CN110723857A - High-salinity water concentration and crystallization treatment system and process - Google Patents
High-salinity water concentration and crystallization treatment system and process Download PDFInfo
- Publication number
- CN110723857A CN110723857A CN201911151568.2A CN201911151568A CN110723857A CN 110723857 A CN110723857 A CN 110723857A CN 201911151568 A CN201911151568 A CN 201911151568A CN 110723857 A CN110723857 A CN 110723857A
- Authority
- CN
- China
- Prior art keywords
- precipitation
- heat exchanger
- tank
- feed liquid
- steam
- 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.)
- Granted
Links
Images
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
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
-
- 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
- C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F2001/5218—Crystallization
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/02—Temperature
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
Landscapes
- 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)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to the technical field of sewage discharge, in particular to a high-salinity water concentration and crystallization treatment system and a high-salinity water concentration and crystallization treatment process. The treatment system sequentially comprises a sewage collecting tank, a pretreatment device, a flocculation and precipitation device, an ultrafiltration device, a reverse osmosis device and an MVR evaporation and concentration device according to a treatment use sequence, wherein the MVR evaporation and concentration device sequentially comprises a plate heat exchanger, a first precipitation and crystallization tank, a second precipitation and crystallization tank and a feed liquid circulating pump according to the treatment use sequence, and a steam outlet end of the first precipitation and crystallization tank and a steam outlet end of the second precipitation and crystallization tank are communicated with the plate heat exchanger through a steam compressor; the plate heat exchanger is provided with a feed end, and the feed end of the plate heat exchanger is communicated with the output end of the reverse osmosis device through a feed pipeline. The high-salinity water concentration crystallization treatment system is novel in structure and simple to operate, crystals of high-salinity water basically precipitate, crystallize and grow at the bottoms of the first precipitation crystallizing tank and the second precipitation crystallizing tank, and the completeness of the crystals is guaranteed.
Description
Technical Field
The invention relates to the technical field of sewage discharge, in particular to a high-salinity water concentration and crystallization treatment system and a high-salinity water concentration and crystallization treatment process.
Background
In recent years, in order to save the concentration cost, a plurality of enterprises, MVR production enterprises and multi-effect concentration enterprises research and produce experiments on the concentrated crystal with zero sewage discharge, and the same result is obtained in the process of research and production experiments: the mixed salt has fine crystal particles, the concentrated solution is turbid liquid, the liquid-solid separation is difficult, pipelines and heat exchangers are seriously blocked in the production process, and the crystal dehydration is difficult, so that zero emission cannot be continuously and virtuously implemented and operated.
Because the concentrated crystal of the reverse osmosis concentrated water has the defects of small crystal particles and poor mechanical strength of the crystal, the feed liquid is forced to circulate by a forced circulation pump in the production process of MVR, because the separator does not have a device for promoting the separation of the crystal and the solution or lacks an effective separation device, the separation of the crystal and the solution is not thorough, and the inlet of the circulation pump is arranged at the bottom of the separator.
Disclosure of Invention
In order to overcome the defects and shortcomings in the prior art, the invention aims to provide a high-salinity water concentration and crystallization treatment system which is novel in structure and simple to operate, so that crystals of high-salinity water are basically precipitated and crystallized at the bottoms of a first precipitation crystallizing tank and a second precipitation crystallizing tank, an impeller of a feed liquid circulating pump is prevented from shearing the crystals, the integrity of the crystals is ensured, and the crystals can be continuously grown into larger crystal particles in a precipitation chamber; meanwhile, the utilization rate of the raw materials is improved through the circulation of steam and the circulation of feed liquid.
The invention aims to provide a high-salinity water concentration crystallization treatment process which is simple to operate, can enable crystals to form and grow at the bottoms of a first precipitation crystallizing tank and a second precipitation crystallizing tank, avoids shearing of an impeller of a feed liquid circulating pump, ensures the integrity of the crystals, and is suitable for large-scale treatment.
