CN112263912A - Oil gas exploitation contains salt ethylene glycol solution desalination device based on electrodialysis technique - Google Patents
Oil gas exploitation contains salt ethylene glycol solution desalination device based on electrodialysis technique Download PDFInfo
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- CN112263912A CN112263912A CN202011316566.7A CN202011316566A CN112263912A CN 112263912 A CN112263912 A CN 112263912A CN 202011316566 A CN202011316566 A CN 202011316566A CN 112263912 A CN112263912 A CN 112263912A
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- electrodialyzer
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- glycol solution
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- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 title claims abstract description 116
- 238000010612 desalination reaction Methods 0.000 title claims abstract description 14
- 150000003839 salts Chemical class 0.000 title claims abstract description 14
- 238000000909 electrodialysis Methods 0.000 title claims abstract description 8
- 238000000034 method Methods 0.000 title claims description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 50
- 239000013535 sea water Substances 0.000 claims abstract description 23
- 238000005516 engineering process Methods 0.000 claims abstract description 6
- 239000000243 solution Substances 0.000 claims description 36
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims description 19
- 238000011033 desalting Methods 0.000 claims description 13
- 239000012528 membrane Substances 0.000 claims description 7
- 239000007864 aqueous solution Substances 0.000 claims description 3
- 238000005341 cation exchange Methods 0.000 claims description 3
- 239000007832 Na2SO4 Substances 0.000 claims 1
- 229910052938 sodium sulfate Inorganic materials 0.000 claims 1
- 239000007789 gas Substances 0.000 abstract description 11
- 238000005265 energy consumption Methods 0.000 abstract description 6
- NMJORVOYSJLJGU-UHFFFAOYSA-N methane clathrate Chemical compound C.C.C.C.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O NMJORVOYSJLJGU-UHFFFAOYSA-N 0.000 abstract description 6
- 239000005431 greenhouse gas Substances 0.000 abstract description 2
- 239000000203 mixture Substances 0.000 abstract description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 10
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 6
- 239000003345 natural gas Substances 0.000 description 5
- 239000011780 sodium chloride Substances 0.000 description 5
- 239000007788 liquid Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- -1 salt ions Chemical class 0.000 description 4
- 230000005540 biological transmission Effects 0.000 description 3
- 150000001768 cations Chemical class 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 2
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 239000008398 formation water Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000012466 permeate Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- WDIHJSXYQDMJHN-UHFFFAOYSA-L barium chloride Chemical compound [Cl-].[Cl-].[Ba+2] WDIHJSXYQDMJHN-UHFFFAOYSA-L 0.000 description 1
- 229910001626 barium chloride Inorganic materials 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- 235000011148 calcium chloride Nutrition 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 229910001629 magnesium chloride Inorganic materials 0.000 description 1
- 239000001103 potassium chloride Substances 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
- B01D61/422—Electrodialysis
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/58—Multistep processes
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Urology & Nephrology (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
本发明涉及一种基于电渗析技术的油气开采含盐乙二醇溶液脱盐装置，属于油气开采技术领域，应用于海上油气田和未来天然气水合物开采。其技术要点是：采用3级串联脱盐方案，主要由3台电渗析器，1台乙二醇溶液输送泵、1台海水输送泵、1台极水循环泵、极水罐、控制箱组成，各部门间通过对应的管路连接；设有控制箱供电并控制脱盐率。本发明在常温下运行，大大减少能源消耗，降低温室气体排放，环境友好；组成简单，操作方便；体积小、布置灵活；投资少，能耗少，运行成本低，具有良好的经济性。
The invention relates to a salt-containing ethylene glycol solution desalination device for oil and gas exploitation based on electrodialysis technology, belongs to the technical field of oil and gas exploitation, and is applied to offshore oil and gas fields and future natural gas hydrate exploitation. Its technical points are: adopting a 3-stage series desalination scheme, mainly composed of 3 electrodialyzers, 1 ethylene glycol solution delivery pump, 1 seawater delivery pump, 1 extreme water circulation pump, extreme water tank, and control box. It is connected by corresponding pipelines; there is a control box to supply power and control the desalination rate. The invention operates at normal temperature, greatly reduces energy consumption, reduces greenhouse gas emissions, and is environmentally friendly; simple in composition, convenient in operation; small in size and flexible in arrangement; low in investment, low in energy consumption, low in operating cost, and good in economy.
Description
Technical Field
The invention relates to a desalting device for oil and gas exploitation saline ethylene glycol solution based on an electrodialysis technology, belongs to the technical field of oil and gas exploitation, and is applied to offshore oil and gas fields and future natural gas hydrate exploitation.
Background
When natural gas is transmitted underwater in the process of exploitation of an offshore oil and gas field and the future exploitation of natural gas hydrate, secondary generation of the natural gas hydrate is easily generated at low temperature and high pressure, a transmission pipeline is blocked or a valve is damaged, normal operation of exploitation activities is influenced, even production is stopped, and huge economic loss is caused. The ethylene glycol is used as a reliable natural gas hydrate generation inhibitor and can be injected into an underwater natural gas conveying pipeline through a pipeline, so that the generation dew point of the natural gas hydrate is reduced to a reasonable range below the transmission temperature, and the safe conveying of the natural gas is ensured.
During the exploitation process, the formation water permeates into the exploitation well and is conveyed to the offshore production platform along with the natural gas for treatment. The formation water contains a large amount of soluble salts (NaCl, KCl, MgCl2, CaCl2, BaCl2 and the like), salt ions are continuously accumulated in the glycol solution, and part of the salt ions are injected into the underwater natural gas transmission pipeline along with the glycol barren solution. The traditional ethylene glycol regeneration and desalination process adopts a distillation crystallization mode, the heating temperature is high, and after long-term operation, salt ions can form scale on the surfaces of a reboiler and a heat exchanger, so that the heat efficiency is reduced, and the problems of serious corrosion and rust are caused.
The factors of economy, environmental protection, safety and the like are considered, ethylene glycol is generally dehydrated and desalted, and the ethylene glycol is recycled after reaching the standard.
A rectification process is adopted for desalting monovalent salt in a traditional offshore ethylene glycol regeneration and recovery (MRU) system. As a traditional desalination method in an ethylene glycol regeneration and recovery (MRU) system, a rectification process needs to be provided with a distillation tower with a large volume, and salt concentration is improved by heating a salt-containing ethylene glycol solution and evaporating ethylene glycol and water to generate salt crystals, so that the aim of finally separating monovalent high-dissolved salt is fulfilled.
The traditional rectification process equipment has the defects of large and complex equipment, high operation difficulty and large consumption of heat energy in the evaporation process.
Disclosure of Invention
In order to solve the defects of the prior art, the invention provides the desalting device for the oil and gas exploitation saline ethylene glycol solution based on the electrodialysis technology, and the desalting device has the advantages of simple system, light weight and low energy consumption.
In order to achieve the purpose, the technical scheme of the invention is as follows: a desalting device for oil and gas exploitation saline ethylene glycol solution based on electrodialysis technology adopts a 3-stage series desalting scheme, mainly comprises 3 electrodialysers, 1 ethylene glycol solution delivery pump, 1 seawater delivery pump, 1 polar water circulating pump, polar water tanks and a control box, wherein all the doors are connected through corresponding pipelines; a control box is arranged to supply power and control the desalination rate;
the method is characterized in that:
the electrodialyzer is provided with 3 electrodialyzers, and consists of a desalting chamber, a concentrating chamber, an anode chamber, a cathode chamber and 100 pairs of special anion-cation exchange membranes; 3 electrodialysers are connected in series; the first-stage electrodialyzer and the second-stage electrodialyzer are respectively communicated through pipelines and are used for transmitting glycol solution and seawater, and the second-stage electrodialyzer and the third-stage electrodialyzer are respectively communicated through pipelines and are used for transmitting glycol solution and seawater; the glycol solution delivery pump is connected with the electrodialyzer through a pipeline; the seawater delivery pump is connected with the electrodialyzer through a pipeline;
the volume of the polar water tank is 100L, and an extremely-high water solution which is 3 percent of Na is stored in the polar water tank2SO4An aqueous solution; the polar water tank is connected with a polar water circulating pump through a pipeline and is divided into two paths, one path is sequentially connected with an anode chamber of the electrodialyzer through the pipeline respectively, and the other path is sequentially connected with a cathode chamber of the electrodialyzer through the pipeline respectively; the anode chamber and the cathode chamber of the electrodialyzer are connected with the polar water tank through pipelines, so that closed circulation is formed between the polar water tank of each electrodialyzer and the polar water circulating pump;
the pressure of the glycol solution delivery pump, the seawater delivery pump and the polar water circulating pump is 5.5bar (maximum 10.0bar), and the flow rate is 150L/h;
the input voltage of the control box is 440V, and the phase is 3; respectively supplying power to an ethylene glycol solution delivery pump, a seawater delivery pump and an extreme water circulating pump; presetting input voltage and current of an electrodialyzer in a control system according to the flow of an ethylene glycol solution, the concentration of ethylene glycol and the concentration of salt; the core direct current control output unit in the control box adjusts the input current and voltage of each electrodialyzer according to the feedback conductivity and flow change parameters, thereby controlling the desalination rate of each electrodialyzer.
Due to the adoption of the technical scheme, the invention has the following advantages and effects:
1. low energy consumption and environmental protection
The traditional rectification desalination needs to heat the solution to a temperature above the boiling point, and consumes a large amount of energy. The system scheme operates at normal temperature, greatly reduces energy consumption, reduces greenhouse gas emission and is environment-friendly.
2. The system is simple to operate
The system is simple in composition and convenient to operate.
3. The system has small volume and flexible arrangement
The system has light weight and small occupied space. The electrodialysers may be arranged horizontally or vertically. The arrangement and installation adaptability is good.
4. Good economical efficiency
The system has the advantages of low initial investment, low energy consumption, low operation cost and good economy.
Drawings
FIG. 1 is a schematic diagram of the overall structure and process flow of the present invention;
FIG. 2 is a schematic view of the construction of an electrodialyzer in accordance with the present invention;
Detailed Description
The invention is described in further detail below with reference to the accompanying drawings:
the oil gas exploitation saline ethylene glycol solution desalting device based on the electrodialysis technology is shown in figure 1, adopts a 3-stage series desalting scheme and mainly comprises 3 electrodialyzers 1, 2 and 3, 1 ethylene glycol solution delivery pump 4, 1 seawater delivery pump 5, 1 polar water circulating pump 6, a polar water tank 7 and a control box 8, wherein the devices 1-7 are connected through corresponding pipelines; a control box 8 is arranged for supplying power and controlling the desalination rate;
the method is characterized in that:
the electrodialyzer 1, 2 and 3 has 3 units as shown in fig. 1 and 2, and is composed of a desalination chamber 9, a concentration chamber 10, an anode chamber 11, a cathode chamber 12 and 100 pairs of special anion-cation exchange membranes; 3 electrodialysers are connected in series; the first-stage electrodialyzer 1 is communicated with the second-stage electrodialyzer 2 through pipelines 1-2 and 1-6 respectively for conveying glycol solution and seawater, and the second-stage electrodialyzer 2 is communicated with the third-stage electrodialyzer 3 through pipelines 1-3 and 1-7 respectively for conveying glycol solution and seawater; the glycol solution delivery pump 4 is connected with the electrodialyzer 1 through a pipeline 1-1; the seawater delivery pump 5 is connected with the electrodialyzer 1 through pipelines 1-5;
the polar water tank 7 has a volume of 100L as shown in FIG. 1, and stores a 3% Na polar water solution2SO4An aqueous solution; the polar water tank 7 is connected with a polar water circulating pump 6 through a pipeline and is divided into two paths, one path is sequentially connected with anode chambers 11 of electrodialysers 1, 2 and 3 through pipelines 1-11, 1-12 and 1-13, and the other path is sequentially connected with cathode chambers 12 of electrodialysers 1, 2 and 3 through pipelines 1-15, 1-16 and 1-17; the anode chamber 11 and the cathode chamber 12 of the electrodialyzer 3 are connected with the polar water tank 7 through pipelines 1-14 and 1-18, so that closed circulation is formed among the electrodialyzers 1, 2 and 3, the polar water tank 7 and the polar water circulating pump 6;
the ethylene glycol solution delivery pump 4, the seawater delivery pump 5 and the polar water circulating pump 6 are shown in figure 1, the pressure is 5.5bar-10.0bar, and the flow rate is 150L/h;
as shown in fig. 1, the input voltage of the control box 8 is 440V, and 3 phases; respectively supplying power to an ethylene glycol solution delivery pump 4, a seawater delivery pump 5 and an extreme water circulating pump 6; presetting input voltage and current of an electrodialyzer in a control system according to the flow of an ethylene glycol solution, the concentration of ethylene glycol and the concentration of salt; the core direct current control output unit in the control box adjusts the input current and voltage of each electrodialyzer according to the feedback conductivity and flow change parameters, thereby controlling the desalination rate of each electrodialyzer. The work flow is shown in figure 1:
(1) the glycol delivery pump 4 pumps high-salt-content glycol solution from the platform through the pipeline 1-1, and the high-salt-content glycol solution sequentially enters the electrodialysers 1, 2 and 3 in each stage. Partial salt in the glycol solution is removed in a desalting chamber 9 of each stage of electrodialyzer 1, 2, 3, the salinity in the glycol solution is gradually reduced, and finally the qualified glycol solution desalted by the three stages of electrodialyzers 3 enters a dehydration link through a pipeline 1-4.
