CN210419611U - Ammonium sulfate waste water MVR evaporation deamination processing system - Google Patents
Ammonium sulfate waste water MVR evaporation deamination processing system Download PDFInfo
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- CN210419611U CN210419611U CN201921341466.2U CN201921341466U CN210419611U CN 210419611 U CN210419611 U CN 210419611U CN 201921341466 U CN201921341466 U CN 201921341466U CN 210419611 U CN210419611 U CN 210419611U
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- evaporation chamber
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- 238000001704 evaporation Methods 0.000 title claims abstract description 149
- 230000008020 evaporation Effects 0.000 title claims abstract description 146
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 title claims abstract description 71
- 229910052921 ammonium sulfate Inorganic materials 0.000 title claims abstract description 71
- 235000011130 ammonium sulphate Nutrition 0.000 title claims abstract description 71
- 239000002351 wastewater Substances 0.000 title claims abstract description 70
- 230000009615 deamination Effects 0.000 title claims abstract description 28
- 238000006481 deamination reaction Methods 0.000 title claims abstract description 28
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 167
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 132
- 239000011552 falling film Substances 0.000 claims abstract description 87
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 56
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 claims abstract description 38
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims abstract description 24
- 235000011941 Tilia x europaea Nutrition 0.000 claims abstract description 24
- 239000004571 lime Substances 0.000 claims abstract description 24
- 239000008267 milk Substances 0.000 claims abstract description 22
- 235000013336 milk Nutrition 0.000 claims abstract description 22
- 210000004080 milk Anatomy 0.000 claims abstract description 22
- 238000000034 method Methods 0.000 claims abstract description 14
- 238000006243 chemical reaction Methods 0.000 claims abstract description 8
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 131
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 64
- 239000000243 solution Substances 0.000 claims description 26
- 239000007788 liquid Substances 0.000 claims description 21
- 239000013078 crystal Substances 0.000 claims description 16
- 238000002347 injection Methods 0.000 claims description 9
- 239000007924 injection Substances 0.000 claims description 9
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 4
- 238000003825 pressing Methods 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 238000004065 wastewater treatment Methods 0.000 abstract description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 abstract description 3
- 239000004566 building material Substances 0.000 abstract description 3
- 229910052791 calcium Inorganic materials 0.000 abstract description 3
- 239000011575 calcium Substances 0.000 abstract description 3
- 239000004568 cement Substances 0.000 abstract description 3
- 230000009467 reduction Effects 0.000 abstract description 2
- 125000004122 cyclic group Chemical group 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 abstract 1
- 238000009854 hydrometallurgy Methods 0.000 abstract 1
- 230000008569 process Effects 0.000 description 9
- 230000000087 stabilizing effect Effects 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 4
- 239000012452 mother liquor Substances 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- 238000004891 communication Methods 0.000 description 3
- 239000013589 supplement Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000006071 cream Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
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- 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
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- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The utility model belongs to the technical field of ammonium sulfate waste water treatment technique and specifically relates to ammonium sulfate waste water MVR evaporation deamination processing system, this processing system includes: the utility model discloses a lime milk and ammonium sulfate reaction are utilized to the preheater, first order evaporimeter, second grade evaporimeter, falling film evaporator, filter and vapor compressor, and the calcium sulfate that produces can be used to building materials production such as cement, and ammonia generates the aqueous ammonia retrieval and utilization production, adopts forced circulation low temperature evaporation concentration simultaneously, has solved the interior calcium scale deposit problem of evaporating chamber; utilize falling film evaporator to absorb ammonia vapor heat, produce pure vapor, get into vapor compressor for heat cyclic utilization is a brand-new green technology that is very suitable for hydrometallurgy, the treatment cost of reduction ammonium sulfate waste water that can be very big, and entire system energy utilization is rateed highly, and is energy-concerving and environment-protective, and it adopts the combination of one-level evaporimeter and second grade evaporimeter, under the circumstances of practicing thrift electric energy and investment, can ensure that the deamination is thorough.
Description
Technical Field
The utility model belongs to the technical field of ammonium sulfate waste water treatment technique and specifically relates to an ammonium sulfate waste water MVR evaporation deamination processing system.
Background
When the ammonium sulfate is industrially produced and utilized, a large amount of ammonium sulfate wastewater is generated, and the ammonium sulfate wastewater easily causes water environment deterioration, so the discharge of the ammonium sulfate wastewater is strictly limited, and how to treat the ammonium sulfate wastewater is a technical problem which needs to be solved urgently by a person skilled in the art; however, it is also described in the market that the concentration process in the treatment process of the ammonium sulfate wastewater MVR evaporative crystallization system disclosed in chinese patent publication No. CN108686393A is only to simply concentrate ammonium sulfate to increase the concentration of ammonium sulfate, and obviously, this process cannot realize the multi-use of ammonium sulfate wastewater treatment, resulting in high treatment cost of ammonium sulfate wastewater.
How to treat the ammonium sulfate wastewater to realize the maximum value utilization of the ammonium sulfate wastewater is a technical problem which needs to be solved urgently by the technical personnel in the field.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is: in order to solve the problem that the treatment cost of the ammonium sulfate wastewater is higher due to the fact that the diversified utilization of the ammonium sulfate wastewater treatment cannot be realized in the prior art, an MVR evaporation deamination treatment system for the ammonium sulfate wastewater is provided.
The utility model provides a technical scheme that its technical problem adopted is:
the utility model provides an ammonium sulfate waste water MVR evaporation deamination processing system, includes:
a wastewater feed tank for holding ammonium sulfate wastewater;
the preheater is communicated with the wastewater feeding tank through a pipeline and is used for preheating the ammonium sulfate wastewater;
a lime milk feed tank for containing lime milk;
the primary evaporator is used for carrying out primary evaporation on mixed liquid generated by the reaction of the ammonium sulfate wastewater and the lime milk to form concentrated liquid containing calcium sulfate crystals and ammonia-containing steam, wherein the primary evaporator is a forced circulation evaporator;
the secondary evaporator is used for carrying out secondary evaporation on the concentrated solution from the primary evaporator to form concentrated solution containing calcium sulfate crystals and ammonia-containing steam, wherein the secondary evaporator is a forced circulation evaporator;
the falling-film evaporator is used for condensing ammonia-containing steam in the primary evaporator and the secondary evaporator to form ammonia water, ammonia gas and steam;
the filter is used for carrying out filter-pressing separation on the concentrated solution in the secondary evaporator to form ammonia water and calcium sulfate crystals;
and the vapor compressor is used for compressing vapor in the falling film evaporator and then conveying the compressed vapor to the first-stage evaporator and the second-stage evaporator for heat supply.
