materials are discharged through the second discharge pump 37, and a small amount of non-absorbed tail gas in the buffer tank II 36 is discharged at high altitude through the vent valve 362.
The primary absorption tank 32 is connected with the secondary balance tank 34, the secondary balance tank 34 is connected with the secondary absorption tank 35, the secondary absorption tank 35 is connected with the primary absorption tank 32, a small amount of unabsorbed tail gas enters the secondary absorption tank 35 for further treatment through the secondary balance tank 34, and the secondary absorption tank 35 is provided with a second temperature sensor 333 so as to facilitate the adjustment of the temperature parameter of the secondary absorption tank 35 by the staff through the measured temperature. The tail gas is further treated by the multistage absorption device 3, so that the absorption effect of the ammonia water is ensured.
In addition, the frozen water supply pump 301 is connected to the secondary absorption tank 35 through a water pipe, the secondary absorption tank 35 sends frozen water to the primary absorption tank 32 through a water pipe, the primary absorption tank 32 sends the frozen water to the secondary buffer tank 36 through a water pipe, the secondary buffer tank 36 is connected to the frozen water return pump 302 through a water pipe, the primary absorption tank 32 and the secondary absorption tank 35 are cooled by the frozen water, so that the absorption of non-condensable gas by the primary absorption tank 32 and the secondary absorption tank 35 is accelerated, the secondary buffer tank 36 is cooled by the frozen water, and qualified ammonia water and organic impurities are separated more fully.
The implementation principle of the embodiment is as follows: the raw material liquid is heated by steam in the rectifying tower 12, gas-phase materials mainly containing ammonia gradually rise and are enriched in the rectifying tower 12, and after the materials coming out of the top of the rectifying tower 12 are condensed by the condensing device 2, high-concentration pure ammonia water can be obtained, and the pure ammonia water can be used as an upstream process of an ammonia water product. The wastewater leaves the rectifying column 12 from the bottom and is discharged from the rectifying column 12 by a discharge pump 14.
Ammonia gas phase materials coming out of the top of the rectifying tower 12 firstly enter a first-stage condenser 23 and a second-stage condenser 24, and ammonia water is condensed; the condensed liquid phase material enters the recooler 25 again to be cooled, and the cooled qualified ammonia water directly enters the buffer tank I26.
The uncondensed tail gas discharged from the condensing device 2 enters the multi-stage absorption device 3 and firstly enters the first-stage absorption tank 32, most of the tail gas is absorbed by water in the first-stage absorption tank 32, a small amount of the uncondensed tail gas enters the second-stage absorption tank 35 through the second-stage balance tank 34, and pure ammonia water product is obtained after the tail gas passes through the multi-stage absorption device 3, so that ammonia water can be efficiently treated, valuable ammonia water resources can be recovered, and waste gas can be effectively purified.
The above embodiments are not intended to limit the scope of the present application, so: all equivalent changes in structure, shape and principle of the application should be covered in the scope of protection of the application.
Claims (8)
1. An ammonia water recovery system is characterized by comprising a rectifying device (1), a condensing device (2) and a multistage absorption device (3) which are sequentially connected through pipelines;
the rectification device (1) is used for separating organic waste materials and impurities in the ammonia water and converting liquid ammonia water into ammonia water steam;
The condensing device (2) is used for condensing ammonia water vapor into liquid and separating organic waste materials and impurities in the liquid again; the condensing device (2) comprises a mixer (21) for receiving ammonia water steam, the mixer (21) is connected with a distillation water valve (221) through a pipeline, the distillation water valve (221) is communicated with a process distillation water tank (22), the mixer (21) is sequentially connected with a primary condenser (23), a secondary condenser (24), a recooler (25) and a buffer tank I (26), the buffer tank I (26) is connected with a first discharging pump (27) and a first ammonia water pump (281), and the condensing device further comprises a circulating water device for assisting the primary condenser (23) and the secondary condenser (24) in cooling and a low-temperature water device for assisting the recooler (25) in continuously cooling;
The multistage absorption device (3) is used for recycling ammonia water, purifying residual waste gas and separating organic waste materials and impurities in the ammonia water.
2. The ammonia water recovery system according to claim 1, wherein the rectifying device (1) comprises a rectifying tower (12), the rectifying tower (12) is connected with a raw material pump (131) through a pipeline, a discharging pump (14) is arranged at the bottom of the rectifying tower (12), and the rectifying tower (12) is connected with a heater (11) through a pipeline.
3. An ammonia recovery system according to claim 2, characterized in that the rectifying means (1) further comprises a first heat exchanger (15) and a second heat exchanger (16) for heat exchanging the waste material discharged from the rectifying column (12) and the raw material to be treated in the rectifying column (12), the raw material pump (131) being connected to the first heat exchanger (15), the first heat exchanger (15) being connected to the second heat exchanger (16), the second heat exchanger (16) being connected to the rectifying column (12), the discharge pump (14) being connected to the first heat exchanger (15).
4. The ammonia water recovery system according to claim 1, wherein the circulating water device comprises a circulating water feed pump (291), a circulating water return pump (292) and a circulating water tank (29), the circulating water feed pump (291) is communicated with the secondary condenser (24) through a water pipe, the secondary condenser (24) is communicated with the primary condenser (23) through a water pipe, the primary condenser (23) is communicated with the circulating water return pump (292) through a water pipe, and the circulating water return pump (292) is communicated with the circulating water tank (29).
5. The ammonia water recovery system according to claim 1, wherein the low-temperature water device comprises a chilled water supply pump (301), a chilled water return pump (302) and a chilled water tank (30), wherein the chilled water supply pump (301) and the chilled water return pump (302) are both connected to the recooler (25) through pipelines, wherein the chilled water supply pump (301) and the chilled water return pump (302) are both connected to the buffer tank one (26) through pipelines, wherein the chilled water supply pump (301) is connected to the chilled water tank (30), and wherein the chilled water return pump (302) is connected to the chilled water tank (30).
6. The ammonia water recovery system according to claim 5, wherein the multistage absorption device comprises a primary balance tank (31), the primary balance tank (31) is communicated with a primary absorption tank (32) through a pipeline, the primary absorption tank (32) is connected with a secondary balance tank (34), the secondary balance tank (34) is connected with a secondary absorption tank (35), the secondary absorption tank (35) is connected with the primary absorption tank (32), the primary absorption tank (32) is connected with a buffer tank two (36), and the buffer tank two (36) is connected with a second discharge pump (37) and a second ammonia water pump (381).
7. The ammonia water recovery system according to claim 6, wherein the primary absorption tank (32) and the secondary absorption tank (35) are each provided with a temperature sensor (33).
8. The ammonia water recovery system according to claim 6, wherein the chilled water supply pump (301) is connected to the secondary absorption tank (35) via a water pipe, the secondary absorption tank (35) is connected to the primary absorption tank (32) via a water pipe, the primary absorption tank (32) is connected to the buffer tank two (36) via a water pipe, and the buffer tank two (36) is connected to the chilled water return pump (302) via a water pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322302977.6U CN220939159U (en) | 2023-08-25 | 2023-08-25 | Ammonia water recovery system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322302977.6U CN220939159U (en) | 2023-08-25 | 2023-08-25 | Ammonia water recovery system |
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| CN220939159U true CN220939159U (en) | 2024-05-14 |
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| CN202322302977.6U Active CN220939159U (en) | 2023-08-25 | 2023-08-25 | Ammonia water recovery system |
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- 2023-08-25 CN CN202322302977.6U patent/CN220939159U/en active Active
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