CN204429105U - A kind of novel membrane separator - Google Patents
A kind of novel membrane separator Download PDFInfo
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- CN204429105U CN204429105U CN201420036967.0U CN201420036967U CN204429105U CN 204429105 U CN204429105 U CN 204429105U CN 201420036967 U CN201420036967 U CN 201420036967U CN 204429105 U CN204429105 U CN 204429105U
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- 239000012528 membrane Substances 0.000 title claims abstract description 125
- 239000012466 permeate Substances 0.000 claims abstract description 87
- 239000012141 concentrate Substances 0.000 claims abstract description 15
- 210000004907 gland Anatomy 0.000 claims abstract description 8
- 239000007788 liquid Substances 0.000 claims description 58
- 239000000463 material Substances 0.000 claims description 26
- 239000012530 fluid Substances 0.000 claims description 13
- 230000007246 mechanism Effects 0.000 claims description 9
- 239000003822 epoxy resin Substances 0.000 claims description 4
- 239000000835 fiber Substances 0.000 claims description 4
- 229920000647 polyepoxide Polymers 0.000 claims description 4
- 239000010977 jade Substances 0.000 claims description 2
- 239000002994 raw material Substances 0.000 claims description 2
- 238000009434 installation Methods 0.000 abstract description 5
- 239000000126 substance Substances 0.000 description 12
- 238000010586 diagram Methods 0.000 description 10
- 238000000034 method Methods 0.000 description 10
- 238000000926 separation method Methods 0.000 description 10
- 238000005516 engineering process Methods 0.000 description 9
- 230000010287 polarization Effects 0.000 description 9
- 238000007599 discharging Methods 0.000 description 8
- 238000005119 centrifugation Methods 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 230000004907 flux Effects 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 230000000903 blocking effect Effects 0.000 description 2
- 235000013305 food Nutrition 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000013049 sediment Substances 0.000 description 2
- 230000004888 barrier function Effects 0.000 description 1
- 235000013361 beverage Nutrition 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 235000013365 dairy product Nutrition 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 235000012489 doughnuts Nutrition 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 235000011389 fruit/vegetable juice Nutrition 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000035515 penetration Effects 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 230000007306 turnover Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
A kind of novel membrane separator, membrane module is arranged on the hypergravity membrane separator with rotary drum differential coaxial rotation on auger conveyor, auger conveyor (6) is by forming auger conveyor left end cap (6-1), auger conveyor stage casing (6-6), auger conveyor membrane module gland (9) forms, auger conveyor left end cap (6-1) is fixedly connected with auger conveyor stage casing (6-6) and jointly forms auger conveyor permeate and converge chamber (5), auger conveyor stage casing (6-6) is fixedly connected with auger conveyor membrane module gland (9) and is fixed on auger conveyor (6) by membrane module (8), the utility model effectively improves the discharge condition that film retains concentrate, substantially increases the draw ratio of rotary drum (4), substantially increases film unit installation, and unit treating capacity increases, and it is high that film retains concentrate concentration.
Description
(1) technical field
The present invention relates to a kind of membrane separator, is a kind of membrane separator worked under hypergravity condition, the membrane separator worked under hypergravity condition that especially a kind of membrane module and rotary drum coaxial differential rotate.
(2) technical background
Membrane separation technique is one of current ten large new and high technologies, be described as 21 century Chemical Engineering Technology most with prospects, at present, be widely used in being separated of the fields such as food, beverage, chemical industry, pharmacy, environmental protection, desalinization, water supply and sewage disposal, concentrated, the process procedure such as purifying.But the extensive existence due to film concentration polarization and fouling membrane causes current membrane separation technique, and also there are the following problems:
1, membrane flux declines fast, film deterioration aggravation, membrane lifetime reduce, UF membrane acquisition cost and operating cost increase considerably.
2, membrane separating process energy consumption increases considerably, and operating cost increases considerably.