Further, the falling-film evaporator is communicated with a first ammonia water tank through a pipeline, and the first ammonia water tank is used for collecting ammonia water discharged by the falling-film evaporator.
Further, the falling-film evaporator is also communicated with a second condenser through a pipeline, the second condenser is communicated with a second ammonia water tank, and the second condenser is used for condensing uncondensed ammonia-containing steam from the falling-film evaporator into ammonia water;
and the second ammonia water tank is used for collecting condensed ammonia water flowing out of the second condenser to form ammonia water with certain concentration.
Further, the aqueous ammonia in the first aqueous ammonia jar gets into total aqueous ammonia jar behind first condenser, the pipeline and the second aqueous ammonia jar intercommunication of intercommunication between first condenser and the total aqueous ammonia jar, the intercommunication has circulating condenser on the second aqueous ammonia jar, the aqueous ammonia in the second aqueous ammonia jar gets back to the second aqueous ammonia jar again after circulating condenser cools off, all be provided with the aqueous ammonia discharge port on total aqueous ammonia jar and the second aqueous ammonia jar.
In order to avoid that the heat exchange space in the first-stage evaporator and the heat exchange space in the second-stage evaporator are occupied by the non-condensed steam in the first-stage evaporator and the second-stage evaporator to cause the reduction of the heat exchange efficiency, further, the first-stage evaporator and the second-stage evaporator are communicated with a pressure stabilizing device, the pressure stabilizing device comprises a vacuum pump, a regulating valve and a non-condensed steam cooler, the vacuum pump is communicated with the non-condensed steam cooler through a pipeline, the non-condensed steam cooler is used for cooling the non-condensed steam from the first-stage evaporator and the second-stage evaporator to condense the steam carried in the non-condensed steam into condensed water and stabilize the pressure at a designed working condition, and the regulating valve is arranged on a communication pipeline;
therefore, the non-condensed steam in the first-stage evaporator and the non-condensed steam in the second-stage evaporator can be discharged in real time through the pressure stabilizing device, the heat exchange efficiency of the first-stage evaporator and the heat exchange efficiency of the second-stage evaporator are ensured, and the evaporation temperature of the first-stage evaporator and the evaporation temperature of the second-stage evaporator are ensured to be within the process requirement range.
In order to prevent ammonia gas from being mixed in the non-condensed steam, the ammonia gas carried in the non-condensed steam is discharged along with the non-condensed steam, furthermore, the vacuum pump is communicated with a water tank through a pipeline, water in the water tank is communicated with a water injection vacuum pump through a pipeline, the water injection vacuum pump is communicated with a second ammonia water tank, and the non-condensed ammonia gas discharged by the second condenser is communicated with an ammonia gas inlet on the side surface of the water injection vacuum pump; dissolving ammonia gas by water in a water tank for recovery; the water in the water jet vacuum pump is extracted from the water tank and is jetted to the second ammonia water tank by high-speed jet, so that the negative pressure formed around the high-speed jet is utilized to ensure that an ammonia gas inlet on the side surface of the water jet vacuum pump is vacuumized, and further uncondensed ammonia gas discharged by the second condenser is sucked, the contact area and the contact probability of the ammonia gas and the water are greatly increased, and the ammonia gas is very easy to dissolve in cold water, so that the ammonia water with a certain concentration is prepared in the second ammonia water tank.
Furthermore, the number of the preheaters is two, and the two preheaters are respectively a first preheater and a second preheater;
the uncondensed ammonia-containing steam of the falling film evaporator exchanges heat through a first preheater and enters a second condenser; the first ammonia water tank is also communicated with the first preheater and is used for collecting ammonia water flowing out of the first preheater;
and the non-condensed steam in the first-stage evaporator and the second-stage evaporator reaches the non-condensed steam cooler after being subjected to heat exchange by the second preheater.
Further, the first-stage evaporator comprises a forced circulation first heat exchanger, a forced circulation second heat exchanger, a first-stage forced evaporation chamber and a first-stage circulating pump; the bottom end of the first-stage forced evaporation chamber is communicated with the top end of the first heat exchanger tube pass through a pipeline, the bottom end of the first heat exchanger tube pass is communicated with the bottom end of the second heat exchanger tube pass through a pipeline, the first-stage circulating pump is arranged on a communicating pipeline between the bottom end of the first heat exchanger tube pass and the bottom end of the second heat exchanger tube pass, and the top end of the second heat exchanger tube pass is communicated with the first-stage forced evaporation chamber;
the second-stage evaporator comprises a forced circulation third heat exchanger, a second-stage forced evaporation chamber and a second-stage circulating pump; the bottom end of the second-stage forced evaporation chamber is communicated with the bottom end of the tube pass of the third heat exchanger through a pipeline, a second-stage circulating pump is arranged on a communication pipeline between the bottom end of the second-stage forced evaporation chamber and the bottom end of the tube pass of the third heat exchanger, and the top end of the tube pass of the third heat exchanger is communicated with the second-stage forced evaporation chamber;
the falling film evaporator comprises a falling film evaporation chamber and a falling film heat exchanger; the bottom end of the tube pass of the falling film heat exchanger is communicated with the bottom end of the falling film evaporation chamber;
an ammonium sulfate wastewater discharge pipeline of the second preheater and a lime milk discharge pipeline of a lime milk feeding tank are converged and then communicated with a primary forced evaporation chamber, the primary forced evaporation chamber is communicated with a secondary forced evaporation chamber through a pipeline, and the secondary forced evaporation chamber is communicated with a filter through a pipeline;
the ammonia-containing steam outlet of the primary forced evaporation chamber and the ammonia-containing steam outlet of the secondary forced evaporation chamber are both communicated with the inlet of the shell pass of the falling film heat exchanger, and the liquid outlet of the shell pass of the falling film heat exchanger is communicated with the first ammonia water tank through a pipeline.
