CN112174413A - Method for realizing zero discharge of MVR evaporation mother liquor - Google Patents
Method for realizing zero discharge of MVR evaporation mother liquor Download PDFInfo
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- CN112174413A CN112174413A CN202010904626.0A CN202010904626A CN112174413A CN 112174413 A CN112174413 A CN 112174413A CN 202010904626 A CN202010904626 A CN 202010904626A CN 112174413 A CN112174413 A CN 112174413A
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- 238000001704 evaporation Methods 0.000 title claims abstract description 65
- 230000008020 evaporation Effects 0.000 title claims abstract description 65
- 239000012452 mother liquor Substances 0.000 title claims abstract description 48
- 238000000034 method Methods 0.000 title claims abstract description 26
- 238000010438 heat treatment Methods 0.000 claims abstract description 131
- 239000013078 crystal Substances 0.000 claims abstract description 8
- 150000003839 salts Chemical class 0.000 claims abstract description 8
- 238000004064 recycling Methods 0.000 claims abstract description 7
- 238000000926 separation method Methods 0.000 claims description 50
- 239000007788 liquid Substances 0.000 claims description 44
- 238000001035 drying Methods 0.000 claims description 18
- 238000007599 discharging Methods 0.000 claims description 8
- 239000000463 material Substances 0.000 claims description 8
- 239000007787 solid Substances 0.000 claims description 8
- 230000008719 thickening Effects 0.000 claims description 7
- 230000000694 effects Effects 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 9
- 230000007613 environmental effect Effects 0.000 abstract description 3
- 238000004065 wastewater treatment Methods 0.000 abstract description 2
- 239000003245 coal Substances 0.000 description 7
- 239000002351 wastewater Substances 0.000 description 7
- 239000000126 substance Substances 0.000 description 6
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 4
- 230000015556 catabolic process Effects 0.000 description 3
- 238000006731 degradation reaction Methods 0.000 description 3
- 230000009291 secondary effect Effects 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 229910000019 calcium carbonate Inorganic materials 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 230000009290 primary effect Effects 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 230000003301 hydrolyzing effect Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000020477 pH reduction Effects 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000012958 reprocessing Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 230000009293 tertiary effect Effects 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/043—Details
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
A method and a system for zero discharge of MVR evaporation mother liquor relate to the technical field of wastewater treatment, and the method comprises the following procedures: heating mother liquor, primary heating concentration, secondary heating concentration, tertiary heating concentration, crystal growth and post-treatment, the system comprises a preheater and a primary heating and separating system, the invention can process MVR evaporation mother liquor, the processed condensate water reaches the recycling standard, and the fine salt obtained after the processing can be directly discharged outside, thereby having obvious economic, social and environmental benefits.
Description
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to a zero discharge method of MVR evaporation mother liquor.
Background
Various waste water produced in the production process of coal chemical industry, organic waste water and high-salinity waste water are waste water which is difficult to treat in the water treatment industry. The existing methods for treating the coal chemical industry wastewater include various pretreatment methods such as an oil separation sedimentation tank, air floatation and the like, biochemical treatment methods such as hydrolytic acidification, anaerobic treatment and aerobic treatment, advanced oxidation advanced treatment methods such as ozone and electrocatalysis and the like, and the problems of the coal chemical industry wastewater cannot be completely solved. Meanwhile, the coal chemical industry is mostly located in water-deficient areas such as northwest China, so the concept of zero discharge of wastewater in the coal chemical industry is widely concerned. From 2004 to date, dozens of zero emission projects have been built and operated domestically. However, during the operation of the zero-emission device, the problem of reprocessing the evaporation mother liquor is mostly faced. The mother liquor has complex components, high concentration of pollutants and great difficulty in secondary evaporation treatment, becomes a difficult point and a pain point in the industry, and also hinders the development of zero emission in the coal chemical industry.
The MVR evaporation mother liquor has extremely complex components, belongs to refractory wastewater, high salt, high silicon and high COD, does not have a good method for removing the MVR evaporation mother liquor at present, and has the following methods applied to decrement at present:
1. the MVR evaporation mother liquor partially reflows to the original MVR evaporation system, although the method has certain decrement, the problem of the mother liquor cannot be thoroughly solved, the load of the system is increased, and the corrosion and heat exchange efficiency of the original MVR system are increased.
