CN220449809U - System for heat pump flash distillation strip deamination produces ammonium sulfate and aqueous ammonia - Google Patents
System for heat pump flash distillation strip deamination produces ammonium sulfate and aqueous ammonia Download PDFInfo
- Publication number
- CN220449809U CN220449809U CN202322070017.1U CN202322070017U CN220449809U CN 220449809 U CN220449809 U CN 220449809U CN 202322070017 U CN202322070017 U CN 202322070017U CN 220449809 U CN220449809 U CN 220449809U
- Authority
- CN
- China
- Prior art keywords
- ammonia
- steam
- tower
- deamination
- stripping
- 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 Natural products N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 174
- 230000009615 deamination Effects 0.000 title claims abstract description 85
- 238000006481 deamination reaction Methods 0.000 title claims abstract description 85
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 title claims abstract description 82
- 229910052921 ammonium sulfate Inorganic materials 0.000 title claims abstract description 47
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 title claims abstract description 46
- 235000011130 ammonium sulphate Nutrition 0.000 title claims abstract description 46
- 238000007701 flash-distillation Methods 0.000 title description 2
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 89
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 81
- 238000001704 evaporation Methods 0.000 claims abstract description 39
- 230000008020 evaporation Effects 0.000 claims abstract description 39
- 239000007788 liquid Substances 0.000 claims abstract description 33
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 24
- 238000003860 storage Methods 0.000 claims abstract description 15
- 239000002351 wastewater Substances 0.000 claims description 36
- 238000010521 absorption reaction Methods 0.000 claims description 35
- 239000002131 composite material Substances 0.000 claims description 34
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 27
- 238000000034 method Methods 0.000 claims description 18
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 15
- 238000010992 reflux Methods 0.000 claims description 15
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- 239000003513 alkali Substances 0.000 claims description 4
- 229910002804 graphite Inorganic materials 0.000 claims description 4
- 239000010439 graphite Substances 0.000 claims description 4
- 238000004134 energy conservation Methods 0.000 abstract description 7
- 238000000926 separation method Methods 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 20
- 238000004064 recycling Methods 0.000 description 11
- 238000004519 manufacturing process Methods 0.000 description 10
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 8
- 239000000243 solution Substances 0.000 description 8
- 238000006722 reduction reaction Methods 0.000 description 6
- 238000004065 wastewater treatment Methods 0.000 description 6
- 230000002378 acidificating effect Effects 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 238000005507 spraying Methods 0.000 description 4
- 238000005272 metallurgy Methods 0.000 description 3
- 238000010793 Steam injection (oil industry) Methods 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 230000006641 stabilisation Effects 0.000 description 2
- 238000011105 stabilization Methods 0.000 description 2
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 description 1
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 239000011737 fluorine Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Physical Water Treatments (AREA)
Abstract
A heat pump flash evaporation, stripping and deamination system for producing ammonium sulfate and ammonia water is characterized in that an ammonia-containing steam output interface of the heat pump flash evaporation, stripping and deamination system is connected with a steam input port of an evaporator, a steam output port of the evaporator is connected with a steam input port of a separator, a liquid output port of the evaporator is connected with an inlet of an ammonia water buffer tank, an outlet of the ammonia water buffer tank is connected with a dilute ammonia water inlet of an ammonia rectifying tower, a steam outlet of the ammonia rectifying tower is connected with a steam inlet of a tower top condenser, and an ammonia water outlet of the tower top condenser is connected with an ammonia water storage tank. The tower bottom liquid of the ammonia rectifying tower circulates in a large amount in a separator, a circulating axial flow pump and an evaporator, and gas-liquid separation is carried out in the separator after the heat of the ammonia-containing steam is pressurized by an ammonia-containing steam compressor. The vaporized water vapor enters the venturi steam ejector through the steam compressor and is recycled as stripping steam. The utility model has the characteristics of energy conservation, no harm and stability.
Description
Technical Field
The utility model discloses an ammonium sulfate and ammonia water production system, in particular to a system for producing ammonium sulfate and ammonia water by flash evaporation, steam stripping and deamination of a heat pump, and belongs to the field of recycling of ammonia nitrogen wastewater treated by a chemical method.