In order to prevent the ammonia-containing steam in the secondary forced evaporation chamber from directly flowing into the shell pass of the falling film heat exchanger and possibly causing bumping to cause material rushing out, the indoor volume of the primary forced evaporation chamber is larger than the indoor volume of the secondary forced evaporation chamber, an ammonia-containing steam outlet of the secondary forced evaporation chamber is communicated with the primary forced evaporation chamber through a pipeline, and an ammonia-containing steam outlet of the primary forced evaporation chamber is communicated with an inlet of the shell pass of the falling film heat exchanger through a pipeline; therefore, the larger space in the first-stage forced evaporation chamber can be utilized to reduce the pressure of the ammonia-containing steam output by the second-stage forced evaporation chamber, and the falling film heat exchanger is prevented from bumping.
Further, the top end of the falling film evaporation chamber is communicated with an inlet of a steam compressor through a pipeline; the outlet of the steam compressor is respectively communicated with the inlet of the first heat exchanger shell pass, the inlet of the second heat exchanger shell pass and the inlet of the third heat exchanger shell pass through pipelines;
and condensed water discharged from the first preheater, the non-condensing cooler, the shell pass liquid outlet of the first heat exchanger, the shell pass liquid outlet of the second heat exchanger and the shell pass liquid outlet of the third heat exchanger is communicated with the tube pass of the falling film heat exchanger through pipelines.
The utility model also provides an ammonium sulfate waste water MVR evaporation deamination treatment process, including following step:
1) preheating ammonium sulfate wastewater: conveying the ammonium sulfate wastewater to a preheater for preheating;
2) mixing: lime milk is conveyed to be converged with the preheated ammonium sulfate wastewater;
3) first-stage forced circulation evaporation: the mixed solution generated by the reaction of the ammonium sulfate wastewater and the lime milk after the confluence enters a first-stage forced evaporation chamber, then enters a tube pass of a first heat exchanger for heating, is pumped into a tube pass of a second heat exchanger through a first-stage circulating pump for continuous heating, and then returns to the first-stage forced evaporation chamber for evaporation to form concentrated solution containing calcium sulfate crystals and ammonia-containing steam;
wherein, a part of concentrated solution in the first-stage forced evaporation chamber is continuously pumped into the second-stage forced evaporation chamber for continuous evaporation, and the other part of concentrated solution continuously circulates among the first heat exchanger, the second heat exchanger and the first-stage forced evaporation chamber through the first-stage circulating pump;
4) secondary forced circulation evaporation: the temperature in the second-stage forced evaporation chamber is higher than that in the first-stage forced evaporation chamber, the concentrated solution entering the second-stage forced evaporation chamber enters the tube side of the third heat exchanger through a second-stage circulating pump to be heated, and then the concentrated solution returns to the second-stage forced evaporation chamber to be evaporated, so that concentrated solution containing calcium sulfate crystals and ammonia-containing steam are formed;
wherein, one part of the concentrated solution in the second-stage forced evaporation chamber enters a filter for solid-liquid separation to form deamination water and calcium sulfate crystals, and the other part of the concentrated solution continuously circulates between the third heat exchanger and the second-stage forced evaporation chamber through a second-stage circulating pump;
5) condensation of ammonia-containing steam: the ammonia-containing steam in the primary forced evaporation chamber and the ammonia-containing steam in the secondary forced evaporation chamber enter the shell pass of the falling film heat exchanger and exchange heat with condensed water in the tube pass of the falling film heat exchanger to form ammonia water and ammonia gas, and the condensed water in the tube pass of the falling film heat exchanger is heated and evaporated and then enters the falling film evaporation chamber to be separated to form pure steam;
ammonia water condensed in the shell pass of the falling film heat exchanger enters a first ammonia water tank; the method comprises the following steps that uncondensed ammonia-containing steam discharged from the shell pass of the falling film heat exchanger enters a first preheater for condensation to form ammonia water and uncondensed ammonia gas, the ammonia water discharged from the first preheater enters a first ammonia water tank, the uncondensed ammonia gas enters a second condenser to form ammonia water, and then the ammonia water enters a second ammonia water tank;
the vapor generated in the falling film evaporation chamber is introduced to a vapor compressor for compression, and the compressed vapor is introduced to the shell side of the first heat exchanger, the shell side of the second heat exchanger and the shell side of the third heat exchanger by the vapor compressor;
and the condensed water discharged by the shell pass of the first heat exchanger, the shell pass of the second heat exchanger and the shell pass of the third heat exchanger is introduced into the tube pass of the falling film heat exchanger so as to supplement the water evaporated from the falling film evaporation chamber.
Further, the ammonium sulfate wastewater is sequentially conveyed to a first preheater and a second preheater for heat exchange;
the non-condensed steam discharged by the shell pass of the first heat exchanger, the shell pass of the second heat exchanger and the shell pass of the third heat exchanger reaches the non-condensed steam cooler after heat exchange by the second preheater and provides a heat source for the second preheater, and the second preheater and the non-condensed steam cooler condense the steam carried in the non-condensed steam into condensed water and simultaneously introduce the condensed water into the tube pass of the falling film heat exchanger.
Furthermore, after the ammonia water in the first ammonia water tank is cooled by the first condenser, one part of the ammonia water is led to the total ammonia water tank or discharged, and the other part of the ammonia water is pumped into the second ammonia water tank to prepare the ammonia water.
