CN207404854U - Sodium chloride and sodium sulphate separation concentration elutriation system in strong brine zero-emission - Google Patents
Sodium chloride and sodium sulphate separation concentration elutriation system in strong brine zero-emission Download PDFInfo
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- CN207404854U CN207404854U CN201721342603.5U CN201721342603U CN207404854U CN 207404854 U CN207404854 U CN 207404854U CN 201721342603 U CN201721342603 U CN 201721342603U CN 207404854 U CN207404854 U CN 207404854U
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Abstract
The utility model discloses sodium chloride in a kind of strong brine zero-emission and sodium sulphate separation concentration elutriation system, mainly include sodium chloride separation concentration technology section, sodium sulphate eluriates separation concentration technology section and reuse water collection system；Strong brine divides salt device except firmly rear into level-one, selects to carry out de- COD, desiliconization, decarburization after the production water concentration of a fraction salt device or drops turbid processing, enters back into two fraction salt devices, produce water evaporation crystallization and prepare sodium chloride；The concentrated water of two fraction salt devices enters level-one washing device after being mixed in proportion with part recycle-water, the concentrated water of generation selects de- COD or the turbid processing of drop after being mixed with the concentrated water of a fraction salt device, it is mixed into two level washing device in proportion with recycle-water again, the concentrated water of generation prepares sodium sulphate after concentrating again.The advantages of the utility model：High pure sodium chloride and high-purity sulphuric acid sodium can be prepared simultaneously；Evaporated crystallization device is stable, and investment is low with operation cost；Each technique unit technology maturation, has a extensive future.
Description
Technical field
The utility model is related to sodium chloride in a kind of strong brine zero-emission and sodium sulphate separation concentration elutriation system, belong to useless
Water zero discharge process field.
Background technology
With national energy implementation and China's water quality water shortage problem getting worse, especially NORTHWEST CHINA area is big
The construction of the water consumptions rich and influential family such as type industrial and mining enterprises and coal chemical industry, recycles water resource to greatest extent, while reduces terminal solid
The generation of discarded object realizes that complete zero-emission seems particularly urgent.In existing zero-emission engineering, can only often it realize " useless
Water zero discharge ", the mixed salt complicated component that end process generates, need to be handled, and intractability is big, costly as dangerous waste.Point
Salt is the essential option for realizing strong brine zero-emission circular economy.Point of monovalent salt and divalent salts can be realized using nanofiltration membrane component
From, production water side can prepare purer sodium chloride, but still there is the sodium chloride of high concentration in concentrated water side, and obtained sodium sulphate purity is relatively low,
It cannot meet and recycle or its industrial requirement.In actual zero-emission engineering practice, while obtain high-purity sodium chloride
The bottleneck of strong brine zero-emission end process is increasingly becoming with sodium sulfate in high purity.
Utility model content
For these problems, the utility model proposes sodium chloride in a kind of strong brine zero-emission and sodium sulphate separation concentration to wash in a pan
System is washed, existing strong brine zero-emission end process is enable to obtain high-purity monovalent salt and divalent salts simultaneously, meets Xun Huan
Recycling or its industrial requirement, realize complete zero-emission；Reduce operation expense simultaneously.