Background
The industries such as petrochemical industry, metallurgy, food and the like often generate a large amount of ammonia nitrogen wastewater, and the wastewater also usually contains sulfur, phenol, fluorine or sulfate radical, silicate and other impurities, so that the wastewater is difficult to treat effectively, or the ammonia nitrogen content in the treated wastewater can not reach the national emission standard, if the wastewater is directly discharged, a water source is polluted, and the environment is greatly damaged. In addition, the cost for treating the ammonia nitrogen wastewater is relatively high, wherein the consumption of steam is generally more than 180kg/t of wastewater, the device in the prior art is not energy-saving, the operation cost is high, and common enterprises cannot bear the device.
Aiming at the problems, a heat pump flash evaporation, steam stripping and deamination method is developed for improving the problem of high steam consumption in the prior art, so that ammonia nitrogen wastewater can be discharged up to the standard, and the method can be specifically referred to the prior Chinese patent application with the application number of 201010123251.0. Although the heat pump flash stripping deamination method improves the problem of high steam consumption in the prior art, the problem of resource utilization is not thoroughly solved.
Disclosure of Invention
Aiming at the problem that the recycling problem cannot be solved in the prior art for treating ammonia nitrogen wastewater, the utility model provides a system for producing ammonium sulfate and ammonia water by flash evaporation, steam stripping and deamination of a heat pump, which can produce ammonia water with a certain concentration while producing ammonium sulfate, and solves the ammonia balance problem in the recycling process of the ammonium sulfate and the ammonia water produced in the running process of the system while ensuring that the discharge of ammonia nitrogen wastewater reaches the standard.
The technical scheme adopted for solving the technical problems is as follows: the system comprises a heat pump flash evaporation stripping deamination system, an evaporator, a separator, an ammonia buffer tank, an ammonia rectifying tower, an ammonia water storage tank and a tower top condenser, wherein an ammonia-containing steam output interface of the heat pump flash evaporation stripping deamination system is connected with a steam input port of the evaporator, a steam output port of the evaporator is connected with a steam input port of the separator, a liquid output port of the evaporator is connected with an inlet of the ammonia buffer tank, an outlet of the ammonia buffer tank is connected with a dilute ammonia water inlet of the ammonia rectifying tower, a steam outlet of the ammonia rectifying tower is connected with a steam inlet of the tower top condenser, and an ammonia water outlet of the tower top condenser is connected with the ammonia water storage tank.
The technical scheme adopted by the utility model for solving the technical problems further comprises the following steps:
an ammonia-containing vapor compressor is arranged between the heat pump flash evaporation stripping deamination system and the evaporator.
The evaporator adopts one of a plate heat exchanger, a sleeve heat exchanger, a shell-and-tube heat exchanger or a graphite heat exchanger; the ammonia-containing vapor compressor is one of a centrifugal compressor, a reciprocating compressor or a turbine compressor.
The liquid outlet of the separator is connected with the liquid inlet of the evaporator through the circulating axial flow pump, the liquid outlet of the separator is arranged at the bottom of the separator, and the liquid inlet of the evaporator is arranged at the bottom of the evaporator.
And a rectification feeding pump is connected between the outlet of the ammonia buffer tank and the dilute ammonia inlet of the ammonia rectification tower.
And a tower kettle conveying pump is connected between the liquid outlet of the ammonia rectifying tower and the separator.
The circulating water system enters the tower top condenser through the circulating water inlet and is discharged through the circulating water return inlet.
The outlet of the ammonia water storage tank is connected with an ammonia water reflux pump, the output end of the ammonia water reflux pump is connected to ammonia water for use, and the output end of the ammonia water reflux pump is also connected with the input end of the ammonia rectifying tower.
The steam outlet of the separator is connected with a steam compressor, and the steam compressor is communicated with a flash evaporation, steam stripping and deamination system of the heat pump.