The utility model has the advantages that: the utility model discloses an ammonium sulfate waste water MVR evaporation deamination processing system, it utilizes lime cream and ammonium sulfate reaction, and the calcium sulfate that produces can be used to building materials production such as cement, and ammonia gas generates the aqueous ammonia retrieval and utilization production, adopts forced circulation low temperature evaporative concentration simultaneously, has solved the interior calcium scale deposit problem of evaporating chamber; the falling film evaporator is used for absorbing ammonia steam heat to generate pure steam, and the pure steam enters the steam compressor, so that the heat is recycled, the process is a brand-new green and environment-friendly process which is very suitable for wet smelting, the treatment cost of ammonium sulfate wastewater can be greatly reduced, and the whole system is high in energy utilization rate, energy-saving and environment-friendly.
Drawings
The present invention will be further explained with reference to the drawings and examples.
FIG. 1 is the schematic diagram of the MVR evaporation deamination treatment system for ammonium sulfate wastewater of the utility model.
In the figure: 1. the system comprises a first-stage evaporator, 1-1, a first heat exchanger, 1-2, a second heat exchanger, 1-3, a first-stage forced evaporation chamber, 1-4 and a first-stage circulating pump;
2. 2-1 parts of a second-stage evaporator, 2-2 parts of a third heat exchanger, 2-2 parts of a second-stage forced evaporation chamber, 2-3 parts of a second-stage circulating pump;
3. 3-1 parts of a falling film evaporator, 3-2 parts of a falling film evaporation chamber and 3-2 parts of a falling film heat exchanger;
4. a wastewater feeding tank 5, a lime milk feeding tank;
6. a first preheater 7 and a second preheater;
8. a filter 9, a vapor compressor;
10. a first ammonia water tank 11 and a second condenser;
12. a second ammonia water tank 13 and a first condenser;
14. total ammonia water tank, 15, circulating condenser;
16. a vacuum pump, 17, a non-condensing cooler;
18. a water tank 19 and a mother liquor tank;
20. a water jet vacuum pump.
Detailed Description
The present invention will now be described in further detail with reference to the accompanying drawings. The drawings are simplified schematic drawings, which illustrate the basic structure of the invention only in a schematic way, and thus show only the components that are relevant to the invention, and the directions and references (e.g., upper, lower, left, right, etc.) may be used only to help describe the features in the drawings. The following detailed description is, therefore, not to be taken in a limiting sense, and the scope of the claimed subject matter is defined only by the appended claims and equivalents thereof.
Example 1
As shown in figure 1, an ammonium sulfate waste water MVR evaporation deamination processing system includes:
a wastewater feed tank 4 for holding ammonium sulfate wastewater;
the preheater is communicated with the wastewater feeding tank 4 through a pipeline and is used for preheating the ammonium sulfate wastewater;
a lime milk feed tank 5 for containing lime milk;
the primary evaporator 1 is used for carrying out primary evaporation on mixed liquid generated by the reaction of the ammonium sulfate wastewater and the lime milk to form concentrated liquid containing calcium sulfate crystals and ammonia-containing steam, wherein the primary evaporator 1 is a forced circulation evaporator;
the secondary evaporator 2 is used for carrying out secondary evaporation on the concentrated solution from the primary evaporator 1 to form concentrated solution containing calcium sulfate crystals and ammonia-containing steam, wherein the secondary evaporator 2 is a forced circulation evaporator;
the falling-film evaporator 3 is used for condensing ammonia-containing steam in the primary evaporator 1 and the secondary evaporator 2 to form ammonia water, ammonia gas and steam;
the filter 8 is used for carrying out filter-pressing separation on the concentrated solution in the secondary evaporator 2 to form ammonia water and calcium sulfate crystals;
and the vapor compressor 9 is used for compressing vapor in the falling-film evaporator 3 and then delivering the compressed vapor to the first-stage evaporator 1 and the second-stage evaporator 2 for heat supply.
The falling-film evaporator 3 is communicated with a first ammonia water tank 10 through a pipeline, and the first ammonia water tank 10 is used for collecting ammonia water discharged by the falling-film evaporator 3.
The falling-film evaporator 3 is also communicated with a second condenser 11 through a pipeline, the second condenser 11 is communicated with a second ammonia water tank 12, and the second condenser 11 is used for condensing the uncondensed ammonia-containing steam from the falling-film evaporator 3 into ammonia water;
the second ammonia tank 12 is used for collecting the condensed ammonia water flowing out of the second condenser 11 to form ammonia water with a certain concentration.
The aqueous ammonia in the first aqueous ammonia jar 10 gets into total aqueous ammonia jar 14 behind first condenser 13, the pipeline and the second aqueous ammonia jar 12 intercommunication of intercommunication between first condenser 13 and the total aqueous ammonia jar 14, the intercommunication has circulating condenser 15 on the second aqueous ammonia jar 12, the aqueous ammonia in the second aqueous ammonia jar 12 gets back to in the second aqueous ammonia jar 12 again after circulating condenser 15 cools off, all be provided with the aqueous ammonia discharge port on total aqueous ammonia jar 14 and the second aqueous ammonia jar 12.
The primary evaporator 1 and the secondary evaporator 2 are communicated with a pressure stabilizing device, the pressure stabilizing device comprises a vacuum pump 16, a regulating valve and a non-condensing cooler 17, the vacuum pump 16 is communicated with the non-condensing cooler 17 through a pipeline, the non-condensing cooler 17 is used for cooling non-condensing steam from the primary evaporator 1 and the secondary evaporator 2, steam carried in the non-condensing steam is condensed into condensed water, and the pressure is stabilized at a designed working condition, and the regulating valve is arranged on a communication pipeline between the vacuum pump 16 and the primary evaporator 1 and the secondary evaporator 2;
therefore, the non-condensed steam in the first-stage evaporator 1 and the non-condensed steam in the second-stage evaporator 2 can be discharged in real time through the pressure stabilizing device, the heat exchange efficiency of the first-stage evaporator 1 and the heat exchange efficiency of the second-stage evaporator 2 are ensured, and the evaporation temperature of the first-stage evaporator 1 and the evaporation temperature of the second-stage evaporator 2 are ensured to be within the process requirement range.