Technical solution is used by the utility model solves its technical problem：In a kind of strong brine zero-emission sodium chloride and
Sodium sulphate separation concentration elutriation system, it is characterised in that：The system includes sodium chloride separation concentration technology section, sodium sulphate is eluriated and divided
From concentration technology section and reuse water collection system；
Wherein, sodium chloride separation concentration technology section includes at least hardness removing device, a fraction salt device, enrichment facility
I, two fraction salt devices and sodium chloride evaporated crystallization device；The outlet of hardness removing device is connected with the water inlet of a fraction salt device,
The production mouth of a river of one fraction salt device is connected with the water inlet of enrichment facility I, the concentrated water spout of enrichment facility I and two fraction salt devices
Water inlet connects, and the production mouth of a river of two fraction salt devices is connected with sodium chloride evaporated crystallization device；
The sodium sulphate is eluriated separation concentration technology section and is washed in a pan including at least level-one washing device, enrichment facility II, two level
Cleaning device, enrichment facility III and sulfate crystal device；The concentrated water spout and reuse water collection system of the two fraction salt devices
The first water outlet connection after connected again by pipeline with the water inlet of level-one washing device；The level-one washing device it is dense
It is washed in a pan again by pipeline and two level after the second water outlet connection at the mouth of a river, the concentrated water spout of a fraction salt device and reuse water collection system
The water inlet connection of cleaning device；The concentrated water spout of the two level washing device passes through concentrated water device III and sulfate crystal device
Connection；
The production mouth of a river of the level-one washing device connected with the production mouth of a river of two level washing device after again by pipeline with it is dense
The water inlet connection of compression apparatus II, the concentrated water spout of the enrichment facility II are connected with the concentrated water spout of enrichment facility I；Described is dense
The production mouth of a river of compression apparatus I, enrichment facility II and enrichment facility III are connected by pipeline with reuse water collection system water inlet.
One fraction salt device, two fraction salt devices, level-one washing device and the two level washing device is using special type
NF membrane carries out the separation of monovalent salt and divalent salts；Enrichment facility I, the enrichment facility II and enrichment facility III select anti-
One kind in contamination type bitter reverse-osmosis membrane element, super-pressure reverse-osmosis membrane element or resistance to anti-pollution reverse osmosis membrane element with high salt
It is or a variety of.
The model FORTILIFE of the extraordinary NF membraneTMXC-N；The reverse osmosis membrane element of antipollution bitter
Part model FORTILIFETMCR100, the super-pressure reverse-osmosis membrane element model XUS180808, the resistance to height
Salt anti-pollution reverse osmosis membrane element model FORTILIFETM XC70。
Machine object removal device I, silica are sequentially set with this between the enrichment facility I and two fraction salt devices
Removal device, carbon dioxide cleaner and ultrafiltration apparatus I；It is sequentially set between the one fraction salt device and two level washing device with this
Machine object removal device II and ultrafiltration apparatus II.
The hardness removing device uses resin softening process, and the resin is resistance to high COD and halophilic weak-type tree
Fat.
The beneficial effects of the utility model are：Since existing process system by nanofiltration divides salt and crystallization apparatus that can only make
The monovalent salt of standby higher degree, divalent purity salt is still relatively low, and the utility model divides salt to concentrate elutriation system using described
1. the high separation of sodium chloride and sodium sulphate can be realized, while prepare high-purity sodium chloride and sodium sulfate in high purity；2. it realizes
While dividing salt, water resource and sodium chloride can be recycled to greatest extent, reduce end evaporative crystallization or Freeze crystallization amount, drop
Low investment and operation expense；3. each technique unit technology maturation, application easy to spread have fabulous application prospect and ring
Border benefit.
Description of the drawings
Fig. 1：Sodium chloride and sodium sulphate separation concentration elutriation system knot in the strong brine zero-emission of the utility model embodiment 1
Structure schematic diagram；
Fig. 2：Sodium chloride and sodium sulphate separation concentration elutriation system knot in the strong brine zero-emission of the utility model embodiment 5
Structure schematic diagram；
In figure：1st, sodium chloride separation concentration technology section；2nd, sodium sulphate eluriates separation concentration technology section；3rd, recycle-water collects system
System；4th, organic matter removal device I；5th, silica removal device；6th, carbon dioxide cleaner；7th, ultrafiltration apparatus I；8th, organic matter removal device
II；9th, ultrafiltration apparatus II；11st, hardness removing device；12nd, a fraction salt device；13rd, enrichment facility I；14th, two fraction salt device；15、
Sodium chloride evaporated crystallization device；21st, level-one washing device；22nd, enrichment facility II；23rd, two level washing device；24th, enrichment facility
III；25th, sulfate crystal device.
Specific embodiment
The utility model is described further with reference to specific embodiment, but the scope of protection of the utility model is simultaneously
It is not limited only to this：
Embodiment 1：
With reference to Fig. 1, sodium chloride and sodium sulphate separation concentration elutriation system in a kind of strong brine zero-emission, including sodium chloride point
Separation concentration technology section 2 and reuse water collection system 3 are eluriated from concentration technology section 1, sodium sulphate；
Wherein, described sodium chloride separation concentration technology section 1 includes at least a hardness removing device 11, fraction salt device 12, dense
Compression apparatus I13, two fraction salt devices 14 and sodium chloride evaporated crystallization device 15；The outlet of hardness removing device 11 and a fraction salt device
12 water inlet connection, the production mouth of a river of a fraction salt device 12 are connected with the water inlet of enrichment facility I13, enrichment facility I13's
Concentrated water spout is connected with the water inlet of two fraction salt devices 14, the production mouth of a river and the sodium chloride evaporated crystallization device of two fraction salt devices 14
15 connections；
The sodium sulphate eluriates separation concentration technology section 2 and includes at least level-one washing device 21, enrichment facility II22, two
Grade washing device 23, enrichment facility III24 and sulfate crystal device 25；The concentrated water spout of the two fraction salt devices 14 and return
It is connected again by pipeline with the water inlet of level-one washing device 21 after being connected with the first water outlet of water collection system 3；Described
Second water outlet of the concentrated water spout of level-one washing device 21, the concentrated water spout of a fraction salt device 12 and reuse water collection system 3 connects
It is connected again by pipeline with the water inlet of two level washing device 23 after logical；The concentrated water spout of the two level washing device 23 passes through dense
Water installations III24 is connected with sulfate crystal device 25；
The production mouth of a river of the level-one washing device 21 passes through pipeline again after being connected with the production mouth of a river of two level washing device 23
It is connected with the water inlet of enrichment facility II22, the concentrated water spout of the enrichment facility II22 connects with the concentrated water spout of enrichment facility I13
It is logical；Enrichment facility I13, the enrichment facility II22 and the production mouth of a river of enrichment facility III24 are received by pipeline and recycle-water
3 water inlet of collecting system connects；
Technique is eluriated in sodium chloride and sodium sulphate separation concentration in a kind of strong brine zero-emission：Zero-emission strong brine is passed through except hard dress
It intakes after putting 11 processing as a fraction salt device 12, the water inlet of the production water of a fraction salt device 12 as enrichment facility I13 is dense
Water inlet of the concentrated water of compression apparatus I13 as two fraction salt devices 14, the production water of two fraction salt devices 14 is evaporated by sodium chloride to be tied
Brilliant device 15 prepares high-purity sodium chloride；The concentrated water of the two fraction salt devices 14 in reuse water collection system 3 with partly returning
Mix the water inlet as level-one washing device 21 in proportion by the use of water；The concentrated water of the level-one washing device 21 is filled with a fraction salt
Put 12 concentrated water mixing mixed in proportion with part recycle-water in reuse water collection system 3 again as two level washing device 23 into
Water；The concentrated water of the two level washing device 23 prepares height after concentrated water device III24 concentrations into sulfate crystal device 25
Purity sodium sulphate；The production water of the level-one washing device 21 is mixed with the production water of two level washing device 23 as enrichment facility
The water inlet of II22；The concentrated water of the enrichment facility II22 is mixed with the concentrated water of enrichment facility I13 carries out subsequent processing；Described
The production water of enrichment facility I13, enrichment facility II22 and enrichment facility III24 enter reuse water collection system 3, then cycle and return again
With.
Embodiment 2
On the basis of embodiment 1, a fraction salt device 12, two fraction salt devices 14, level-one washing device 21
The separation of monovalent salt and divalent salts is carried out using extraordinary NF membrane with two level washing device 23；It is the enrichment facility I13, dense
Compression apparatus II22 and enrichment facility III24 select pollution-resistant bitter reverse-osmosis membrane element, super-pressure reverse-osmosis membrane element or
The one or more of resistance to anti-pollution reverse osmosis membrane element with high salt.
The model FORTILIFE of the extraordinary NF membraneTMXC-N；The special separation NF membrane is a kind of helical coil
There is the poly- piperazine laminated film element of formula highly selective and higher monovalention transmitance and higher divalent ion to cut
Rate is stayed, the major part in strong brine can be converted to salting liquid that is pure, being more easy to crystallization.
The antipollution bitter reverse-osmosis membrane element model FORTILIFETMCR100, the super-pressure are anti-
Permeable membrane device model XUS180808, the resistance to anti-pollution reverse osmosis membrane element model FORTILIFE with high saltTM
XC70。
The concentrated water of the two fraction salt devices 14 uses part recycle-water in reuse water collection system 3 to be diluted, then
Elutriation purifying is carried out into level-one washing device 21；In the concentrated water of the two fraction salt devices 14 and reuse water collection system 3
Recycle-water mixed water in part is 9-11 times of two fraction salt devices, 14 concentrated water amount, is realized with this and is depressed low into water-driven
The further separation of monovalent salt and divalent salts improves the purity of divalent salts while increasing monovalent salt yield.
After the concentrated water of the level-one washing device 21 is mixed with the concentrated water of a fraction salt device 12, collected using recycle-water
Part recycle-water is diluted in system 3, is entered back into two level washing device 23 and is carried out elutriation purifying；The level-one washing device
21 concentrated water and the concentrated water of a fraction salt device 12 and recycle-water mixed water in part in reuse water collection system 3 are level-one
2-2.5 times of the concentrated water total Water of the concentrated water of washing device 21 and a fraction salt device 12, is realized low with this into water-driven pressure
The further separation of lower monovalent salt and divalent salts improves the purity of divalent salts while increasing monovalent salt yield.
The hardness removing device 11 uses resin softening process, and the resin is resistance to high COD and halophilic weak-type
Resin.
Embodiment 3
On the basis of embodiment 1 or 2, the two fraction salt devices 14 divide salt technique and two level washing device 23
It can increase the one or more works taken off in COD, desiliconization, decarburization or the turbid technique of drop according to the specific water quality of strong brine before eluriating technique
Skill.
Embodiment 4
On the basis of embodiment 3, the de- COD techniques use advanced oxidation processes；The desilication process uses
Magnesia mixture removes silicon, and the magnesia mixture selects magnesium chloride or magnesia；The decarbonization process uses decarbonizing tower or carbon dioxide cleaner；Described
Turbid technique is dropped using ultrafiltration membrane system.
Embodiment 5
With reference to Fig. 2, sodium chloride and sodium sulphate separation concentration elutriation system in a kind of strong brine zero-emission, including sodium chloride point
Separation concentration technology section 2 and reuse water collection system 3 are eluriated from concentration technology section 1, sodium sulphate；
Wherein, described sodium chloride separation concentration technology section 1 includes at least a hardness removing device 11, fraction salt device 12, dense
Compression apparatus I13, organic matter removal device I4, silica removal device 5, carbon dioxide cleaner 6, ultrafiltration apparatus I7, two fraction salt devices
14 and sodium chloride evaporated crystallization device 15；The outlet of hardness removing device 11 is connected with the water inlet of a fraction salt device 12, a fraction
The production mouth of a river of salt device 12 is connected with the water inlet of enrichment facility I13, and the concentrated water spout of enrichment facility I13 passes sequentially through the removal of machine object
Device I4, silica removal device 5, carbon dioxide cleaner 16 and ultrafiltration apparatus I7 are connected with the water inlet of two fraction salt devices 14, and two
The production mouth of a river of fraction salt device 14 is connected with sodium chloride evaporated crystallization device 15；
The sodium sulphate eluriates separation concentration technology section 2 and includes at least level-one washing device 21, enrichment facility II22, has
Machine object removal device II8, ultrafiltration apparatus II9, two level washing device 23, enrichment facility III24 and sulfate crystal device 25；Institute
Again by pipeline and level-one after the first water outlet connection of the concentrated water spout and reuse water collection system 3 of the two fraction salt devices 14 stated
The water inlet connection of washing device 21；The concentrated water spout of the level-one washing device 21, the concentrated water spout of a fraction salt device 12 connect
It is connected again by pipeline with organic matter removal device II8 water inlets after logical, organic matter removal device II8 water outlets are filled by ultrafiltration
It puts and is connected again by the water inlet of pipeline and two level washing device 23 after II9 is connected with the second water outlet of reuse water collection system 3
It is logical；The concentrated water spout of the two level washing device 23 is connected by concentrated water device III24 with sulfate crystal device 25；
The production mouth of a river of the level-one washing device 21 passes through pipeline again after being connected with the production mouth of a river of two level washing device 23
It is connected with the water inlet of enrichment facility II22, the concentrated water spout of the enrichment facility II22 connects with the concentrated water spout of enrichment facility I13
It is logical；Enrichment facility I13, the enrichment facility II22 and the production mouth of a river of enrichment facility III24 are received by pipeline and recycle-water
3 water inlet of collecting system connects.
Technique is eluriated in sodium chloride and sodium sulphate separation concentration in a kind of strong brine zero-emission：Zero-emission strong brine is passed through except hard dress
It intakes after putting 11 processing as a fraction salt device 12, the water inlet of the production water of a fraction salt device 12 as enrichment facility I13 is dense
The concentrated water of compression apparatus I13 is taken off through organic matter removal device I4, silica removal device 5, carbon dioxide cleaner 6 and ultrafiltration apparatus 7
Water inlet after COD, desiliconization, decarburization and the turbid technique of drop as two fraction salt devices 14, the production water of two fraction salt devices 14 pass through chlorine
Change sodium evaporated crystallization device 15 and prepare high-purity sodium chloride（Sodium chloride content>99%）；The concentrated water of the two fraction salt devices 14
Mix the water inlet as level-one washing device 21 in proportion with part recycle-water in reuse water collection system 3；
The concentrated water of the level-one washing device 21 is mixed with the concentrated water of a fraction salt device 12 through organic matter removal device
II8 and ultrafiltration apparatus II9 carry out de- COD and drop after turbid process again with part recycle-water in reuse water collection system 3 by than
Water inlet of the example mixing as two level washing device 23；The concentrated water of the two level washing device 23 is concentrated through concentrated water device III24
Afterwards sodium sulfate in high purity is prepared into sulfate crystal device 25（Sodium sulphate content>95%）；The level-one washing device 21
Production water mixes the water inlet as enrichment facility II22 with the production water of two level washing device 23；The concentrated water of the enrichment facility II22
It is mixed with the concentrated water of enrichment facility I13 and carries out subsequent processing；Enrichment facility I13, enrichment facility II22 and the enrichment facility
The production water of III24 enters reuse water collection system 3, then cycles reuse again.
One fraction salt device 12, two fraction salt devices 14, level-one washing device 21 and the two level washing device 23 is equal
The separation of monovalent salt and divalent salts is carried out using extraordinary NF membrane；Enrichment facility I13, the enrichment facility II22 and concentration dress
It puts III24 and selects pollution-resistant bitter reverse-osmosis membrane element, super-pressure reverse-osmosis membrane element or resistance to anti-pollution reverse-osmosis with high salt
Membrane component.
The model FORTILIFE of the extraordinary NF membraneTMXC-N；The special separation NF membrane is a kind of helical coil
There is the poly- piperazine laminated film element of formula highly selective and higher monovalention transmitance and higher divalent ion to cut
Rate is stayed, the major part in strong brine can be converted to salting liquid that is pure, being more easy to crystallization.
The antipollution bitter reverse-osmosis membrane element model FORTILIFETMCR100, the super-pressure are anti-
Permeable membrane device model XUS180808, the resistance to anti-pollution reverse osmosis membrane element model FORTILIFE with high saltTM
XC70。
The one fraction salt device 12, two fraction salt devices 13 carry out point of monovalent salt and divalent salts using NF membrane
From；Level-one washing device 21 and two level washing device 25 are using selective ion isolation membrane component.
The concentrated water of the two fraction salt devices 14 uses part recycle-water in reuse water collection system 3 to be diluted, then
Elutriation purifying is carried out into level-one washing device 21；In the concentrated water of the two fraction salt devices 14 and reuse water collection system 3
Recycle-water mixed water in part is 9-11 times of two fraction salt devices, 14 concentrated water amount.The level-one washing device 21 it is dense
After water is mixed with the concentrated water of a fraction salt device 12, it is diluted, is entered back into using part recycle-water in reuse water collection system 3
Two level washing device 23 carries out elutriation purifying；The concentrated water of the level-one washing device 21 and the concentrated water of a fraction salt device 12 with
Recycle-water mixed water in part is the concentrated water and a fraction salt device 12 of level-one washing device 21 in reuse water collection system 3
2-2.5 times of concentrated water total Water.
The hardness removing device 11 uses resin softening process, and the resin is resistance to high COD and halophilic weak-type
Resin.
The organic matter removal device I and organic matter removal device II uses advanced oxidation processes organics removal.
Advanced oxidation processes belong to the prior art, with the characteristics of generating the hydroxyl radical free radical (OH) with Strong oxdiative ability, in high temperature
Under the reaction conditions such as high pressure, electricity, sound, light irradiation, catalyst, macromolecular hardly degraded organic substance is made to be oxidized to low toxicity or nontoxic small
Molecular substance.According to the mode and the difference of reaction condition generated free radicals, photochemical oxidation, catalytic wet oxygen can be classified as
Change, sonochemical oxidation, ozone oxidation, electrochemical oxidation and Fenton oxidation etc..Here just no longer it is described in detail.
The silica removal device uses magnesia mixture silicon removing process.The magnesia mixture is magnesium chloride or magnesia.Magnesium
Agent silicon removing process is medicament of the addition containing magnesium chloride or magnesia during lime treatment, by magnesium chloride or magnesia with
The complex reaction of silicate compound in water achievees the purpose that remove silicic acid.Its advantages of is except silicon is cheaply permitted than ion-exchange
It is more, and product is that precipitation particle is not soluble in water, is not polluted；Compared with ion exchange is except silicon, the soda acid that can save 96% is used
Amount.
Evaporative crystallization or freezing and crystallizing may be selected in the sulfate crystal device.
The system of the utility model can prepare high pure sodium chloride and high-purity sulphuric acid sodium simultaneously；Evaporated crystallization device operation is steady
Fixed, investment is low with operation cost；Each technique unit technology maturation, has a extensive future.
Various devices and reuse water collection system involved by the present embodiment belong to the well-known components of the industry and common knot
Structure or conventional means, do not describe one by one here.
Claims (5)
1. sodium chloride and sodium sulphate separation concentration elutriation system in a kind of strong brine zero-emission, it is characterised in that：The system includes
Sodium chloride separates concentration technology section（1）, sodium sulphate eluriate separation concentration technology section（2）With reuse water collection system（3）；
Wherein, sodium chloride separation concentration technology section（1）Including at least hardness removing device（11）, a fraction salt device（12）、
Enrichment facility I（13）, two fraction salt devices（14）With sodium chloride evaporated crystallization device（15）；Hardness removing device（11）Outlet and one
Fraction salt device（12）Water inlet connection, a fraction salt device（12）The production mouth of a river and enrichment facility I（13）Water inlet connect
It is logical, enrichment facility I（13）Concentrated water spout and two fraction salt devices（14）Water inlet connection, two fraction salt devices（14）Production water
Mouth and sodium chloride evaporated crystallization device（15）Connection；
The sodium sulphate eluriates separation concentration technology section（2）Including at least level-one washing device（21）, enrichment facility II（22）、
Two level washing device（23）, enrichment facility III（24）With sulfate crystal device（25）；The two fraction salt devices（14）'s
Concentrated water spout and reuse water collection system（3）The first water outlet connection after pass through pipeline and level-one washing device again（21）Water inlet
Mouth connection；The level-one washing device（21）Concentrated water spout, a fraction salt device（12）Concentrated water spout and recycle-water collect system
System（3）The second water outlet connection after pass through pipeline and two level washing device again（23）Water inlet connection；The two level is washed in a pan
Cleaning device（23）Concentrated water spout pass through concentrated water device III（24）With sulfate crystal device（25）Connection；
The level-one washing device（21）The production mouth of a river and two level washing device（23）The production mouth of a river connection after pass through pipeline again
With enrichment facility II（22）Water inlet connection, the enrichment facility II（22）Concentrated water spout and enrichment facility I（13）It is dense
The mouth of a river connects；The enrichment facility I（13）, enrichment facility II（22）With enrichment facility III（24）The production mouth of a river pass through pipe
Road and reuse water collection system（3）Water inlet connects.
2. sodium chloride and sodium sulphate separation concentration elutriation system in a kind of strong brine zero-emission according to claim 1,
It is characterized in that：The one fraction salt device（12）, two fraction salt devices（14）, level-one washing device（21）It eluriates and fills with two level
It puts（23）The separation of monovalent salt and divalent salts is carried out using extraordinary NF membrane；The enrichment facility I（13）, enrichment facility II
（22）With enrichment facility III（24）Select pollution-resistant bitter reverse-osmosis membrane element, super-pressure reverse-osmosis membrane element or resistance to height
One or more in salt anti-pollution reverse osmosis membrane element.
3. sodium chloride and sodium sulphate separation concentration elutriation system in a kind of strong brine zero-emission according to claim 2,
It is characterized in that：The model FORTILIFE of the extraordinary NF membraneTM XC-N；The reverse osmosis membrane element of antipollution bitter
Part model FORTILIFETMCR100, the super-pressure reverse-osmosis membrane element model XUS180808, the resistance to height
Salt anti-pollution reverse osmosis membrane element model FORTILIFETM XC70。
4. sodium chloride and sodium sulphate separation concentration are washed in a pan in a kind of strong brine zero-emission according to claim 1-3 any one
Wash system, it is characterised in that：The enrichment facility I（13）With two fraction salt devices（14）Between machine object is sequentially set with this
Removal device I（4）, silica removal device（5）, carbon dioxide cleaner（6）With ultrafiltration apparatus I（7）；The one fraction salt device
（12）With two level washing device（23）Between machine object removal device II is sequentially set with this（8）With ultrafiltration apparatus II（9）.
5. sodium chloride and sodium sulphate separation concentration elutriation system in a kind of strong brine zero-emission according to claim 1,
It is characterized in that：The hardness removing device（11）Using resin softening process, the resin is resistance to high COD and halophilic weak acid
Type resin.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721342603.5U CN207404854U (en) | 2017-10-18 | 2017-10-18 | Sodium chloride and sodium sulphate separation concentration elutriation system in strong brine zero-emission |
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|---|---|---|---|
| CN201721342603.5U CN207404854U (en) | 2017-10-18 | 2017-10-18 | Sodium chloride and sodium sulphate separation concentration elutriation system in strong brine zero-emission |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107662929A (en) * | 2017-10-18 | 2018-02-06 | 西安聚方环境科技有限公司 | Technique and system are eluriated in sodium chloride and sodium sulphate separation concentration in strong brine zero-emission |
-
2017
- 2017-10-18 CN CN201721342603.5U patent/CN207404854U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107662929A (en) * | 2017-10-18 | 2018-02-06 | 西安聚方环境科技有限公司 | Technique and system are eluriated in sodium chloride and sodium sulphate separation concentration in strong brine zero-emission |
| CN107662929B (en) * | 2017-10-18 | 2024-01-19 | 西安聚方环境科技有限公司 | Sodium chloride and sodium sulfate separation concentration elutriation process and system in strong brine zero emission |
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