The heat pump flash evaporation, steam stripping and deamination system comprises a composite steam stripping and deamination tower, a saturation tower and an absorption tower, wherein high ammonia nitrogen wastewater is input into the composite steam stripping and deamination tower through a venturi water injector, the high ammonia nitrogen wastewater in the composite steam stripping and deamination tower is input into the lower layer of the composite steam stripping and deamination tower through a venturi wastewater injector, a flash evaporation feed pump is connected in series with the venturi wastewater injector, the bottom of the composite steam stripping and deamination tower is connected to the upper part of the composite steam stripping and deamination tower through a steam stripping and deamination feed pump, an alkali liquor input interface is connected between the composite steam stripping and deamination tower and the steam stripping and deamination feed pump, steam is input into the composite steam stripping and deamination tower through a steam injection compressor, a steam outlet of a separator is input into the composite steam injection compressor together, the top of the composite steam stripping and deamination tower is connected with a steam circulation heat pump through the steam circulation heat pump, the output end of the steam circulation heat pump is also connected to the top of the saturation tower, the bottom of the saturation tower is connected with an ammonium sulfate circulation pump, the ammonium sulfate solution is pumped to the upper part of the saturation tower through the ammonium sulfate circulation pump, the lower part is provided with the ammonium sulfate outlet, the upper part is connected to the absorption tower through the absorption tower, the lower part is connected to the absorption tower, the absorption tower is connected to the top of the absorption tower through the absorption tower, and the absorption tower is connected to the absorption tower through the absorption tower.
The beneficial effects of the utility model are as follows: because of the enterprises generating ammonia nitrogen wastewater, the former production working conditions generally use an acidic ammonia solution (namely ammonium sulfate) and an alkaline ammonia solution (namely ammonia water). The utility model organically combines the technologies of stripping deamination technology, flash evaporation technology, heat pump technology, rectification and the like, provides an innovative technical system for the recycling utilization of ammonia nitrogen wastewater treatment and energy conservation and consumption reduction, effectively solves the problems of high steam consumption, easy scaling and blocking of equipment and high operation cost of the high ammonia nitrogen wastewater treatment method, and realizes the treatment of energy conservation, innocuity, reduction, stabilization and recycling. According to the utility model, the flash evaporation technology is utilized to directly mix the steam obtained by flash evaporation with the wastewater to recover heat, so that the heat exchange between deamination wastewater and pretreated ammonia nitrogen wastewater is realized, thereby fundamentally solving the problems of scaling and blockage existing in the conventional stripping deamination technology when a heat exchanger is utilized for energy recovery, and solving the problems of scaling and blockage caused by a common heat exchanger due to suspended matters in the wastewater. The utility model adopts the combined technology of the Venturi vapor injection compressor and the vapor circulation heat pump, realizes a closed circulation system of deamination vapor, and greatly reduces the consumption of stripping vapor. The utility model has low steam consumption, adopts the flash evaporation technology, the Venturi steam jet compressor and the steam circulation heat pump combination technology in the early stage, greatly reduces the consumption of stripping steam, adopts the heat pump rectification technology in the ammonia water production in the later stage, and returns the heat energy of the ammonia-containing steam to the steam stripping system through the heat pump evaporation device, thereby greatly reducing the steam consumption of rectification and greatly reducing the external energy requirement of the whole system. The utility model not only realizes the purposes of up-to-standard emission of ammonia nitrogen wastewater and energy conservation and consumption reduction, but also obtains the acidic ammonia solution (namely ammonium sulfate) and the alkaline ammonia solution (namely ammonia water) at the same time, meets the production and recycling requirements of a production device, and generates economic value. Can be widely applied to the inorganic ammonia nitrogen wastewater treatment industries such as petrifaction, metallurgy, food and the like, and has wide application prospect. The utility model can produce ammonia water with certain concentration while producing ammonium sulfate, and solves the ammonia balance problem in the recycling process of ammonium sulfate and ammonia water produced in the running process of the system while ensuring that the discharge of ammonia nitrogen sewage reaches the standard.
The utility model will be further described with reference to the drawings and detailed description.
Drawings
FIG. 1 is a schematic diagram of the system of the present utility model.
In the figure, 1-venturi water injector, 2-venturi wastewater injector, 3-composite stripping deamination tower, 4-saturation tower, 5-absorption tower, 6-liquid ring vacuum pump, 7-flash evaporation feed pump, 8-stripping deamination feed pump, 9-ammonium sulfate circulating pump, 10-sulfuric acid absorption circulating pump, 11-steam circulation heat pump, 12-steam jet compressor, 13-ammonia-containing steam compressor, 14-evaporator, 15-separator, 16-circulation axial flow pump, 17-ammonia buffer tank, 18-rectification feed pump, 19-tower kettle conveying pump, 20-ammonia rectification tower, 21-ammonia reflux pump, 22-ammonia water storage tank, 23-tower top condenser and 24-steam compressor.