The purpose of the invention is realized by the following technical scheme: a high saline water concentration crystallization treatment system sequentially comprises a sewage collecting pool, a pretreatment device, a flocculation precipitation device, an ultrafiltration device, a reverse osmosis device and an MVR evaporation concentration device according to a treatment use sequence, wherein the MVR evaporation concentration device sequentially comprises a plate heat exchanger, a first precipitation crystallizing tank, a second precipitation crystallizing tank and a feed liquid circulating pump according to the treatment use sequence, and a steam outlet end of the first precipitation crystallizing tank and a steam outlet end of the second precipitation crystallizing tank are communicated with the plate heat exchanger through a steam compressor; the plate heat exchanger is provided with a feed end, and the feed end of the plate heat exchanger is communicated with the output end of the reverse osmosis device through a feed pipeline.
According to the invention, the crystals are precipitated and crystallized by arranging the first precipitation crystallizing tank and the second precipitation crystallizing tank, and the feed liquid is circulated for multiple times through the first precipitation crystallizing tank and the second precipitation crystallizing tank by adopting a feed liquid circulating mode, wherein the feed liquid overflows from the first precipitation crystallizing tank to the second precipitation crystallizing tank, and mixed salt crystals are respectively precipitated at the bottoms of the two tanks, so that the phenomenon that the crystals are sheared by an impeller when passing through a centrifugal pump or a circulating pump to damage the integrity of the crystals is avoided, the crystals grow at the bottoms of the tanks, the integrity of the crystals is ensured, and the salt components in the feed liquid are easy to separate. The high-salt water comprises salt components such as sodium sulfate, sodium carbonate, sodium chloride and the like, and the salt components in the high-salt water are precipitated and crystallized at the bottom of the tank body to form mixed salt crystals by the secondary precipitation separation method.
On the other hand, in each circulation, part of the feed liquid is evaporated in the first precipitation crystallizing tank and the second precipitation crystallizing tank, and flows to the steam compressor through the steam outlet end of the tank body to be compressed, the heat energy of the compressed feed liquid steam is increased, and the compressed feed liquid steam flows into the plate heat exchanger again to provide heat energy, so that the heat energy is provided for the preheating of the feed liquid in the plate heat exchanger, the energy consumption of the heat energy provided by the plate heat exchanger from the outside is reduced, and the energy consumption is saved.
Preferably, the plate heat exchanger is further provided with a circulating feed liquid inlet end and a circulating feed liquid outlet end, the middle upper part of the first precipitation crystallizing tank is provided with a first feed end and a first feed liquid outlet end, and the middle upper part of the second precipitation crystallizing tank is provided with a second feed end and a second feed liquid outlet end;
the plate heat exchanger's circulation feed liquid entrance point pass through the feed pipeline with the first feed end intercommunication of first precipitation crystallizer, the second feed end of second precipitation crystallizer pass through the connecting tube with the first feed liquid exit end intercommunication of first precipitation crystallizer, the second feed liquid exit end of second precipitation crystallizer pass through first circulating line with the entrance point intercommunication of feed liquid circulating pump, the exit end of feed liquid circulating pump pass through the second circulating line with plate heat exchanger's circulation feed liquid entrance point intercommunication.
According to the invention, through the components, the feed liquid is circulated among the plate heat exchanger, the first precipitation crystallizing tank, the second precipitation crystallizing tank and the feed liquid circulating pump, and then circularly passes through the first precipitation crystallizing tank and the second precipitation crystallizing tank, so that salt components in the feed liquid are precipitated and crystallized at the bottom of the tank body, and after multiple circulations, mixed salt crystals are generated and grow at the bottom of the tank body, thereby preventing the crystals from being sheared by an impeller when passing through a centrifugal pump or a circulating pump to damage the integrity of the crystals, growing the crystals at the bottom of the tank body, ensuring the integrity of the crystals, and realizing easy separation of the salt components in the feed liquid. Wherein, be provided with the feed pump on the feed pipeline to feed the feed liquid among the plate heat exchanger into in the first crystallization tank that deposits.
Preferably, the plate heat exchanger is further provided with a circulating steam inlet end, the upper part of the first precipitation crystallizing tank is provided with a first steam outlet end, and the upper part of the second precipitation crystallizing tank is provided with a second steam outlet end;
the first steam outlet end of the first precipitation crystallizing tank is communicated with the inlet end of the steam compressor through a first steam pipeline, the second steam outlet end of the second precipitation crystallizing tank is communicated with the inlet end of the steam compressor through a second steam pipeline, and the outlet end of the steam compressor is communicated with the circulating steam inlet end of the plate heat exchanger through a circulating steam pipeline.
According to the invention, through the components, steam in the feed liquid flows to the steam compressor through the first steam outlet end, the first steam pipeline, the second steam outlet end and the second steam pipeline for compression, the heat energy of the compressed feed liquid steam is increased and flows into the plate heat exchanger again to provide heat energy, so that heat energy is provided for preheating the feed liquid in the plate heat exchanger, the energy consumption of providing heat energy for the plate heat exchanger from the outside is reduced, the energy consumption is saved, and the cyclic utilization of resources is realized. Wherein, the end connection of first steam pipeline and second steam pipeline has the steam to converge the pipeline, converges steam to the entrance point of vapor compressor.
Preferably, the plate heat exchanger still is provided with the comdenstion water exit end, the comdenstion water exit end is connected with the comdenstion water holding vessel through the comdenstion water pipeline, be provided with first valve on the comdenstion water pipeline.
The heat energy of the feed liquid steam compressed by the steam compressor is increased and flows into the plate heat exchanger again to provide heat energy, and after the feed liquid steam provides the heat energy, the heat energy of the feed liquid steam is reduced, the feed liquid steam is cooled and condensed into condensate water, the condensate water flows to the condensate water pipeline through the condensate water outlet end and is stored in the condensate water storage tank, the condensate water is collected and can be used for cooling the steam compressor and the feed liquid circulating pump again, the material cyclic utilization rate in the system is improved, the energy consumed by cooling the steam compressor and the feed liquid circulating pump from the outside is reduced, the energy consumption is saved, and the cyclic utilization of resources is realized.
Wherein, the first valve of setting can be convenient for control the velocity of flow of comdenstion water.
Preferably, be provided with the feed pump on the feed pipeline, can improve feed liquid circulation process's power with the feed liquid pump in the plate heat exchanger to first sediment crystallizer, avoid mixed salt crystal deposit in plate heat exchanger, the practicality is high.
Preferably, spiral guide vanes are arranged in the first precipitation crystallizing tank and the second precipitation crystallizing tank, and guide the feed liquid with high heat to the bottom of the tank body, so that the crystal is separated from the mother liquid and the steam at the bottom of the tank body, the crystal sinks to the bottom and continues growing, and the steam rises and overflows to the steam compressor for compression and reutilization.
The other purpose of the invention is realized by the following technical scheme: a treatment process applying the high-salinity water concentration and crystallization treatment system comprises the following steps:
(1) collecting factory sewage into a sewage collecting tank, performing oil and slag removal treatment by a pretreatment device, and then performing impurity removal treatment by a flocculation precipitation device, an ultrafiltration device and a reverse osmosis device; wherein, the flocculation and precipitation device is the suspended solid that takes off in the sewage, and ultrafiltration device's filter fineness is 10nm, and the tiny impurity in the filtration sewage, reverse osmosis unit adopt the ionic membrane, and filter fineness is 0.1nm, can filter the dissolved salt more than 90%, detach a large amount of impurity for the high salt solution feed liquid that gets into MVR evaporative concentration device can deposit and form complete crystal.
(2) Feeding the feed liquid subjected to impurity removal treatment in the step (1) into a plate heat exchanger through a feed end of the plate heat exchanger for heating, then sequentially flowing into a first precipitation crystallizing tank and a second precipitation crystallizing tank for precipitation separation, pumping the separated feed liquid into the plate heat exchanger through a feed liquid circulating pump for heating again, and performing cyclic precipitation separation;
simultaneously, evaporating the heated feed liquid in a first precipitation crystallizing tank and a second precipitation crystallizing tank, compressing the evaporated steam by a steam compressor, and circulating the compressed steam to a plate heat exchanger to provide heat energy for the feed liquid;
after multiple circulating precipitation separation, the high-salinity water is concentrated and crystallized at the bottoms of the first precipitation crystallizing tank and the second precipitation crystallizing tank to obtain mixed salt crystals.
Preferably, in the step (2), the feed liquid is heated to 85-100 ℃ in a plate heat exchanger and then enters a first precipitation crystallization tank and a second precipitation crystallization tank for cyclic precipitation separation.
