CN104829031A - Comprehensive desalting recovering method and system of MEG saline wastewater - Google Patents
Comprehensive desalting recovering method and system of MEG saline wastewater Download PDFInfo
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Abstract
The invention discloses a comprehensive desalting recovering method and system of MEG saline wastewater. The method comprises the following steps: dehydrating and concentrating the MEG saline wastewater in a multi-level membrane distilling-crystallizing process, when the concentration of the salt in the MEG saline wastewater reaches the hyper-saturated state, adding a certain amount of seed crystals into a crystallizing kettle to induce the salt in the MEG saline wastewater to separate out in certain size distribution, so that the MEG concentration and recovery, the high-purity infiltration water recovery and the inorganic salt crystal recovery with specific size distribution can be synchronously processed, the zero discharge of the MEG saline wastewater can be reached and the comprehensive utilization value of the MEG saline wastewater can be increased. The processed raw material is a rich liquid raw material or a barren liquid raw material, the temperature of the processed raw material is 45-80 DEG C, and the transportation flow rate of the raw material is 0.2-3 m/s. The operation flow is continuous operation or intermittent operation. The direct contact membrane distillation or vacuum membrane distillation can be used in the membrane distillation process.
Description
Technical field
The total score of the MEG brine waste the invention belongs to trade effluent and reclaim field, particularly recover the oil, producing in chemical process is from, desalination recovery method and system.
Background technology
In oil recovery and Chemical Manufacture, the normal MEG that uses avoids pipeline frozen block as the absorption agent of free-water, and this will produce a large amount of MEG waste water.Containing plurality of inorganic salt, organism and water in this waste water.For effectively saving production cost, reaching the requirement of country to environmental protection, this MEG waste water effectively to be processed and the MEG reclaimed wherein just becomes particularly important.
At present, process oil field MEG waste water reclamation ethylene glycol wherein and have two kinds of methods: conventional regeneration method and the comprehensive regeneration techniques comprising desalination.Conventional regeneration method uses rectifying to carry out except hydrocarbon and processed MEG rich solution (in liquid, water-content is larger), and salinity and nonvolatile impurity still retain in MEG lean solution (in liquid, water-content is less) after regeneration.Because the salinity crystallization in MEG rich solution, deposition make the easy fouling of reboiler, run after for some time will clear up, scale removal, greatly reduce efficiency and the economy of process.Along with recent Offshore Oil Industry is to the development in deep water field, traditional means is only adopted to remove the moisture in MEG rich solution and cause the problem of salt separating/enriching crystallization more and more to seem serious.Some companies start to adopt the comprehensive regeneration techniques comprising desalination: MEG rich solution after holomorphosis, then adopts the salinity in distillation method removing MEG lean solution, can not contain salt and nonvolatile impurity in the lean solution obtained.But use distillation method water and MEG to be steamed, institute's heat requirement is large, and running cost is high simultaneously, limits the method and reclaiming the application in MEG desalination.
Along with the fast development of membrane science and technology, there is a kind of novel water technology---film distillation technology in recent years.This technology can be separated the larger material of boiling point difference under lower service temperature.At present, existing patent report uses film distillation technology to be separated the mixing solutions of MEG and water, as Chinese patent CN104415664A, CN104415665A and CN104415666A, it is 60 ~ 70% that these patents make the MEG aqueous solution be concentrated into massfraction by film distillation technology effectively, but only the salinity in MEG waste water can not be removed by film distillation technology.
Simultaneously, along with the development of film distillation technology in recent years, research is had membrane distillation and crystallization technique to be coupled together process waste water, as Chinese patent 200910169389.1 employs the technical process of " acid adjustment+membrane distillation+reverse osmosis+crystallisation by cooling " to process nitro-chlorobenzene height salt organic waste water, take full advantage of the low-grade energy of waste water self, be effectively stripped of the salinity in waste water and organism.But the method can only process the lower waste water of organic concentration, and higher with reverse-osmosis treated membrane distillation infiltration water solution cost; Flow process adopts crystallisation by cooling simultaneously, and energy expenditure is comparatively large, not easily completes the continuity process of waste water raw material.