Detailed Description
This example is a preferred embodiment of the present utility model, and other principles and basic structures are the same as or similar to those of this example, and all fall within the scope of the present utility model.
The utility model mainly protects a system for producing ammonium sulfate and ammonia water by heat pump flash evaporation, stripping and deamination, which comprises a heat pump flash evaporation, stripping and deamination system, an evaporator 14, a separator 15, an ammonia water buffer tank 17, an ammonia rectifying tower 20, an ammonia water storage tank 22 and a tower top condenser 23, wherein an ammonia-containing steam output interface of the heat pump flash evaporation, stripping and deamination system is connected with a steam input port of the evaporator 14, a steam output port of the evaporator 14 is connected with a steam input port of the separator 15, a liquid output port of the evaporator 14 is connected with an inlet of the ammonia water buffer tank 17, an outlet of the ammonia water buffer tank 17 is connected with a dilute ammonia water inlet of the ammonia rectifying tower 20, a steam outlet of the ammonia rectifying tower 20 is connected with a steam inlet of the tower top condenser 23, and an ammonia water outlet of the tower top condenser 23 is connected with the ammonia water storage tank 22.
In this embodiment, an ammonia-containing vapor compressor 13 is disposed between the heat pump flash stripping deamination system and the evaporator 14, and ammonia-containing vapor is compressed by the ammonia-containing vapor compressor 13 and then input to the evaporator 14. In this embodiment, the evaporator 14 may be one of a plate heat exchanger, a double pipe heat exchanger, a shell-and-tube heat exchanger, or a graphite heat exchanger; the ammonia-containing vapor compressor 13 can adopt one of a centrifugal compressor, a reciprocating compressor and a turbine compressor, and the pressure boost of the ammonia-containing vapor compressor 13 is more than or equal to 60kPa.
In this embodiment, the liquid outlet of the separator 15 is connected to the liquid inlet of the evaporator 14 by a circulation axial flow pump 16, the liquid outlet of the separator 15 is disposed at the bottom of the separator 15, and the liquid inlet of the evaporator 14 is disposed at the bottom of the evaporator 14. In this embodiment, the separator 15 may be a container type device; the circulating axial flow pump 16 may be an axial flow pump or a centrifugal pump.
In this embodiment, a rectification feed pump 18 is connected between the outlet of the ammonia buffer tank 17 and the dilute ammonia inlet of the ammonia rectification tower 20, and the dilute ammonia in the ammonia buffer tank 17 is fed into the ammonia rectification tower 20 through the rectification feed pump 18. In this embodiment, the ammonia buffer tank 17 may be a container type device; the rectifying feed pump 18 may employ a centrifugal pump type device.
In this embodiment, a tank transfer pump 19 is connected between the liquid outlet of the ammonia rectifying tower 20 and the separator 15, and the rectified liquid is fed into the separator 15 by the tank transfer pump 19 to be separated again. In this embodiment, the tower transporting pump 19 may be a centrifugal pump type device.
In this embodiment, a circulating water system is connected to the top condenser 23, and enters the top condenser 23 through a water inlet of circulating water, and is discharged through a water return inlet of circulating water, so as to form circulating water, and the circulating water exchanges heat with ammonia-containing steam output by the ammonia rectifying tower 20 in the top condenser 23, is concentrated into ammonia water, and is sent into the ammonia water storage tank 22 for storage. In this embodiment, the tower top condenser 23 may be one of a plate heat exchanger, a double pipe heat exchanger, a shell-and-tube heat exchanger, or a graphite heat exchanger; the ammonia water tank 22 may be a container type device.
In this embodiment, the outlet of the ammonia water storage tank 22 is connected with the ammonia water reflux pump 21, the output end of the ammonia water reflux pump 21 is used for being connected to ammonia water for use, and meanwhile, the output end of the ammonia water reflux pump 21 is also connected with the input end of the ammonia rectifying tower 20, so as to reflux the redundant ammonia water into the ammonia rectifying tower 20 for recirculation. In this embodiment, the ammonia water reflux pump 21 may be a centrifugal pump type device.
In this embodiment, the steam outlet of the separator 15 is connected to a steam compressor 24, the steam compressor 24 is in communication with a heat pump flash evaporation, steam stripping and deamination system, and the steam separated by the separator 15 is sent to the heat pump flash evaporation, steam stripping and deamination system through the steam compressor 24 for recirculation. In this embodiment, the vapor compressor 24 may be one of a compressor and a fan, and the pressure boost of the vapor compressor 24 is greater than or equal to 8000Pa.