2. The drying method is directly adopted, and due to the large amount of the evaporation mother liquor and high drying investment and operation cost, few enterprises can afford the method.
Disclosure of Invention
Aiming at the defects in the prior art, one of the purposes of the invention is to provide a method for realizing zero emission of MVR evaporation mother liquor, which can realize the zero emission of the MVR evaporation mother liquor, can also realize that the final condensed liquid reaches the recycling standard, reduces the operation cost of enterprises and reduces the total pollutant emission amount, and the specific scheme is as follows:
a method for realizing zero emission of MVR evaporation mother liquor comprises the following steps:
heating mother liquor: the MVR evaporation mother liquor enters a preheater and is heated to 50-100 ℃ from normal temperature;
primary heating and concentrating: the heated mother liquor enters a first-effect heating chamber, evaporation concentration is carried out by utilizing raw steam, and secondary steam generated by first-effect evaporation is used as a heat source of a second-effect heating chamber after defoaming;
secondary heating and concentrating: the obtained first-effect concentrated solution enters a second-effect heating chamber for further evaporation and concentration, and tertiary steam generated by the second-effect evaporation is used as a heat source of a third-effect heating chamber after defoaming;
and (3) heating and concentrating for three times: the obtained two-effect concentrated solution enters a three-effect heating chamber for further evaporation and concentration, and the four times of steam generated by three-effect evaporation is cooled by a heat exchanger and reaches the recycling standard;
crystal growth: the obtained triple-effect concentrated solution enters a thickening chamber to carry out crystal growth;
and (3) post-treatment: and discharging the material from the thickening chamber, allowing the material to enter a centrifugal chamber for solid-liquid separation, allowing part of the separated liquid to circularly flow back to a three-effect heating chamber for further evaporation and concentration, allowing part of the separated liquid to flow back to a solid-liquid separation system for continuous solid-liquid separation, discharging the solid, allowing the finally separated liquid to enter drying equipment, and drying the liquid to obtain condensate.
Further, the heat source of the preheater is raw steam condensate in a one-effect heating chamber.
Further, in the primary heating concentration step and the secondary heating concentration step, secondary defoaming is performed during defoaming.
Further, in the steps of primary heating concentration, secondary heating concentration and tertiary heating concentration, the MVR evaporation mother liquor, the first-effect concentrated solution and the second-effect concentrated solution are separated by the separation chamber and then respectively enter the first-effect heating chamber, the second-effect heating chamber and the third-effect heating chamber.
Further, in the steps of the primary heating concentration, the secondary heating concentration and the tertiary heating concentration, the first-effect concentrated solution and the second-effect concentrated solution in the separation chamber can flow back to the first-effect heating chamber and the second-effect heating chamber corresponding to the previous unit or the second-effect heating chamber and the third-effect heating chamber corresponding to the next unit.
The invention also aims to provide a zero discharge system of MVR evaporation mother liquor, and the specific scheme is as follows:
the utility model provides a MVR evaporation mother liquor zero release system, the system includes the pre-heater, one imitates heating and piece-rate system, two imitates heating and piece-rate system, three imitate heating and piece-rate system, viscous crude room, centrifugal chamber, solid-liquid separation system and drying equipment, one effect heating and piece-rate system is connected to the pre-heater, one imitates heating and piece-rate system and connects two imitates heating and piece-rate system, two imitates heating and piece-rate system and connect three imitate heating and piece-rate system, three imitates heating and piece-rate system and connect the viscous crude room, the centrifugal chamber is connected to the viscous crude room, solid-liquid separation system is connected to the centrifugal chamber, solid-liquid separation system.
Further, the preheater is a tubular or plate heat exchanger, and the drying equipment is a roller scraper dryer.
Further, the first-effect heating and separating system, the second-effect heating and separating system and the third-effect heating and separating system respectively comprise a separating chamber and a heating chamber which are connected with each other.
Further, the centrifugal chamber is set to be a two-stage material-pushing type centrifugal machine, and the water content of salt discharged by the centrifugal machine is not higher than 3%.
Further, the solid-liquid separation system is a plate frame.
Compared with the prior art, the invention has the following beneficial effects:
the MVR evaporation mother liquor is subjected to triple-effect heating, evaporation, concentration and solid-liquid separation and then dried, the generated solid fine salt is discharged outside, the generated condensed liquid is recycled, zero discharge of the MVR evaporation mother liquor is realized, the purpose of environmental protection is achieved, secondary steam and tertiary steam generated in the invention are used as heat sources, the quaternary steam is treated and then reaches the recycling standard or is discharged at high altitude, and the economic benefit, the social benefit and the environmental protection benefit are obvious.
Drawings
FIG. 1 is a schematic structural diagram of an MVR evaporation mother liquor zero-emission system in the invention.
Reference numerals: 1. a preheater; 2. a primary heating and separation system; 3. a dual effect heating and separation system; 4. a three-effect heating and separation system; 5. a thickening chamber; 6. a centrifugal chamber; 7. a solid-liquid separation system; 8. and (5) drying equipment.
Detailed Description
The present invention will be described in further detail with reference to examples and drawings, but the present invention is not limited to these examples.
The utility model provides a MVR evaporation mother liquor zero release system, this system includes pre-heater 1, one imitates heating and piece-rate system 2, two imitates heating and piece-rate system 3, three imitates heating and piece-rate system 4, viscous crude room 5, centrifugal chamber 6, solid-liquid separation system 7 and drying equipment 8, pre-heater 1 is connected one and is imitated heating and piece-rate system 2, one imitates heating and piece-rate system 2 and connects two imitates heating and piece-rate system 3, two imitates heating and piece-rate system 3 and connect three imitate heating and piece-rate system 4, three imitates heating and piece-rate system 4 and connect viscous crude room 5, viscous crude room 5 is connected centrifugal chamber 6, centrifugal chamber 6 is connected solid-liquid separation system 7, solid-liquid separation system 7 is connected drying equipment 8.
Specifically, the preheater 1 is a tubular or plate heat exchanger. The first-effect heating and separating system 2, the second-effect heating and separating system 3 and the third-effect heating and separating system 4 respectively comprise a separating chamber and a heating chamber which are connected with each other, the heating chamber is a heating evaporator, and correspondingly for convenience of description, the first-effect heating and separating system 2 comprises a first-effect separating chamber and a first-effect heating chamber, the second-effect heating and separating system 3 comprises a second-effect separating chamber and a second-effect heating chamber, and the third-effect heating and separating system 4 comprises a third-effect separating chamber and a third-effect heating chamber. The centrifugal chamber 6 is a two-stage pusher centrifuge, and the water content of the salt discharged by the centrifuge is not higher than 3%. The solid-liquid separation system 7 is a plate frame, and the drying equipment 8 is a roller scraper dryer.
The system is provided with a method for realizing zero discharge of MVR evaporation mother liquor in a matching manner, and comprises the following procedures:
heating mother liquor: the MVR evaporation mother liquor enters a preheater 1, and the temperature is heated to 50-100 ℃ from the normal temperature by using the raw steam condensate in the one-effect heating chamber;
primary heating and concentrating: after the material is discharged by the preheater 1, the heated mother liquor enters a first-effect separation chamber for separation and then enters a first-effect heating chamber, raw steam is used for evaporation concentration, and secondary steam generated by the first-effect evaporation is used as a heat source of a second-effect heating chamber after being subjected to secondary defoaming by a demister;
secondary heating and concentrating: the obtained first-effect concentrated solution enters a second-effect separation chamber for separation and then enters a second-effect heating chamber for further evaporation and concentration, and tertiary steam generated by the second-effect evaporation is used as a heat source of the third-effect heating chamber after being subjected to secondary defoaming by a demister;
and (3) heating and concentrating for three times: the obtained two-effect concentrated solution enters a three-effect separation chamber for separation and then enters a three-effect heating chamber for further evaporation and concentration, and the four-time steam generated by three-effect evaporation is cooled by a heat exchanger and then reaches the recycling standard;
crystal growth: the obtained triple-effect concentrated solution enters a thickening chamber 5 for crystal growth;
and (3) post-treatment: and discharging the material from the thickening chamber 5, feeding the material into a centrifugal chamber 6 for solid-liquid separation, discharging the solid, circulating a part of the separated liquid to a three-effect heating chamber for further evaporation and concentration, refluxing a part of the separated liquid to a solid-liquid separation system 7 for continuous solid-liquid separation, discharging the solid, feeding the finally separated liquid into a drying device 8, and drying the liquid to obtain a condensate.
In order to improve the treatment efficiency of the mother liquor, in the steps of primary heating concentration, secondary heating concentration and tertiary heating concentration, the primary effect concentrated solution and the secondary effect concentrated solution which are separated by the separation chamber can flow back to the primary effect heating chamber corresponding to the previous unit, the secondary effect heating chamber or the secondary effect heating chamber and the tertiary effect heating chamber corresponding to the next unit.
In the invention, the recycling standards of the condensate are that the conductivity is not higher than 500 mu S/cm, the COD is not higher than 30mg/L and the hardness is not higher than 10mg/L (calculated by calcium carbonate).
And (3) experimental test: the MVR evaporation mother liquor zero emission system and the method are applied to the original MVR evaporation mother liquor of a coal yard in actual production, and the following examples are specifically provided:
COD of the original MVR evaporation mother liquor is 1180mg/L, the conductivity is 255mS/cm, the chloride ions are 58800mg/L, the sulfate radicals are 17500mg/L, the total nitrogen is 716mg/L, and the hardness is 84mg/L (calculated by calcium carbonate).
The original MVR evaporation mother liquor enters a preheater 1, the temperature is heated to 80 ℃ from the normal temperature by using raw steam condensate in a one-effect heating chamber, the raw steam consumption is reduced, after the discharge of the preheater 1, the heated mother liquor enters a one-effect separation chamber to be separated and then enters the one-effect heating chamber, the raw steam is used for evaporation concentration, and the degradation of the MVR evaporation mother liquor is realized. The obtained first-effect concentrated solution enters a second-effect separation chamber for separation and then enters a second-effect heating chamber for further evaporation and concentration, so that further degradation is realized. The obtained two-effect concentrated solution enters a three-effect separation chamber for separation and then enters a three-effect heating chamber for further evaporation and concentration, so that greater degradation is realized. The obtained triple-effect concentrated solution enters a thickening chamber 5 for crystal growth, the thick chamber 5 discharges the material and enters a centrifugal chamber 6 for solid-liquid separation, the solid is discharged outside, part of the separated liquid circularly flows back to the triple-effect heating chamber for further evaporation and concentration, part of the separated liquid flows back to a solid-liquid separation system 7 for continuous solid-liquid separation, the solid is discharged outside, the finally separated liquid enters a drying device 8, and the liquid is dried to obtain condensate.
After the treatment by the system and the method, the zero discharge of MVR evaporation mother liquor is realized, the condensate water quality COD is less than 26mg/L, the conductivity is 233 MuS/cm, the hardness is 4mg/L, and the system and the method are mainly used for circulating water replenishing, fire fighting, greening, sprinkling and the like. The water content of the separated mixed salt is 2.7 percent, and the mixed salt can be directly buried.
The above description is only a preferred embodiment of the present invention, and the protection scope of the present invention is not limited to the above embodiments, and all technical solutions belonging to the idea of the present invention belong to the protection scope of the present invention. It should be noted that modifications and embellishments within the scope of the invention may occur to those skilled in the art without departing from the principle of the invention, and are considered to be within the scope of the invention.
Claims (10)
1. A method for realizing zero emission of MVR evaporation mother liquor is characterized by comprising the following steps:
heating mother liquor: the MVR evaporation mother liquor enters a preheater and is heated to 50-100 ℃ from normal temperature;
primary heating and concentrating: the heated mother liquor enters a first-effect heating chamber, evaporation concentration is carried out by utilizing raw steam, and secondary steam generated by first-effect evaporation is used as a heat source of a second-effect heating chamber after defoaming;
secondary heating and concentrating: the obtained first-effect concentrated solution enters a second-effect heating chamber for further evaporation and concentration, and tertiary steam generated by the second-effect evaporation is used as a heat source of a third-effect heating chamber after defoaming;
and (3) heating and concentrating for three times: the obtained two-effect concentrated solution enters a three-effect heating chamber for further evaporation and concentration, and the four times of steam generated by three-effect evaporation is cooled by a heat exchanger and reaches the recycling standard;
crystal growth: the obtained triple-effect concentrated solution enters a thickening chamber to carry out crystal growth;
and (3) post-treatment: and discharging the material from the thick chamber, allowing the material to enter a centrifugal chamber for solid-liquid separation, discharging the solid, allowing part of the separated liquid to circularly flow back to a three-effect heating chamber for further evaporation and concentration, allowing part of the separated liquid to flow back to a solid-liquid separation system for continuous solid-liquid separation, discharging the solid, allowing the finally separated liquid to enter drying equipment, and drying the liquid to obtain a condensate.
2. The method of claim 1, wherein the heat source of the preheater is raw steam condensate in a single effect heating chamber.
3. The method of claim 1, wherein two-stage defoaming is performed during the primary heating concentration step and the secondary heating concentration step.
4. The method of claim 2, wherein in the steps of the first heating concentration, the second heating concentration and the third heating concentration, the MVR evaporation mother liquor, the first-effect concentrated solution and the second-effect concentrated solution are separated by a separation chamber and then enter the first-effect heating chamber, the second-effect heating chamber and the third-effect heating chamber, respectively.
5. The method of claim 4, wherein in the steps of the first heating concentration, the second heating concentration and the third heating concentration, the first-effect concentrated solution and the second-effect concentrated solution in the separation chamber can flow back to the first-effect heating chamber, the second-effect heating chamber corresponding to the previous unit, or the second-effect heating chamber and the third-effect heating chamber corresponding to the next unit.
6. The utility model provides a MVR evaporation mother liquor zero release system, a serial communication port, the system includes pre-heater, one imitates heating and piece-rate system, two imitate heating and piece-rate system, three imitate heating and piece-rate system, viscous chamber, centrifugal chamber, solid-liquid separation system and drying equipment, a heating and piece-rate system is connected to the pre-heater, one imitates heating and piece-rate system and connects two imitate heating and piece-rate system, two imitates heating and piece-rate system and connect three imitate heating and piece-rate system, three imitates heating and piece-rate system and connect the viscous chamber, the centrifugal chamber is connected to the viscous chamber, solid-liquid separation system is connected to the centrifugal chamber, solid-liquid separation system connects drying equipment.
7. The MVR evaporation mother liquor zero-emission system according to claim 6, wherein the preheater is a tubular or plate heat exchanger and the drying equipment is a roller scraper dryer.
8. The MVR evaporation mother liquor zero-emission system of claim 6, wherein the first-effect heating and separation system, the second-effect heating and separation system, and the third-effect heating and separation system each comprise a separation chamber and a heating chamber connected with each other.
9. The MVR evaporation mother liquor zero-emission system according to claim 6, wherein the centrifugal chamber is arranged as a two-stage pusher centrifuge, and the moisture content of salt discharged from the centrifuge is not higher than 3%.
10. The MVR evaporation mother liquor zero-emission system according to claim 6, wherein the solid-liquid separation system is a plate and frame.
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| CN202010904626.0A CN112174413A (en) | 2020-09-01 | 2020-09-01 | Method for realizing zero discharge of MVR evaporation mother liquor |
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| CN202010904626.0A CN112174413A (en) | 2020-09-01 | 2020-09-01 | Method for realizing zero discharge of MVR evaporation mother liquor |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104261429A (en) * | 2014-10-10 | 2015-01-07 | 山东诺贝丰化学有限公司 | Continuous triple-effect falling-film concentration and vacuum crystallization system and method in potassium nitrate production through double-decomposition method |
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-
2020
- 2020-09-01 CN CN202010904626.0A patent/CN112174413A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104261429A (en) * | 2014-10-10 | 2015-01-07 | 山东诺贝丰化学有限公司 | Continuous triple-effect falling-film concentration and vacuum crystallization system and method in potassium nitrate production through double-decomposition method |
| CN205473157U (en) * | 2016-03-22 | 2016-08-17 | 石家庄鼎威化工设备工程有限公司 | Acrylonitrile effluent treatment plant |
| CN205549631U (en) * | 2016-04-01 | 2016-09-07 | 石家庄鼎威化工设备工程有限公司 | High enriched salt effluent treatment plant of coal industry |
| CN208716886U (en) * | 2018-08-24 | 2019-04-09 | 石家庄鼎威化工设备工程有限公司 | A kind of high calcium high sodium waste-water evaporating |
| CN110183017A (en) * | 2019-05-10 | 2019-08-30 | 江苏华晖环保科技有限公司 | A kind of multiple-effect evaporation technique of strong brine zero-emission |
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| Title |
|---|
| 杨青等: "《化工单元操作》", 31 January 2017, 西南交通大学出版社, pages: 116 * |
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Application publication date: 20210105 |