3, when high concentration charging and high power concentrate, film concentration polarization and fouling membrane are more serious, cause UF membrane be difficult at technique occasion performance difficulties such as high input concentration and high powers concentrated (as dairy products, Juice) or can not implement at all.
Film concentration polarization and fouling membrane cause UF membrane to be purchased with operating cost height to be the main reason limiting its application, to have become general common recognition.
In addition, film causes film back permeate pressure large through side runner narrow (especially hollow-fibre membrane), is another main cause that doughnut membrane flux is low.
For solving the problem, there is people through studying intensively, successfully membrane separation technique and high-gravity technology two new and high technologies being organically combined, found hypergravity membrane separation technique, propose hypergravity UF membrane concept, operation principle, design principle, obtain following patent of invention:
The membrane module (zl200810054213.7) that A, dependence rigid rotatable barrel body work under being supported on hypergravity condition
B, rotating centrifugal hypergravity membrane separator (zl200910068949.4)
C, the hypergravity membrane separator (zl200910070253.5) be made up of multiple membrane module be independently fixed on rotating disk
Hypergravity membrane separation technique is the combination of the large new and high technology of membrane separation technique and high-gravity technology two, this technology is that each key element (diffusion barrier, feeding liquid, permeate, cleaning fluid) in membrane separating process is placed in the super gravity field produced by rotating centrifugal, 1. utilize the density contrast that the concentration difference of film surface concentration polarization layer and main body feed liquid in membrane separating process causes, the powerful centrifugal force produced by means of centrifugal rotation makes concentration polarization pull-up from film surface, thus reduces film concentration polarization and fouling membrane.2. the centrifugal force utilizing centrifugal rotation to produce makes film throw away permeate passage after film through the permeate of side, thus pressure after reducing film, and then improve membrane flux.
The advantage of hypergravity membrane separation technique
1, film concentration polarization and fouling membrane can effectively be reduced.
2, membrane flux and membrane efficiency can greatly be improved.
3, film device acquisition cost and operating cost can significantly be reduced.
4, greatly can expand the application space of membrane separation technique, the film that especially high input concentration and high concentration retain product concentrates.
But the membrane separator worked under relying on above-mentioned patent A and patent B to make hypergravity condition has: 1, film trapped substance is not easily discharged, and film trapped substance concentration is not high, 2, rotary drum draw ratio is low, film charge weight is low, the shortcoming that equipment not easily amplifies.Although the hypergravity membrane separator relying on patent C to make can apply larger feed pressure, have film charge weight lower, equipment not easily amplifies, the shortcoming that single machine yield (treating capacity) is low.
(3) summary of the invention
The object of the invention is to overcome the deficiencies in the prior art, thus provide a kind of novel membrane separator, the present invention has: 1, film unit installation is high, and 2, unit treating capacity is large, 3, film retains the high advantage of concentrate concentration.
Technical scheme of the present invention is:
A kind of novel membrane separator, membrane module is arranged on the hypergravity membrane separator with rotary drum differential coaxial rotation on auger conveyor, by rotary drum (4), auger conveyor (6), membrane module (8), raw material input pipe (16), light liquid bubble discharge pipe (15) support (13), permeate collector (1), retain collector (2), differential mechanism (25), rotary drum driving wheel (12), auger conveyor driving wheel (19) form; Membrane module (8) is fixedly mounted on auger conveyor (6), and rotates with auger conveyor (6) and rotary drum (4) coaxial differential; Described auger conveyor (6) by forming auger conveyor left end cap (6-1), auger conveyor stage casing (6-6), auger conveyor membrane module gland (9) form, auger conveyor left end cap (6-1) is fixedly connected with auger conveyor stage casing (6-6) and jointly forms auger conveyor permeate and converge chamber (5), and auger conveyor stage casing (6-6) is fixedly connected with auger conveyor membrane module gland (9) and is fixed on auger conveyor (6) by membrane module (8).