In the embodiment, the heat pump flash evaporation stripping deamination system mainly comprises a composite stripping deamination tower 3, a saturation tower 4 and an absorption tower 5, wherein high ammonia nitrogen wastewater is input into the composite stripping deamination tower 3 through a venturi water injector 1, the high ammonia nitrogen wastewater in the composite stripping deamination tower 3 is input into the lower layer of the composite stripping deamination tower 3 through a venturi wastewater injector 2, a flash evaporation feed pump 7 is connected in series with the venturi wastewater injector 2, the bottom of the composite stripping deamination tower 3 is connected to the upper part of the composite stripping deamination tower 3 through a stripping deamination feed pump 8 and is sprayed into the composite stripping deamination tower 3 in a spraying mode, an alkali liquid input interface is connected between the composite stripping deamination tower 3 and the stripping deamination feed pump 8 for inputting alkali liquid, steam is input into the composite stripping deamination tower 3 through a steam jet compressor 12, the steam outlet of the separator 15 is input into the steam jet compressor 12 through the steam jet compressor 12, the steam is input into the composite stripping deamination tower 3 through the steam jet compressor 12, the top of the composite stripping deamination tower 3 is connected with the steam circulation heat pump 11, the steam is input into the ammonia-containing steam compressor 13 through the steam circulation heat pump 11, the output end of the steam circulation heat pump 11 is also divided into the top of the saturation tower 4, the bottom of the saturation tower 4 is connected with the ammonium sulfate circulation pump 9, the ammonium sulfate solution is pumped above the saturation tower 4 through the ammonium sulfate circulation pump 9 and is sprayed into the saturation tower 4 through a spraying mode, the ammonium sulfate is generated by reacting with the ammonia-containing steam output by the steam circulation heat pump 11, the lower part of the saturation tower 4 is provided with the ammonium sulfate outlet for outputting the ammonium sulfate solution, the middle lower part (above the liquid level of the saturation tower 4) of the saturation tower 4 is communicated with the absorption tower 5, the ammonia-containing steam can be input into the absorption tower 5, the lower part of the absorption tower 5 (below the liquid level of the absorption tower 5) is communicated with the saturation tower 4, so that an ammonium sulfate solution can be input into the saturation tower 4, the bottom of the absorption tower 5 is connected to the upper part of the absorption tower 5 through a sulfuric acid absorption circulating pump 10, the ammonium sulfate solution is sprayed into the absorption tower 5 through a spraying mode, a process water inlet and a dilute sulfuric acid inlet are connected between the sulfuric acid absorption circulating pump 10 and the upper part of the absorption tower 5, process water and dilute sulfuric acid can be sprayed into the absorption tower 5 together through a spraying mode, the top of the absorption tower 5 is communicated with a steam jet compressor 12, and redundant ammonia-containing steam of the absorption tower 5 is sprayed into the composite stripping deamination tower 3 through the steam jet compressor 12 for recirculation.
When in use, the utility model comprises the following steps:
step S1, directly conveying a dilute ammonium sulfate solution with the mass concentration of 10-30% obtained by adopting a heat pump flash evaporation, steam stripping and deamination method to a boundary area where the ammonium sulfate solution is needed, wherein the part of the heat pump flash evaporation, steam stripping and deamination method, namely the use method of a heat pump flash evaporation, steam stripping and deamination system, can be seen from the prior Chinese patent application with the application number of 201010123251.0;
s2, introducing one strand of ammonia-containing steam into a saturation tower 4 at the outlet of a steam circulation heat pump 11 to produce ammonium sulfate, and introducing the other strand of ammonia-containing steam into a subsequent heat pump rectification system;
step S3, pressurizing ammonia-containing steam input by the steam circulation heat pump 11 through the ammonia-containing steam compressor 13, inputting the ammonia-containing steam into the evaporator 14 for heating circulating liquid at the bottom of the separator 15, and condensing the ammonia-containing steam into dilute ammonia water to enter the ammonia water buffer tank 17 after self heat is utilized;
in the step S4, the dilute ammonia water in the ammonia buffer tank 17 is transported into the ammonia rectifying tower 20 by the rectifying feed pump 18, and is rectified in the ammonia rectifying tower 20. In the rectification process, the generated ammonia-containing steam and the reflux ammonia water which is conveyed into the top of the ammonia rectification tower 20 through the reflux pump 21 are subjected to vapor-liquid mass transfer in the ammonia rectification tower 20, 5-30% of concentrated ammonia gas with different concentrations can be produced according to production requirements, and the rectified concentrated ammonia gas is condensed in the tower top condenser 23 and then enters the ammonia water storage tank 22. The concentrated ammonia water in the ammonia water storage tank 22 flows back to the top of the ammonia rectifying tower 20 through the ammonia reflux pump 21, one part is used in the rectifying process, and the other part is extracted and conveyed to a boundary area needing ammonia water solution;
in step S5, the tower bottom liquid of the ammonia rectifying tower 20 is conveyed to the separator 15 through the tower bottom conveying pump 19, the liquid in the separator 15 is circulated in a large amount in the separator 15, the circulating axial flow pump 16 and the evaporator 14 through the circulating axial flow pump 16, and the separator 15, the circulating axial flow pump 16 and the evaporator 14 form one of typical MVR systems.
In step S6, the circulating liquid is separated into gas and liquid in the separator 15 by using the heat of the ammonia-containing vapor pressurized by the ammonia-containing vapor compressor 13 in the evaporator 14.
In step S7, the water vapor evaporated in the separator 15 enters the venturi steam ejector 12 through the steam compressor 24 and is recycled as stripping steam.
Compared with the traditional stripping deamination, the heat pump rectifying system for producing ammonia water can greatly reduce the heat loss of the tower top condenser, and has remarkable energy-saving effect.
Because of the enterprises generating ammonia nitrogen wastewater, the former production working conditions generally use an acidic ammonia solution (namely ammonium sulfate) and an alkaline ammonia solution (namely ammonia water). The utility model organically combines the technologies of stripping deamination technology, flash evaporation technology, heat pump technology, rectification and the like, provides an innovative technical system for the recycling utilization of ammonia nitrogen wastewater treatment and energy conservation and consumption reduction, effectively solves the problems of high steam consumption, easy scaling and blocking of equipment and high operation cost of the high ammonia nitrogen wastewater treatment method, and realizes the treatment of energy conservation, innocuity, reduction, stabilization and recycling. According to the utility model, the flash evaporation technology is utilized to directly mix the steam obtained by flash evaporation with the wastewater to recover heat, so that the heat exchange between deamination wastewater and pretreated ammonia nitrogen wastewater is realized, thereby fundamentally solving the problems of scaling and blockage existing in the conventional stripping deamination technology when a heat exchanger is utilized for energy recovery, and solving the problems of scaling and blockage caused by a common heat exchanger due to suspended matters in the wastewater. The utility model adopts the combined technology of the Venturi vapor injection compressor and the vapor circulation heat pump, realizes a closed circulation system of deamination vapor, and greatly reduces the consumption of stripping vapor. The utility model has low steam consumption, adopts the flash evaporation technology, the Venturi steam jet compressor and the steam circulation heat pump combination technology in the early stage, greatly reduces the consumption of stripping steam, adopts the heat pump rectification technology in the ammonia water production in the later stage, and returns the heat energy of the ammonia-containing steam to the steam stripping system through the heat pump evaporation device, thereby greatly reducing the steam consumption of rectification and greatly reducing the external energy requirement of the whole system. The utility model not only realizes the purposes of up-to-standard emission of ammonia nitrogen wastewater and energy conservation and consumption reduction, but also obtains the acidic ammonia solution (namely ammonium sulfate) and the alkaline ammonia solution (namely ammonia water) at the same time, meets the production and recycling requirements of a production device, and generates economic value. Can be widely applied to the inorganic ammonia nitrogen wastewater treatment industries such as petrifaction, metallurgy, food and the like, and has wide application prospect. The utility model can produce ammonia water with certain concentration while producing ammonium sulfate, and solves the ammonia balance problem in the recycling process of ammonium sulfate and ammonia water produced in the running process of the system while ensuring that the discharge of ammonia nitrogen sewage reaches the standard.
Claims (10)
1. A system for producing ammonium sulfate and ammonia water by flash evaporation, steam stripping and deamination of a heat pump is characterized in that: the system comprises a heat pump flash evaporation stripping deamination system, an evaporator (14), a separator (15), an ammonia buffer tank (17), an ammonia rectifying tower (20), an ammonia storage tank (22) and a tower top condenser (23), wherein an ammonia-containing steam output interface of the heat pump flash evaporation stripping deamination system is connected with a steam input port of the evaporator (14), a steam output port of the evaporator (14) is connected with a steam input port of the separator (15), a liquid output port of the evaporator (14) is connected with an inlet of the ammonia buffer tank (17), an outlet of the ammonia buffer tank (17) is connected with a dilute ammonia inlet of the ammonia rectifying tower (20), a steam outlet of the ammonia rectifying tower (20) is connected with a steam inlet of the tower top condenser (23), and an ammonia outlet of the tower top condenser (23) is connected with the ammonia storage tank (22).
2. The system for producing ammonium sulfate and ammonia water by flash stripping deamination of heat pump according to claim 1, wherein: an ammonia-containing vapor compressor (13) is arranged between the heat pump flash evaporation stripping deamination system and the evaporator (14).
3. The system for producing ammonium sulfate and ammonia water by flash stripping deamination of heat pump according to claim 2, wherein: the evaporator (14) adopts one of a plate heat exchanger, a sleeve heat exchanger, a shell-and-tube heat exchanger or a graphite heat exchanger; the ammonia-containing vapor compressor (13) is one of a centrifugal compressor, a reciprocating compressor or a turbine compressor.
4. The system for producing ammonium sulfate and ammonia water by flash stripping deamination of heat pump according to claim 1, wherein: the liquid outlet of the separator (15) is connected with the liquid inlet of the evaporator (14) through a circulating axial flow pump (16), the liquid outlet of the separator (15) is arranged at the bottom of the separator (15), and the liquid inlet of the evaporator (14) is arranged at the bottom of the evaporator (14).
5. The system for producing ammonium sulfate and ammonia water by flash stripping deamination of heat pump according to claim 1, wherein: a rectification feeding pump (18) is connected between the outlet of the ammonia buffer tank (17) and the dilute ammonia inlet of the ammonia rectification tower (20).
6. The system for producing ammonium sulfate and ammonia water by flash stripping deamination of heat pump according to claim 1, wherein: a tower kettle conveying pump (19) is connected between the liquid outlet of the ammonia rectifying tower (20) and the separator (15).
7. The system for producing ammonium sulfate and ammonia water by flash stripping deamination of heat pump according to claim 1, wherein: the top condenser (23) is connected with a circulating water system, and the circulating water system enters the top condenser (23) through a circulating water inlet and is discharged through a circulating water return port.
8. The system for producing ammonium sulfate and ammonia water by flash stripping deamination of heat pump according to claim 1, wherein: the outlet of the ammonia water storage tank (22) is connected with an ammonia water reflux pump (21), the output end of the ammonia water reflux pump (21) is connected to ammonia water for use, and the output end of the ammonia water reflux pump (21) is also connected with the input end of the ammonia rectifying tower (20).
9. The system for producing ammonium sulfate and ammonia water by flash stripping deamination of heat pump according to claim 1, wherein: the steam outlet of the separator (15) is connected with a steam compressor (24), and the steam compressor (24) is communicated with a heat pump flash evaporation stripping deamination system.
10. The system for producing ammonium sulfate and ammonia water by flash stripping deamination of heat pump according to claim 1, wherein: the heat pump flash evaporation, steam stripping and deamination system comprises a composite steam stripping and deamination tower (3), a saturation tower (4) and an absorption tower (5), wherein high ammonia nitrogen wastewater is input into the composite steam stripping and deamination tower (3) through a venturi water injector (1), the high ammonia nitrogen wastewater in the composite steam stripping and deamination tower (3) is input into the lower layer of the composite steam stripping and deamination tower (3) through a venturi wastewater injector (2), a flash evaporation feed pump (7) is connected in series with the venturi wastewater injector (2), the bottom of the composite steam stripping and deamination tower (3) is connected to the upper part of the composite steam stripping and deamination tower (3) through a steam stripping and deamination feed pump (8), an alkali liquor input interface is connected between the composite steam stripping and deamination tower (3) and the steam stripping and deamination feed pump (8), steam is input into the composite steam stripping and deamination tower (3) through a steam jet compressor (12), a steam outlet of a separator (15) is input into the steam jet compressor (12) through a steam jet compressor (24), is input into the composite steam stripper 3) together, the composite steam stripping and the top of the composite steam stripping and deamination tower (3) is connected to the top of the heat pump (11) through a circulation pump (11), the top of the circulating steam circulation (11) and the circulating steam circulation (11) to the top of the circulating steam pump (11), the bottom of the saturation tower (4) is connected with an ammonium sulfate circulating pump (9), an ammonium sulfate solution is pumped to the upper part of the saturation tower (4) through the ammonium sulfate circulating pump (9), an ammonium sulfate outlet is formed in the lower part of the saturation tower (4), the middle lower part of the saturation tower (4) is communicated with an absorption tower (5), the lower part of the absorption tower (5) is communicated with the saturation tower (4), the bottom of the absorption tower (5) is connected to the upper part of the absorption tower (5) through a sulfuric acid absorption circulating pump (10), a process water inlet and a dilute sulfuric acid inlet are connected between the sulfuric acid absorption circulating pump (10) and the upper part of the absorption tower (5), and the top of the absorption tower (5) is communicated with a steam jet compressor (12).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322070017.1U CN220449809U (en) | 2023-08-03 | 2023-08-03 | System for heat pump flash distillation strip deamination produces ammonium sulfate and aqueous ammonia |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322070017.1U CN220449809U (en) | 2023-08-03 | 2023-08-03 | System for heat pump flash distillation strip deamination produces ammonium sulfate and aqueous ammonia |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220449809U true CN220449809U (en) | 2024-02-06 |
Family
ID=89724715
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322070017.1U Active CN220449809U (en) | 2023-08-03 | 2023-08-03 | System for heat pump flash distillation strip deamination produces ammonium sulfate and aqueous ammonia |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220449809U (en) |
-
2023
- 2023-08-03 CN CN202322070017.1U patent/CN220449809U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104860464A (en) | Energy-saving ammonia-nitrogen wastewater treatment method and device | |
| CN212864613U (en) | Synthetic leather waste water treatment and DMF recovery system | |
| CN104843816A (en) | Method for combined production of ammonium sulfate and ammonia water through heat pump flash evaporation, stripping and deamination | |
| CN111825145A (en) | Method and device for treating ammonia nitrogen wastewater and recovering ammonia | |
| CN110937744B (en) | Dimethylamine treatment process in synthetic leather DMF (dimethyl formamide) wastewater heat pump rectification process | |
| CN111392947A (en) | Ammonia water resource utilization process and device | |
| CN106964174B (en) | Method and system for rectifying/purifying ammonia | |
| CN111943865A (en) | Synthetic leather waste water treatment and DMF recovery system | |
| CN220449809U (en) | System for heat pump flash distillation strip deamination produces ammonium sulfate and aqueous ammonia | |
| CN114230071A (en) | Treatment method of DMF (dimethyl formamide) -containing wastewater | |
| CN212222702U (en) | High-efficient low temperature negative pressure ammonia nitrogen waste water strip system | |
| CN101445226B (en) | Novel technology of two-effect evaporation of phosphoric acid with wet method | |
| CN210419611U (en) | Ammonium sulfate waste water MVR evaporation deamination processing system | |
| CN112374561A (en) | High-efficiency energy-saving double-heat-pump deamination method and device | |
| CN117069125A (en) | Method for producing ammonium sulfate and ammonia water by flash evaporation, steam stripping and deamination of heat pump | |
| CN204644041U (en) | A kind of ammonia nitrogen waste water treatment system | |
| CN218435358U (en) | Device for treating ammonia-nitrogen wastewater easy to scale and recovering ammonia | |
| CN104829032A (en) | Ammonia-nitrogen wastewater treatment system | |
| CN202072574U (en) | Ammonium nitrate waste water processing unit | |
| CN106809896B (en) | A kind of organic wastewater treating system and method | |
| CN211367028U (en) | Low boiling point grease class contains salt waste water multiple-effect evaporation processing system | |
| CN112742047A (en) | Method and device for pumping negative pressure of urea production evaporation system | |
| CN211752569U (en) | Multistage series horizontal tube falling film TVR steam jet evaporator | |
| CN114409004A (en) | Energy-saving recycling process for treating wastewater containing volatile substances | |
| CN108325227B (en) | System for recycling heat in multi-effect evaporation system and treatment method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |