CN101890301A - Air-lift membrane filtration complete equipment - Google Patents
Air-lift membrane filtration complete equipment Download PDFInfo
- Publication number
- CN101890301A CN101890301A CN 201010222881 CN201010222881A CN101890301A CN 101890301 A CN101890301 A CN 101890301A CN 201010222881 CN201010222881 CN 201010222881 CN 201010222881 A CN201010222881 A CN 201010222881A CN 101890301 A CN101890301 A CN 101890301A
- Authority
- CN
- China
- Prior art keywords
- gas
- kettle
- membrane
- tail gas
- circulation pipe
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Abstract
The invention relates to air-lift membrane filtration complete equipment. The air-lift membrane filtration complete equipment consists of a membrane filtration system, a feed pump, a gas supply system, a tail gas solvent reclaiming system and an energy reclaimer, wherein the membrane filtration system consists of a kettle body 2, a circulating pipe 9 and a membrane component 10; the gas supply system consists of a compressed gas source and a gas flowmeter; the tail gas solvent reclaiming system consists of a tail gas condenser, a gas-liquid separating tank, an adsorption column and a dryer; in the kettle body, an upper cylinder body is a circulating area and a lower cone body is a sedimentation area; the circulating pipe is arranged on the side wall of the kettle body; the membrane component is encapsulated in the circulating pipe and is connected with the compressed gas source; a transmembrane pressure and a membrane surface gas speed are controlled by adjusting a gas inlet and outlet valve of the kettle body, so that positive pressure filtration concentration is realized; membrane flux is improved through the strengthening effect of gas-liquid two-phase flow; and the tail gas solvent reclaiming system can reclaim air-lift solvent and convert tail gas pressure into electric energy or mechanical energy. The air-lift membrane filtration complete equipment has the advantages of low energy consumption, high reclaiming efficiency, mild filtration condition and the like.
Description
Technical field
The present invention relates to a kind of air-lift membrane filtration complete equipment, this device integrates membrane filtration system, feeding system, air supply system, tail gas solvent recovering system and energy-recuperation system, is specially adapted to high pressure (the serialization filtering and concentrating of 0.3～2.5MPa) time biochemical preparation extract.
Technical background
In the biochemical pharmacy technology, modern fermentation technique is in middle cardiac status, and the production of most biochemical preparations realizes that by Fermentation Engineering the product that is suitable for the industrial system fermentation has antibiotic, amino acid, enzyme preparation, steroid hormone, single cell protein etc.A series of subsequent treatment operations such as the zymotic fluid that obtains by fermentation needs after filtration, ion-exchange, absorption, wash-out, extraction, distillation just finally obtain product, often have problems such as complex technical process, the operating time is long, consumption of raw materials is big, product yield is low, and the sex change inactivation may take place in product in very long leaching process.In extraction-still-process, solvent adopts the way of distillation to reclaim, and power consumption is big, is the main power consumption section in the production technology, and the use of a large amount of solvents has also produced problems such as the solvent loss amount is big, water-washing process produces a large amount of organic wastewaters, the subsequent technique load increases the weight of simultaneously.
Membrane separation technique is as a kind of new and effective isolation technics, have that equipment is simple, normal-temperature operation, no phase transformation and chemical change, selectivity height and low power consumption and other advantages, be specially adapted to the separation and purification of thermal sensitivity biogenetic products, be widely applied to chemical industry, food, biology, medicine and other fields.Adopt membrane separation technique concentration biochemical preparation extract can overcome many shortcomings of above-mentioned traditional handicraft, be subjected to extensive concern in recent years.
In the film separation field, provide cross-flow membrane concentration technique that power drives feed liquid circulation comparative maturity with pump, be widely applied in the concentrating of products such as dairy products, Juice.But the cross-flow membrane enrichment facility is when filtering, and concentrated medium at face accumulation, obstruction fenestra, has a strong impact on the film permeation flux easily, needs to improve the feed liquid crossflow velocity and alleviate the film pollution, and flow velocity generally reaches 2～10m/s, and the energy that is consumed is higher; The shearing force of impeller generation simultaneously is also bigger, and this makes that the activity of tiring of biochemical preparation is destroyed easily, even causes inactivation; Pump for ultrafiltration or NF membrane system, often needs very high pressure also for membrane filtration system provided osmolality simultaneously, and this just needs centrifugal multistage pump multiple centrifugal pump and single-stage pump combination, and equipment investment and equipment energy consumption are all higher.
Aeration is incorporated in the membrane filtration processes, can increases the face shearing force, alleviate film and pollute, improve membrane flux.A kind of ceramic film tube bioreaction and separation system that ZL01108189.9 proposes effectively solves membrane pollution problem by recoil aeration and gas lift aeration, but this system is an opened type, adopt the negative pressure suction that transmembrane pressure is provided, transmembrane pressure is less than 0.1MPa, and the molecular weight of biochemical preparation is less, between 200～70000Da, needs ultrafiltration or NF membrane system, this just needs higher transmembrane pressure, so this system is not suitable for the filtering and concentrating of biochemical preparation extract.A kind of air-lift membrane filtration device that ZL200610040552.0 proposes is similarly opened type, adopts the negative pressure suction that transmembrane pressure is provided, and transmembrane pressure is less than 0.1MPa.
Gas lift type membrane reactor is that airlift reactor is separated the new membrane reactor that is integrated in one with film, by the reactor kettle, stalk, downspout, parts such as membrane component are formed, the fluid density official post reactor inner fluid that relies on the different gas holdups with downspout of stalk to produce circulates, belong to strength agitating type reactor, difference according to structure can be divided into outside circulation gas lift type membrane reactor and built-in gas lift type membrane reactor, outside circulation gas lift type membrane reactor is subjected to extensive studies owing to have higher cycle rate and better mass transfer effect in recent years.The ZL200510094204.7 reported first have an outside circulation gas lift type membrane reactor of integral structure, the continuous aeration that this reactor can realize relating to gas-liquid-solid phase reaction with separate continuously, have higher mixing efficiency and mass-transfer efficiency, strengthen course of reaction, and can effectively reduce the film pollution.ZL200910026442.2 is on the basis of above-mentioned outside circulation gas lift type membrane reactor, add gas distributor replacement air lift and return pipe and be used to the reflux gas that distributes, Compressed Gas after circulation finishes has played the effect that gas is proposed again, make the removal of volatile product propose common control with gas, strengthened the mass transfer effect of reactor by the film separation.Although these reactors at biochemical reaction design have separation function, operation or adopt the mode of negative pressure suction to realize under lower pressure usually, thereby the energy of not considering high pressure exhaust gas utilizes again, the carrying secretly and problem such as solvent recovery of liquid.
Summary of the invention
The objective of the invention is: in order to solve the problems referred to above that exist in the cross-flow membrane enrichment facility, gas lift type membrane reactor is incorporated in the filtering and concentrating of biochemical preparation extract, and a kind of improved air-lift membrane filtration complete equipment proposed, feeding system, tail gas solvent recovering system and energy-recuperation system are coupled in the gas lift type membrane reactor, effectively reclaim the gas extraction solvent, further reduce the energy consumption of concentration process, the serialization operation of implement device.
Main technical schemes of the present invention is as follows: a kind of air-lift membrane filtration complete equipment, form by membrane filtration system, charging pump A-1, air supply system, tail gas solvent recovering system and recuperator E-1; Wherein membrane filtration system is made up of kettle 2, circulation pipe 9, membrane module 10; Air supply system is made up of compressed gas source C-1 and gas flowmeter C-2; The tail gas solvent recovering system is made up of tail gas condenser D-1, knockout drum D-2, adsorption column D-3 and drier D-4; It is characterized in that kettle 2 is divided into two parts, the top cylindrical shell is the race way, and the bottom centrum is the decanting zone; Circulation pipe 9 is contained in kettle 2 side arm positions, is communicated with kettle; Kettle 2 upper ends have charging aperture 6, exhaust outlet 7, the lower end has discharge port 1, charging aperture 6 links to each other with charging pump A-1 by valve V-2, and exhaust outlet 7 links to each other with tail gas condenser D-1, knockout drum D-2, adsorption column D-3, drier D-4, recuperator E-1 successively by valve V-3; Aeration head 14 is equipped with in circulation pipe 9 lower ends, and aeration head 14 links to each other with gas flowmeter C-2, compressed gas source C-1 successively by valve V-4; Membrane component 12 fills in the membrane module 10, and membrane module 10 is encapsulated in the circulation pipe 9, is provided with filtrate (liquid 11 and recoil compressed gas source import 13.
Described kettle race way ratio of height to diameter is 2～20, and the kettle decanting zone sedimentation gradient and horizontal plane angle are 30～60 °.Circulation pipe is gone into head piece and is opened in the kettle race way bottom, and the circulation pipe height is 1/5～4/5 of a kettle race way height, and the circulation pipe internal diameter is 1/5～1 of a kettle race way internal diameter.
Preferred described charging pump A-1 is plunger displacement pump, membrane pump or Pneumatic liquid booster pump; Described recuperator E-1 is tail gas turbine, air motor or air driven pump.
Described membrane component is that the aperture is single tube or the multichannel ceramic membrane of 0.9～50nm; Its material is at least TiO
2, ZrO
2, SiO
2Or Al
2O
3In a kind of.
Described kettle has water-bath chuck 3, is convenient to control feed temperature, and kettle has form 4, in time observes situation in the still, and fluid level controller 5 is installed.
The present invention also provides the method for utilizing said apparatus filtering and concentrating biochemical preparation extract, and its concrete steps are: at first material liquid A is joined the kettle 2 from charging aperture 6; Subsequently Compressed Gas C is fed circulation pipe 9 through aeration head 14, rely on kettle 2 to circulate with the fluid density official post kettle inner fluid that circulation pipe 9 different gas holdups produce, control valve V-3, V-4 control transmembrane pressure and face gas speed, valve-off V-6 opens valve V-5, under pressure-driven, penetrating fluid F flows out from filtrate (liquid 11, concentrates medium and is held back by ceramic membrane, realizes the malleation filtering and concentrating, during filtering and concentrating, A-1 adds feed liquid to kettle by charging pump; Gas after circulation finishes improves presses tail gas D flow through tail gas condenser D-1, knockout drum D-2, adsorption column D-3, drier D-4, reclaim the gas extraction solvent, dried purification high pressure exhaust gas E can convert tail gas pressure to electric energy or mechanical energy through recuperator E-1; Wait to concentrate and finish, draw concentrate B by discharge port 1.
In the filtering and concentrating process, valve-off V-5 opens valve V-6, presses ceramic membrane to realize that recoil cleans from the recoil compressed gas source import 13 Compressed Gas G that intermittently will recoil, helps the membrane flux recovery.
It is 0.3～2.5MPa that the present invention controls transmembrane pressure; Control face gas speed is 0.05～1m/s.
Method of the present invention is characterized in that the highest row pressure of charging pump is 0.5～5.0MPa, by the switch of fluid level controller control charging pump.
Beneficial effect:
1, this device kettle bottom is provided with the decanting zone, makes suspended particulate in the feed liquid and solid impurity easily break away from the race way and settles down, and alleviates film and pollutes, and improves membrane flux, thereby improves the thickening efficiency of device.
2, the same successively tail gas condenser of this device exhaust outlet, knockout drum, adsorption column, drier, recuperator link to each other, tail gas condenser, knockout drum can reclaim the condensation of gas extraction solvent, adsorption column further removes the solvent in the tail gas, promptly saved cost, avoided the pollution of solvent again atmosphere; Dry purification high pressure exhaust gas can convert tail gas pressure to electric energy or mechanical energy through recuperator, wherein the tail gas turbine regenerative power can reach compressed gas source wasted work 30%～65%, saved energy consumption cost greatly, played huge impetus installing further industrialization.
3, this device charging aperture links to each other with charging pump, when filtering and concentrating is carried out, can add feed liquid to kettle by charging pump, waits to concentrate and finishes, and draws concentrate by discharge port, the serialization operation of implement device.
4, Compressed Gas feeds circulation pipe through aeration head, forms biphase gas and liquid flow with the feed liquid contact, has increased the face shearing force, make that concentrating medium is not easy to accumulate at face, effectively alleviate the film pollution, improved membrane flux, can under lower crossflow velocity, obtain higher membrane flux; Compressed Gas after circulation finishes enters kettle through gas distributor and has played the effect that gas is proposed, and makes concentration process finally be separated with gas by film and proposes common control, has efficiently utilized Compressed Gas, has improved the thickening efficiency of device.
5, this device relies on the fluid density official post kettle inner fluid of the different gas holdups generations with circulation pipe of kettle to circulate, belong to strength agitating type device, the condition that produces is gentle, can better protect concentrates the activity of medium, is applicable to the filtering and concentrating of thermal sensitivity biochemical preparation; In addition, import and export tolerance by regulating kettle, can realize malleation filtering and concentrating under high pressure, transmembrane pressure can reach 2.5MPa, is applicable to small-bore (0.9～50nm) ultrafiltration and NF membrane system; Once more, this device relies on Compressed Gas to drive the feed liquid circulation and transmembrane pressure is provided, and need not to establish kinetic pump, greatly reduces equipment investment and equipment energy consumption.In general, this installs under high pressure the biochemical preparation extracting liquid filtering and embodies bigger advantage in concentrating.
6, membrane component adopt have high temperature resistant, acid and alkali-resistance, the ceramic membrane of advantageous property such as organic solvent-resistant, make this device both can be used for the filtering and concentrating of water solution system, also can be used for the filtering and concentrating of organic solvent systems such as methyl alcohol, ethanol, butanols, n-hexane, benzinum, ethyl acetate, range of application is very extensive.
Description of drawings
Fig. 1 is a kind of air-lift membrane filtration complete equipment schematic diagram;
Wherein A is a material liquid, and B is a concentrate, and C is a Compressed Gas, and D is that gas improves pressure tail gas, and E is for purifying high pressure exhaust gas, and F is a penetrating fluid, and G is the recoil Compressed Gas; 1 is discharge port, and 2 is kettle, and 3 are the water-bath chuck, and 4 is form, and 5 is fluid level controller, 6 is charging aperture, and 7 is exhaust outlet, and 8 is gas distributor, and 9 is circulation pipe, and 10 is membrane module, 11 is filtrate (liquid, and 12 is membrane component, and 13 are the recoil inlet for pressurised gas, and 14 is aeration head; A-1 is a charging pump, and C-1 is a compressed gas source, and C-2 is a gas flowmeter, and D-1 is a tail gas condenser, and D-2 is a knockout drum, and D-3 is an adsorption column, and D-4 is a drier, and E-1 is a recuperator, and V-1, V-2, V-3, V-4, V-5, V-6 are valve.
The specific embodiment
Specify embodiments of the present invention below in conjunction with accompanying drawing.
Air-lift membrane filtration complete equipment provided by the present invention is made up of membrane filtration system (kettle 2, circulation pipe 9, membrane module 10), feeding system (charging pump A-1), air supply system (compressed gas source C-1, gas flowmeter C-2), tail gas solvent recovering system (tail gas condenser D-1, knockout drum D-2, adsorption column D-3, drier D-4) and energy-recuperation system (recuperator E-1), as shown in Figure 1.Kettle 2 is divided into two parts, and the top cylindrical shell is the race way, and the bottom centrum is the decanting zone; Circulation pipe 9 is contained in kettle 2 side arm positions, is communicated with kettle; Kettle 2 upper ends have charging aperture 6, exhaust outlet 7, the lower end has discharge port 1, charging aperture 6 links to each other with charging pump A-1 by valve V-2, and exhaust outlet 7 links to each other with tail gas condenser D-1, knockout drum D-2, adsorption column D-3, drier D-4, recuperator E-1 successively by valve V-3; Aeration head 14 is equipped with in circulation pipe 9 lower ends, and aeration head 14 links to each other with gas flowmeter C-2, compressed gas source C-1 successively by valve V-4; Membrane component 12 fills in the membrane module 10, and membrane module 10 is encapsulated in the circulation pipe 9.
The membrane component that air-lift membrane filtration complete equipment provided by the present invention adopted is that the aperture is 0.9～50nm TiO
2, ZrO
2, SiO
2, Al
2O
3And the single tube of compound or multichannel ceramic membrane; Charging pump is plunger displacement pump, membrane pump or Pneumatic liquid booster pump; Recuperator is tail gas turbine, air motor or air driven pump.
The mode of operation of air-lift membrane filtration complete equipment provided by the present invention is as follows: at first material liquid A is joined the kettle 2 from charging aperture 6, subsequently Compressed Gas C is measured through aeration head 14 through gas flowmeter C-2 and feed circulation pipe 9, Compressed Gas is provided by compressed gas source C-1, relies on kettle 2 to circulate with the fluid density official post kettle inner fluid that circulation pipe 9 different gas holdups produce.Control valve V-3, V-4 control transmembrane pressure and face gas speed, valve-off V-6, open valve V-5, under pressure-driven, penetrating fluid F flows out from filtrate (liquid 11, concentrating medium is held back by ceramic membrane, realize the malleation filtering and concentrating, during filtering and concentrating, A-1 adds feed liquid to kettle by charging pump, control the switch of charging pump by fluid level controller 5, keep liquid level equilibrium.Compressed Gas after circulation finishes contacts with kettle top feed liquid through gas distributor 8, played the effect that gas is proposed, gas improve to be pressed tail gas D flow through tail gas condenser D-1, knockout drum D-2, the gas extraction solvent is reclaimed in condensation, adsorption column D-3 is used for further removing the tail gas solvent, and the purification Compressed Gas E of the drying device D-4 recuperator E-1 that flows through can convert tail gas pressure to electric energy or mechanical energy again.In the filtering and concentrating process, valve-off V-5 opens valve V-6, presses ceramic membrane to realize that recoil cleans from the recoil compressed gas source import 13 Compressed Gas G that intermittently will recoil, helps the membrane flux recovery.Wait to concentrate and finish, draw concentrate B, implement device serialization operation by discharge port 1.
This routine air-lift membrane filtration complete equipment kettle race way ratio of height to diameter is 5, and the kettle decanting zone sedimentation gradient and horizontal plane angle are 60 °, and the circulation pipe height is 2/5 of a kettle race way height, and the circulation pipe internal diameter is 1/2 of a kettle race way internal diameter.As the filtering and concentrating system, selecting the aperture for use is the 19 passage ZrO of 50nm with bovine serum albumin (molecular weight 67000Da) solution
2Ceramic membrane is as membrane component.At first regulating bovine serum albumen solution pH is 4.7, with concentration is that the bovine serum albumen solution of 2g/L joins in the air-lift membrane filtration complete equipment, feed Compressed Gas subsequently, the adjusting transmembrane pressure is 0.3MPa, face gas speed 0.15m/s, carry out the malleation filtering and concentrating, the bovine serum albumin rejection is 80%～90%, and the film stabilized flux reaches 88～140L/ (m
2H).The high pressure exhaust gas that the drying device purifies is as the motive force of Pneumatic liquid booster pump, and the Pneumatic liquid booster pump is realized feed supplement as charging pump, controls the switch of Pneumatic liquid booster pump by fluid level controller, keeps liquid level equilibrium.The Pneumatic liquid booster pump has rationally utilized high pressure exhaust gas pressure energy, has realized the energy recovery, carries out feed supplement as charging pump again.Continuous concentration 24h can obtain to concentrate 8 times bovine serum albumen solution.
This routine air-lift membrane filtration complete equipment kettle race way ratio of height to diameter is 8, and the kettle decanting zone sedimentation gradient and horizontal plane angle are 60 °, and the circulation pipe height is 3/5 of a kettle race way height, and the circulation pipe internal diameter is 1/3 of a kettle race way internal diameter.As the filtering and concentrating system, selecting the aperture for use is the Al of 10.0nm with chicken egg white (molecular weight 43000Da) solution
2O
3The ceramic membrane single tube is as membrane component.At first regulating the ovalbumin pH value of solution is 10.0, with concentration is that the ovalbumin solution of 300mg/L joins in the air-lift membrane filtration complete equipment, feed Compressed Gas subsequently, the adjusting transmembrane pressure is 0.8MPa, face gas speed 0.3m/s, carry out the malleation filtering and concentrating, the ovalbumin rejection is 90%～96%, and the film stabilized flux reaches 98～132L/ (m
2H).The high pressure exhaust gas that the drying device purifies is as the motive force of pneumatic gas booster pump, and the pneumatic gas booster pump can be used as compressed gas source, has realized the recycling of Compressed Gas, thereby has reduced plant energy consumption.When filtering and concentrating was carried out, selecting the highest row pressure was that the 1.0MPa diaphragm metering pump is added feed liquid to kettle, controlled the switch of diaphragm metering pump by fluid level controller, kept liquid level equilibrium.Continuous concentration 24h can obtain to concentrate 4 times ovalbumin solution.
This routine air-lift membrane filtration complete equipment kettle race way ratio of height to diameter is 8, and the kettle decanting zone sedimentation gradient and horizontal plane angle are 45 °, and the circulation pipe height is 3/5 of a kettle race way height, and the circulation pipe internal diameter is 1/3 of a kettle race way internal diameter.As the filtering and concentrating system, selecting the aperture for use is that titanium-zircon ceramic composite membrane single tube of 2.3nm is as membrane component with bacitracin (molecular weight 1422Da) butanols extract.At first preheating bacitracin butanols extract temperature is 50 ℃, with concentration is that the bacitracin butanols extract of 100mg/L joins in the air-lift membrane filtration complete equipment, feed Compressed Gas subsequently, the adjusting transmembrane pressure is 1.5MPa, face gas speed 0.6m/s, carry out the malleation filtering and concentrating, the bacitracin rejection is 89%～93%, and the film stabilized flux reaches 96～154L/ (m
2H).Tail gas condenser, knockout drum can be carried gas the butanols condensation and reclaim, and adsorption column further removes the butanols in the tail gas, and the rate of recovery of butanols reaches more than 99% in the tail gas.The high pressure exhaust gas that the drying device purifies flows into recuperator can convert tail gas pressure to electric energy or mechanical energy, and wherein the air motor regenerative power can reach compressed gas source wasted work 30%～50%.When filtering and concentrating was carried out, selecting the highest row pressure was that the 2.0MPa plunger type metering pump is added feed liquid to kettle, controlled the switch of plunger type metering pump by fluid level controller, kept liquid level equilibrium.Continuous concentration 36h can obtain to concentrate 10 times bacitracin butanols extract.
This routine air-lift membrane filtration complete equipment kettle race way ratio of height to diameter is 3, and the kettle decanting zone sedimentation gradient and horizontal plane angle are 30 °, and the circulation pipe height is 4/5 of a kettle race way height, and the circulation pipe internal diameter is 1/5 of a kettle race way internal diameter.As the filtering and concentrating system, selecting the aperture for use is the 19 passage TiO of 0.9nm with lanolin extract (60～90 ℃ of boiling range benzinums are solvent)
2Ceramic membrane is as membrane component.At first preheating lanolin extract temperature is 50 ℃, with concentration is that the lanolin extract of 1g/L joins in the air-lift membrane filtration complete equipment, feed Compressed Gas subsequently, the adjusting transmembrane pressure is 2.5MPa, face gas speed 0.45m/s, carry out the malleation filtering and concentrating, the lanolin rejection is 96%～99%, and the film stabilized flux reaches 46～105L/ (m
2H).Tail gas condenser, knockout drum can be carried gas the benzinum condensation and reclaim, and adsorption column further removes the benzinum in the tail gas, and the rate of recovery of tail gas PetroChina Company Limited. ether reaches more than 98%.The high pressure exhaust gas that the drying device purifies flows into recuperator can convert tail gas pressure to electric energy or mechanical energy, and wherein the tail gas turbine regenerative power can reach compressed gas source wasted work 30%～65%.When filtering and concentrating was carried out, selecting the highest row pressure was that the 5.0MPa plunger type metering pump is added feed liquid to kettle, controlled the switch of plunger type metering pump by fluid level controller, kept liquid level equilibrium.Continuous concentration 30h can obtain to concentrate 20 times lanolin extract.
Claims (9)
1. an air-lift membrane filtration complete equipment is made up of membrane filtration system, charging pump A-1, air supply system, tail gas solvent recovering system and recuperator E-1; Wherein membrane filtration system is made up of kettle (2), circulation pipe (9), membrane module (10); Air supply system is made up of compressed gas source C-1 and gas flowmeter C-2; The tail gas solvent recovering system is made up of tail gas condenser D-1, knockout drum D-2, adsorption column D-3 and drier D-4; It is characterized in that kettle (2) is divided into two parts, the top cylindrical shell is the race way, and the bottom centrum is the decanting zone; Circulation pipe (9) is contained in kettle (2) side arm position, is communicated with kettle; Kettle (2) upper end has charging aperture (6), exhaust outlet (7), the lower end has discharge port (1), charging aperture (6) links to each other with charging pump A-1 by valve V-2, and exhaust outlet (7) links to each other with tail gas condenser D-1, knockout drum D-2, adsorption column D-3, drier D-4, recuperator E-1 successively by valve V-3; Aeration head (14) is equipped with in circulation pipe (9) lower end, and aeration head (14) links to each other with gas flowmeter C-2, compressed gas source C-1 successively by valve V-4; Membrane component (12) fills in the membrane module (10), and membrane module (10) is encapsulated in the circulation pipe (9), is provided with filtrate (liquid (11) and recoil compressed gas source import (13).
2. device according to claim 1 is characterized in that kettle race way ratio of height to diameter is 2～20, and the kettle decanting zone sedimentation gradient and horizontal plane angle are 30～60 °.
3. device according to claim 1 is characterized in that circulation pipe goes into head piece and open in the kettle race way bottom; The circulation pipe height is 1/5～4/5 of a kettle race way height; The circulation pipe internal diameter is 1/5～1 of a kettle race way internal diameter.
4. device according to claim 1 is characterized in that described charging pump A-1 is plunger displacement pump, membrane pump or Pneumatic liquid booster pump; Described recuperator E-1 is tail gas turbine, air motor or air driven pump.
5. device according to claim 1 is characterized in that described membrane component is that the aperture is single tube or the multichannel ceramic membrane of 0.9～50nm; Its material is at least TiO
2, ZrO
2, SiO
2Or Al
2O
3In a kind of.
6. device according to claim 1 is characterized in that kettle has water-bath chuck (3), the control feed temperature; Kettle has form (4), observes situation in the still; Fluid level controller (5) is installed.
7. method by the described device filtering and concentrating of claim 1 biochemical preparation extract, its concrete steps are: at first material liquid A is joined the kettle (2) from charging aperture (6); Subsequently Compressed Gas C is fed circulation pipe (9) through aeration head (14), the fluid density official post kettle inner fluid that relies on the different gas holdups with circulation pipe (9) of kettle (2) to produce circulates, control valve V-3, V-4 control transmembrane pressure and face gas speed, valve-off V-6 opens valve V-5, under pressure-driven, penetrating fluid F flows out from filtrate (liquid (11), concentrates medium and is held back by ceramic membrane, realizes the malleation filtering and concentrating, during filtering and concentrating, A-1 adds feed liquid to kettle by charging pump; Gas after circulation finishes improves presses tail gas D flow through tail gas condenser D-1, knockout drum D-2, adsorption column D-3, drier D-4, reclaim the gas extraction solvent, dried purification high pressure exhaust gas E can convert tail gas pressure to electric energy or mechanical energy through recuperator E-1; Wait to concentrate and finish, draw concentrate B by discharge port (1).
8. method according to claim 7, it is characterized in that controlling transmembrane pressure is 0.3～2.5Mpa; Control face gas speed is 0.05～1m/s.
9. method according to claim 7 is characterized in that in the filtering and concentrating process valve-off V-5 opens valve V-6, presses ceramic membrane to realize that recoil cleans from recoil compressed gas source import (13) the Compressed Gas G that intermittently will recoil, helps the membrane flux recovery.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102228813A CN101890301B (en) | 2010-07-09 | 2010-07-09 | Air-lift membrane filtration complete equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102228813A CN101890301B (en) | 2010-07-09 | 2010-07-09 | Air-lift membrane filtration complete equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101890301A true CN101890301A (en) | 2010-11-24 |
| CN101890301B CN101890301B (en) | 2012-05-30 |
Family
ID=43099740
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010102228813A Active CN101890301B (en) | 2010-07-09 | 2010-07-09 | Air-lift membrane filtration complete equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101890301B (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102649499A (en) * | 2012-05-14 | 2012-08-29 | 高鼎精细化工(昆山)有限公司 | Solvent storage tank |
| CN103691322A (en) * | 2013-12-26 | 2014-04-02 | 利穗科技(苏州)有限公司 | Automatic ultrafiltration system and method for implementing ultrafiltration under constant transmembrane pressure by utilizing same |
| CN104089496A (en) * | 2014-07-02 | 2014-10-08 | 天津金海兴业科技有限公司 | System for converting industrial steam into industrial water |
| CN104973660A (en) * | 2015-07-10 | 2015-10-14 | 盐城琛丹低碳技术研究院有限公司 | Nanometer concentration filtration apparatus |
| CN106629958A (en) * | 2017-01-20 | 2017-05-10 | 南京工业大学 | Closed continuous high-pressure gas dissolving apparatus and method |
| CN107551817A (en) * | 2016-06-30 | 2018-01-09 | 国统国际股份有限公司 | Membrane filtration and energy recycle device |
| CN109534581A (en) * | 2018-12-30 | 2019-03-29 | 南京霄祥工程技术有限公司 | A kind of Zero-discharge treating process of Cutting Liquid Wastewater |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1560222A (en) * | 2004-03-04 | 2005-01-05 | 江南大学 | Coupling biologic reactor |
| CN1751780A (en) * | 2005-09-02 | 2006-03-29 | 南京工业大学 | Outside circulation gas lift type membrane reactor |
| CN101130744A (en) * | 2007-07-26 | 2008-02-27 | 上海交通大学 | Airlift type bioreactor system for continuously bottling and culturing medicinal plant histiocyte |
| CN101538532A (en) * | 2009-04-23 | 2009-09-23 | 南京工业大学 | External loop air lift type membrane bioreactor |
| CN201701877U (en) * | 2010-07-09 | 2011-01-12 | 南京工业大学 | Gas rising membrane filtration set device |
-
2010
- 2010-07-09 CN CN2010102228813A patent/CN101890301B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1560222A (en) * | 2004-03-04 | 2005-01-05 | 江南大学 | Coupling biologic reactor |
| CN1751780A (en) * | 2005-09-02 | 2006-03-29 | 南京工业大学 | Outside circulation gas lift type membrane reactor |
| CN101130744A (en) * | 2007-07-26 | 2008-02-27 | 上海交通大学 | Airlift type bioreactor system for continuously bottling and culturing medicinal plant histiocyte |
| CN101538532A (en) * | 2009-04-23 | 2009-09-23 | 南京工业大学 | External loop air lift type membrane bioreactor |
| CN201701877U (en) * | 2010-07-09 | 2011-01-12 | 南京工业大学 | Gas rising membrane filtration set device |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102649499A (en) * | 2012-05-14 | 2012-08-29 | 高鼎精细化工(昆山)有限公司 | Solvent storage tank |
| CN103691322A (en) * | 2013-12-26 | 2014-04-02 | 利穗科技(苏州)有限公司 | Automatic ultrafiltration system and method for implementing ultrafiltration under constant transmembrane pressure by utilizing same |
| CN103691322B (en) * | 2013-12-26 | 2016-03-30 | 利穗科技(苏州)有限公司 | A kind of automatic ultrafiltration system and the hyperfiltration process of this system under constant transmembrane pressure |
| CN104089496A (en) * | 2014-07-02 | 2014-10-08 | 天津金海兴业科技有限公司 | System for converting industrial steam into industrial water |
| CN104973660A (en) * | 2015-07-10 | 2015-10-14 | 盐城琛丹低碳技术研究院有限公司 | Nanometer concentration filtration apparatus |
| CN104973660B (en) * | 2015-07-10 | 2017-04-19 | 盐城琛丹低碳技术研究院有限公司 | Nanometer concentration filtration apparatus |
| CN107551817A (en) * | 2016-06-30 | 2018-01-09 | 国统国际股份有限公司 | Membrane filtration and energy recycle device |
| CN106629958A (en) * | 2017-01-20 | 2017-05-10 | 南京工业大学 | Closed continuous high-pressure gas dissolving apparatus and method |
| CN106629958B (en) * | 2017-01-20 | 2023-02-14 | 南京工业大学 | Closed continuous high-pressure gas dissolving device and method |
| CN109534581A (en) * | 2018-12-30 | 2019-03-29 | 南京霄祥工程技术有限公司 | A kind of Zero-discharge treating process of Cutting Liquid Wastewater |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101890301B (en) | 2012-05-30 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101890301B (en) | Air-lift membrane filtration complete equipment | |
| CN101870722B (en) | Process for concentrating protein in soy protein wastewater by two-stage foam separation method | |
| CN102030698B (en) | Method for separating and extracting L-tryptophan in fermentation liquor by utilizing organic film | |
| CN201701877U (en) | Gas rising membrane filtration set device | |
| CN101671324B (en) | Production method of glucolactone | |
| CN101643408A (en) | Production method of gulonic acid in production of vitamin C | |
| CN103041705B (en) | Device and method for coupling catalyst recovery process with dynamic disc membrane separation process | |
| CN109925742A (en) | Chromatographic separation device and the method for separating vitamin C mother liquor using it | |
| CN102107101A (en) | High-temperature condensed water recycling and purifying system with ceramic membrane filter | |
| CN102382203B (en) | High-efficiency extraction process for polysaccharide of lotus seeds | |
| CN102559817A (en) | Method for recovering protein from soybean whey wastewater | |
| CN104176714A (en) | Method for concentrating titanium dioxide waste acid by adopting reverse osmosis process | |
| CN104418724B (en) | A kind of oxalic rare earth precipitates water wash system | |
| CN203075844U (en) | Dynamic disc film device applied to recovery of superfine solid catalyst | |
| CN207708846U (en) | A kind of nanofiltration film condensing device producing natural pigment | |
| CN2853796Y (en) | Ketogulonic acid production device in vitamin C cleaning production | |
| CN207545889U (en) | One kind isolates and purifies system | |
| CN103007755B (en) | Be applied to dynamic video disc film device and the technique thereof of ultrafine solids catalyst recovery | |
| CN211688995U (en) | Organic acid circulation fermenting installation | |
| CN111714925A (en) | Self-assembled tank countercurrent extraction method | |
| CN210085323U (en) | Tributyl citrate esterification reaction device with circulating system | |
| CN103450041A (en) | Extraction process of lysine fermentation liquor | |
| CN211689038U (en) | Organic acid circulation fermentation and separation extraction element | |
| CN212998521U (en) | Membrane extraction and separation device | |
| CN212757595U (en) | Galactomannan incomplete degradation product purification device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20180129 Address after: 211816 Jiangsu, Nanjing, Pu Pu Road, Pukou District No. 30 Patentee after: Nanjing Industrial University Ketu Ding Energy Technology Co., Ltd. Address before: 210009 Zhongshan North Road, Jiangsu, No. 200, Patentee before: Nanjing University of Technology |
|
| TR01 | Transfer of patent right |