In the existing water treatment process, the concentrated water subjected to reverse osmosis treatment mainly contains soluble salts such as sodium and potassium and partial COD, salt in the concentrated liquid is separated out due to saturation along with evaporation of liquid moisture, the generated salt is mixed salt due to complex material components in the liquid, the particles of the mixed salt crystals are small and about 60-80 meshes, the mechanical strength of crystals is general, and the crystals are easily broken into small particles under the action of external force, so that the crystals are continuously sheared by a circulating pump impeller in the circulating process in the MVR treatment process at present, the crystals are continuously broken to form fine-particle crystals, the concentrated liquid forms suspension, solid-liquid separation is difficult to perform, and meanwhile, pipelines and a heat exchanger in the production process are seriously blocked, and the crystals are difficult to dehydrate.
Therefore, by arranging the first precipitation crystallizing tank and the second precipitation crystallizing tank, the feed liquid is heated by the plate heat exchanger and then enters the first precipitation crystallizing tank and the second precipitation crystallizing tank for precipitation separation, meanwhile, part of steam of the heated feed liquid volatilizes to form secondary steam, the secondary steam is compressed by the steam compressor, the heat energy of the secondary steam is increased and enters the plate heat exchanger again to provide heat energy for the plate heat exchanger, the feed liquid circulated into the plate heat exchanger is heated by the heat energy compressed by the secondary steam, and the cyclic utilization rate of the steam heat energy is improved. And steam provides after providing the heat energy for the heating of feed liquid, self heat energy reduces, and cooling and condensation are the comdenstion water, through the comdenstion water outlet end, the comdenstion water pipeline flow direction is stored in the comdenstion water holding vessel, collects the comdenstion water and can be used for steam compressor and feed liquid circulating pump's cooling once more, has improved the material cyclic utilization in the system, reduces the external energy of cooling down the consumption to steam compressor and feed liquid circulating pump, practices thrift the energy consumption, has realized the cyclic utilization of resource.
After the liquid is precipitated and crystallized by the first precipitation crystallizing tank and the second precipitation crystallizing tank, the liquid is precipitated and separated at the bottom of the tank body to form high-salt water crystals, and the high-salt water crystals are basically remained at the bottoms of the tank bodies of the first precipitation crystallizing tank and the second precipitation crystallizing tank, so that the liquid is prevented from being sheared by an impeller of a liquid circulating pump, the completeness of the crystals is ensured, and the crystals can be continuously grown into larger crystal particles in a precipitation chamber.
Wherein, the internal portion of jar of first sediment crystallizer and second sediment crystallizer sets up spiral guide vane, can be with the superheated liquid water conservancy diversion of newly-pumping to room bottom, and the crystal separates with mother liquor and vapor in first sediment crystallizer bottom afterwards, and the crystal sinks to the bottom and continues growing greatly, and the mother liquor rises to overflow mouth overflow to second sediment crystallizer, and vapor then rises and overflows the surface of water and is compressed by the compressor once more and recycle, has improved the utilization ratio of raw materials.
The invention has the beneficial effects that: the high-salinity water concentration and crystallization treatment system is novel in structure and simple to operate, crystals of high-salinity water are basically precipitated and crystallized at the bottoms of the first precipitation crystallizing tank and the second precipitation crystallizing tank, the crystals are prevented from being sheared by an impeller of a feed liquid circulating pump, the integrity of the crystals is ensured, and the crystals can continue to grow into larger crystal particles in the precipitation chamber; meanwhile, the utilization rate of the raw materials is improved through the circulation of steam and the circulation of feed liquid.
The high-salinity water concentration crystallization treatment process is simple to operate, crystals can form and grow at the bottoms of the first precipitation crystallizing tank and the second precipitation crystallizing tank, the crystals are prevented from being sheared by an impeller of a feed liquid circulating pump, the completeness of the crystals is ensured, the zero emission and resource recycling of sewage are realized, no precipitation auxiliary agent is required to be added in the treatment process, the crystals with good crystallization can be obtained, and the high-salinity water concentration crystallization treatment process is suitable for large-scale treatment.
Drawings
FIG. 1 is a block diagram of the present invention;
FIG. 2 is a schematic view of the MVR evaporation and concentration device according to the present invention;
the reference signs are: 1-sewage collecting tank, 2-pretreatment device, 3-flocculation and precipitation device, 4-ultrafiltration device, 5-reverse osmosis device, 6-MVR evaporation and concentration device, 61-plate heat exchanger, 611-feed pipeline, 62-first precipitation and crystallization tank, 621-feed pipeline, 6211-feed pump, 622-connecting pipeline, 623-first steam pipeline, 63-second precipitation and crystallization tank, 631-first circulating pipeline, 632-second steam pipeline, 633-steam converging pipeline, 64-feed liquid circulating pump, 641-second circulating pipeline, 65-steam compressor, 651-circulating steam pipeline, 66-condensed water pipeline, 67-first valve, 68-condensed water storage tank, 69-spiral guide vane.
Detailed Description
For the understanding of those skilled in the art, the present invention will be further described with reference to the following examples and accompanying fig. 1-2, which are not intended to limit the present invention.
Example 1
Referring to the attached drawings 1-2, the high-salinity water concentration and crystallization treatment system sequentially comprises a sewage collection tank 1, a pretreatment device 2, a flocculation and precipitation device 3, an ultrafiltration device 4, a reverse osmosis device 5 and an MVR evaporation and concentration device 6 according to a treatment and use sequence, wherein the MVR evaporation and concentration device 6 sequentially comprises a plate heat exchanger 61, a first precipitation and crystallization tank 62, a second precipitation and crystallization tank 63 and a feed liquid circulating pump 64 according to the treatment and use sequence, and a steam outlet end of the first precipitation and crystallization tank 62 and a steam outlet end of the second precipitation and crystallization tank 63 are communicated with the plate heat exchanger 61 through a steam compressor 65; the plate heat exchanger 61 is provided with a feed end, and the feed end of the plate heat exchanger 61 is communicated with the output end of the reverse osmosis device 5 through a feed pipeline 611.
The plate heat exchanger 61 is also provided with a circulating feed liquid inlet end and a circulating feed liquid outlet end, the middle upper part of the first precipitation crystallizing tank 62 is provided with a first feed end and a first feed liquid outlet end, and the middle upper part of the second precipitation crystallizing tank 63 is provided with a second feed end and a second feed liquid outlet end;
the inlet end of the circulating feed liquid of the plate heat exchanger 61 is communicated with the first feed end of the first precipitation crystallizing tank 62 through a feed pipeline 621, the second feed end of the second precipitation crystallizing tank 63 is communicated with the first feed liquid outlet end of the first precipitation crystallizing tank 62 through a connecting pipeline 622, the second feed liquid outlet end of the second precipitation crystallizing tank 63 is communicated with the inlet end of the feed liquid circulating pump 64 through a first circulating pipeline 631, and the outlet end of the feed liquid circulating pump 64 is communicated with the inlet end of the circulating feed liquid of the plate heat exchanger 61 through a second circulating pipeline 641.
The plate heat exchanger 61 is also provided with a circulating steam inlet end, the upper part of the first precipitation crystallizing tank 62 is provided with a first steam outlet end, and the upper part of the second precipitation crystallizing tank 63 is provided with a second steam outlet end;
the first steam outlet end of the first precipitation crystallization tank 62 is communicated with the inlet end of the steam compressor 65 through a first steam pipeline 623, the second steam outlet end of the second precipitation crystallization tank 63 is communicated with the inlet end of the steam compressor 65 through a second steam pipeline 632, and the outlet end of the steam compressor 65 is communicated with the circulating steam inlet end of the plate heat exchanger 61 through a circulating steam pipeline 651.
The plate heat exchanger 61 is further provided with a condensed water outlet end, the condensed water outlet end is connected with a condensed water storage tank 68 through a condensed water pipeline 66, and a first valve 67 is arranged on the condensed water pipeline 66.
A supply pump 6211 is disposed on the supply conduit 621.