The vacuum pump 16 is communicated with a water tank 18 through a pipeline, water in the water tank 16 is communicated with a water injection vacuum pump 20 through a pipeline, the water injection vacuum pump 20 is communicated with a second ammonia water tank 12, and uncondensed ammonia gas discharged by the second condenser 11 is communicated with an ammonia gas inlet on the side surface of the water injection vacuum pump 20; the purpose of the method is as follows; first, ammonia gas that is not condensed is recovered by water in the water tank 18; secondly, the water jet vacuum pump 20 can extract water in the water tank 16 or the second ammonia water tank 12 and jet the water to the second ammonia water tank 12 by high-speed jet flow, so that the negative pressure formed around the high-speed jet flow is utilized to enable an ammonia gas inlet on the side surface of the water jet vacuum pump 20 to generate vacuum, further the uncondensed ammonia gas discharged from the second condenser 11 is sucked, the contact area and the contact probability of the ammonia gas and the water are greatly increased, and the characteristic that the ammonia gas is very easy to dissolve in cold water is utilized, so that the ammonia water with a certain concentration is prepared in the second ammonia water tank 12.
The number of the preheaters is two, and the two preheaters are respectively a first preheater 6 and a second preheater 7;
the uncondensed ammonia-containing steam of the falling-film evaporator 3 enters a second condenser 11 after being subjected to heat exchange by a first preheater 6; the first ammonia water tank 10 is also communicated with the first preheater 6 and is used for collecting ammonia water flowing out of the first preheater 6;
the non-condensed steam in the first-stage evaporator 1 and the second-stage evaporator 2 is subjected to heat exchange by the second preheater 7 and then reaches the non-condensed steam cooler 17.
The first-stage evaporator 1 comprises a forced circulation first heat exchanger 1-1, a forced circulation second heat exchanger 1-2, a first-stage forced evaporation chamber 1-3 and a first-stage circulating pump 1-4; the bottom end of the first-stage forced evaporation chamber 1-3 is communicated with the top end of the tube side of the first heat exchanger 1-1 through a pipeline, the bottom end of the tube side of the first heat exchanger 1-1 is communicated with the bottom end of the tube side of the second heat exchanger 1-2 through a pipeline, a first-stage circulating pump 1-4 is arranged on a communicating pipeline between the bottom end of the tube side of the first heat exchanger 1-1 and the bottom end of the tube side of the second heat exchanger 1-2, and the top end of the tube side of the second heat exchanger 1-2 is communicated with the first-stage forced evaporation chamber 1-3;
the second-stage evaporator 2 comprises a forced circulation third heat exchanger 2-1, a second-stage forced evaporation chamber 2-2 and a second-stage circulation pump 2-3; the bottom end of the second-stage forced evaporation chamber 2-2 is communicated with the bottom end of the tube side of the third heat exchanger 2-1 through a pipeline, a second-stage circulating pump 2-3 is arranged on a communicating pipeline between the bottom end of the second-stage forced evaporation chamber 2-2 and the bottom end of the tube side of the third heat exchanger 2-1, and the top end of the tube side of the third heat exchanger 2-1 is communicated with the second-stage forced evaporation chamber 2-2;
the falling film evaporator 3 comprises a falling film evaporation chamber 3-1 and a falling film heat exchanger 3-2; the bottom end of the tube pass of the falling film heat exchanger 3-2 is communicated with the bottom end of the falling film evaporation chamber 3-1;
an ammonium sulfate wastewater discharge pipeline of the second preheater 7 and a lime milk discharge pipeline of the lime milk feeding tank 5 are converged and then communicated with a primary forced evaporation chamber 1-3, the primary forced evaporation chamber 1-3 is communicated with a secondary forced evaporation chamber 2-2 through a pipeline, and the secondary forced evaporation chamber 2-2 is communicated with a filter 8 through a pipeline; specifically, the filter 8 is communicated with a mother liquor tank 19, and the mother liquor tank 19 is used for containing the deammoniated water discharged by the filter 8.
An ammonia-containing steam outlet of the primary forced evaporation chamber 1-3 and an ammonia-containing steam outlet of the secondary forced evaporation chamber 2-2 are both communicated with an inlet of a shell pass of the falling film heat exchanger 3-2, and a liquid outlet of the shell pass of the falling film heat exchanger 3-2 is communicated with the first ammonia water tank 10 through a pipeline.
The indoor volume of the first-stage forced evaporation chamber 1-3 is larger than the indoor volume of the second-stage forced evaporation chamber 2-2, an ammonia-containing steam outlet of the second-stage forced evaporation chamber 2-2 is communicated with the first-stage forced evaporation chamber 1-3 through a pipeline, and an ammonia-containing steam outlet of the first-stage forced evaporation chamber 1-3 is communicated with an inlet of a shell pass of the falling film heat exchanger 3-2 through a pipeline; therefore, the larger space in the first-stage forced evaporation chamber 1-3 can be utilized to reduce the pressure of the ammonia-containing steam output by the second-stage forced evaporation chamber 2-2, and the falling film heat exchanger 3-2 is prevented from bumping.
The top end of the falling film evaporation chamber 3-1 is communicated with an inlet of a vapor compressor 9 through a pipeline; an outlet of the vapor compressor 9 is respectively communicated with an inlet of a shell pass of the first heat exchanger 1-1, an inlet of a shell pass of the second heat exchanger 1-2 and an inlet of a shell pass of the third heat exchanger 2-1 through pipelines;
and condensed water discharged from the first preheater 6, the non-condensing cooler 17, the shell pass liquid outlet of the first heat exchanger 1-1, the shell pass liquid outlet of the second heat exchanger 1-2 and the shell pass liquid outlet of the third heat exchanger 2-1 is communicated with the tube pass of the falling film heat exchanger 3-2 through pipelines.
The principle and the advantage of the ammonium sulfate waste water MVR evaporation deamination processing apparatus in this embodiment are explained as follows:
the first-stage evaporator 1 adopts two heat exchangers, namely a first heat exchanger 1-1 and a second heat exchanger 1-2, and aims to: the primary evaporator 1 is used as a main evaporator, the heat exchange area is large, and the arrangement of the two heat exchangers can reduce the flow rate of the primary circulating pump 1-4 by 50% under the condition that the flow rate in the tube pass of the heat exchangers is not changed, so that the electricity is saved by 50%; and the secondary evaporator 2 only adopts a third heat exchanger 2-1, and aims to: and the deamination is ensured to be thorough under the condition of saving investment.