Therefore, in order to make up the deficiency of existing MEG saliferous wastewater processing technology and existing membrane distillation-crystallization coupling technique, this patent establishes the membrane distillation-crystallization coupled system that effectively can process MEG salt-containing solution, comparatively pure infiltration water and the inorganic salt crystal with specified particle diameter distribution is obtained while concentration and recovery MEG, realize MEG concentration and recovery, synchronously the completing of dehydration and desalination, zero discharge of industrial waste water, improves the rate of recovery and the comprehensive utilization value of MEG waste water.
Summary of the invention
The present invention proposes to belong to trade effluent and reclaims field, and the total score of the MEG waste water particularly recover the oil, produced in chemical process is from, desalination recovery method and system.Adopt membrane distillation method that the concentration of salt in MEG brine waste is constantly raised, after reaching hypersaturated state, by adding crystal seed in crystallization kettle, the salinity in MEG brine waste is separated out with certain size-grade distribution, realize MEG concentration and recovery, synchronously the completing of dehydration and desalination, realize the zero release of MEG brine waste, improve the rate of recovery and the comprehensive utilization value of MEG brine waste.
Technical scheme of the present invention:
A kind of comprehensive desalination recovery method of MEG brine waste and system, it is characterized in that, 5 valves are provided with in this system, valve 1 enters first-level buffer tank for controlling rich solution raw material, valve 2 enters crystallization kettle for controlling lean solution raw material, valve 3 is arranged between crystallization kettle and first-level buffer tank, and valve 4 is arranged between crystallization kettle and level 2 buffering tank, and valve 5 is arranged between rich solution raw material and crystallization kettle; Step is as follows:
(1) when pending raw material be MEG massfraction be less than the rich solution raw material of 60% time, Open valve 1 and valve 4, valve-off 2, valve 3 and valve 5, make rich solution raw material enter first-level buffer tank and heat; Rich solution raw material, after the first surge tank heating, enters one-level distillation film component; The infiltration gas of one-level membrane component becomes to concentrate after liquid through condenser condenses and is transported to penetrating fluid storage tank, and the rich solution raw material after one-level membrane component concentrates is concentrated and is transported to level 2 buffering tank and heats;
(2) rich solution raw material is after the heating of level 2 buffering tank, is delivered in secondary membrane component and processes; The infiltration gas of secondary membrane component becomes after liquid to be delivered to penetrating fluid storage tank through condenser condenses, rich solution feedstock transportation simultaneously after secondary membrane component concentrates, to crystallization kettle, realizes rich solution raw material and concentrates in crystallization kettle, circulation between level 2 buffering tank and secondary membrane component;
(3) when the salt concentration of rich solution raw material reaches hypersaturated state in crystallization kettle, in crystallization kettle, add crystal seed, bring out the salinity crystallization in crystallization kettle in rich solution raw material; When the concentration of MEG reaches aimed concn in crystallization kettle, open whizzer, carry out the centrifugation of MEG Ethylene recov and inorganic salt crystal; Kind to the crystal seed described in crystallization is identical with the kind of salinity in pending raw material, and the quality adding crystal seed is 0.1 ~ 5% of salinity quality in pending raw material;
(4) when pending raw material be MEG massfraction be greater than the lean solution raw material of 60% time, Open valve 2 and valve 4, valve-off 1, valve 3 and valve 5, directly by lean solution feedstock transportation to crystallization kettle, realize lean solution raw material and concentrate in crystallization kettle, circulation between level 2 buffering tank and secondary membrane component; The same step of last handling process (3).
Described treating processes is operate continuously process or batch process procedures.
When using periodical operation process rich solution raw material, open valve 3 and valve 5, valve-off 1, valve 2 and valve 4, join in crystallization kettle by disposable for rich solution raw material, realize rich solution raw material and concentrate in first-level buffer tank, one-level membrane component, level 2 buffering tank, circulation between secondary membrane component and crystallization kettle; When in rich solution raw material in crystallization kettle, the massfraction of MEG is greater than 60%, valve-off 3, opens valve 4, realizes rich solution raw material and concentrates in level 2 buffering tank, circulation between secondary membrane component and crystallization kettle; When the salt concentration of rich solution raw material reaches hypersaturated state in crystallization kettle, in crystallization kettle, add a certain amount of crystal seed, bring out the salinity crystallization in crystallization kettle in rich solution raw material; When in rich solution raw material in crystallization kettle, the massfraction of MEG reaches target call, valve-off 4, opens whizzer, carries out the centrifugation of MEG Ethylene recov and inorganic salt crystal; The kind of described crystal seed is identical with the kind of salinity in pending raw material, and the quality adding crystal seed is 0.1 ~ 5% of salinity quality in pending raw material;
When using periodical operation process lean solution raw material, open valve 2 and valve 4, valve-off 1, valve 3 and valve 5, join in crystallization kettle by disposable for lean solution raw material, realizes lean solution raw material and concentrate in level 2 buffering tank, circulation between secondary membrane component and crystallization kettle; When the salt concentration of lean solution raw material reaches hypersaturated state in crystallization kettle, in crystallization kettle, add a certain amount of crystal seed, bring out the salinity crystallization in crystallization kettle in lean solution raw material; When in lean solution raw material in crystallization kettle, the massfraction of MEG reaches target call, valve-off 4, opens whizzer, carries out the centrifugation of MEG Ethylene recov and inorganic salt crystal; The kind of described crystal seed is identical with the kind of salinity in pending raw material, and the quality adding crystal seed is 0.1 ~ 5% of salinity quality in pending raw material.
Described crystallization kettle, first-level buffer tank and level 2 buffering tank all have temperature control equipment, in crystallization kettle, the temperature of raw material controls to be 45 ~ 80 DEG C, and the temperature maintenance of first-level buffer tank and raw material in level 2 buffering tank is identical and higher than the temperature of raw material in crystallization kettle 5 ~ 10 DEG C; The circulation conveying of whole treatment system Raw is having transported by pump, and raw material flow velocity is in the duct 0.2 ~ 3m/s.
In operating process, one-level membrane distillation uses per-meate side temperature of cooling water to be the direct contact membrane distillation of 15 ~ 25 DEG C or per-meate side vacuum tightness to be the vacuum type membrane distillation of 0.01 ~ 0.09MPa, and one-level membrane component uses multistage parallel form; Secondary membrane distillation use per-meate side vacuum tightness is the vacuum type membrane distillation of 0.01 ~ 0.09MPa; The material of the membrane distillation in membrane component all adopts the microporous membrane material with hydrophobic property, and the surperficial mean pore size of microporous membrane is 0.01 ~ 1 μm, and microporous membrane mean porosities is 30 ~ 85%.
Mould material in described film distillation film component is tetrafluoroethylene, polyvinylidene difluoride (PVDF), polyethylene or polypropylene, and passes through the obtained hydrophobic material of tetrafluoroethylene, polyvinylidene difluoride (PVDF), polyethylene or polypropylene modification.
The method and system of the process MEG brine waste that the present invention proposes possesses following advantage:
(1) concentration range processing raw material is wide, flexible operation mode.
(2) service temperature is low, and working pressure is low, save energy.
(3) crystallographic granularity is controlled, is beneficial to crystal and recycles.
(4) in penetrating fluid, quality mark is high, can recycle, and avoids the discharge of sewage.
(5) membrane module integrated level is high, and volume is little, simultaneously hydrophobic microporous membrane low price, easily obtain.
Accompanying drawing explanation
Accompanying drawing is the system schematic of membrane distillation-crystallization coupling processing MEG brine waste.
In figure: 1 crystallization kettle; 2 first-level buffer tanks; 3 one-level membrane component; 4 condensers; 5 penetrating fluid storages
Tank; 6 level 2 buffering tanks; 7 secondary membrane component; 8 valves 1; 9 valves 2; 10 valves 3;
11 valves 4; 12 valves 5; 13 whizzers.
Embodiment
Below in conjunction with accompanying drawing and technical scheme, further illustrate the specific embodiment of the present invention.
Embodiment 1
Pending raw material is 70 DEG C, salt (kind is NaCl) concentration to be 96g/L, MEG massfraction be 50% rich solution raw material, the flow velocity of feedstock transportation is 0.5m/s.First Open valve 1 and valve 4, valve-off 2, valve 3 and valve 5, make rich solution raw material enter first-level buffer tank and heat; Raw material rich solution raw material is after the first surge tank is heated to 75 DEG C, (membrane module mould material used is hydrophobic polyvinylidene fluoride microporous film to divide three strands to enter the one-level membrane component be made up of direct contact membrane distillation, film mean pore size is 1.0 μm, mean porosities is 70%), direct contact membrane distillation per-meate side use temperature is the pure water cooling of 20 DEG C; The infiltration gas of one-level membrane component becomes to concentrate after liquid through condenser condenses and is transported to infiltration water holding tank, and the rich solution raw material simultaneously after one-level membrane component concentrates is concentrated and is transported to level 2 buffering tank and heats.Rich solution raw material after being concentrated by one-level membrane component is after level 2 buffering tank is heated to 75 DEG C, (membrane module mould material used is hydrophobic polyvinylidene fluoride microporous film to be delivered to secondary membrane component, film mean pore size is 1.0 μm, mean porosities is 70%) process, the vacuum tightness of secondary membrane distillation module permeate side is 0.09MPa; The infiltration gas of secondary membrane component becomes after liquid to be delivered to infiltration water holding tank through condenser condenses, rich solution feedstock transportation simultaneously after secondary membrane component concentrates is to crystallization kettle, in crystallization control still, the temperature of rich solution raw material is 70 DEG C, realizes rich solution raw material and concentrates in crystallization kettle, circulation between level 2 buffering tank and second membrane module.When salt concn is 100g/L in rich solution raw material in crystallization kettle, in crystallization kettle, adds the crystal seed (kind is NaCl) that quality is rich solution raw material salt point quality 5% in crystallization kettle, start to carry out salinity crystallization; When the massfraction (disregarding salinity) of MEG in rich solution raw material in crystallization kettle is 90%, valve-off 4, opens whizzer, carries out the centrifugation of MEG Ethylene recov and inorganic salt crystal.
Embodiment 2
Pending raw material is 50 DEG C, salt (kind is NaCl) concentration to be 70g/L, MEG massfraction be 65% lean solution raw material, the flow velocity of feedstock transportation is 2.5m/s.First Open valve 2 and valve 4, valve-off 1, valve 3 and valve 5, directly by lean solution feedstock transportation to crystallization kettle, in crystallization control still, the temperature of lean solution raw material is 50 DEG C, the temperature controlling lean solution raw material in level 2 buffering tank is 55 DEG C, (membrane module mould material used is hydrophobic microporous teflon membran to secondary membrane component, film mean pore size is 0.02 μm, mean porosities is 50%) per-meate side vacuum degree is 0.05MPa, realize lean solution raw material at crystallization kettle, (membrane module mould material used is hydrophobic microporous teflon membran for level 2 buffering tank and secondary membrane component, film mean pore size is 0.08 μm, mean porosities is 50%) between circulation concentrate, when salt concn is 80g/L in lean solution raw material in crystallization kettle, in crystallization kettle, adds the crystal seed (kind is NaCl) that quality is lean solution raw material salt point quality 0.1%, start to carry out salinity crystallization, when in crystallization kettle lean solution raw material, the massfraction (disregarding salinity) of MEG is 90%, valve-off 4, opens whizzer, carries out the centrifugation of MEG Ethylene recov and inorganic salt crystal.
Embodiment 3
Pending raw material is 65 DEG C, salt (kind is NaCl) concentration to be 80g/L, MEG massfraction be 55% rich solution raw material, the flow velocity of feedstock transportation is 2.0m/s.Open valve 3 and valve 5, valve-off 1, valve 2 and valve 4, join in crystallization kettle by disposable for rich solution raw material, in crystallization control still, the temperature of rich solution raw material is 65 DEG C, controlling rich solution material temperature in first-level buffer tank is 75 DEG C, (membrane module mould material used is hydrophobic microporous polypropylene membrane to one-level membrane distillation, film mean pore size is 0.01 μm, mean porosities is 40%) use vacuum type membrane distillation, vacuum tightness is 0.07MPa, controlling rich solution material temperature in level 2 buffering tank is 75 DEG C, (membrane module mould material used is hydrophobic microporous polypropylene membrane in secondary membrane distillation, film mean pore size is 0.06 μm, mean porosities is 40%) use vacuum membrane distillation, vacuum tightness is 0.08MPa, realize rich solution raw material at first-level buffer tank, one-level membrane module, level 2 buffering tank, circulation between second membrane module and crystallization kettle concentrates, when the massfraction (disregarding salinity) of MEG in rich solution raw material in crystallization kettle is greater than 60%, valve-off 3, opens valve 4, realizes rich solution raw material and concentrates in level 2 buffering tank, circulation between second membrane module and crystallization kettle, when salt concn is 85g/L in lean solution raw material in crystallization kettle, in crystallization kettle, adds the crystal seed (kind is NaCl) that quality is lean solution raw material salt point quality 3%, start to carry out salinity crystallization, when the massfraction (disregarding salinity) 90% of MEG in rich solution raw material in crystallization kettle, valve-off 4, opens whizzer, carries out the centrifugation of MEG Ethylene recov and inorganic salt crystal.
Embodiment 4
Pending raw material is 65 DEG C, salt (kind is NaCl) concentration to be 60g/L, MEG massfraction be 75% lean solution raw material, the flow velocity of feedstock transportation is 1.5m/s.Open valve 4 and valve 5, valve-off 1, valve 2 and valve 3, join in crystallization kettle by disposable for lean solution raw material, the temperature of crystallization control still is 65 DEG C, the temperature controlling lean solution raw material in level 2 buffering tank is 75 DEG C, (membrane module mould material used is hydrophobic polyvinylidene fluoride microporous film to secondary membrane component, film mean pore size is 1.0 μm, mean porosities is 70%) per-meate side vacuum degree is 0.05MPa, realizes lean solution raw material and concentrates in crystallization kettle, circulation between level 2 buffering tank and secondary membrane component; When salt concn is 70g/L in lean solution raw material in crystallization kettle, in crystallization kettle, adds the crystal seed (kind is NaCl) that quality is lean solution raw material salt point quality 1%, start to carry out salinity crystallization; When in crystallization kettle lean solution raw material, the massfraction (disregarding salinity) of MEG is 90%, valve-off 4, opens whizzer, carries out the centrifugation of MEG Ethylene recov and inorganic salt crystal.
Open and the treatment process that proposes of the present invention and system are described by good embodiment, and those skilled in the art can according to present disclosure, and appropriate change processing links realizes.Of particular note, all similar changes are all deemed to be included in spirit of the present invention, scope and content.
Claims (8)
1. the comprehensive desalination recovery method of a MEG brine waste and system, it is characterized in that, 5 valves are provided with in this system, valve 1 enters first-level buffer tank for controlling rich solution raw material, valve 2 enters crystallization kettle for controlling lean solution raw material, valve 3 is arranged between crystallization kettle and first-level buffer tank, and valve 4 is arranged between crystallization kettle and level 2 buffering tank, and valve 5 is arranged between rich solution raw material and crystallization kettle; Step is as follows:
(1) when pending raw material be MEG massfraction be less than the rich solution raw material of 60% time, Open valve 1 and valve 4, valve-off 2, valve 3 and valve 5, make rich solution raw material enter first-level buffer tank and heat; Rich solution raw material, after the first surge tank heating, enters one-level distillation film component; The infiltration gas of one-level membrane component becomes to concentrate after liquid through condenser condenses and is transported to penetrating fluid storage tank, and the rich solution raw material after one-level membrane component concentrates is concentrated and is transported to level 2 buffering tank and heats;
(2) rich solution raw material is after the heating of level 2 buffering tank, is delivered in secondary membrane component and processes; The infiltration gas of secondary membrane component becomes after liquid to be delivered to penetrating fluid storage tank through condenser condenses, rich solution feedstock transportation simultaneously after secondary membrane component concentrates, to crystallization kettle, realizes rich solution raw material and concentrates in crystallization kettle, circulation between level 2 buffering tank and secondary membrane component;
(3) when the salt concentration of rich solution raw material reaches hypersaturated state in crystallization kettle, in crystallization kettle, add crystal seed, bring out the salinity crystallization in crystallization kettle in rich solution raw material; When the concentration of MEG reaches aimed concn in crystallization kettle, open whizzer, carry out the centrifugation of MEG Ethylene recov and inorganic salt crystal; Kind to the crystal seed described in crystallization is identical with the kind of salinity in pending raw material, and the quality adding crystal seed is 0.1 ~ 5% of salinity quality in pending raw material;
(4) when pending raw material be MEG massfraction be greater than the lean solution raw material of 60% time, Open valve 2 and valve 4, valve-off 1, valve 3 and valve 5, directly by lean solution feedstock transportation to crystallization kettle, realize lean solution raw material and concentrate in crystallization kettle, circulation between level 2 buffering tank and secondary membrane component; The same step of last handling process (3).
2. comprehensive desalination recovery method according to claim 1 and system, is characterized in that, described treating processes is operate continuously process or batch process procedures.
3. comprehensive desalination recovery method according to claim 2 and system, it is characterized in that, when using periodical operation process rich solution raw material, open valve 3 and valve 5, valve-off 1, valve 2 and valve 4, join in crystallization kettle by disposable for rich solution raw material, realize rich solution raw material and concentrate in first-level buffer tank, one-level membrane component, level 2 buffering tank, circulation between secondary membrane component and crystallization kettle; When in rich solution raw material in crystallization kettle, the massfraction of MEG is greater than 60%, valve-off 3, opens valve 4, realizes rich solution raw material and concentrates in level 2 buffering tank, circulation between secondary membrane component and crystallization kettle; When the salt concentration of rich solution raw material reaches hypersaturated state in crystallization kettle, in crystallization kettle, add a certain amount of crystal seed, bring out the salinity crystallization in crystallization kettle in rich solution raw material; When in rich solution raw material in crystallization kettle, the massfraction of MEG reaches target call, valve-off 4, opens whizzer, carries out the centrifugation of MEG Ethylene recov and inorganic salt crystal; The kind of described crystal seed is identical with the kind of salinity in pending raw material, and the quality adding crystal seed is 0.1 ~ 5% of salinity quality in pending raw material;
When using periodical operation process lean solution raw material, open valve 2 and valve 4, valve-off 1, valve 3 and valve 5, join in crystallization kettle by disposable for lean solution raw material, realizes lean solution raw material and concentrate in level 2 buffering tank, circulation between secondary membrane component and crystallization kettle; When the salt concentration of lean solution raw material reaches hypersaturated state in crystallization kettle, in crystallization kettle, add a certain amount of crystal seed, bring out the salinity crystallization in crystallization kettle in lean solution raw material; When in lean solution raw material in crystallization kettle, the massfraction of MEG reaches target call, valve-off 4, opens whizzer, carries out the centrifugation of MEG Ethylene recov and inorganic salt crystal; The kind of described crystal seed is identical with the kind of salinity in pending raw material, and the quality adding crystal seed is 0.1 ~ 5% of salinity quality in pending raw material.
4. according to the arbitrary described comprehensive desalination recovery method of claim 1-3 and system, it is characterized in that, described crystallization kettle, first-level buffer tank and level 2 buffering tank all have temperature control equipment, in crystallization kettle, the temperature of raw material controls to be 45 ~ 80 DEG C, and the temperature maintenance of first-level buffer tank and raw material in level 2 buffering tank is identical and higher than the temperature of raw material in crystallization kettle 5 ~ 10 DEG C; The circulation conveying of whole treatment system Raw is having transported by pump, and raw material flow velocity is in the duct 0.2 ~ 3m/s.
5. according to the arbitrary described comprehensive desalination recovery method of claim 1-3 and system, it is characterized in that, in operating process, one-level membrane distillation uses per-meate side temperature of cooling water to be the direct contact membrane distillation of 15 ~ 25 DEG C or per-meate side vacuum tightness to be the vacuum type membrane distillation of 0.01 ~ 0.09MPa, and one-level membrane component uses multistage parallel form; Secondary membrane distillation use per-meate side vacuum tightness is the vacuum type membrane distillation of 0.01 ~ 0.09MPa; The material of the membrane distillation in membrane component all adopts the microporous membrane material with hydrophobic property, and the surperficial mean pore size of microporous membrane is 0.01 ~ 1 μm, and microporous membrane mean porosities is 30 ~ 85%.
6. comprehensive desalination recovery method according to claim 4 and system, it is characterized in that, in operating process, one-level membrane distillation uses per-meate side temperature of cooling water to be the direct contact membrane distillation of 15 ~ 25 DEG C or per-meate side vacuum tightness to be the vacuum type membrane distillation of 0.01 ~ 0.09MPa, and one-level membrane component uses multistage parallel form; Secondary membrane distillation use per-meate side vacuum tightness is the vacuum type membrane distillation of 0.01 ~ 0.09MPa; The material of the membrane distillation in membrane component all adopts the microporous membrane material with hydrophobic property, and the surperficial mean pore size of microporous membrane is 0.01 ~ 1 μm, and microporous membrane mean porosities is 30 ~ 85%.
7. comprehensive desalination recovery method according to claim 5 and system, it is characterized in that, mould material in described film distillation film component is tetrafluoroethylene, polyvinylidene difluoride (PVDF), polyethylene or polypropylene, and passes through the obtained hydrophobic material of tetrafluoroethylene, polyvinylidene difluoride (PVDF), polyethylene or polypropylene modification.
8. comprehensive desalination recovery method according to claim 6 and system, it is characterized in that, mould material in described film distillation film component is tetrafluoroethylene, polyvinylidene difluoride (PVDF), polyethylene or polypropylene, and passes through the obtained hydrophobic material of tetrafluoroethylene, polyvinylidene difluoride (PVDF), polyethylene or polypropylene modification.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2017052377A1 (en) * | 2015-09-25 | 2017-03-30 | Statoil Petroleum As | Method for removing sodium chloride |
| CN108623062A (en) * | 2017-03-17 | 2018-10-09 | 中国科学院城市环境研究所 | A kind of system of multistage membrane crystallization integrated treatment brine waste |
| CN111039354A (en) * | 2018-10-12 | 2020-04-21 | 卫风科技股份有限公司 | Filter system and operation method thereof |
| CN111948112A (en) * | 2020-08-10 | 2020-11-17 | 盐城新海川机电科技有限公司 | Penetrating fluid constant-pressure quantitative supply method and device |
| WO2022062315A1 (en) * | 2020-09-27 | 2022-03-31 | 江苏科技大学 | Desalination system for glycol lean liquid containing high-solubility salt in deep-sea natural gas extraction, and desalination method thereof |
-
2015
- 2015-05-19 CN CN201510259292.5A patent/CN104829031B/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2017052377A1 (en) * | 2015-09-25 | 2017-03-30 | Statoil Petroleum As | Method for removing sodium chloride |
| CN108623062A (en) * | 2017-03-17 | 2018-10-09 | 中国科学院城市环境研究所 | A kind of system of multistage membrane crystallization integrated treatment brine waste |
| CN111039354A (en) * | 2018-10-12 | 2020-04-21 | 卫风科技股份有限公司 | Filter system and operation method thereof |
| CN111948112A (en) * | 2020-08-10 | 2020-11-17 | 盐城新海川机电科技有限公司 | Penetrating fluid constant-pressure quantitative supply method and device |
| WO2022062315A1 (en) * | 2020-09-27 | 2022-03-31 | 江苏科技大学 | Desalination system for glycol lean liquid containing high-solubility salt in deep-sea natural gas extraction, and desalination method thereof |
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| Publication number | Publication date |
|---|---|
| CN104829031B (en) | 2016-08-24 |
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