Example 2
A treatment process applying the high-salinity water concentration and crystallization treatment system comprises the following steps:
1, collecting factory sewage into a sewage collecting tank 1, performing oil and slag removal treatment by a pretreatment device 2, and then performing impurity removal treatment by a flocculation precipitation device 3, an ultrafiltration device 4 and a reverse osmosis device 5;
2, feeding the feed liquid subjected to impurity removal treatment in the step 1 into a plate heat exchanger 61 through a feed end of the plate heat exchanger 61 to heat up, then sequentially flowing into a first precipitation crystallizing tank 62 and a second precipitation crystallizing tank 63 to carry out precipitation separation, pumping the separated feed liquid into the plate heat exchanger 61 through a feed liquid circulating pump 64 to heat up again, and carrying out circulating precipitation separation;
meanwhile, the heated feed liquid is evaporated in a first precipitation crystallizing tank 62 and a second precipitation crystallizing tank 63, and the evaporated steam is compressed by a steam compressor 65 and then circulated to a plate heat exchanger 61 to provide heat energy for the feed liquid;
after multiple circulating precipitation separation, the high-salinity water is concentrated and crystallized at the bottoms of the first precipitation crystallizing tank 62 and the second precipitation crystallizing tank 63 to obtain mixed salt crystals.
Preferably, in the step 2, the feed liquid is heated to 85-100 ℃ in the plate heat exchanger 61 and then enters the first precipitation crystallization tank 62 and the second precipitation crystallization tank 63 for cyclic precipitation separation; specifically, the temperature rise temperature is 85 ℃, 90 ℃, 95 ℃ or 100 ℃.
The above-described embodiments are preferred implementations of the present invention, and the present invention may be implemented in other ways without departing from the spirit of the present invention.
Claims (8)
1. The utility model provides a concentrated crystallization processing system of high salt water which characterized in that: the device comprises a sewage collecting tank (1), a pretreatment device (2), a flocculation and precipitation device (3), an ultrafiltration device (4), a reverse osmosis device (5) and an MVR evaporation and concentration device (6) in turn according to the treatment use sequence, wherein the MVR evaporation and concentration device (6) comprises a plate heat exchanger (61), a first precipitation and crystallization tank (62), a second precipitation and crystallization tank (63) and a feed liquid circulating pump (64) in turn according to the treatment use sequence, and the steam outlet end of the first precipitation and crystallization tank (62) and the steam outlet end of the second precipitation and crystallization tank (63) are communicated with the plate heat exchanger (61) through a steam compressor (65); the plate heat exchanger (61) is provided with a feed end, and the feed end of the plate heat exchanger (61) is communicated with the output end of the reverse osmosis device (5) through a feed pipeline (611).
2. The high salinity water concentration crystallization processing system of claim 1, characterized in that: the plate heat exchanger (61) is also provided with a circulating feed liquid inlet end and a circulating feed liquid outlet end, the middle upper part of the first precipitation crystallizing tank (62) is provided with a first feed end and a first feed liquid outlet end, and the middle upper part of the second precipitation crystallizing tank (63) is provided with a second feed end and a second feed liquid outlet end;
the circulation feed liquid entrance point of plate heat exchanger (61) pass through feed pipeline (621) with the first feed end intercommunication of first precipitation crystallizer (62), the second feed end of second precipitation crystallizer (63) pass through connecting tube (622) with the first feed liquid exit end intercommunication of first precipitation crystallizer (62), the second feed liquid exit end of second precipitation crystallizer (63) pass through first circulation pipeline (631) with the entrance point intercommunication of feed liquid circulating pump (64), the exit end of feed liquid circulating pump (64) pass through second circulation pipeline (641) with the circulation feed liquid entrance point intercommunication of plate heat exchanger (61).
3. The high salinity water concentration crystallization processing system of claim 1, characterized in that: the plate heat exchanger (61) is also provided with a circulating steam inlet end, the upper part of the first precipitation crystallizing tank (62) is provided with a first steam outlet end, and the upper part of the second precipitation crystallizing tank (63) is provided with a second steam outlet end;
the first steam outlet end of the first precipitation crystallization tank (62) is communicated with the inlet end of the steam compressor (65) through a first steam pipeline (623), the second steam outlet end of the second precipitation crystallization tank (63) is communicated with the inlet end of the steam compressor (65) through a second steam pipeline (632), and the outlet end of the steam compressor (65) is communicated with the circulating steam inlet end of the plate-type heat exchanger (61) through a circulating steam pipeline (651).
4. The high salinity water concentration crystallization processing system of claim 3, characterized in that: the plate heat exchanger (61) is further provided with a condensed water outlet end, the condensed water outlet end is connected with a condensed water storage tank (68) through a condensed water pipeline (66), and a first valve (67) is arranged on the condensed water pipeline (66).