The purified water vapor generated in the falling film evaporation chamber 3-1 is introduced into a vapor compressor 9 to be compressed, and then heat sources are provided for the shell pass of the first heat exchanger 1-1, the shell pass of the second heat exchanger 1-2 and the shell pass of the third heat exchanger 2-1 again, so that the heat is recycled, and the energy conservation and environmental protection are realized; condensed water generated after heat exchange of the first preheater 6, the non-condensing cooler 17, the first heat exchanger 1-1 shell pass, the second heat exchanger 1-2 shell pass and the third heat exchanger 2-1 shell pass is introduced into the tube pass of the falling film heat exchanger 3-2 so as to supplement water evaporated in the falling film evaporation chamber 3-1 and recycle the condensed water;
thirdly, uncondensed ammonia-containing steam discharged from the shell pass of the falling film heat exchanger 3-2 firstly passes through the first preheater (6) to exchange heat with the ammonium sulfate wastewater which also passes through the first preheater 6, so that the temperature of the ammonium sulfate wastewater can be increased, and the uncondensed ammonia-containing steam discharged from the shell pass of the falling film heat exchanger 3-2 can be condensed, thereby improving the energy utilization rate;
the noncondensable gas discharged from the first heat exchanger 1-1, the second heat exchanger 1-2 and the third heat exchanger 2-1 through the vacuum pump 16 passes through the second preheater 7 to exchange heat with the ammonium sulfate wastewater which also passes through the second preheater 7, so that the heat exchange efficiency of the first heat exchanger 1-1, the second heat exchanger 1-2 and the third heat exchanger 2-1 can be ensured, and the temperature of the ammonium sulfate wastewater can be increased again.
Fourthly, ammonia water formed by condensation in the shell pass of the falling film heat exchanger 3-2 enters a first ammonia water tank 10 to be collected, ammonia water generated by condensation of uncondensed ammonia-containing steam discharged from the shell pass of the falling film heat exchanger 3-2 sequentially passes through a first preheater 6 and a second condenser 11 also enters the first ammonia water tank 10 to be collected, part of the ammonia water in the first ammonia water tank 10 is cooled by a first condenser 13 and then is led to a total ammonia water tank 14 or discharged, and the other part of the ammonia water is pumped into a second ammonia water tank 12 to prepare ammonia water; so as to recycle the ammonia water.
Fifthly, the utility model discloses utilize lime and ammonium sulfate reaction, the calcium sulfate of production can be used to building materials production such as cement, and the ammonia generates ammonia water retrieval and utilization production, and adopts the combination of one-level evaporimeter 1 and second grade evaporimeter 2 can realize forced circulation low temperature evaporative concentration, has solved the interior calcium scale deposit problem of evaporating chamber when guaranteeing that the deamination is thorough.
The utility model also provides an ammonium sulfate waste water MVR evaporation deamination treatment process, including following step:
1) preheating ammonium sulfate wastewater: conveying the ammonium sulfate wastewater to a first preheater 6 for primary preheating, and raising the temperature of the ammonium sulfate wastewater to 43 +/-2 ℃; then the wastewater reaches a second preheater 7 for preheating again, and the temperature of the ammonium sulfate wastewater is raised to 65 +/-2 ℃;
2) mixing: lime milk is conveyed to be converged with the preheated ammonium sulfate wastewater;
3) first-stage forced circulation evaporation: the mixed solution generated by the reaction of the ammonium sulfate wastewater and the lime milk after the confluence enters a first-stage forced evaporation chamber 1-3, then enters a tube pass of a first heat exchanger 1-1 for heating, is pumped into a tube pass of a second heat exchanger 1-2 through a first-stage circulating pump 1-4 for continuous heating, and then returns to the first-stage forced evaporation chamber 1-3 for evaporation to form concentrated solution containing calcium sulfate crystals and ammonia-containing steam, wherein the temperature of the concentrated solution in the first-stage forced evaporation chamber 1-3 is 65 +/-2 ℃;
wherein, a part of concentrated solution in the first-stage forced evaporation chamber 1-3 is continuously pumped into the second-stage forced evaporation chamber 2-2 for continuous evaporation, and the other part of concentrated solution is continuously circulated among the first heat exchanger 1-1, the second heat exchanger 1-2 and the first-stage forced evaporation chamber 1-3 through a first-stage circulating pump 1-4;
4) secondary forced circulation evaporation: the concentrated solution entering the second-stage forced evaporation chamber 2-2 enters the tube pass of the third heat exchanger 2-1 through a second-stage circulating pump 2-3 to be heated, and then returns to the second-stage forced evaporation chamber 2-2 to be evaporated to form concentrated solution containing calcium sulfate crystals and ammonia-containing steam, wherein the temperature of the concentrated solution in the second-stage forced evaporation chamber 2-2 is 67 +/-2 ℃;
wherein, one part of the concentrated solution in the second-stage forced evaporation chamber 2-2 enters the filter 8 to be subjected to solid-liquid separation to form deamination water and calcium sulfate crystals, the other part of the concentrated solution is continuously circulated between the third heat exchanger 2-1 and the second-stage forced evaporation chamber 2-2 through the second-stage circulating pump 2-3, the deamination water discharged from the filter 8 is conveyed to the mother liquor tank 19 so as to be convenient for recycling production, and the calcium sulfate crystals separated by the filter 8 are recycled;
5) condensation of ammonia-containing steam: the ammonia-containing steam in the primary forced evaporation chamber 1-3 and the ammonia-containing steam in the secondary forced evaporation chamber 2-2 enter the shell pass of the falling film heat exchanger 3-2 and exchange heat with condensed water in the tube pass of the falling film heat exchanger 3-2 to form ammonia water and ammonia gas, the condensed water in the tube pass of the falling film heat exchanger 3-2 is heated and evaporated, and then enters the falling film evaporation chamber 3-1 to be separated to form pure steam;
ammonia water condensed in the shell pass of the falling film heat exchanger 3-2 enters a first ammonia water tank 10; the uncondensed ammonia-containing steam discharged from the shell pass of the falling film heat exchanger 3-2 enters a first preheater 6 for condensation to form ammonia water and uncondensed ammonia gas, the ammonia water discharged from the first preheater 6 enters a first ammonia water tank 10, the uncondensed ammonia gas enters a second condenser 12 to form ammonia water and then enters a second ammonia water tank 12, and meanwhile, the uncondensed ammonia-containing steam discharged from the shell pass of the falling film heat exchanger 3-2 provides a heat source for the first preheater 6;
