CN106422810A - After-treatment device and method for preparing hollow fiber membrane through thermally induced phase separation - Google Patents
After-treatment device and method for preparing hollow fiber membrane through thermally induced phase separation Download PDFInfo
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- CN106422810A CN106422810A CN201610903834.2A CN201610903834A CN106422810A CN 106422810 A CN106422810 A CN 106422810A CN 201610903834 A CN201610903834 A CN 201610903834A CN 106422810 A CN106422810 A CN 106422810A
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- 239000012528 membrane Substances 0.000 title claims abstract description 71
- 238000002145 thermally induced phase separation Methods 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims abstract description 18
- 239000012510 hollow fiber Substances 0.000 title abstract 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 285
- 238000000605 extraction Methods 0.000 claims abstract description 88
- 238000000926 separation method Methods 0.000 claims abstract description 32
- 239000003085 diluting agent Substances 0.000 claims abstract description 19
- 238000001816 cooling Methods 0.000 claims abstract description 12
- 230000008569 process Effects 0.000 claims abstract description 8
- 239000000835 fiber Substances 0.000 claims description 64
- 239000007788 liquid Substances 0.000 claims description 38
- 239000000284 extract Substances 0.000 claims description 22
- 238000012544 monitoring process Methods 0.000 claims description 18
- 238000010438 heat treatment Methods 0.000 claims description 12
- 238000002425 crystallisation Methods 0.000 claims description 10
- 230000008025 crystallization Effects 0.000 claims description 10
- 238000005452 bending Methods 0.000 claims description 9
- 229920006395 saturated elastomer Polymers 0.000 claims description 9
- 230000001413 cellular effect Effects 0.000 claims description 6
- 238000003756 stirring Methods 0.000 claims description 6
- 238000013459 approach Methods 0.000 claims description 5
- 238000001035 drying Methods 0.000 claims description 5
- 238000012805 post-processing Methods 0.000 claims description 5
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 238000010790 dilution Methods 0.000 claims description 4
- 239000012895 dilution Substances 0.000 claims description 4
- 238000000746 purification Methods 0.000 claims description 3
- 239000011247 coating layer Substances 0.000 claims description 2
- 238000003912 environmental pollution Methods 0.000 abstract description 7
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 238000013461 design Methods 0.000 description 31
- 230000006872 improvement Effects 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 5
- DOIRQSBPFJWKBE-UHFFFAOYSA-N dibutyl phthalate Chemical compound CCCCOC(=O)C1=CC=CC=C1C(=O)OCCCC DOIRQSBPFJWKBE-UHFFFAOYSA-N 0.000 description 4
- 239000002904 solvent Substances 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- MQIUGAXCHLFZKX-UHFFFAOYSA-N Di-n-octyl phthalate Natural products CCCCCCCCOC(=O)C1=CC=CC=C1C(=O)OCCCCCCCC MQIUGAXCHLFZKX-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- BJQHLKABXJIVAM-UHFFFAOYSA-N bis(2-ethylhexyl) phthalate Chemical compound CCCCC(CC)COC(=O)C1=CC=CC=C1C(=O)OCC(CC)CCCC BJQHLKABXJIVAM-UHFFFAOYSA-N 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000013618 particulate matter Substances 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 235000010469 Glycine max Nutrition 0.000 description 1
- 244000068988 Glycine max Species 0.000 description 1
- 125000002252 acyl group Chemical group 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000000110 cooling liquid Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 235000012489 doughnuts Nutrition 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000000409 membrane extraction Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000009897 systematic effect Effects 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
- B01D69/08—Hollow fibre membranes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D11/00—Solvent extraction
- B01D11/02—Solvent extraction of solids
- B01D11/028—Flow sheets
- B01D11/0284—Multistage extraction
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D11/00—Solvent extraction
- B01D11/02—Solvent extraction of solids
- B01D11/0288—Applications, solvents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D11/00—Solvent extraction
- B01D11/02—Solvent extraction of solids
- B01D11/0292—Treatment of the solvent
- B01D11/0296—Condensation of solvent vapours
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D67/00—Processes specially adapted for manufacturing semi-permeable membranes for separation processes or apparatus
- B01D67/0081—After-treatment of organic or inorganic membranes
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Manufacturing & Machinery (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses an after-treatment device and an after-treatment method for preparing a hollow fiber membrane through thermally induced phase separation. The device comprises a purified ethanol storage tank, a primary high-pressure extraction pump, a primary extraction pool, a secondary extraction pool, a third-level extraction pool and a cooling separation tower, wherein the purified ethanol storage tank, the high-pressure extraction pump, the primary extraction pool, the secondary extraction pool and the third-level extraction pool are sequentially connected with the cooling separation tower. According to the device disclosed by the invention, the after-treatment efficiency of the hollow fiber membrane is improved, the ethanol utilization rate in a diluents extraction process is improved, the production cost is reduced, the environmental pollution is reduced, and modern process requirements on energy conservation and environment friendliness are met.
Description
Technical field
The present invention relates to thermally induced phase separation and prepare doughnut technical field of membrane, particularly to a kind of thermally induced phase separation
Prepare after-treatment device and the method for hollow-fibre membrane.
Background technology
Membrane separation technique is the new technology separating the present age, has the outstanding advantages such as efficient, energy-conservation, cleaning.China and the world
Developed country also has very big gap in terms of membrane technology, and many membrane materials still rely on import.Therefore, strengthening membrane material energetically
Research and development tool is of great significance.
Thermal inactive (TIPS) method is that the one proposing the eighties in 20th century is changed by temperature and causes being separated and prepare
The method of microporous barrier.Use higher boiling, low molecular weight diluent to form homogeneous phase solution at high temperature with high polymer, all mix during cooling
Liquid generation solid-liquid or liquid-liquid phase separation, then remove diluent, thus obtain the high polymer microcellular film with a fixed structure.With
Other film-forming methods compare, and the film-strength that TIPS method prepares is high, anti-pollution, and have that pore-size distribution is narrow, porosity is high, aperture is easy
In advantages such as regulation and control, therefore suffer from the concern of people and obtain more systematic research.In fact, diluent is a kind of potential molten
Agent, is non-solvent at normal temperatures, and is at high temperature solvent, i.e. " high temperature mixes, low temperature split-phase ".
When prior art uses thermally induced phase separation to prepare hollow-fibre membrane, the dilute agent of use includes acyl in oneself
Amine, soya-bean oil, atoleine, dibutyl phthalate (DBP), dioctyl phthalate (DOP) etc., at hollow-fibre membrane
Preparation later stage workshop section, is extracted by above-mentioned diluent, i.e. can get hollow-fibre membrane.
When the diluent that prior art remains when preparing hollow-fibre membrane to thermally induced phase separation extracts, to ethanol
Very big Deng the waste of extractant, add production cost, and easily cause environmental pollution, produce potential safety hazard, it is impossible to meet joint
The modern crafts of energy environmental protection require.
Content of the invention
It is an object of the invention to, the technology preparing the existence of hollow-fibre membrane aftertreatment technology for thermally induced phase separation is asked
Topic, designs a kind of thermally induced phase separation and prepares after-treatment device and the method for hollow-fibre membrane, improve the rear place of hollow-fibre membrane
Reason efficiency, improves the ethanol utilization rate in diluent extraction process, reduces production cost, reduces environmental pollution, meets energy-saving ring
The modern crafts protected require.
The present invention is achieved through the following technical solutions：
A kind of thermally induced phase separation prepares the after-treatment device of hollow-fibre membrane, it is characterised in that include that purifying ethanol stores up
Deposit tank (1), one-level high-pressure extraction pump (2), one-level abstraction pool (3), two grades of abstraction pools (4), three grades of abstraction pools (5) and refrigerated separation
Tower (6), described purifying ethanol holding vessel (1), high-pressure extraction pump (2), one-level abstraction pool (3), two grades of abstraction pools (4), three grades of extractions
Take pond (5) and refrigerated separation tower (6) connects successively；
Described one-level abstraction pool (3), two grades of abstraction pools (4) and three grades of abstraction pools (5) are set to identical structure；
Described purifying ethanol holding vessel (1) lower right is provided with ethanol raffinate crystallizing tank (7), ethanol raffinate crystallizing tank (7)
External rectifying column (8), rectifying column (8) is respectively communicated to one-level abstraction pool (3), two grades of extractions by two grades of high-pressure extraction pumps (9)
Pond (4) and three grades of abstraction pools (5)；
Described one-level abstraction pool (3) liquid outlet end and two grades of abstraction pool (4) inlet ends are connected by feed-line, and one
It is provided with one-level threeway control on feed-line between level abstraction pool (3) liquid outlet end and two grades of abstraction pool (4) inlet ends
Valve (305) and one-level elevator pump (306), one-level abstraction pool (3) is communicated to ethanol raffinate knot by one-level three-way control valve (305)
Brilliant tank (7)；
Described two grades of abstraction pool (4) liquid outlet ends and three grades of abstraction pool (5) inlet ends are connected by feed-line, and two
It is provided with two grades of threeway controls on feed-line between level abstraction pool (4) liquid outlet end and three grades of abstraction pool (5) inlet ends
Valve (405) and two-stage hoisting pump (406), two grades of abstraction pools (4) are communicated to ethanol raffinate knot by two grades of three-way control valves (405)
Brilliant tank (7)；
Described three grades of abstraction pool (5) liquid outlet ends are provided with three grades of three-way control valves (505) and three grades of elevator pumps (506),
Three grades of abstraction pools (5) are communicated to ethanol raffinate crystallizing tank (7) by three grades of three-way control valves (505)；
Described purifying ethanol holding vessel (1) bottom is provided with cellular heated base (101)；
Described one-level three-way control valve (305) is circumscribed with extractant saturation degree monitor one, two grades of three-way control valves (405)
Being circumscribed with extractant saturation degree monitor two, three grades of three-way control valves (505) are circumscribed with extractant saturation degree monitor three.
Further, it is provided with heat exchanger (10) between described ethanol raffinate crystallizing tank (7) and purifying ethanol holding vessel (1).
Further, described one-level abstraction pool (3) is circumscribed with primary cycle pump (301), and two grades of abstraction pools (4) are circumscribed with two grades
Circulating pump (401), three grades of abstraction pools (5) are circumscribed with three grades of circulating pumps (501).
Further, described one-level abstraction pool (3) inner side is provided with one-level overlay film frame (302), and two grades of abstraction pool (4) inner sides set
Being equipped with two grades of overlay film framves (402), three grades of abstraction pool (5) inner sides are provided with three grades of overlay film framves (502)；
One-level overlay film frame (302) is removably assemblied on one-level abstraction pool (3)；Two grades of overlay film framves (402) are removably
It is assemblied on two grades of abstraction pools (4)；Three grades of overlay film framves (502) are removably assemblied on three grades of abstraction pools (5), and described one-level is covered
Film frame (302), two grades of overlay film framves (402) and three grades of overlay film framves (502) are set to identical structure.
Further, described one-level overlay film frame (302) is provided with one-level overlay film laminate (303), two grades of abstraction pools (4) set
It is equipped with two grades of overlay film laminates (403), three grades of abstraction pools (5) are provided with three grades of overlay film laminates (503), described one-level overlay film laminate
(303), two grades of overlay film laminates (403) and three grades of overlay film laminates (503) are set to identical structure.
Further, described one-level abstraction pool (3) inside bottom is provided with one-level agitator arm (304), two grades of abstraction pools (4)
Inside bottom is provided with two grades of agitator arms (404), and three grades of abstraction pool (5) inside bottom are provided with three grades of agitator arms (504).
Further, described one-level abstraction pool (3) lateral wall is provided with one-level heating mantle (307), and lateral wall is provided with two grades
Heating mantle (407), three grades of abstraction pool (5) lateral walls are provided with three grades of heating mantles (507).
Further, described refrigerated separation tower (6) entrance point is provided with check-valves (11), one-level abstraction pool (3), two grades of extractions
Pond (4) and three grades of abstraction pools (5) are communicated to refrigerated separation tower (6) by check-valves (11) respectively, and refrigerated separation tower (6) bottom sets
Being equipped with condensate liquid collecting tank (601), refrigerated separation tower (6) top is provided with drying tube (602).
Further, the connecting pipe between described ethanol raffinate crystallizing tank (7) and rectifying column (8) is positioned at the crystallization of ethanol raffinate
The part of tank (7) inner side is set to filter screen type bending tube structure (703), and ethanol raffinate crystallizing tank (7) center is provided with
Insulated column (702), ethanol raffinate crystallizing tank (7) is divided into left chamber and right chamber, left chamber and right chamber by insulated column (702)
Being connected, filter screen type bending tube structure (703) is arranged at left chamber one end, one-level abstraction pool (3), two grades of abstraction pools (4) and
The liquid outlet end of three grades of abstraction pools (5) is communicated in right chamber.
Further, described ethanol raffinate crystallizing tank (7) bottom is provided with cooling coil (701).
A kind of thermally induced phase separation prepares the post-processing approach of hollow-fibre membrane, it is characterised in that comprise the following steps：
Step 1)：Pending hollow-fibre membrane is layed in one-level overlay film laminate (303) of one-level overlay film frame (302)
On, and be assemblied in one-level overlay film frame (302) in one-level abstraction pool (3)；
Step 2)：Inject abstraction purification ethanol in purifying ethanol holding vessel (1), utilize cellular heated base (101)
Heating the ethanol in purifying ethanol holding vessel (1), the ethanol after being heated by high-pressure extraction pump (2) is pumped to one-level
In abstraction pool (3), two grades of abstraction pools (4) and three grades of abstraction pools (5), one-level abstraction pool (3), two grades of abstraction pools (4) and three grades
Abstraction pool (5) is respectively completed one-level extraction, two grades of extractions and three grades of extractions of dilution；
Step 3)：Open primary cycle pump (301), secondary cycle pump (401) and three grades of circulating pumps (501), open one-level
Agitator arm (304), two grades of agitator arms (404) and three grades of agitator arms (504), utilize primary cycle pump (301) and one-level
Extract flowing in one-level abstraction pool (3) is accelerated in the cooperation of agitator arm (304), utilize secondary cycle pump (401) and two grades stir
Extract flowing in two grades of abstraction pools (4) is accelerated in the cooperation mixing impeller (404), utilizes three grades of circulating pumps (501) and three grades of stirrings
Extract flowing in three grades of abstraction pools (5) is accelerated in the cooperation of impeller (504)；
Step 4)：Open extractant saturation degree monitor the first, extractant saturation degree monitor two and extractant saturation degree prison
Surveying instrument three, one-level three-way control valve (305) is crystallized by the Monitoring Data according to extractant saturation degree monitor one with ethanol raffinate
The connectedness of tank (7) is controlled, and utilizes the Monitoring Data of extractant saturation degree monitor two to two grades of three-way control valves (405)
Being controlled with the connectedness of ethanol raffinate crystallizing tank (7), the Monitoring Data according to extractant saturation degree monitor three is to three grades
Three-way control valve (505) is controlled with the connectedness of ethanol raffinate crystallizing tank (7)；
When extractant saturation degree monitor three detects the extractant saturation degree in three grades of abstraction pools (5) at three grades of extraction knots
When bundle is also in unsaturation state, utilize the cooperation of two grades of three-way control valves (405) and two-stage hoisting pump (406), by three grades of extractions
Take unsaturated extractant in pond (5) to be transferred to two grades of abstraction pools (4) reuse, if extractant saturation degree monitor three is examined
Measure extractant saturation degree in three grades of abstraction pools (5) when three grades of extraction end are in saturation state, utilize three grades of threeway controls
Three grades of abstraction pools (5) are connected by valve processed (505) with ethanol raffinate crystallizing tank (7), and saturated extractant is directly discharged to ethanol
Raffinate crystallizing tank crystallizes in (7)；
When extractant saturation degree monitor two detects the extractant saturation degree in two grades of abstraction pools (4) at two grades of extraction knots
When bundle is also in unsaturation state, utilize one-level three-way control valve (305) and the cooperation of one-level elevator pump (306), by two grades of extractions
Take unsaturated extractant in pond (4) to be transferred to one-level abstraction pool (3) reuses, if extractant saturation degree monitor two is examined
Measure extractant saturation degree in two grades of abstraction pools (4) when two grades of extraction end are in saturation state, utilize two grades of threeway controls
Two grades of abstraction pools (4) are connected by valve processed (405) with ethanol raffinate crystallizing tank (7), and saturated extractant is directly discharged to ethanol
Raffinate crystallizing tank crystallizes in (7)；
When extractant saturation degree monitor one detects the extractant saturation degree in one-level abstraction pool (3) when one-level extracts
When being in saturation state, utilize one-level three-way control valve (305) by one-level abstraction pool (3) with ethanol raffinate crystallizing tank (7) even
Logical, saturated extractant is directly discharged to ethanol raffinate crystallizing tank (7) crystallizes；
Step 5)：Open cooling coil (701), utilize cooling coil (701) to collection in ethanol raffinate crystallizing tank (7)
Extractant raffinate carries out Crystallization Separation, it is thus achieved that ethanol raffinate is delivered to rectifying column (8)；
Step 6)：Open rectifying column (8), residual to being delivered to the internal ethanol of rectifying column (8) via ethanol raffinate crystallizing tank (7)
Liquid carries out rectification process, and the clean ethanol obtaining after rectification process is sent to one-level extraction respectively via two grades of high-pressure extraction pumps (9)
Take pond (3), two grades of abstraction pools (4) or three grades of abstraction pools (5), be re-used for the extraction of diluent；
Step 7)：Supervise according to extractant saturation degree monitor the first, extractant saturation degree monitor two and extractant saturation degree
Survey the Monitoring Data of instrument three, one-level abstraction pool (3) will be equipped with one-level overlay film frame (302) of pending hollow-fibre membrane successively
It is transferred in two grades of abstraction pools (4), two grades of abstraction pools (4) will be equipped with two grades of overlay film framves of pending hollow-fibre membrane
(402) it is transferred in three grades of abstraction pools (5)；
Step 8)：According to the Monitoring Data of extractant saturation degree monitor three, to remnants in pending hollow-fibre membrane
Diluent judges, when the content of the diluent monitoring is less than setting value, takes out three grades of overlay film framves (502), and takes out
It is layed in the hollow-fibre membrane of three grades of overlay film laminates (503), hollow-fibre membrane finished product can be obtained.
The invention provides a kind of cutting dipper carrying conditioning ring, compared with prior art, have the beneficial effects that：
1st, the thermally induced phase separation of present invention design prepares the after-treatment device of hollow-fibre membrane, is integrated with successively mutually in succession
Logical one-level abstraction pool (3), two grades of abstraction pools (4), three grades of abstraction pools (5), utilize one-level abstraction pool (3), two grades of abstraction pools (4)
Carrying out gradient extraction with three grades of abstraction pools (5) to the remaining diluent in pending hollow-fibre membrane, extraction efficiency is significantly
Promote, and avoid the waste to extractant.
2nd, the thermally induced phase separation of present invention design prepares the after-treatment device of hollow-fibre membrane, one-level abstraction pool (3), two
Level abstraction pool (4) and three grades of abstraction pools (5) are set to identical structure；One-level overlay film frame (302), two grades of overlay film framves (402) and three
Level overlay film frame (502) is set to identical structure；One-level overlay film laminate (303), two grades of overlay film laminates (403) and three grades of overlay film laminates
(503) it is set to identical structure；Above-mentioned design structure, it is simple to pending hollow-fibre membrane is in one-level abstraction pool (3), two grades of extractions
Fast transfer in pond (4) and three grades of abstraction pools (5), improves extraction efficiency, reduces operator's labour intensity.
3rd, the thermally induced phase separation of present invention design prepares the after-treatment device of hollow-fibre membrane, purifying ethanol holding vessel
(1) lower right is provided with ethanol raffinate crystallizing tank (7), the external rectifying column of ethanol raffinate crystallizing tank (7) (8), and rectifying column (8) passes through
Two grades of high-pressure extraction pumps (9) are respectively communicated to one-level abstraction pool (3), two grades of abstraction pools (4) and three grades of abstraction pools (5)；One-level extracts
Take pond (3) liquid outlet end and two grades of abstraction pool (4) inlet ends are connected by feed-line, one-level abstraction pool (3) liquid outlet
It is provided with one-level three-way control valve (305) on feed-line between end and two grades of abstraction pool (4) inlet ends and one-level promotes
Pump (306), one-level abstraction pool (3) is communicated to ethanol raffinate crystallizing tank (7) by one-level three-way control valve (305)；Two grades of extractions
Pond (4) liquid outlet end and three grades of abstraction pool (5) inlet ends are connected by feed-line, two grades of abstraction pool (4) liquid outlet ends
And it is provided with two grades of three-way control valves (405) and two-stage hoisting pump on the feed-line between three grades of abstraction pool (5) inlet ends
(406), two grades of abstraction pools (4) are communicated to ethanol raffinate crystallizing tank (7) by two grades of three-way control valves (405)；Three grades of abstraction pools
(5) liquid outlet end is provided with three grades of three-way control valves (505) and three grades of elevator pumps (506), and three grades of abstraction pools (5) pass through three grade three
Logical control valve (505) is communicated to ethanol raffinate crystallizing tank (7)；Above-mentioned design structure, be conducive to via one-level abstraction pool (3),
Two grades of abstraction pools (4) carry out crystallization with the ethanol raffinate after the extraction that three grades of abstraction pools (5) are discharged and separate with rectifying, it is thus achieved that pure
Ethanol, it is achieved the recycling of ethanol in extraction process, production cost is substantially reduced, and it also avoid raffinate directly outer row and makes
The environmental pollution becoming.