(2) The seawater delivery pump 5 pumps seawater from the platform through a pipeline 1-5, sequentially enters each stage of electrodialysers 1, 2 and 3, salt ions permeated through an anode membrane (a cathode membrane) are absorbed in concentration chambers 10 of the electrodialysers 1, 2 and 3, the ion concentration is gradually increased, and finally concentrated seawater with high salt content is led out from the electrodialysers 3 and enters a platform production water system or is discharged into the sea through pipelines 1-8.
2 modes of forward flow and reverse flow of seawater are considered. Forward flow: the seawater enters a first-stage electrodialyzer 1, a second-stage electrodialyzer 2 and a third-stage electrodialyzer 3 in sequence; countercurrent flow: the seawater is opposite in direction, firstly passes through the pipelines 1-10, then enters the three-stage electrodialyser 3, the two-stage electrodialyser 2 and the first-stage electrodialyser 1 respectively, and finally enters the platform production water system or is discharged into the sea through the pipelines 1-9.
(3) The polar water circulating pump 6 pumps the polar water liquid from the polar water tank 7 and divides the polar water liquid into two paths, one path of the polar water circulating pump sequentially enters the anode chambers 11 of the electrodialysers 1, 2 and 3 of each stage through pipelines 1-11, 1-12 and 1-13 respectively, and the other path of the polar water circulating pump sequentially enters the cathode chambers 12 of the electrodialysers 1, 2 and 3 of each stage through pipelines 1-15, 1-16 and 1-17 respectively; cations in the polar water solution entering the anode chamber 11 permeate the anode membrane to enter the concentration chamber 10 and present a negative charge characteristic; the polar liquid entering the cathode chamber 12 receives the cations entering from the concentrating chamber 10 through the cation membrane, and exhibits a positive charge characteristic; the polar liquid respectively returned from the anode chamber 11 and the cathode chamber 12 through pipelines 1-14 and 1-18 is neutralized, mixed and reduced in the polar water tank 7; thereby forming a closed cycle among the electrodialysers 1, 2, 3, the polar water tank 7 and the polar water circulating pump 6.
Claims (1)
1. The desalting device for the salt-containing glycol solution for oil and gas exploitation based on the electrodialysis technology adopts a 3-stage series desalting scheme and mainly comprises 3 electrodialysers (1), (2) and (3), 1 glycol solution delivery pump (4), 1 seawater delivery pump (5), 1 polar water circulating pump (6), a polar water tank (7) and a control box (8), wherein the devices (1-7) are connected through corresponding pipelines; a control box (8) is arranged for supplying power and controlling the desalination rate; the method is characterized in that: the electrodialyzer (1), (2) and (3) has 3 sets, which consists of a desalting chamber (9), a concentrating chamber (10), an anode chamber (11), a cathode chamber (12) and 100 pairs of special anion-cation exchange membranes; 3 electrodialysers are connected in series; the first-stage electrodialyzer (1) and the second-stage electrodialyzer (2) are respectively communicated through pipelines (1-2) and (1-6), and the second-stage electrodialyzer (2) and the third-stage electrodialyzer (3) are respectively communicated through pipelines (1-3) and (1-7); the ethylene glycol solution delivery pump (4) is connected with the electrodialyzer (1) through a pipeline (1-1); the seawater delivery pump (5) is connected with the electrodialyzer (1) through pipelines (1-5); the volume of the polar water tank (7) is 100L, and the polar water tank stores the polar water which is 3 percent Na2SO4An aqueous solution; the polar water tank (7) is connected with a polar water circulating pump (6) through a pipeline and is divided into two paths, one path is sequentially connected with the anode chambers (11) of the electrodialysers (1), (2) and (3) through pipelines (1-11), (1-12) and (1-13), and the other path is sequentially connected with the cathode chambers (12) of the electrodialysers (1), (2) and (3) through pipelines (1-15), (1-16) and (1-17); the anode chamber (11) and the cathode chamber (12) of the electrodialyzer (3) are connected with the inside of the polar water tank (7) through pipelines (1-14), (1-18), thereby the electrodialyzer (1), (2), (3) of each stage, the polar water tank (7) and the polar water circulating pump(6) A closed loop is formed; the pressure of the glycol solution delivery pump (4), the seawater delivery pump (5) and the polar water circulating pump (6) is 5.5bar-10.0bar, and the flow rate is 150L/h; the input voltage of the control box (8) is 440V, and the phase is 3; the power is supplied to the glycol solution delivery pump (4), the seawater delivery pump (5) and the polar water circulating pump (6) respectively.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011316566.7A CN112263912A (en) | 2020-11-20 | 2020-11-20 | Oil gas exploitation contains salt ethylene glycol solution desalination device based on electrodialysis technique |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202011316566.7A CN112263912A (en) | 2020-11-20 | 2020-11-20 | Oil gas exploitation contains salt ethylene glycol solution desalination device based on electrodialysis technique |
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH1085755A (en) * | 1996-09-10 | 1998-04-07 | Hitachi Plant Eng & Constr Co Ltd | Desalting method using electrodialysis equipment |
| CN1522997A (en) * | 2003-02-21 | 2004-08-25 | 清华大学 | Desalination Process of 1,3-Propanediol Fermentation Broth by Electrodialysis |
| CN101143301A (en) * | 2007-07-13 | 2008-03-19 | 天津大学 | Electrodialyzer and method for removing salt in corn production polyol reaction solution |
| CN102963966A (en) * | 2012-11-12 | 2013-03-13 | 中国科学院过程工程研究所 | Electrodialysis device applicable to treatment on high-salinity wastewater from industries such as coal chemical industry |
| CN206384902U (en) * | 2016-12-01 | 2017-08-08 | 北京高能时代环境技术股份有限公司 | Salt separation concentration integral type ion-exchange membrane facility |
| CN108602700A (en) * | 2016-02-11 | 2018-09-28 | 富士胶片制造欧洲有限公司 | Desalination |
| CN110510712A (en) * | 2019-08-09 | 2019-11-29 | 南开大学 | An electrodialysis system and method for desalination of brackish water |
| CN214319761U (en) * | 2020-11-20 | 2021-10-01 | 中船重工船舶设计研究中心有限公司 | Oil gas exploitation contains salt ethylene glycol solution desalination device based on electrodialysis technique |
-
2020
- 2020-11-20 CN CN202011316566.7A patent/CN112263912A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH1085755A (en) * | 1996-09-10 | 1998-04-07 | Hitachi Plant Eng & Constr Co Ltd | Desalting method using electrodialysis equipment |
| CN1522997A (en) * | 2003-02-21 | 2004-08-25 | 清华大学 | Desalination Process of 1,3-Propanediol Fermentation Broth by Electrodialysis |
| CN101143301A (en) * | 2007-07-13 | 2008-03-19 | 天津大学 | Electrodialyzer and method for removing salt in corn production polyol reaction solution |
| CN102963966A (en) * | 2012-11-12 | 2013-03-13 | 中国科学院过程工程研究所 | Electrodialysis device applicable to treatment on high-salinity wastewater from industries such as coal chemical industry |
| CN108602700A (en) * | 2016-02-11 | 2018-09-28 | 富士胶片制造欧洲有限公司 | Desalination |
| CN206384902U (en) * | 2016-12-01 | 2017-08-08 | 北京高能时代环境技术股份有限公司 | Salt separation concentration integral type ion-exchange membrane facility |
| CN110510712A (en) * | 2019-08-09 | 2019-11-29 | 南开大学 | An electrodialysis system and method for desalination of brackish water |
| CN214319761U (en) * | 2020-11-20 | 2021-10-01 | 中船重工船舶设计研究中心有限公司 | Oil gas exploitation contains salt ethylene glycol solution desalination device based on electrodialysis technique |
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