the non-condensed steam discharged by the shell pass of the first heat exchanger 1-1, the shell pass of the second heat exchanger 1-2 and the shell pass of the third heat exchanger 2-1 is subjected to heat exchange by the second preheater 7 under the action of a vacuum pump 16 and then reaches the non-condensed steam cooler 17, a heat source is provided for the second preheater 7, the non-condensed steam discharged by the non-condensed steam cooler 17 is cooled by water in a water tank 18 through a circulating condenser 15, and then ammonia mixed in the non-condensed steam is recovered so as to be discharged conveniently;
steam generated in the falling film evaporation chamber 3-1 is introduced to a steam compressor 9 for compression, and the compressed steam is introduced to the shell side of the first heat exchanger 1-1, the shell side of the second heat exchanger 1-2 and the shell side of the third heat exchanger 2-1 by the steam compressor 9;
wherein, condensed water discharged by the second preheater 7, the non-condensing cooler 17, the shell pass of the first heat exchanger 1-1, the shell pass of the second heat exchanger 1-2 and the shell pass of the third heat exchanger 2-1 is introduced into the tube pass of the falling film heat exchanger 3-2 to supplement water evaporated by the falling film evaporation chamber 3-1
After being cooled by the first condenser 13, part of the ammonia water in the first ammonia water tank 10 is led to the total ammonia water tank 14 or discharged, the other part of the ammonia water is pumped into the second ammonia water tank 12, and the liquid in the second ammonia water tank 12 is cooled by the circulating condenser 15 and then returns to the second ammonia water tank 12 again so as to prepare ammonia water; the second ammonia tank 12 and the total ammonia tank 14 periodically discharge a part of the ammonia.
In light of the foregoing, it will be apparent to those skilled in the art from this disclosure that various changes and modifications can be made without departing from the spirit and scope of the invention. The technical scope of the present invention is not limited to the content of the specification, and must be determined according to the scope of the claims.
Claims (10)
1. The utility model provides an ammonium sulfate waste water MVR evaporation deamination processing system which characterized in that: the method comprises the following steps:
a wastewater feed tank (4) for containing ammonium sulfate wastewater;
the preheater is communicated with the wastewater feeding tank (4) through a pipeline and is used for preheating the ammonium sulfate wastewater;
a lime milk feed tank (5) for containing lime milk;
the system comprises a primary evaporator (1), ammonium sulfate wastewater in a wastewater feeding tank (4) is preheated by a preheater and then is converged with lime milk, and then enters the primary evaporator (1), the primary evaporator (1) is used for carrying out primary evaporation on mixed liquid generated by the reaction of the ammonium sulfate wastewater and the lime milk to form concentrated liquid containing calcium sulfate crystals and ammonia-containing steam, and the primary evaporator (1) is a forced circulation evaporator;
the secondary evaporator (2) is used for carrying out secondary evaporation on the concentrated solution from the primary evaporator (1) to form concentrated solution containing calcium sulfate crystals and ammonia-containing steam, wherein the secondary evaporator (2) is a forced circulation evaporator;
the falling-film evaporator (3) is used for condensing ammonia-containing steam in the primary evaporator (1) and the secondary evaporator (2) to form ammonia water, ammonia gas and steam;
the filter (8) is used for carrying out filter-pressing separation on the concentrated solution in the secondary evaporator (2) to form ammonia water and calcium sulfate crystals;
and the vapor compressor (9) is used for compressing vapor in the falling film evaporator (3) and then conveying the compressed vapor to the first-stage evaporator (1) and the second-stage evaporator (2) for supplying heat.
2. The ammonium sulfate waste water MVR evaporation deamination processing system of claim 1, wherein: the falling-film evaporator (3) is communicated with a first ammonia water tank (10) through a pipeline, and the first ammonia water tank (10) is used for collecting ammonia water discharged by the falling-film evaporator (3).
3. The ammonium sulfate waste water MVR evaporation deamination processing system of claim 2, wherein: the falling-film evaporator (3) is also communicated with a second condenser (11) through a pipeline, the second condenser (11) is communicated with a second ammonia water tank (12), and the second condenser (11) is used for condensing uncondensed ammonia-containing steam from the falling-film evaporator (3) into ammonia water;
the second ammonia water tank (12) is used for collecting condensed ammonia water flowing out of the second condenser (11) to form ammonia water with a certain concentration.
4. The ammonium sulfate waste water MVR evaporation deamination processing system of claim 3, wherein: the ammonia water in the first ammonia water jar (10) gets into total ammonia water jar (14) behind first condenser (13), the pipeline and second ammonia water jar (12) intercommunication of intercommunication between first condenser (13) and total ammonia water jar (14), the intercommunication has circulating condenser (15) on second ammonia water jar (12), the ammonia water in the second ammonia water jar (12) gets back to in second ammonia water jar (12) again after circulating condenser (15) cooling, all be provided with the aqueous ammonia discharge port on total ammonia water jar (14) and second ammonia water jar (12).
5. The ammonium sulfate waste water MVR evaporation deamination processing system of claim 4, wherein: one-level evaporimeter (1) and second grade evaporimeter (2) and voltage regulator device intercommunication, voltage regulator device includes vacuum pump (16), governing valve and non-condensing condenser (17), vacuum pump (16) are through pipeline and non-condensing condenser (17) intercommunication, non-condensing condenser (17) are arranged in the cooling to come from the non-condensing of one-level evaporimeter (1) and second grade evaporimeter (2), make the steam condensation that smugglies secretly among the non-condensing become the comdenstion water to make pressure stable in the design condition, the governing valve configuration is on the communicating pipe between vacuum pump (16) and one-level evaporimeter (1) and second grade evaporimeter (2).
6. The ammonium sulfate waste water MVR evaporation deamination processing system of claim 5, wherein: the vacuum pump (16) is communicated with a water tank (18) through a pipeline, water in the water tank (18) is communicated with a water injection vacuum pump (20) through a pipeline, the water injection vacuum pump (20) is communicated with a second ammonia water tank (12), and uncondensed ammonia gas discharged by the second condenser (11) is communicated with an ammonia gas inlet on the side surface of the water injection vacuum pump (20).
7. The ammonium sulfate waste water MVR evaporation deamination processing system of claim 5, wherein: the number of the preheaters is two, and the two preheaters are respectively a first preheater (6) and a second preheater (7);
the uncondensed ammonia-containing steam of the falling film evaporator (3) enters a second condenser (11) after heat exchange by a first preheater (6); the first ammonia water tank (10) is also communicated with the first preheater (6) and is used for collecting ammonia water flowing out of the first preheater (6);
the non-condensed steam in the first-stage evaporator (1) and the non-condensed steam in the second-stage evaporator (2) reach the non-condensed steam cooler (17) after being subjected to heat exchange by the second preheater (7).
8. The ammonium sulfate waste water MVR evaporation deamination processing system of claim 7, wherein: the primary evaporator (1) comprises a forced circulation first heat exchanger (1-1), a forced circulation second heat exchanger (1-2), a primary forced evaporation chamber (1-3) and a primary circulating pump (1-4); the bottom end of the first-stage forced evaporation chamber (1-3) is communicated with the top end of the tube side of the first heat exchanger (1-1) through a pipeline, the bottom end of the tube side of the first heat exchanger (1-1) is communicated with the bottom end of the tube side of the second heat exchanger (1-2) through a pipeline, a first-stage circulating pump (1-4) is arranged on a communicating pipeline between the bottom end of the tube side of the first heat exchanger (1-1) and the bottom end of the tube side of the second heat exchanger (1-2), and the top end of the tube side of the second heat exchanger (1-2) is communicated with the first-stage forced evaporation chamber (1-3);
the secondary evaporator (2) comprises a forced circulation third heat exchanger (2-1), a secondary forced evaporation chamber (2-2) and a secondary circulation pump (2-3); the bottom end of the second-stage forced evaporation chamber (2-2) is communicated with the bottom end of the tube side of the third heat exchanger (2-1) through a pipeline, a second-stage circulating pump (2-3) is arranged on a communicating pipeline between the bottom end of the second-stage forced evaporation chamber (2-2) and the bottom end of the tube side of the third heat exchanger (2-1), and the top end of the tube side of the third heat exchanger (2-1) is communicated with the second-stage forced evaporation chamber (2-2);
the falling film evaporator (3) comprises a falling film evaporation chamber (3-1) and a falling film heat exchanger (3-2); the tube pass bottom end of the falling film heat exchanger (3-2) is communicated with the bottom end of the falling film evaporation chamber (3-1);
an ammonium sulfate wastewater discharge pipeline of the second preheater (7) and a lime milk discharge pipeline of the lime milk feeding tank (5) are converged and then communicated with a primary forced evaporation chamber (1-3), the primary forced evaporation chamber (1-3) is communicated with a secondary forced evaporation chamber (2-2) through a pipeline, and the secondary forced evaporation chamber (2-2) is communicated with a filter (8) through a pipeline;
an ammonia-containing steam outlet of the primary forced evaporation chamber (1-3) and an ammonia-containing steam outlet of the secondary forced evaporation chamber (2-2) are both communicated with an inlet of a shell pass of the falling film heat exchanger (3-2), and a liquid outlet of the shell pass of the falling film heat exchanger (3-2) is communicated with the first ammonia tank (10) through a pipeline.
9. The ammonium sulfate waste water MVR evaporation deamination processing system of claim 8, wherein: the indoor volume of the primary forced evaporation chamber (1-3) is larger than the indoor volume of the secondary forced evaporation chamber (2-2), an ammonia-containing steam outlet of the secondary forced evaporation chamber (2-2) is communicated with the primary forced evaporation chamber (1-3), and an ammonia-containing steam outlet of the primary forced evaporation chamber (1-3) is communicated with an inlet of a shell side of the falling film heat exchanger (3-2) through a pipeline.
10. The ammonium sulfate waste water MVR evaporation deamination processing system of claim 9, wherein: the top end of the falling film evaporation chamber (3-1) is communicated with an inlet of a vapor compressor (9) through a pipeline; an outlet of the vapor compressor (9) is respectively communicated with an inlet of a shell pass of the first heat exchanger (1-1), an inlet of a shell pass of the second heat exchanger (1-2) and an inlet of a shell pass of the third heat exchanger (2-1) through pipelines;
and condensed water discharged from the first preheater (6), the non-condensing cooler (17), the shell pass liquid outlet of the first heat exchanger (1-1), the shell pass liquid outlet of the second heat exchanger (1-2) and the shell pass liquid outlet of the third heat exchanger (2-1) is communicated with the tube pass of the falling film heat exchanger (3-2) through pipelines.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110342720A (en) * | 2019-08-19 | 2019-10-18 | 常州中源工程技术有限公司 | Ammonium sulfate waste water MVR evaporates deamination processing system and its treatment process |
| CN113735362A (en) * | 2021-10-08 | 2021-12-03 | 江苏瑞升华能源科技有限公司 | Ternary or quaternary precursor deamination wastewater MVR treatment system and process |
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2019
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110342720A (en) * | 2019-08-19 | 2019-10-18 | 常州中源工程技术有限公司 | Ammonium sulfate waste water MVR evaporates deamination processing system and its treatment process |
| CN113735362A (en) * | 2021-10-08 | 2021-12-03 | 江苏瑞升华能源科技有限公司 | Ternary or quaternary precursor deamination wastewater MVR treatment system and process |
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