5. The high salinity water concentration crystallization processing system of claim 2, characterized in that: and a feeding pump is arranged on the feeding pipeline (621).
6. The high salinity water concentration crystallization processing system of claim 2, characterized in that: spiral guide vanes (69) are arranged in the first precipitation crystallizing tank (62) and the second precipitation crystallizing tank (63).
7. A treatment process using the high-salinity water concentration and crystallization treatment system as defined in any one of claims 1 to 6, which is characterized in that: the method comprises the following steps:
(1) collecting factory sewage into a sewage collecting tank (1), performing oil and slag removal treatment by a pretreatment device (2), and then performing impurity removal treatment by a flocculation precipitation device (3), an ultrafiltration device (4) and a reverse osmosis device (5);
(2) feeding the feed liquid subjected to impurity removal treatment in the step (1) into a plate heat exchanger (61) through a feed end of the plate heat exchanger (61) for heating, then sequentially flowing into a first precipitation crystallizing tank (62) and a second precipitation crystallizing tank (63) for precipitation separation, pumping the separated feed liquid into the plate heat exchanger (61) through a feed liquid circulating pump (64) for heating again, and performing circulating precipitation separation;
meanwhile, the feed liquid heated by temperature rise is evaporated in a first precipitation crystallizing tank (62) and a second precipitation crystallizing tank (63), and the evaporated steam is compressed by a steam compressor (65) and then circulated to a plate heat exchanger (61) to provide heat energy for the feed liquid;
after multiple circulating precipitation separation, the high-salinity water is concentrated and crystallized at the bottoms of a first precipitation crystallizing tank (62) and a second precipitation crystallizing tank (63) to obtain mixed salt crystals.
8. The high salinity water concentration and crystallization treatment process according to claim 7, characterized in that: in the step (2), the feed liquid is heated to 85-100 ℃ in a plate heat exchanger (61) and then enters a first precipitation crystallization tank (62) and a second precipitation crystallization tank (63) for cyclic precipitation separation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911151568.2A CN110723857B (en) | 2019-11-21 | 2019-11-21 | High-salinity water concentration and crystallization treatment system and process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911151568.2A CN110723857B (en) | 2019-11-21 | 2019-11-21 | High-salinity water concentration and crystallization treatment system and process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110723857A true CN110723857A (en) | 2020-01-24 |
| CN110723857B CN110723857B (en) | 2022-04-12 |
Family
ID=69225582
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911151568.2A Active CN110723857B (en) | 2019-11-21 | 2019-11-21 | High-salinity water concentration and crystallization treatment system and process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110723857B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115465994A (en) * | 2022-09-20 | 2022-12-13 | 张敏 | Organic wastewater treatment system and method with high salt concentration |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101891330A (en) * | 2010-07-23 | 2010-11-24 | 深圳市能源环保有限公司 | Power plant wastewater treatment system and method |
| CN103991997A (en) * | 2014-05-30 | 2014-08-20 | 中国石油集团东北炼化工程有限公司吉林设计院 | Strong brine evaporating and crystallizing system |
| CN104341072A (en) * | 2014-11-12 | 2015-02-11 | 湖北加德科技股份有限公司 | Energy-saving waste-water continuous evaporating crystallizing system |
| CN104445786A (en) * | 2014-12-15 | 2015-03-25 | 宁波摩尔森膜环保科技有限公司 | Process and device for treating high-concentration salt-containing wastewater |
| CN204848322U (en) * | 2015-04-12 | 2015-12-09 | 中山中珠环保科技有限公司 | High salt solution processing system |
| CN205099370U (en) * | 2015-11-08 | 2016-03-23 | 黄生根 | High concentration contains salt waste water evaporation crystallization process device |
| CN205275243U (en) * | 2015-12-04 | 2016-06-01 | 武汉宏澳绿色能源工程有限责任公司 | Evaporation plant of board -like forced circulation's of MVR landfill leachate reverse osmosis dope |
| CN108409018A (en) * | 2018-05-15 | 2018-08-17 | 上海奕茂环境科技有限公司 | The online desalination of dangerous waste incineration flue gas washes and reclaiming system and method |