And, described membrane module (8) is made up of membrane module upper cover (8-1), membrane module lower cover (8-8), film curtain shape assembly (8-16), and the symmetry axis (8-17) of film curtain shape assembly (8-16) outwards radiates layout along membrane module (8) diametric(al) and is fixedly connected with common component film assembly (8) with membrane module upper cover (8-1), membrane module lower cover (8-8).
And, described auger conveyor left end cap (6-1) bottom has auger conveyor left end helical form ridge (6-2), auger conveyor left end cap (6-1) is installed with permeate passing away and forms cover plate (20).
And, auger conveyor stage casing (6-6), the outer ancient piece of jade, round, flat and with a hole in its centre of its tubular has auger conveyor spiral (6-4), have auger conveyor trapped fluid and have permeate outlet (7) through hole (6-3), its left end, centripetal discharge pump impeller bearing (21) can be installed in middle part.
And, auger conveyor membrane module gland (9), it is fixedly connected with dividing plate (6-7), dividing plate (6-8), blade (6-11) is fixedly connected with between large base plate (6-9) and dividing plate (6-7), blade (6-5) is fixedly connected with between dividing plate (6-7) and dividing plate (6-8), large base plate (6-9) has material liquid membrane module hand-hole M, light liquid bubble chamber film module vent port G, its cylindrical portion (6-10) has material liquid hand-hole O, material liquid hand-hole N.
And, film curtain shape assembly (8-16) is by film bottom fixed head (8-2), film top fixed head (8-5), film (8-3), epoxy resin (8-4) forms, film (8-3) lower end is by epoxy resin (8-4) and film bottom fixed head (8-2), film top fixed head (8-5) is fixedly connected with, film (8-3) bottom film is communicated with permeate collection chamber (8-11) through side opening (8-10), film (8-3) top closure, film bottom fixed head (8-2) left and right sides has the left valley gutter of film bottom fixed head (8-14), the right valley gutter of fixed head at the bottom of film (8-15) jointly forms film and retains concentrate passing away S, upper fixing termination (8-6) on film top fixed head (8-5) and membrane module upper cover (8-1) are fixedly linked, lower fixing termination (8-7) and film bottom fixed head (8-2) on film top fixed head (8-5) are fixedly linked, the left and right sides on film top fixed head (8-5) has the left valley gutter of film top fixed head (8-12), the right valley gutter of film top fixed head (8-13) forms material liquid admission passage T.
And described film (8-3) adopts hollow-fibre membrane, capillary-pipe film, tubular membrane, Flat Membrane.
Advantage of the present invention is: 1, effectively improve the discharge condition that film retains concentrate.2, substantially increase the draw ratio of rotary drum (4), substantially increase film unit installation, 2, unit treating capacity is large, 3, that film retains concentrate concentration is high.
(4) accompanying drawing explanation
It is that centripetal discharge pump is discharged that Fig. 1 is through liquid from the mode that auger conveyor permeate convergence chamber (5) is discharged, the schematic diagram that the differential degree between rotary drum (4) and auger conveyor (6) is realized by auger conveyor driving wheel (19) input torque.
It is that centripetal discharge pump is discharged that Fig. 2 is through liquid from the mode that auger conveyor permeate convergence chamber (5) is discharged, the schematic diagram that the differential degree between rotary drum (4) and auger conveyor (6) is realized by material liquid, permeate, the pressure of trapped fluid, flow velocity, flow, the adjustment of inflow and outflow direction.
It is that centrifugal siphon is discharged that Fig. 3 is through liquid from auger conveyor permeate convergence chamber (5) discharge mode, the schematic diagram that the differential degree between rotary drum (4) and auger conveyor (6) is realized by auger conveyor driving wheel (19) input torque.
It is that centrifugal siphon is discharged that Fig. 4 is through liquid from the mode that auger conveyor permeate convergence chamber (5) is discharged, the schematic diagram that the differential degree between rotary drum (4) and auger conveyor (6) is realized by material liquid, permeate, the pressure of trapped fluid, flow velocity, flow, the adjustment of inflow and outflow direction.
It is that permeate outlet D negative-pressure ward is discharged that Fig. 5 is through liquid from the mode that auger conveyor permeate convergence chamber (5) is discharged, the schematic diagram that the differential degree between rotary drum (4) and auger conveyor (6) is realized by auger conveyor driving wheel (19) input torque.
It is that permeate outlet D negative-pressure ward is discharged that Fig. 6 is through liquid from the mode that auger conveyor permeate convergence chamber (5) is discharged, the schematic diagram that the differential degree between rotary drum (4) and auger conveyor (6) is realized by material liquid, permeate, the pressure of trapped fluid, flow velocity, flow, the adjustment of inflow and outflow direction.
It is that centripetal discharge pump is discharged that Fig. 7 is through liquid from the mode that auger conveyor permeate convergence chamber (5) is discharged, the schematic diagram that the differential degree between rotary drum (4) and auger conveyor (6) is realized by differential mechanism (25).
It is that centrifugal siphon is discharged that Fig. 8 is through liquid from the mode that auger conveyor permeate convergence chamber (5) is discharged, the schematic diagram that the differential degree between rotary drum (4) and auger conveyor (6) is realized by differential mechanism (25).
It is that permeate outlet D negative-pressure ward is discharged that Fig. 9 is through liquid from the mode that auger conveyor permeate convergence chamber (5) is discharged, the schematic diagram that the differential degree between rotary drum (4) and auger conveyor (6) is realized by differential mechanism (25).
Figure 10 is the profile of auger conveyor (6).
Figure 11 is the A-A profile of Figure 10.Express section configuration and the spread pattern of blade (6-5).
Figure 12 is the C direction view of Figure 10.Expression auger conveyor left end cap (6-1) retains concentrate and discharges the structure adopted.
Figure 13 is the D-D enlarged drawing of Figure 12.
Figure 14 is the profile of membrane module (8).
The profile of Figure 15 film curtain shape assembly (8-16) level.
Figure 16 is the vertical cross section of film curtain shape assembly (8-16).
Figure 17 is that film curtain shape assembly (8-16) horizontal direction in membrane module (8) arranges schematic diagram.
Detailed description of the invention
The problem that the technology of the present invention will solve is: the membrane separator worked under relying on above-mentioned patent A and patent B to make hypergravity condition exists: the problem that film trapped substance is not easily discharged, and cause thus: 1, film trapped substance concentration is not high, 2, rotary drum draw ratio is low, film charge weight is low, the shortcoming that equipment not easily amplifies.
Solve the problem that problem that film trapped substance not easily discharges not easily is discharged, most effective method is: the film of the high concentration that film (8-3) separation process is produced retains product along the direction of centrifugal force from the bottom of the film of the close rotary drum (4) of membrane module (8) and discharges, according to above-mentioned patent A, B, UF membrane principle under the hypergravity condition of C, permeate also must be discharged from the bottom of film, above-mentioned patent A, B, C permeate is discharged from the bottom of film, and the concentrate that retains of film is stayed in membrane module, because membrane module internal channel is narrow and small, the concentration of film trapped substance is high, viscosity is large, even also have particle, so be difficult to discharge in membrane module.
The technology of the present invention solves the problems referred to above.Below from Figure 14, Figure 15, Figure 16, Figure 17, Figure 10, Figure 11, Figure 12, Figure 13, composition graphs 1, Fig. 2, Fig. 3, Fig. 4, Fig. 5, Fig. 6 Fig. 7, Fig. 8, Fig. 9 etc., according to practical operation situation, elaborate the solution of the problems referred to above.
Material liquid enters rotary drum (4), through dividing plate 6-7 through material liquid input pipe (16) by outlet F in material liquid rotary drum by material liquid entrance A), passage Q between dividing plate (6-8) and dividing plate 6-7) and large base plate (6-9) between passage R enter membrane module (8) by material liquid membrane module hand-hole M.Passage Q, passage R are built with blade (6-5), and blade (6-5) can accelerate centrifugation, are separated the sediment produced and sink to rotary drum (4) bottom, promoted forward by auger conveyor (6) through initial centrifugation.
Be separated through initial centrifugation material liquid admission passage T that the material liquid that enters membrane module (8) formed with the right valley gutter of film top fixed head (8-13) through film top fixed head (8-5) the film left valley gutter of top fixed head (8-12) to enter in membrane module (8) and contact with film (8-3) UF membrane carried out under hypergravity condition.The left and right valley gutter that film top fixed head (8-5) both sides have, left and right tiltedly can avoid film top fixed head (8-5) laminate blocking material liquid pass through.
In membrane separating process under hypergravity condition, film transparent liquid enters film through side, enter permeate collection chamber (8-11) at film through side opening (8-10) place under the influence of centrifugal force to converge, converge chamber (5) in auger conveyor permeate collect through permeate collection chamber discharge port (8-9), permeate outlet (7).Because permeate arranges membrane penetration side under the influence of centrifugal force, greatly can reduce the net pressure of film through side like this, thus the net pressure greatly improving film both sides is poor, increases substantially membrane flux.This usefulness meaning in the application of the film hollow-fibre membrane minimum through wing passage is huge.
Film trapped substance is trapped within film surface and forms concentration polarization layer, the feed concentration of concentration polarization layer is much higher than the concentration of main body feed liquid, its density is higher than the density of main body feed liquid in most cases, get rid of to film bottom fixed head (8-2) under the influence of centrifugal force, film bottom fixed head (8-2) has the left valley gutter of film bottom fixed head (8-14), the right valley gutter of fixed head at the bottom of film (8-15) formed film retain concentrate passing away S discharge membrane module (8) by the auger conveyor trapped fluid that auger conveyor (6) has through hole (6-3) enter rotary drum (4) bottom, the sediment one being separated generation with initial centrifugation coexist auger conveyor (6) effect under through auger conveyor right-hand member concentrate passing away I, retain collector (2) trapped fluid outlet C to discharge.
Auger conveyor left end cap (6-1) has auger conveyor left end helical form ridge (6-2) to contribute to the discharge of film trapped substance.
Film bottom fixed head (8-2) has the right valley gutter of fixed head (8-15) at the bottom of the left valley gutter of film bottom fixed head (8-14), film, the left and right valley gutter that both sides have, left and right tiltedly can avoid film bottom fixed head (8-2) laminate blocking trapped fluid pass through.
The light liquid that passage Q centrifugation produces, bubble enter light liquid bubble discharge pipe (15) through light liquid bubble outlet V, the light liquid that passage R centrifugation produces, bubble enter light liquid bubble discharge pipe (15) through light liquid bubble outlet U, and the light liquid bubble produced through hypergravity UF membrane in membrane module (8) enters light liquid bubble discharge pipe (15) through light liquid bubble chamber film module vent port G.The light liquid bubble entering light liquid bubble discharge pipe (15) is discharged by light liquid bubble outlet B.
Gather auger conveyor permeate converge chamber (5) permeate, by three kinds of modes through permeate tap K, permeate collector (1) collect after, discharge through permeate outlet D.Three kinds of modes are respectively: 1, centripetal discharge pump is discharged, and 2, centrifugal siphon, 3, permeate outlet D negative-pressure ward.Now be described below respectively:
1, centripetal discharge pump is discharged
Centripetal discharge pump impeller (22) is installed by centripetal discharge pump impeller bearing (21) in auger conveyor stage casing (6-6), centripetal discharge pump impeller (22) is fixedly connected with centripetal discharge pump impeller shaft (23), when support (13) is static relatively for centripetal discharge pump impeller shaft (23), the permeate of centripetal discharge pump impeller (22) opposed helical conveyer permeate convergence chamber (5) has higher speed, and permeate relies on the kinetic energy of self to discharge.When not needing discharge permeate and utilize through liquid film back flush, centripetal discharge pump impeller (22) can rotate with auger conveyor (6), and does not increase energy ezpenditure.
2, centrifugal siphon is discharged
Auger conveyor left end cap (6-1) and permeate passing away form cover plate (20) and are fixedly connected with, form permeate passing away H, under siphonage, permeate is collected at permeate collector (1), discharges through permeate outlet D.
3, permeate outlet D negative-pressure ward is discharged
Apply negative pressure permeate at permeate outlet D to discharge through permeate outlet D through permeate passing away H permeate collector (1).
No matter be through the centrifugal siphon of liquid to discharge or permeate outlet D negative-pressure ward is discharged auger conveyor permeate and converged chamber (5) and all will keep normal pressure, gas turnover device (26) can ensure freeing in and out of auger conveyor permeate convergence chamber (5) intracavity gas.
Auger conveyor (6) and the speed difference between the membrane module (8) be fixedly mounted on auger conveyor (6) and rotary drum (4) realize by three kinds of modes:
1, realized by differential mechanism
2, realized by auger conveyor driving wheel (19) input torque
3, realized by the pressure of material liquid, permeate, trapped fluid, flow velocity, flow, inflow and the adjustment of outflow direction
Three kinds of permeate are discharged mode and three kinds of auger conveyors (6) and the membrane module (8) that is fixedly mounted on auger conveyor (6) and are combined with rotary drum (4) speed difference implementation and can realize nine kinds of types, are specially:
1, it is that centripetal discharge pump is discharged that the permeate shown in Fig. 1 converges the mode of discharging in chamber (5) from auger conveyor permeate, and the differential degree between rotary drum (4) and auger conveyor (6) is by the hypergravity membrane separator of auger conveyor driving wheel (19) input torque
2, it is that centripetal discharge pump is discharged that the permeate shown in Fig. 2 converges the mode of discharging in chamber (5) from auger conveyor permeate, the hypergravity membrane separator that the differential degree between rotary drum (4) and auger conveyor (6) is realized by material liquid, permeate, the pressure of trapped fluid, flow velocity, flow, the adjustment of inflow and outflow direction.
3, it is that centrifugal siphon is discharged that the permeate shown in Fig. 3 converges chamber (5) discharge mode from auger conveyor permeate, the hypergravity membrane separator that the differential degree between rotary drum (4) and auger conveyor (6) is realized by auger conveyor driving wheel (19) input torque.
4, it is that centrifugal siphon is discharged that the permeate shown in Fig. 4 converges the mode of discharging in chamber (5) from auger conveyor permeate, the hypergravity membrane separator that the differential degree between rotary drum (4) and auger conveyor (6) is realized by material liquid, permeate, the pressure of trapped fluid, flow velocity, flow, the adjustment of inflow and outflow direction.
5, it is that permeate outlet D negative-pressure ward is discharged that the permeate shown in Fig. 5 converges the mode of discharging in chamber (5) from auger conveyor permeate, the hypergravity membrane separator that the differential degree between rotary drum (4) and auger conveyor (6) is realized by auger conveyor driving wheel (19) input torque.
6, it is that permeate outlet D negative-pressure ward is discharged that the permeate shown in Fig. 6 converges the mode of discharging in chamber (5) from auger conveyor permeate, the hypergravity membrane separator that the differential degree between rotary drum (4) and auger conveyor (6) is realized by material liquid, permeate, the pressure of trapped fluid, flow velocity, flow, the adjustment of inflow and outflow direction.
7, it is that centripetal discharge pump is discharged that the permeate shown in Fig. 7 converges the mode of discharging in chamber (5) from auger conveyor permeate, the hypergravity membrane separator that the differential degree between rotary drum (4) and auger conveyor (6) is realized by differential mechanism (25).
8, it is that centrifugal siphon is discharged that the permeate shown in Fig. 8 converges the mode of discharging in chamber (5) from auger conveyor permeate, the hypergravity membrane separator that the differential degree between rotary drum (4) and auger conveyor (6) is realized by differential mechanism (25).
9, it is that permeate outlet D negative-pressure ward is discharged that the permeate shown in Fig. 9 converges the mode of discharging in chamber (5) from auger conveyor permeate, the hypergravity membrane separator that the differential degree between rotary drum (4) and auger conveyor (6) is realized by differential mechanism (25).
The kind of drive and the general structure of above-mentioned type are specially:
Rotary drum (4) passes through to rouse the end bearing (11) that turns right, drum turns left, and end bearing (3) is arranged on support (13), and rotary drum driving wheel (12) drives rotary drum (4) to rotate.Auger conveyor (6) is arranged on rotary drum (4) by auger conveyor left end bearing (17), auger conveyor right-hand member bearing (18).Because the installation of auger conveyor (6) can realize rotary drum (4), auger conveyor (6) coaxial rotation with the axis location of rotary drum (4) by auger conveyor left end bearing (17), auger conveyor right-hand member bearing (18) connection.
Material liquid input pipe bracket (14) is fixed for the location of material liquid input pipe (16), and ensures that material liquid input pipe (16) is placed on the center line of rotary drum (4).
The above analysis, instant invention overcomes the membrane separator worked under the above-mentioned patent A of existing support and patent B make hypergravity condition had: 1, film trapped substance is not easily discharged, and film trapped substance concentration is not high, 2, rotary drum draw ratio is low, film charge weight is low, the shortcoming that equipment not easily amplifies.Although the hypergravity membrane separator relying on patent C to make can apply larger feed pressure, have film charge weight lower, equipment not easily amplifies, the shortcoming that single machine yield (treating capacity) is low.The present invention has: 1, effectively improve the discharge condition that film retains concentrate.2, substantially increase the draw ratio of rotary drum (4), substantially increase film unit installation, 2, unit treating capacity is large, 3, film retains concentrate concentration advantages of higher.There is good feasibility, the separation in the fields such as chemical industry, food, pharmacy, purifying, the process procedure such as concentrated can be widely used in.
Claims (7)
1. a novel membrane separator, it is characterized in that: membrane module is arranged on the hypergravity membrane separator with rotary drum differential coaxial rotation on auger conveyor, by rotary drum (4), auger conveyor (6), membrane module (8), raw material input pipe (16), light liquid bubble discharge pipe (15) support (13), permeate collector (1), retain collector (2), differential mechanism (25), rotary drum driving wheel (12), auger conveyor driving wheel (19) form; Membrane module (8) is fixedly mounted on auger conveyor (6), and rotates with auger conveyor (6) and rotary drum (4) coaxial differential; Described auger conveyor (6) by forming auger conveyor left end cap (6-1), auger conveyor stage casing (6-6), auger conveyor membrane module gland (9) form, auger conveyor left end cap (6-1) is fixedly connected with auger conveyor stage casing (6-6) and jointly forms auger conveyor permeate and converge chamber (5), and auger conveyor stage casing (6-6) is fixedly connected with auger conveyor membrane module gland (9) and is fixed on auger conveyor (6) by membrane module (8).
2. a kind of novel membrane separator according to claim 1, it is characterized in that: described membrane module (8) is made up of membrane module upper cover (8-1), membrane module lower cover (8-8), film curtain shape assembly (8-16), the symmetry axis (8-17) of film curtain shape assembly (8-16) outwards radiates layout along membrane module (8) diametric(al) and is fixedly connected with common component film assembly (8) with membrane module upper cover (8-1), membrane module lower cover (8-8).
3. a kind of novel membrane separator according to claim 1, it is characterized in that: described auger conveyor left end cap (6-1) bottom has auger conveyor left end helical form ridge (6-2), auger conveyor left end cap (6-1) is installed with permeate passing away and forms cover plate (20).
4. a kind of novel membrane separator according to claim 1, it is characterized in that: auger conveyor stage casing (6-6), the outer ancient piece of jade, round, flat and with a hole in its centre of its tubular has auger conveyor spiral (6-4), have auger conveyor trapped fluid and have permeate outlet (7) through hole (6-3), its left end, centripetal discharge pump impeller bearing (21) can be installed in middle part.
5. a kind of novel membrane separator according to claim 1, it is characterized in that: auger conveyor membrane module gland (9), it is fixedly connected with dividing plate (6-7), dividing plate (6-8), blade (6-11) is fixedly connected with between large base plate (6-9) and dividing plate (6-7), blade (6-5) is fixedly connected with between dividing plate (6-7) and dividing plate (6-8), large base plate (6-9) has material liquid membrane module hand-hole M, light liquid bubble chamber film module vent port G, its cylindrical portion (6-10) has material liquid hand-hole O, material liquid hand-hole N.
6. a kind of novel membrane separator according to claim 2, it is characterized in that: film curtain shape assembly (8-16) is by film bottom fixed head (8-2), film top fixed head (8-5), film (8-3), epoxy resin (8-4) forms, film (8-3) lower end is by epoxy resin (8-4) and film bottom fixed head (8-2), film top fixed head (8-5) is fixedly connected with, film (8-3) bottom film is communicated with permeate collection chamber (8-11) through side opening (8-10), film (8-3) top closure, film bottom fixed head (8-2) left and right sides has the left valley gutter of film bottom fixed head (8-14), the right valley gutter of fixed head at the bottom of film (8-15) jointly forms film and retains concentrate passing away S, upper fixing termination (8-6) on film top fixed head (8-5) and membrane module upper cover (8-1) are fixedly linked, lower fixing termination (8-7) and film bottom fixed head (8-2) on film top fixed head (8-5) are fixedly linked, the left and right sides on film top fixed head (8-5) has the left valley gutter of film top fixed head (8-12), the right valley gutter of film top fixed head (8-13) forms material liquid admission passage T.
7. a kind of novel membrane separator according to claim 6, is characterized in that: described film (8-3) adopts hollow-fibre membrane, capillary-pipe film, tubular membrane, Flat Membrane.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420036967.0U CN204429105U (en) | 2014-01-16 | 2014-01-16 | A kind of novel membrane separator |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201420036967.0U CN204429105U (en) | 2014-01-16 | 2014-01-16 | A kind of novel membrane separator |
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| CN204429105U true CN204429105U (en) | 2015-07-01 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104785115A (en) * | 2014-01-16 | 2015-07-22 | 大连盛仁能源科技发展有限公司 | Hypergravity membrane separator with membrane assembly arranged on screw conveyor and coaxially rotating with rotary drum in differential velocity manner |
| CN109045952A (en) * | 2018-07-03 | 2018-12-21 | 华南理工大学 | A kind of novel gas-liquid membrane contactor |
-
2014
- 2014-01-16 CN CN201420036967.0U patent/CN204429105U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104785115A (en) * | 2014-01-16 | 2015-07-22 | 大连盛仁能源科技发展有限公司 | Hypergravity membrane separator with membrane assembly arranged on screw conveyor and coaxially rotating with rotary drum in differential velocity manner |
| CN104785115B (en) * | 2014-01-16 | 2018-02-13 | 周志杰 | Membrane module is arranged on the hypergravity membrane separator rotated coaxially on auger conveyor with rotary drum differential |
| CN109045952A (en) * | 2018-07-03 | 2018-12-21 | 华南理工大学 | A kind of novel gas-liquid membrane contactor |
| CN109045952B (en) * | 2018-07-03 | 2020-11-27 | 华南理工大学 | Novel gas-liquid membrane contactor |
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Effective date of registration: 20160706 Address after: 301800 Guangzhou Road, Tanggu District, Shiyan, No. 3, No. 4, building No. 102 Patentee after: Zhou Zhijie Address before: 116600 bonded Building No. 1, Dongting Road, Dalian Free Trade Zone, Liaoning, 733F-18 Patentee before: Dalian Sheng Ren energy science and technology Development Co., Ltd |
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Granted publication date: 20150701 Effective date of abandoning: 20180213 |