4th, the thermally induced phase separation of present invention design prepares the after-treatment device of hollow-fibre membrane, one-level three-way control valve
(305) being circumscribed with extractant saturation degree monitor one, two grades of three-way control valves (405) are circumscribed with extractant saturation degree monitor
Two, three grades of three-way control valves (505) are circumscribed with extractant saturation degree monitor three；Above-mentioned design structure, the extractant of design is satisfied
With degree monitor the first, extractant saturation degree monitor two and extractant saturation degree monitor three be easy to one-level abstraction pool (3), two
Extract saturation degree in level abstraction pool (4) and three grades of abstraction pools (5) is monitored in real time, changes in time or shifts,
Use more convenient.
5th, the thermally induced phase separation of present invention design prepares the after-treatment device of hollow-fibre membrane, and one-level abstraction pool (3) is outward
Being connected to primary cycle pump (301), two grades of abstraction pools (4) are circumscribed with secondary cycle pump (401), and three grades of abstraction pools (5) are circumscribed with three
Level circulating pump (501)；One-level abstraction pool (3) inside bottom is provided with one-level agitator arm (304), two grades of abstraction pool (4) inner sides
Bottom is provided with two grades of agitator arms (404), and three grades of abstraction pool (5) inside bottom are provided with three grades of agitator arms (504)；Above-mentioned
Design structure, accelerates the mobility of extract in one-level abstraction pool (3), two grades of abstraction pools (4) and three grades of abstraction pools (5), has
It is beneficial to promote extraction efficiency.
6th, the thermally induced phase separation of present invention design prepares the after-treatment device of hollow-fibre membrane, and refrigerated separation tower (6) enters
Mouth end is provided with check-valves (11), and one-level abstraction pool (3), two grades of abstraction pools (4) and three grades of abstraction pools (5) pass through check-valves respectively
(11) being communicated to refrigerated separation tower (6), refrigerated separation tower (6) bottom is provided with condensate liquid collecting tank (601), refrigerated separation tower
(6) top is provided with drying tube (602)；Above-mentioned design structure, it is to avoid the alcohol gas after gasification and other other extractants
The environmental pollution that outer row causes.
7th, the thermally induced phase separation of present invention design prepares the after-treatment device of hollow-fibre membrane, ethanol raffinate crystallizing tank
(7) part that the connecting pipe and between rectifying column (8) is positioned at ethanol raffinate crystallizing tank (7) inner side is set to filter screen type bending
Tubular construction (703), ethanol raffinate crystallizing tank (7) center is provided with insulated column (702), and insulated column (702) is by ethanol raffinate
Crystallizing tank (7) is divided into left chamber and right chamber, and left chamber is connected with right chamber, and filter screen type bending tube structure (703) sets
Being placed in left chamber one end, the liquid outlet end of one-level abstraction pool (3), two grades of abstraction pools (4) and three grades of abstraction pools (5) is communicated in right chamber
One end, room；Above-mentioned design structure, is conducive to entering the extract raffinate rapid crystallization in ethanol raffinate crystallizing tank (7), keeps away simultaneously
Having exempted from large particulate matter entrance rectifying column (8) causes rectifying column (8) to block, and causes the system failure.
8th, the thermally induced phase separation of present invention design prepares the post-processing approach of hollow-fibre membrane, uses the extraction of gradient extraction
Take mode, be greatly improved the extraction efficiency of diluent in hollow-fibre membrane.
Brief description
Fig. 1 is the structural representation of the after-treatment device that thermally induced phase separation of the present invention prepares hollow-fibre membrane.
Detailed description of the invention
Refering to accompanying drawing 1, the present invention is described further.
The present invention relates to a kind of thermally induced phase separation and prepare the after-treatment device of hollow-fibre membrane, it is characterised in that include
Purifying ethanol holding vessel (1), one-level high-pressure extraction pump (2), one-level abstraction pool (3), two grades of abstraction pools (4), three grades of abstraction pools (5)
With refrigerated separation tower (6), described purifying ethanol holding vessel (1), high-pressure extraction pump (2), one-level abstraction pool (3), two grades of abstraction pools
(4), three grades of abstraction pools (5) and refrigerated separation tower (6) connect successively；
Described one-level abstraction pool (3), two grades of abstraction pools (4) and three grades of abstraction pools (5) are set to identical structure；
Described purifying ethanol holding vessel (1) lower right is provided with ethanol raffinate crystallizing tank (7), ethanol raffinate crystallizing tank (7)
External rectifying column (8), rectifying column (8) is respectively communicated to one-level abstraction pool (3), two grades of extractions by two grades of high-pressure extraction pumps (9)
Pond (4) and three grades of abstraction pools (5)；
Described one-level abstraction pool (3) liquid outlet end and two grades of abstraction pool (4) inlet ends are connected by feed-line, and one
It is provided with one-level threeway control on feed-line between level abstraction pool (3) liquid outlet end and two grades of abstraction pool (4) inlet ends
Valve (305) and one-level elevator pump (306), one-level abstraction pool (3) is communicated to ethanol raffinate knot by one-level three-way control valve (305)
Brilliant tank (7)；
Described two grades of abstraction pool (4) liquid outlet ends and three grades of abstraction pool (5) inlet ends are connected by feed-line, and two
It is provided with two grades of threeway controls on feed-line between level abstraction pool (4) liquid outlet end and three grades of abstraction pool (5) inlet ends
Valve (405) and two-stage hoisting pump (406), two grades of abstraction pools (4) are communicated to ethanol raffinate knot by two grades of three-way control valves (405)
Brilliant tank (7)；
Described three grades of abstraction pool (5) liquid outlet ends are provided with three grades of three-way control valves (505) and three grades of elevator pumps (506),
Three grades of abstraction pools (5) are communicated to ethanol raffinate crystallizing tank (7) by three grades of three-way control valves (505)；
Described purifying ethanol holding vessel (1) bottom is provided with cellular heated base (101)；
Described one-level three-way control valve (305) is circumscribed with extractant saturation degree monitor one, two grades of three-way control valves (405)
Being circumscribed with extractant saturation degree monitor two, three grades of three-way control valves (505) are circumscribed with extractant saturation degree monitor three.
It as improvement, between described ethanol raffinate crystallizing tank (7) and purifying ethanol holding vessel (1), is provided with heat exchanger
(10).
As improvement, described one-level abstraction pool (3) is circumscribed with primary cycle pump (301), and two grades of abstraction pools (4) are circumscribed with two
Level circulating pump (401), three grades of abstraction pools (5) are circumscribed with three grades of circulating pumps (501).
As improvement, described one-level abstraction pool (3) inner side is provided with one-level overlay film frame (302), two grades of abstraction pool (4) inner sides
Being provided with two grades of overlay film framves (402), three grades of abstraction pool (5) inner sides are provided with three grades of overlay film framves (502)；
One-level overlay film frame (302) is removably assemblied on one-level abstraction pool (3)；Two grades of overlay film framves (402) are removably
It is assemblied on two grades of abstraction pools (4)；Three grades of overlay film framves (502) are removably assemblied on three grades of abstraction pools (5), and described one-level is covered
Film frame (302), two grades of overlay film framves (402) and three grades of overlay film framves (502) are set to identical structure.
As improvement, described one-level overlay film frame (302) is provided with one-level overlay film laminate (303), on two grades of abstraction pools (4)
It is provided with two grades of overlay film laminates (403), three grades of abstraction pools (5) are provided with three grades of overlay film laminates (503), described one-level coating layer
Plate (303), two grades of overlay film laminates (403) and three grades of overlay film laminates (503) are set to identical structure.
As improvement, described one-level abstraction pool (3) inside bottom is provided with one-level agitator arm (304), two grades of abstraction pools
(4) inside bottom is provided with two grades of agitator arms (404), and three grades of abstraction pool (5) inside bottom are provided with three grades of agitator arms
(504).
As improvement, described one-level abstraction pool (3) lateral wall is provided with one-level heating mantle (307), and lateral wall is provided with two
Level heating mantle (407), three grades of abstraction pool (5) lateral walls are provided with three grades of heating mantles (507).
As improvement, described refrigerated separation tower (6) entrance point is provided with check-valves (11), one-level abstraction pool (3), two grades of extractions
Take pond (4) and three grades of abstraction pools (5) are communicated to refrigerated separation tower (6), refrigerated separation tower (6) bottom by check-valves (11) respectively
Being provided with condensate liquid collecting tank (601), refrigerated separation tower (6) top is provided with drying tube (602).
As improvement, the connecting pipe between described ethanol raffinate crystallizing tank (7) and rectifying column (8) is positioned at ethanol raffinate knot
The part of brilliant tank (7) inner side is set to filter screen type bending tube structure (703), and ethanol raffinate crystallizing tank (7) center is arranged
Having insulated column (702), ethanol raffinate crystallizing tank (7) is divided into left chamber and right chamber, left chamber and right chamber by insulated column (702)
Room is connected, and filter screen type bending tube structure (703) is arranged at left chamber one end, one-level abstraction pool (3), two grades of abstraction pools (4)
And the liquid outlet end of three grades of abstraction pools (5) is communicated in right chamber.
As improvement, described ethanol raffinate crystallizing tank (7) bottom is provided with cooling coil (701).
A kind of thermally induced phase separation prepares the post-processing approach of hollow-fibre membrane, it is characterised in that comprise the following steps：
Step 1)：Pending hollow-fibre membrane is layed in one-level overlay film laminate (303) of one-level overlay film frame (302)
On, and be assemblied in one-level overlay film frame (302) in one-level abstraction pool (3)；
Step 2)：Inject abstraction purification ethanol in purifying ethanol holding vessel (1), utilize cellular heated base (101)
Heating the ethanol in purifying ethanol holding vessel (1), the ethanol after being heated by high-pressure extraction pump (2) is pumped to one-level
In abstraction pool (3), two grades of abstraction pools (4) and three grades of abstraction pools (5), one-level abstraction pool (3), two grades of abstraction pools (4) and three grades
Abstraction pool (5) is respectively completed one-level extraction, two grades of extractions and three grades of extractions of dilution；
Step 3)：Open primary cycle pump (301), secondary cycle pump (401) and three grades of circulating pumps (501), open one-level
Agitator arm (304), two grades of agitator arms (404) and three grades of agitator arms (504), utilize primary cycle pump (301) and one-level
Extract flowing in one-level abstraction pool (3) is accelerated in the cooperation of agitator arm (304), utilize secondary cycle pump (401) and two grades stir
Extract flowing in two grades of abstraction pools (4) is accelerated in the cooperation mixing impeller (404), utilizes three grades of circulating pumps (501) and three grades of stirrings
Extract flowing in three grades of abstraction pools (5) is accelerated in the cooperation of impeller (504)；
Step 4)：Open extractant saturation degree monitor the first, extractant saturation degree monitor two and extractant saturation degree prison
Surveying instrument three, one-level three-way control valve (305) is crystallized by the Monitoring Data according to extractant saturation degree monitor one with ethanol raffinate
The connectedness of tank (7) is controlled, and utilizes the Monitoring Data of extractant saturation degree monitor two to two grades of three-way control valves (405)
Being controlled with the connectedness of ethanol raffinate crystallizing tank (7), the Monitoring Data according to extractant saturation degree monitor three is to three grades
Three-way control valve (505) is controlled with the connectedness of ethanol raffinate crystallizing tank (7)；
When extractant saturation degree monitor three detects the extractant saturation degree in three grades of abstraction pools (5) at three grades of extraction knots
When bundle is also in unsaturation state, utilize the cooperation of two grades of three-way control valves (405) and two-stage hoisting pump (406), by three grades of extractions
Take unsaturated extractant in pond (5) to be transferred to two grades of abstraction pools (4) reuse, if extractant saturation degree monitor three is examined
Measure extractant saturation degree in three grades of abstraction pools (5) when three grades of extraction end are in saturation state, utilize three grades of threeway controls
Three grades of abstraction pools (5) are connected by valve processed (505) with ethanol raffinate crystallizing tank (7), and saturated extractant is directly discharged to ethanol
Raffinate crystallizing tank crystallizes in (7)；
When extractant saturation degree monitor two detects the extractant saturation degree in two grades of abstraction pools (4) at two grades of extraction knots
When bundle is also in unsaturation state, utilize one-level three-way control valve (305) and the cooperation of one-level elevator pump (306), by two grades of extractions
Take unsaturated extractant in pond (4) to be transferred to one-level abstraction pool (3) reuses, if extractant saturation degree monitor two is examined
Measure extractant saturation degree in two grades of abstraction pools (4) when two grades of extraction end are in saturation state, utilize two grades of threeway controls
Two grades of abstraction pools (4) are connected by valve processed (405) with ethanol raffinate crystallizing tank (7), and saturated extractant is directly discharged to ethanol
Raffinate crystallizing tank crystallizes in (7)；
When extractant saturation degree monitor one detects the extractant saturation degree in one-level abstraction pool (3) when one-level extracts
When being in saturation state, utilize one-level three-way control valve (305) by one-level abstraction pool (3) with ethanol raffinate crystallizing tank (7) even
Logical, saturated extractant is directly discharged to ethanol raffinate crystallizing tank (7) crystallizes；
Step 5)：Open cooling coil (701), utilize cooling coil (701) to collection in ethanol raffinate crystallizing tank (7)
Extractant raffinate carries out Crystallization Separation, it is thus achieved that ethanol raffinate is delivered to rectifying column (8)；
Step 6)：Open rectifying column (8), residual to being delivered to the internal ethanol of rectifying column (8) via ethanol raffinate crystallizing tank (7)
Liquid carries out rectification process, and the clean ethanol obtaining after rectification process is sent to one-level extraction respectively via two grades of high-pressure extraction pumps (9)
Take pond (3), two grades of abstraction pools (4) or three grades of abstraction pools (5), be re-used for the extraction of diluent；
Step 7)：Supervise according to extractant saturation degree monitor the first, extractant saturation degree monitor two and extractant saturation degree
Survey the Monitoring Data of instrument three, one-level abstraction pool (3) will be equipped with one-level overlay film frame (302) of pending hollow-fibre membrane successively
It is transferred in two grades of abstraction pools (4), two grades of abstraction pools (4) will be equipped with two grades of overlay film framves of pending hollow-fibre membrane
(402) it is transferred in three grades of abstraction pools (5)；
Step 8)：According to the Monitoring Data of extractant saturation degree monitor three, to remnants in pending hollow-fibre membrane
Diluent judges, when the content of the diluent monitoring is less than setting value, takes out three grades of overlay film framves (502), and takes out
It is layed in the hollow-fibre membrane of three grades of overlay film laminates (503), hollow-fibre membrane finished product can be obtained.
Compared with prior art, the thermally induced phase separation of present invention design prepares the after-treatment device of hollow-fibre membrane, collection
Become and have the one-level abstraction pool (3) of the connection that connects successively, two grades of abstraction pools (4), three grades of abstraction pools (5), utilize one-level abstraction pool
(3), two grades of abstraction pools (4) and three grades of abstraction pools (5) carry out gradient to the remaining diluent in pending hollow-fibre membrane
Extraction, extraction efficiency is greatly promoted, and avoids the waste to extractant.
The thermally induced phase separation of present invention design prepares the after-treatment device of hollow-fibre membrane, one-level abstraction pool (3), two grades
Abstraction pool (4) and three grades of abstraction pools (5) are set to identical structure；One-level overlay film frame (302), two grades of overlay film framves (402) and three grades
Overlay film frame (502) is set to identical structure；One-level overlay film laminate (303), two grades of overlay film laminates (403) and three grades of overlay film laminates
(503) it is set to identical structure；Above-mentioned design structure, it is simple to pending hollow-fibre membrane is in one-level abstraction pool (3), two grades of extractions
Fast transfer in pond (4) and three grades of abstraction pools (5), improves extraction efficiency, reduces operator's labour intensity.
The thermally induced phase separation of present invention design prepares the after-treatment device of hollow-fibre membrane, purifying ethanol holding vessel (1)
Lower right is provided with ethanol raffinate crystallizing tank (7), the external rectifying column of ethanol raffinate crystallizing tank (7) (8), and rectifying column (8) passes through two
Level high-pressure extraction pump (9) is respectively communicated to one-level abstraction pool (3), two grades of abstraction pools (4) and three grades of abstraction pools (5)；One-level extracts
Pond (3) liquid outlet end and two grades of abstraction pool (4) inlet ends are connected by feed-line, one-level abstraction pool (3) liquid outlet end
And it is provided with one-level three-way control valve (305) and one-level elevator pump on the feed-line between two grades of abstraction pool (4) inlet ends
(306), one-level abstraction pool (3) is communicated to ethanol raffinate crystallizing tank (7) by one-level three-way control valve (305)；Two grades of abstraction pools
(4) liquid outlet end and three grades of abstraction pool (5) inlet ends are connected by feed-line, two grades of abstraction pool (4) liquid outlet ends with
It is provided with two grades of three-way control valves (405) and two-stage hoisting pump on feed-line between three grades of abstraction pool (5) inlet ends
(406), two grades of abstraction pools (4) are communicated to ethanol raffinate crystallizing tank (7) by two grades of three-way control valves (405)；Three grades of abstraction pools
(5) liquid outlet end is provided with three grades of three-way control valves (505) and three grades of elevator pumps (506), and three grades of abstraction pools (5) pass through three grade three
Logical control valve (505) is communicated to ethanol raffinate crystallizing tank (7)；Above-mentioned design structure, be conducive to via one-level abstraction pool (3),
Two grades of abstraction pools (4) carry out crystallization with the ethanol raffinate after the extraction that three grades of abstraction pools (5) are discharged and separate with rectifying, it is thus achieved that pure
Ethanol, it is achieved the recycling of ethanol in extraction process, production cost is substantially reduced, and it also avoid raffinate directly outer row and makes
The environmental pollution becoming.
The thermally induced phase separation of present invention design prepares the after-treatment device of hollow-fibre membrane, one-level three-way control valve
(305) being circumscribed with extractant saturation degree monitor one, two grades of three-way control valves (405) are circumscribed with extractant saturation degree monitor
Two, three grades of three-way control valves (505) are circumscribed with extractant saturation degree monitor three；Above-mentioned design structure, the extractant of design is satisfied
With degree monitor the first, extractant saturation degree monitor two and extractant saturation degree monitor three be easy to one-level abstraction pool (3), two
Extract saturation degree in level abstraction pool (4) and three grades of abstraction pools (5) is monitored in real time, changes in time or shifts,
Use more convenient.
The thermally induced phase separation of present invention design prepares the after-treatment device of hollow-fibre membrane, and one-level abstraction pool (3) is external
Having primary cycle pump (301), two grades of abstraction pools (4) are circumscribed with secondary cycle pump (401), and three grades of abstraction pools (5) are circumscribed with three grades
Circulating pump (501)；One-level abstraction pool (3) inside bottom is provided with one-level agitator arm (304), two grades of abstraction pool (4) inner side ends
Portion is provided with two grades of agitator arms (404), and three grades of abstraction pool (5) inside bottom are provided with three grades of agitator arms (504)；Above-mentioned set
Meter structure, accelerates the mobility of extract in one-level abstraction pool (3), two grades of abstraction pools (4) and three grades of abstraction pools (5), favorably
In lifting extraction efficiency.
The thermally induced phase separation of present invention design prepares the after-treatment device of hollow-fibre membrane, refrigerated separation tower (6) import
End is provided with check-valves (11), and one-level abstraction pool (3), two grades of abstraction pools (4) and three grades of abstraction pools (5) pass through check-valves respectively
(11) being communicated to refrigerated separation tower (6), refrigerated separation tower (6) bottom is provided with condensate liquid collecting tank (601), refrigerated separation tower
(6) top is provided with drying tube (602)；Above-mentioned design structure, it is to avoid the alcohol gas after gasification and other other extractants
The environmental pollution that outer row causes.
The thermally induced phase separation of present invention design prepares the after-treatment device of hollow-fibre membrane, ethanol raffinate crystallizing tank (7)
And the part that the connecting pipe between rectifying column (8) is positioned at ethanol raffinate crystallizing tank (7) inner side is set to filter screen type bending tube
Structure (703), ethanol raffinate crystallizing tank (7) center is provided with insulated column (702), and ethanol raffinate is tied by insulated column (702)
Brilliant tank (7) is divided into left chamber and right chamber, and left chamber is connected with right chamber, and filter screen type bending tube structure (703) is arranged
In left chamber one end, the liquid outlet end of one-level abstraction pool (3), two grades of abstraction pools (4) and three grades of abstraction pools (5) is communicated in right chamber
One end；Above-mentioned design structure, is conducive to entering the extract raffinate rapid crystallization in ethanol raffinate crystallizing tank (7), avoids simultaneously
Large particulate matter enters rectifying column (8) and causes the rectifying column (8) to block, and causes the system failure.
The thermally induced phase separation of present invention design prepares the post-processing approach of hollow-fibre membrane, uses the extraction of gradient extraction
Mode, is greatly improved the extraction efficiency of diluent in hollow-fibre membrane.
The present invention in use, utilizes cooling coil (701) to ethanol raffinate crystallizing tank (7) to carrying out supplement heat rejecter, sharp
It with heat exchanger (10) by the heat fast transfer in ethanol raffinate crystallizing tank (7) to purifying ethanol holding vessel (1), and is used for purifying
The heating of ethanol holding vessel (1), it is achieved heat exchange, improves efficiency of utilization, reduces thermal losses.
As described above, the present invention can be applied.
The above, the only present invention preferably detailed description of the invention, but protection scope of the present invention is not limited thereto,
Any those familiar with the art in the technical scope that the invention discloses, according to technical scheme and
Inventive concept in addition equivalent or change, all should cover within protection scope of the present invention, especially set out, and the present invention designs
Device can be used for the process technique of other similar solvent.
Claims (10)
1. a thermally induced phase separation prepares the after-treatment device of hollow-fibre membrane, it is characterised in that include that purifying ethanol stores
Tank (1), one-level high-pressure extraction pump (2), one-level abstraction pool (3), two grades of abstraction pools (4), three grades of abstraction pools (5) and refrigerated separation tower
(6), described purifying ethanol holding vessel (1), high-pressure extraction pump (2), one-level abstraction pool (3), two grades of abstraction pools (4), three grades of extractions
Pond (5) and refrigerated separation tower (6) connect successively；
Described one-level abstraction pool (3), two grades of abstraction pools (4) and three grades of abstraction pools (5) are set to identical structure；
Described purifying ethanol holding vessel (1) lower right is provided with ethanol raffinate crystallizing tank (7), and ethanol raffinate crystallizing tank (7) is external
Rectifying column (8), rectifying column (8) is respectively communicated to one-level abstraction pool (3), two grades of abstraction pools (4) by two grades of high-pressure extraction pumps (9)
With three grades of abstraction pools (5)；
Described one-level abstraction pool (3) liquid outlet end and two grades of abstraction pool (4) inlet ends are connected by feed-line, and one-level extracts
Take and be provided with one-level three-way control valve on the feed-line between pond (3) liquid outlet end and two grades of abstraction pool (4) inlet ends
(305) and one-level elevator pump (306), one-level abstraction pool (3) is communicated to the crystallization of ethanol raffinate by one-level three-way control valve (305)
Tank (7)；
Described two grades of abstraction pool (4) liquid outlet ends and three grades of abstraction pool (5) inlet ends are connected by feed-line, two grades of extractions
Take and be provided with two grades of three-way control valves on the feed-line between pond (4) liquid outlet end and three grades of abstraction pool (5) inlet ends
(405) and two-stage hoisting pump (406), two grades of abstraction pools (4) are communicated to the crystallization of ethanol raffinate by two grades of three-way control valves (405)
Tank (7)；
Described three grades of abstraction pool (5) liquid outlet ends are provided with three grades of three-way control valves (505) and three grades of elevator pumps (506), three grades
Abstraction pool (5) is communicated to ethanol raffinate crystallizing tank (7) by three grades of three-way control valves (505)；
Described purifying ethanol holding vessel (1) bottom is provided with cellular heated base (101)；
Described one-level three-way control valve (305) is circumscribed with extractant saturation degree monitor one, and two grades of three-way control valves (405) are external
Having extractant saturation degree monitor two, three grades of three-way control valves (505) are circumscribed with extractant saturation degree monitor three；
Described ethanol raffinate crystallizing tank (7) bottom is provided with cooling coil (701).
2. thermally induced phase separation according to claim 1 prepares the after-treatment device of hollow-fibre membrane, it is characterised in that institute
State and between ethanol raffinate crystallizing tank (7) and purifying ethanol holding vessel (1), be provided with heat exchanger (10).
3. thermally induced phase separation according to claim 1 prepares the after-treatment device of hollow-fibre membrane, it is characterised in that institute
Stating one-level abstraction pool (3) and being circumscribed with primary cycle pump (301), two grades of abstraction pools (4) are circumscribed with secondary cycle pump (401), three grades
Abstraction pool (5) is circumscribed with three grades of circulating pumps (501).
4. thermally induced phase separation according to claim 1 prepares the after-treatment device of hollow-fibre membrane, it is characterised in that institute
Stating one-level abstraction pool (3) inner side and being provided with one-level overlay film frame (302), two grades of abstraction pool (4) inner sides are provided with two grades of overlay film framves
(402), three grades of abstraction pool (5) inner sides are provided with three grades of overlay film framves (502)；
One-level overlay film frame (302) is removably assemblied on one-level abstraction pool (3)；Two grades of overlay film framves (402) are removably assembled
On two grades of abstraction pools (4)；Three grades of overlay film framves (502) are removably assemblied on three grades of abstraction pools (5), described one-level overlay film frame
(302), two grades of overlay film framves (402) and three grades of overlay film framves (502) are set to identical structure.
5. thermally induced phase separation according to claim 1 prepares the after-treatment device of hollow-fibre membrane, it is characterised in that institute
State and in one-level overlay film frame (302), be provided with one-level overlay film laminate (303), two grades of abstraction pools (4) are provided with two grades of overlay film laminates
(403), three grades of abstraction pools (5) are provided with three grades of overlay film laminates (503), described one-level overlay film laminate (303), two grades of coating layers
Plate (403) and three grades of overlay film laminates (503) are set to identical structure.
6. thermally induced phase separation according to claim 1 prepares the after-treatment device of hollow-fibre membrane, it is characterised in that institute
Stating one-level abstraction pool (3) inside bottom and being provided with one-level agitator arm (304), two grades of abstraction pool (4) inside bottom are provided with two
Level agitator arm (404), three grades of abstraction pool (5) inside bottom are provided with three grades of agitator arms (504).
7. thermally induced phase separation according to claim 1 prepares the after-treatment device of hollow-fibre membrane, it is characterised in that institute
Stating one-level abstraction pool (3) lateral wall and being provided with one-level heating mantle (307), lateral wall is provided with two grades of heating mantles (407), three grades of extractions
Take pond (5) lateral wall and be provided with three grades of heating mantles (507).
8. thermally induced phase separation according to claim 1 prepares the after-treatment device of hollow-fibre membrane, it is characterised in that institute
State refrigerated separation tower (6) entrance point and be provided with check-valves (11), one-level abstraction pool (3), two grades of abstraction pools (4) and three grades of abstraction pools
(5) being communicated to refrigerated separation tower (6) by check-valves (11) respectively, refrigerated separation tower (6) bottom is provided with condensate liquid collecting tank
(601), refrigerated separation tower (6) top is provided with drying tube (602).
9. thermally induced phase separation according to claim 1 prepares the after-treatment device of hollow-fibre membrane, it is characterised in that institute
State the connecting pipe between ethanol raffinate crystallizing tank (7) and rectifying column (8) be positioned at ethanol raffinate crystallizing tank (7) inner side part set
Being set to filter screen type bending tube structure (703), ethanol raffinate crystallizing tank (7) center is provided with insulated column (702), insulated column
(702) ethanol raffinate crystallizing tank (7) being divided into left chamber and right chamber, left chamber is connected with right chamber, and filter screen type is rolled over
Bend pipe structure (703) is arranged at left chamber one end, one-level abstraction pool (3), the going out of two grades of abstraction pools (4) and three grades abstraction pool (5)
Liquid mouth end is communicated in right chamber.
10. a thermally induced phase separation prepares the post-processing approach of hollow-fibre membrane, it is characterised in that comprise the following steps：
Step 1)：Pending hollow-fibre membrane is layed in one-level overlay film laminate (303) of one-level overlay film frame (302), and
It is assemblied in one-level overlay film frame (302) in one-level abstraction pool (3)；
Step 2)：Inject abstraction purification ethanol in the purifying ethanol holding vessel (1), utilize cellular heated base (101) to pure
The ethanol changed in ethanol holding vessel (1) heats, and the ethanol after being heated by high-pressure extraction pump (2) is pumped to one-level extraction
In pond (3), two grades of abstraction pools (4) and three grades of abstraction pools (5), in one-level abstraction pool (3), two grades of abstraction pools (4) and three grades of extractions
Pond (5) is respectively completed one-level extraction, two grades of extractions and three grades of extractions of dilution；
Step 3)：Open primary cycle pump (301), secondary cycle pump (401) and three grades of circulating pumps (501), open one-level stirring
Impeller (304), two grades of agitator arms (404) and three grades of agitator arms (504), utilize primary cycle pump (301) and one-level stirring
Extract flowing in one-level abstraction pool (3) is accelerated in the cooperation of impeller (304), utilizes secondary cycle pump (401) and two grades of paddles
Extract flowing in two grades of abstraction pools (4) is accelerated in the cooperation of wheel (404), utilizes three grades of circulating pumps (501) and three grades of agitator arms
(504) extract flowing in three grades of abstraction pools (5) is accelerated in cooperation；
Step 4)：Open extractant saturation degree monitor the first, extractant saturation degree monitor two and extractant saturation degree monitor
Three, the Monitoring Data according to extractant saturation degree monitor one is to one-level three-way control valve (305) and ethanol raffinate crystallizing tank (7)
Connectedness be controlled, utilize the Monitoring Data of extractant saturation degree monitor two to two grades of three-way control valves (405) and second
The connectedness of alcohol raffinate crystallizing tank (7) is controlled, and the Monitoring Data according to extractant saturation degree monitor three is to three grades of threeways
Control valve (505) is controlled with the connectedness of ethanol raffinate crystallizing tank (7)；
The extractant saturation degree detecting in three grades of abstraction pools (5) when extractant saturation degree monitor three terminates also three grades of extractions
When being in unsaturation state, utilize the cooperation of two grades of three-way control valves (405) and two-stage hoisting pump (406), by three grades of abstraction pools
(5) in, unsaturated extractant is transferred to reuse in two grades of abstraction pools (4), if extractant saturation degree monitor three detects
Extractant saturation degree in three grades of abstraction pools (5), when three grades of extraction end are in saturation state, utilizes three grades of three-way control valves
(505) three grades of abstraction pools (5) are connected with ethanol raffinate crystallizing tank (7), saturated extractant is directly discharged to ethanol raffinate
Crystallizing tank crystallizes in (7)；
The extractant saturation degree detecting in two grades of abstraction pools (4) when extractant saturation degree monitor two terminates also two grades of extractions
When being in unsaturation state, utilize one-level three-way control valve (305) and the cooperation of one-level elevator pump (306), by two grades of abstraction pools
(4) in, unsaturated extractant is transferred to reuse in one-level abstraction pool (3), if extractant saturation degree monitor two detects
Extractant saturation degree in two grades of abstraction pools (4), when two grades of extraction end are in saturation state, utilizes two grades of three-way control valves
(405) two grades of abstraction pools (4) are connected with ethanol raffinate crystallizing tank (7), saturated extractant is directly discharged to ethanol raffinate
Crystallizing tank crystallizes in (7)；
When extractant saturation degree monitor one detects that the extractant saturation degree in one-level abstraction pool (3) is located when one-level extracts
When saturation state, one-level three-way control valve (305) is utilized to connect one-level abstraction pool (3) with ethanol raffinate crystallizing tank (7), will
Saturated extractant is directly discharged to crystallize in ethanol raffinate crystallizing tank (7)；
Step 5)：Open cooling coil (701), utilize cooling coil (701) to the extraction collected in ethanol raffinate crystallizing tank (7)
Agent raffinate carries out Crystallization Separation, it is thus achieved that ethanol raffinate is delivered to rectifying column (8)；
Step 6)：Open rectifying column (8), enter to being delivered to the internal ethanol raffinate of rectifying column (8) via ethanol raffinate crystallizing tank (7)
Row rectification process, the clean ethanol obtaining after rectification process is sent to one-level abstraction pool respectively via two grades of high-pressure extraction pumps (9)
(3), two grades of abstraction pools (4) or three grades of abstraction pools (5), be re-used for the extraction of diluent；
Step 7)：According to extractant saturation degree monitor the first, extractant saturation degree monitor two and extractant saturation degree monitor
One-level overlay film frame (302) being equipped with pending hollow-fibre membrane in one-level abstraction pool (3) is shifted by the Monitoring Data of three successively
To two grades of abstraction pools (4), the two grades of overlay film framves (402) being equipped with pending hollow-fibre membrane in two grades of abstraction pools (4) are turned
Move in three grades of abstraction pools (5)；
Step 8)：According to the Monitoring Data of extractant saturation degree monitor three, to dilution remaining in pending hollow-fibre membrane
Agent judges, when the content of the diluent monitoring is less than setting value, takes out three grades of overlay film framves (502), and takes out laying
In the hollow-fibre membrane of three grades of overlay film laminates (503), hollow-fibre membrane finished product can be obtained.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
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