| CN110330165A (en) * | 2019-06-05 | 2019-10-15 | 中国石油天然气集团有限公司 | Strong brine zero-emission and sub-prime crystallizing treatment process and processing system |
-
2019
- 2019-11-21 CN CN201911151568.2A patent/CN110723857B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101891330A (en) * | 2010-07-23 | 2010-11-24 | 深圳市能源环保有限公司 | Power plant wastewater treatment system and method |
| CN103991997A (en) * | 2014-05-30 | 2014-08-20 | 中国石油集团东北炼化工程有限公司吉林设计院 | Strong brine evaporating and crystallizing system |
| CN104341072A (en) * | 2014-11-12 | 2015-02-11 | 湖北加德科技股份有限公司 | Energy-saving waste-water continuous evaporating crystallizing system |
| CN104445786A (en) * | 2014-12-15 | 2015-03-25 | 宁波摩尔森膜环保科技有限公司 | Process and device for treating high-concentration salt-containing wastewater |
| CN204848322U (en) * | 2015-04-12 | 2015-12-09 | 中山中珠环保科技有限公司 | High salt solution processing system |
| CN205099370U (en) * | 2015-11-08 | 2016-03-23 | 黄生根 | High concentration contains salt waste water evaporation crystallization process device |
| CN205275243U (en) * | 2015-12-04 | 2016-06-01 | 武汉宏澳绿色能源工程有限责任公司 | Evaporation plant of board -like forced circulation's of MVR landfill leachate reverse osmosis dope |
| CN108409018A (en) * | 2018-05-15 | 2018-08-17 | 上海奕茂环境科技有限公司 | The online desalination of dangerous waste incineration flue gas washes and reclaiming system and method |
| CN110330165A (en) * | 2019-06-05 | 2019-10-15 | 中国石油天然气集团有限公司 | Strong brine zero-emission and sub-prime crystallizing treatment process and processing system |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115465994A (en) * | 2022-09-20 | 2022-12-13 | 张敏 | Organic wastewater treatment system and method with high salt concentration |
| CN115465994B (en) * | 2022-09-20 | 2023-09-08 | 浙江宣达环境科技股份有限公司 | Organic wastewater treatment system and method with high salt concentration |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110723857B (en) | 2022-04-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN204417272U (en) | A kind of crystallization treatment device of high slat-containing wastewater | |
| CN104692574A (en) | Treatment method of high saline wastewater | |
| CN104692575A (en) | Crystallization treatment method and device of high salt wastewater | |
| CN108328831B (en) | Method and equipment for concentrating reverse osmosis strong brine | |
| CN104926011B (en) | The evaporative crystallization zero-discharge treatment system and processing method of a kind of high-COD waste water | |
| CN110040908A (en) | A kind of sodium chloride and sodium sulphate ultrasonic type evaporative crystallization divide salt system and method | |
| CN204185326U (en) | A kind of power plant desulfurization Wastewater zero-discharge treatment system | |
| CN109534568A (en) | Integrated seawater resources utilization system | |
| CN112919505A (en) | Device and method for continuously producing lithium hydroxide from salt lake lithium-rich brine | |
| CN206538490U (en) | A kind of cleaning of sea water desalinization strong brine puies forward magnesium system | |
| WO2018018864A1 (en) | Membrane distillation crystallization treatment device and method | |
| CN110723857B (en) | High-salinity water concentration and crystallization treatment system and process | |
| CN102849756A (en) | Device and method for nitre extraction of sodium sulfate type bittern | |
| CN205974124U (en) | Coal chemical wastewater's processing system | |
| CN110451529A (en) | A kind of method of purification of sodium chloride for injection | |
| CN207608448U (en) | Utilize the seawater desalination system of power station thermal energy production and living water | |
| CN216837160U (en) | Sodium carbonate waste salt recovery device system | |
| CN208249911U (en) | The continuous salt making system of brackish water | |
| CN207259308U (en) | Integrated seawater resources utilization system | |
| CN206886879U (en) | Membrane separation process concentrates the processing unit of brackish water | |
| CN211813952U (en) | Seawater resource utilization system | |
| CN210261447U (en) | Ultrasonic evaporative crystallization salt separation system for sodium chloride and sodium sulfate | |
| CN210736429U (en) | Resourceful coupling integrated system for salt-containing wastewater | |
| CN102344152A (en) | Method for preparing high-quality salt by using salt manufacturing mother liquor | |
| CN206886880U (en) | A kind of processing system containing high-salt wastewater |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |