CN1162929A - Method and system for extracting a solute from a fluid using dense gas and a porous membrane - Google Patents
Method and system for extracting a solute from a fluid using dense gas and a porous membrane Download PDFInfo
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- CN1162929A CN1162929A CN 95196162 CN95196162A CN1162929A CN 1162929 A CN1162929 A CN 1162929A CN 95196162 CN95196162 CN 95196162 CN 95196162 A CN95196162 A CN 95196162A CN 1162929 A CN1162929 A CN 1162929A
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
A method and system (10) for extracting a solute from a fluid or a dense gas may include a dense gas supply (12) and a gas supply line (48) for delivering a dense gas to a pressure equalization chamber (122) and to a pressurizable module (16) containing a bundle of porous hollow fibers. The system (10) also may include a fluid supply (14) and fluid supply line (40) for delivering a fluid to the chamber (122) and to the module (16). The chamber (122) includes a floating diaphragm (26) and serves to substantially equalize the pressure of the fluid and dense gas so that the pressure on both sides of the membranes in the module (16) is essentially the same. At least one of the fluid and dense gas contains a solute to be extracted, while the other one serves as an extracting medium. Solute extraction is driven by the concentration gradient of the solute across the membrane.
Description
Invention field
The present invention relates to fluid extraction, more specifically, relate to and use the hollow fiber film assembly extract solutes, wherein at least a fluid is a dense gas.
Background of invention
One of solute method of extraction is traditional liquid-liquid extraction method based on balance, uses contact device as the filler in extraction tower.An example of this kind extracting process is described in the United States Patent (USP) 3,477,856 of Schultz.This `856 patent disclosure a kind of method of from the material that contains spices, separating spices, relate to and use extraction tower to extract spices with liquid CO 2.In this exemplary systems, the aqueous solution is introduced cat head.Simultaneously, liquid CO
2From tower, enter than low spot.Because the density difference, the aqueous solution moves down, and liquid CO
2In tower, move up liquid CO
2Form solution with organic solute.Then, this liquid CO
2-spices shifts out from the top that extracts molten device, carbon dioxide evaporation and isolate organic solute.
One of restriction of traditional extraction based on balance is: because system is based on diffusion with depend on gravity, so must use the solvent of different densities.Another restriction of traditional liquid-liquid extraction is to form stable emulsion, will not extract in the case.In addition, the contact area in the extractor may reduce because of channel.Because two alternate mutual dispersions, in tower, will be tending towards forming the path of resistance minimum and flow along it.If filler is not tight, then may damage the diffusion of two-phase, thereby the infringement mass-transfer efficiency.
The nearer development of in the liquid-liquid extraction another is to use the microporous hollow fiber film.In film abstractor, a lot of fibers formation fibre bundle that is packaged together is in the shell of packing into.Typically, a kind of liquid is by the chamber of fiber, and another kind of liquid passes through along the shell-side of fiber, and solute strides across the transmission of porous fibre film.Because membrane extraction is no scatter operation, so system does not need the white density difference.In addition, stablized two alternate interfaces because of film, the potentiality that form emulsion reduce.Seibert，A.F.，et?al.，“Hydraulics?and?Mass?Transfer?Efficiency?ofa?Commercial-Scale?Membrane?Extractor”，Separation?Science?and?Technology，28(1-3)，pp.343-359(1993)。
Yet the extraction of finishing with hollow fiber film assembly has only obtained limited success.The mass-transfer efficiency of these assemblies is lower than desired, mainly due to a large amount of shell-side fiber bypasses (the same).The bypass of shell-side fiber be in the finger assembly most of fiber by a kind of phenomenon of shell fluid bypass.Thereby, only utilized the sub-fraction of fiber total surface area, make that the efficient of assembly is low relatively.This phenomenon can make the 70%-90% of film surface area invalid (the same).
Some assemblies are attempted to reduce this bypass problem by setting up baffle plate to force shell fluid to contact more film surface area in assembly.Yet this technology can not solve shell-side fiber bypass problem, has also increased the production cost of assembly.Therefore need a kind of method and system, wherein reduce the bypass of shell-side fiber and improve mass-transfer efficiency with porous hollow fiber membrane extract solutes from fluid.
In view of the general description of above-mentioned background and prior art, need improve the method and apparatus of extract solutes.
Summary of the invention
The present invention relates to a kind of from fluid or dense gas the method for extract solutes, and be used to carry out the system of the inventive method.This method is used the perforated membrane that has relative both sides in adding the assembly of depressing, and this film is nonselective to solute, and as the barrier layer between fluid and the dense gas.Described dense gas adds assembly in a side of film, and described fluid adds assembly at the opposite side of film.Described fluid and dense gas contain one of at least the solute that remains to be extracted, and be another kind of as spe medium.The density of described dense gas is at least about 0.5g/cc, thereby and in described fluid basically unmixing two-phase is provided.When carrying out described method, the pressure of film both sides is substantially the same in the assembly, is driven by the concentration gradient of solute between fluid and the dense gas and strides across the membrane extraction solute.As needs, the opposite side that described method also can be included in film provides before the step of fluid the step with the described film of described dense gas drying.
Preferably, described dense gas passes through in the relative both sides of film with fluid, and more preferably, described dense gas passes through in the relative both sides of film adverse current with fluid.When static system reached balance rapidly, fluid that passes through and dense gas kept concentration gradient in the whole time, and counter-current flow increases described gradient.
Described dense gas can be selected from various gas, preferably carbon dioxide.Except that cheap and easy to get, carbon dioxide is also nontoxic, nonflammable, relative inertness and do not stay remnants in extracted products.The example of other dense gas comprises methane, ethane, propane, butane, iso-butane, ethene, propylene, tetrafluoromethane, F-22, nitrous oxide, sulfur hexafluoride, ammonia, chloromethane and fluorohydrocarbon (hydroflurocarbon).Described fluorohydrocarbon comprises methane, ethane and the propane of partly fluoridizing, as fluomethane, fluoroform, HFC-134a (being commonly referred to HFC-134a), 1,1,1,2,3,3,3-heptafluoro-propane (being commonly referred to P227), HFC-143a and HFC-125, and composition thereof.
Described fluid can be any different fluid, for example fruit juice, jam, dish juice, puree, emulsion oil-in-water, living cells fermentation broth and enzyme-added meat soup.As needs, described fluid can be second dense gas of density at least about 0.5g/cc.The solute that is extracted can be any solute that some solubility are all arranged in described fluid and dense gas, typically spices, essence, medicine and sting the metal that closes.
Described method is typically carried out under the following conditions: temperature approximately-10 ℃ to about 200 ℃ scope, pressure is at about 2bar extremely in the scope of about 700bar.This temperature range consists essentially of all moisture biosystems, and this pressure limit comprises the operating pressure of analysis and commercial scale system.
But the system according to principle of the invention extract solutes from fluid and dense gas comprises dense gas source of supply, fluid provider and the pressure-applying unit described in above method, and described assembly operationally links to each other with fluid provider with described dense gas.Described system also can comprise and being used in the relative both sides of film by the device of dense gas and fluid, and is used for before described dense gas and fluid enter assembly the device of the pressure of balance dense gas and fluid substantially.As needs, described pressure equaliser can comprise and is used for preventing substantially in pressure-applying unit the device of the extraction of the solute in described pressure equaliser before the extraction.In addition, described system can comprise the device that is used to monitor described dense gas, fluid and solute transmission capacity, and is used for making described gas and fluid return the device of described dense gas and fluid provider after the solute extraction.
About perforated membrane, preferred described film is hollow-fibre membrane or hollow fiber membrane bundle.Use hollow-fibre membrane can make to the contact area height in the locking assembly.As needs, can use the film of other type, as the membrane module of spiral winding or the flat sheet membrane in the sheet frame.Film itself can be made by any different material, comprises for example polypropylene, polyethylene, polytetrafluoroethylene (PTFE), polyvinylidene fluoride, nylon, polysulfonates, Merlon, polyester, cellulose acetate, celluloid, cellulose and acrylic acid.
Described hole is preferably substantial symmetry so that described film be subjected to the film surface the aciculiform hole defect influence minimum.The diameter in described hole preferably about 0.001 micron to about 1 micron scope, more preferably from about 0.1 micron to about 0.2 micron.0.1 micron to about 0.2 micron scope typically provides the optimum balance of flow behavior and symmetrical holes structure.The thickness of film preferably about 0.005 millimeter to about 3 millimeters scope, more preferably from about 0.2 millimeter to about 0.6 milli.These scopes provide the better balance between the flow behavior of film-strength and integrality and requirement.
One of advantage of the inventive method and system is to improve mass-transfer efficiency by reducing the bypass of shell-side fiber.Opposite with traditional liquid, the low diffusion coefficient of the general viscosity of dense gas is higher.These characteristics can be distributed in dense gas and permeate much more fiber surface in assembly, thereby improve mass-transfer efficiency.
Further advantage be beyond thought dense gas can be before adding fluid dry perforated membrane, thereby when the adding fluid the wetting potentiality minimum of film, and improve mass-transfer efficiency.
Another advantage is that dense gas can pass through assembly with the speed faster than traditional liquid solvent.Flow velocity is the key factor in the transmission efficiency, but because the shell-side fiber bypass of reverse frictional force and increase has limited the flow velocity of traditional liquid.Because the friction that dense gas produces in assembly is little, thus can higher speed pass through, and improve transmission efficiency.
Further advantage is dense gas can be full of film during extracting hole, thereby reduces the boundary layer thickness that extraction takes place, and improves mass-transfer efficiency.
Another advantage is that dense gas causes the hole of film not by fluid wets when fluid enters assembly again.Therefore, do not replace dense gas in the hole by assembly in the speed that the fluid of the film side opposite with dense gas can be higher, thereby improve mass-transfer efficiency.
Will be further understood that these and other advantage and benefit with reference to following accompanying drawing and description:
The accompanying drawing summary
Fig. 1 is the schematic flow diagram that is used for from a preferred embodiment of the system of the present invention of fluid extract solutes; Black arrow is represented highly dense air-flow, and white arrow is represented fluid stream;
Fig. 2 is the perspective illustration of part section of the porous hollow fiber membrane assembly of Fig. 1 system;
Fig. 3 is the schematic flow diagram of another preferred embodiment, and black arrow is represented highly dense air-flow, and white arrow is represented fluid stream; With
Fig. 4 is the schematic flow diagram of the system that is used to test among the embodiment, and black arrow is represented highly dense air-flow, and white arrow is represented fluid stream.
DESCRIPTION OF THE PREFERRED
Fig. 1 illustrates according to the present invention and is used for from the system of fluid extract solutes.System 10 comprises that dense gas supply source 12 and fluid supply source 14 are used to the pressure-applying unit 16 that the solute extraction takes place that dense gas and fluid are provided.System 10 also comprises U type pipe separator 18, and this separator operationally links to each other with pressure-applying unit 16, is used for reclaiming the solute that is extracted from spe medium.
Dense gas supply source 12 comprises gas reservoir 20 and volume control device 22.Gas reservoir 20 is that the calibrating gas storage tank is as being full of the CO that is forced into 1000psi
2Jar.Volume control device 22 is applicable to that for a whole set of pumping system of pressure, temperature and flow-control is arranged gas is changed into density to be controlled at least about the dense gas of 0.5g/cc and for the dense gas that enters system's 10 remainders provides total flow.
But fluid supply source 14 is contained in the pressurized reservoir 24 of sealable opening (not shown).Holder 24 can be opened to add additional fluid and/or solute.In this embodiment, but pressurized reservoir 24 also as the device of the pressure of balance dense gas substantially and fluid, and since holder 24 be positioned at before the assembly 16, so dense gas will have identical substantially pressure with fluid during by assembly 16.But pressurized reservoir 24 also comprises the unsteady barrier film 26 between fluid and dense gas.Barrier film 26 has the diameter approaching with the internal diameter of holder 24, but prevents any solute extraction in pressurized reservoir 24 substantially.Because described solute is all dissolvings in described fluid and dense gas, so before assembly 16 in, extracting, but some extractions may take place in the border that strides across two-phase in pressurized reservoir 24.Therefore, extract, use the barrier film 26 that floats for eliminating basically in holder 24.
But pressure-applying unit 16 is illustrated in greater detail among Fig. 2.The assembly 16 that illustrates in simplified form is included in the fibre bundle 30 that axially extended four hollow-fibre membranes 28 are formed in the assembly 16.Yet fibre bundle 30 comprises many films 28 in the industrial implementation scheme.The end of every hollow-fibre membrane 28 is all in the end-blocking spare 31 of assembly 16 opposite ends.Fibre bundle 30 is surrounded by shell 32, an end of each end-blocking spare 31 capsuls 32.Shell 32 is contained in again in the shell 34, with Buna N O type ring 56 shell 32 is fixed in the shell 34.
Shell 34 is typically made by stainless steel, also can use other metal or the material that can operate under system pressure as needs.Film 28, end-blocking spare 31 and shell 32 are typically made by polypropylene, but also can make, as polyethylene, polytetrafluoroethylene (PTFE), polyvinylidene fluoride, nylon, polysulfonates, Merlon, polyester, cellulose acetate, celluloid, cellulose or acrylic acid by any other material.
Membrane material can be selected based on required hydrophobic or hydrophily.For example, if aqueous fluid then may need hydrophobic film 28 by assembly 16.Hydrophobic film 28 repels aqueous fluid outside fenestra, makes fluid not replace dense gas in the hole by assembly 16 with higher rate.On the other hand, if use oil or other hydrophobic fluid, then because of identical former thereby need hydrophilic membrane 28.In both cases, all can improve mass-transfer efficiency.
U type pipe separator 18 links to each other with dense gas outlet 42 through dense gas export pipeline 52.When the dense gas that is loaded with solute when the separator 18, gas expands and the solute that is extracted is recovered in the separator 18.As needs, also can be made into solute is extracted to system in the fluid from dense gas.In the case, the product retracting device will link to each other with fluid issuing 38 through fluid output tube line 54, thereby reclaim solute with any known separation techniques as distillation etc. from fluid.
Extracting system shown in Figure 1 also comprises other part.Fluid pump 70 is positioned on the fluid supply tube line 50, but is used for actively making fluid to pass through pressure-applying unit 16.In addition, pump 70 can be set under the different speed, thereby the user can control the speed of fresh fluid by assembly 16.System 10 comprises that several volume control devices are used to control by before the assembly 16 and afterwards fluid and dense gas.Dense gas inlet valve 72 control dense gas enter dense gas supply line 48, but are positioned at the flow of fluid intake valve 74 controls of pressurized reservoir 24 bottoms from the fluid of fluid supply source 14.Dense gas flow by system 10 is also controlled by dense gas flow control valve 76, and valve 76 is on the dense gas export pipeline 52 between dense gas outlet 42 and the U type pipe separator 18.
Extraction with light absorption detecting instrument 90 measurement solutes.Detector 90 links to each other with fluid output tube line 52,54 with dense gas by multiposition valve 96, makes the user optionally make dense gas or fluid sample by detector 90.In addition, carrier fluid pump 94 pumping carrier fluids enter detector 90 by carrier fluid pipeline 92 and multiposition valve 96.Carrier fluid can be used for diluting dense gas or the fluid that detected instrument 90 is measured, and it should be a kind of carrier fluid that does not absorb the ultraviolet ray and can dissolve described fluid and dense gas solvent.For example, when making water and highly dense CO2, the carrier fluid of methyl alcohol for being fit to.
The fluid that is not sampled to light absorption detector 90 moves to fluid return line 98 through multiposition valve 96, but and flows back to pressurized reservoir 24.Simultaneously, unsampled dense gas drains in the atmosphere under environmental pressure by after the dense gas volumetric expansion device 100 that links to each other with dense gas export pipeline 52.As needs, can make system 10 be suitable for described gas is used for pressurizeing and utilization again through gas return line (not shown) circulating reflux amount control device 22 from dense gas export pipeline 52 again.
In addition, system 10 has the pressure that links to each other with fluid output tube line 54 with dense gas supply line 48 to keep pipeline 102.This pipeline 102 has a check valve 104, for the pressure of keeping in the system 10 provides an additional means.Check valve 106 in the fluid output tube line 54 also helps steady pressure.In addition, also comprise mass flow sensor 112 and heat exchanger 110 along the fluid supply tube line 50 that causes assembly 16.
In the operation, but the fluid that will contain the solute that will be extracted is put into pressurized reservoir 24, seals described holder then.Dried, hollow tunica fibrosa 28 is opened dense gas inlet valve 72 lentamente and is given system 10 pressurizations, this during starts dense gas flow control valve 76 close.After this pressurization steps, the chamber side 44 of hollow-fiber module 16 and shell-side 46 contain the dense gas under the selected operation pressure.But dense gas also is full of the upper space of pressurized reservoir 24, thus the pressure of balance sysmte 10 interior dense gas and fluid.
Then, the required stroke of opening fluid intake valve 74 and selecting to set on pump 70 pumps into fluid in the assembly 16.Simultaneously, open dense gas flow control valve 76, so that the dense gas flow as the requirement shown on the dense gas flowmeter 86 to be provided.
At this moment, fluid passes through assembly 16 in a side of porous hollow fiber membrane 28, and dense gas passes through assembly 16 in the opposite side adverse current of film 28.Preferably, fluid passes through in chamber side 44, and dense gas passes through at shell-side 46.Yet, otherwise also can make each supply and the position opposite of export pipeline and.In assembly 16, concentration gradient drives the solute extraction.But since pressurized reservoir 24 basically balance the pressure between dense gas and the fluid, so it is very little to stride across the pressure reduction of film 28.
As shown in Figure 1, the dense gas that is loaded with solute enters dense gas export pipeline 52 by dense gas outlet 42.Described dense gas continues reclaim solute at this from described gas, and gas to be disposed in the atmosphere by multiposition valve 96 and dense gas flow control valve 76 to U type pipe separators 18.Simultaneously, the fluid of removing solute enters fluid output tube line 54 by fluid issuing 38, and continues by fluid sampling valve 78 and multiposition valve 96.But described then fluid flows back to pressurized reservoir 24 through fluid return line 98.The user also can make dense gas or fluid sample measure the solute extraction by light absorption detector 90.As needs, described system can be configured to from dense gas extract solutes to fluid again.In the case, longshore current body export pipeline 54 is provided with product retracting device such as distillery etc., thereby can reclaim solute from fluid.
Shown in Fig. 3 according to another preferred embodiment of the present invention.This embodiment is a continuous system, and wherein dense gas is in by retrieval system after the assembly.This substituting embodiment is similar to the principle of Fig. 1 system, and difference is very little.The main distinction is to have increased gas return line 126, and gas is sent back to the gas flow control device 22 from solute retracting device 120, at this described gas is changed into dense gas again, continues to use in system.In addition, fluid supply source 14 separates with the pressure balance part.Fluid supply source 14 has a sealable filling mouthful (not shown) and links to each other with the fluid-flow control apparatus 118 of giving pressurized with fluid.Pressure fluid and dense gas feed fluid supply tube line 50 and dense gas supply lines 48 from its volume control device 118,22 separately respectively, by their pressure of the pressure equalizing chamber that links to each other with these two supply lines 122 balance basically.There is a barrier film 26 that floats chamber 122, and is similar to the barrier film among Fig. 1.Yet different with system 10 shown in Figure 1, this embodiment does not have fluid pump 70.In addition, fluid flow control valve 124 makes user's controllable flow body flow into the fluid line 98 after the extraction and the speed of the fluid collector 128 after the extraction from fluid output tube line 54.As needs, this embodiment also can comprise above-mentioned various control and monitoring device.
Embodiment
This embodiment illustrates the method according to this invention and system, makes spe medium with highly dense CO2 and extract caffeine from water.The used extracting system of present embodiment is shown among Fig. 4, is a kind of reduced form of above-mentioned system illustrated in fig. 1.
With containing the CO that pressure is 1000psi
2But calibrating gas jar 20 and 300cc pressurized reservoir 24 extract.Pump 70 has the discharge opeing positive displacement pump of saphire piston for the LDC board, and 100% stroke down-off is 7.5cc/min.Holder 24 used materials are No. 316 stainless steels, and the pipe that connects each element is 1/8 " stainless steel.
But pressure-applying unit 16 used in the present embodiment is made of polypropylene and stainless steel.Polypropylene is used to do porous hollow fiber membrane 28, shell 32 and end-blocking spare 31.The shell that surrounds described shell is 0.109 by wall thickness, and " No. 316 stainless 1 " pipe is made, and with Buna N O type ring 56 described shell is fixed in this shell.
The length of polypropylene shell 32 is 16 ", external diameter is 0.7/8 ".Contain three porous hollow fiber membranes 28 in the assembly, the length of every film is 16 ".In addition, the internal diameter of every film is 0.6mm, and external diameter is 1.0mm, and hole dimension is that 0.2 μ and porosity are 75%.The total surface area that three films 28 are provided is 40cm
2The hold-up volume of assembly is 0.33ml to liquid, to highly dense CO
2Be 5.1ml.Flowmeter 86 is a spinner flowmeter, and accumulator 88 is traditional flow summer/dried taking temperature.
The present embodiment system for use in carrying also comprises some annexes.Dense gas supply line 48 has a humidifier 134, is used for the dense gas with the water saturation input.Humidifier 134 is for being equipped with the 100cc cylinder of 3mm glass marble and 15cc water.Dense gas export pipeline 52 comprises thermal expansion valve 130, and it heated dense gas before gas feeds U type pipe separator 18.Fluid output tube line 54 comprises fluid sampling pipeline 138, and fluid sampling valve 136 is arranged, and the user can be taken out by the fluid sample after the assembly 16.In addition, fluid return line 98 comprises a check valve 132.
Carry out ten tests with the system shown in Fig. 4.Test at every turn and under specific pressure and temperature, carry out certain hour, concrete CO
2The flow and the aqueous solution (aqueous solution of caffeine) flow is as shown in table 1.In each test, but the distilled water solution of the caffeine that one of 150g percentage is heavy is sealed in the pressurized reservoir 24.Expansion valve 130 is in the closed position, opens dense gas inlet valve 72 lentamente, pressurizes to whole system.After system's pressurization, the chamber side of assembly 16 and shell-side 44,46 all contain the highly dense CO under the test pressure
2Highly dense CO
2But also be full of the upper space of pressurized reservoir 24, thereby the highly dense CO of balance basically
2Pressure with the aqueous solution.
Time is when being zero, with 30% or 100% stroke starting fluid pump 70, corresponding to 2.25 shown in table 1 or 7.5cc/min.Simultaneously, open thermal expansion valve 130, to provide as the selected CO shown on the flowmeter 86
2Flow.The selected extraction time cycle (as shown in table 1) stops dense gas and fluid stream when finishing.Used CO
2Total amount is illustrating with liter on accumulator 88 under one atmospheric pressure and the environment temperature.This volume is converted into CO
2The gram number, be shown in Table 1.
In all tests, temperature is environment temperature, thereby CO
2For subcritical.Yet, under used pressure 1400,3000 and 4000psi, CO
2Density be respectively about 0.8,0.9 and 0.95g/cc.In test 8,9 and 10, highly dense CO
2During by humidifier 134 by 0.1-0.2%H
2O is saturated.
The caffeine aqueous solution of the material that reclaims in the U type pipe separator 18 for concentrating.With acetone rinsing separator 18, and wash residue in the thermal expansion valve 130 with acetone.After the evaporation, the weight of weighing crystallization caffeine is 0.1mg in dish, and the amount that reclaims caffeine in each test is shown in Table 1.
Table 1 test data
* CO
2By 0.1-0.2%H
2O is saturated.
| Tested number | ??1 | ??2 | ??3 | ??4 | ??5 | ??6 | ??7 | ??8 | ??9 | ??10 |
| Pressure p si | ??1400 | ??3000 | ??3000 | ??1400 | ??1400 | ??4000 | ??3000 | ??3000 | ??3000 | ??3000 |
| Temperature ℃ | ??25 | ??23-24 | ??24 | ??24-25 | ??24 | ??23 | ??23 | ??24 | ??24 | ??24 |
| CO 2Stream g | ??258 | ??263 | ??263 | ??261 | ??263 | ??263 | ??263 | ??185* | ??261* | ??261* |
| Time min | ??30 | ??31 | ??29 | ??28 | ??15 | ??30 | ??30 | ??19 | ??23 | ??28 |
| H 2O flows cc/min | ??2.25 | ??2.25 | ??7.5 | ??7.5 | ??7.5 | ??7.5 | ??2.25 | ??0 | ??2.25 | ??2.25 |
| From CO 2The middle caffeine mg that reclaims | ??53.2 | ??30.0 | ??24.3 | ??24.5 | ??14.6 | ??9.1 | ??21.3 | ??5.7 | ??24.1 | ??27.3 |
Claims (33)
1. the method for an extract solutes from fluid or dense gas comprises:
Provide the perforated membrane of relative both sides in adding the assembly of depressing, described film is as the interlayer between fluid and the dense gas, and described film is nonselective to described solute;
Described dense gas adds in the described assembly in a side of described film, described fluid adds in the described assembly at the opposite side of described film, described fluid and dense gas contain one of at least the solute that will extract, another of described fluid and dense gas is as spe medium, the density of described dense gas is at least 0.5g/cc, and described fluid and dense gas are not miscible so that two-phase to be provided mutually basically;
Carry out described method, wherein basic identical at the pressure of film both sides described in the described assembly; With
Stride across the described solute of described membrane extraction by the concentration gradient driving of described solute between described fluid and described dense gas.
2. the method for claim 1 before the opposite side of described film adds the described step of described fluid, also comprises the step with the dry described film of described dense gas.
3. the process of claim 1 wherein that described dense gas and fluid pass through in the described both sides of described film adverse current.
4. the process of claim 1 wherein that described perforated membrane is a hollow-fibre membrane.
5. the method for claim 1, wherein said perforated membrane is made by the material that is selected from following group, is made up of polypropylene, polyethylene, polytetrafluoroethylene (PTFE), polyvinylidene fluoride, nylon, polysulfonates, Merlon, polyester, cellulose acetate, celluloid, cellulose and acrylic acid for described group.
6. the process of claim 1 wherein the aperture of described perforated membrane in the scope of 0.001 μ to 1 μ, the thickness of described film is in the scope of 0.005mm to 3mm.
7. the method for claim 5, the aperture of wherein said perforated membrane is in the scope of 0.1 μ to 0.2 μ, and the thickness of described film is in the scope of 0.2mm to 0.6mm.
8. the process of claim 1 wherein the hole substantial symmetry of described perforated membrane.
9. the process of claim 1 wherein that described dense gas is selected from methane, ethane, propane, butane, iso-butane, ethene, propylene, fluorohydrocarbon, tetrafluoromethane, F-22, carbon dioxide, nitrous oxide, sulfur hexafluoride, ammonia and chloromethane.
10. the method for claim 9, wherein said fluorohydrocarbon is selected from partially fluorinated methane, ethane and propane.
11. the process of claim 1 wherein that described dense gas is a carbon dioxide.
12. the process of claim 1 wherein that described fluid is selected from fruit juice, jam, dish juice, puree, emulsion oil-in-water, living cells fermentation broth and enzyme-added meat soup.
13. the process of claim 1 wherein that described fluid can be second dense gas of density at least about 0.5g/cc.
14. the process of claim 1 wherein that described solute is spices, essence, medicine and chelated metal.
15. the process of claim 1 wherein that described method carrying out under-10 ℃ of temperature to about 200 ℃ of scopes approximately.
16. the process of claim 1 wherein that described method carries out under the pressure of about 2bar to about 700bar scope.
17. a method that extracts spices or essence from fluid comprises:
Provide the perforated membrane of relative both sides in adding the assembly of depressing, described film is as fluid and highly dense CO
2Between interlayer, described film is nonselective to described spices or essence;
Add described fluid and highly dense CO in the opposite direction in the described relative both sides of described film
2, wherein, described fluid and highly dense CO
2One of at least contain the spices or the essence that will extract, described fluid and highly dense CO
2Another as spe medium, described highly dense CO
2Density be at least O.5g/cc and described fluid and highly dense CO
2Basically not miscible so that two-phase to be provided mutually;
Carry out described method, wherein basic identical at the pressure of film both sides described in the described assembly; With
By described spices or essence at described fluid and described highly dense CO
2Between concentration gradient drive and to stride across described spices of described membrane extraction or essence.
18. one kind is used for comprising from the system of fluid or dense gas extract solutes:
One dense gas supply source;
One fluid supply source;
But the pressure-applying unit that comprises perforated membrane with relative both sides, described assembly operationally links to each other with the fluid supply source with described dense gas, accept dense gas and accept fluid from described source with a side at the opposite side of described film at described film, described film is nonselective to described solute, described perforated membrane is as the interlayer between described fluid and the described dense gas, described fluid and dense gas contain one of at least the solute that will extract by the concentration gradient of described solute between described fluid and described dense gas, and another of described fluid and dense gas is as spe medium; With
Be used to reclaim the device of described extract solutes.
19. the system of claim 18 also comprises the device that is used for feeding in the relative both sides of described film described dense gas and fluid.
20. the system of claim 19, wherein said device is suitable for feeding described dense gas and fluid in the relative both sides of described film adverse current.
21. the system of claim 18 also comprises being used for before described dense gas and fluid enter described assembly the device of the pressure of the described dense gas of balance and fluid basically.
22. the system of claim 21, but wherein said device comprises and is used for preventing basically in described pressure-applying unit before the extraction device of solute extraction in described pressure equaliser.
23. the system of claim 22 is used for wherein preventing basically that the described device that extracts from being a barrier film that floats in described pressure equaliser.
24. the system of claim 18 also comprises the device of the flow that is used to control described dense gas and fluid.
25. the system of claim 18 also comprises being used to monitor described dense gas and fluid, and the device of solute transmission capacity.
26. the system of claim 18 also comprises the device that is used for after the described solute of extraction described dense gas and fluid being returned described dense gas and fluid supply source.
27. the system of claim 18, wherein said perforated membrane is a hollow-fibre membrane.
28. the system of claim 18, wherein said perforated membrane is made by the material that is selected from following group, form by polypropylene, polyethylene, polytetrafluoroethylene (PTFE), polyvinylidene fluoride, nylon, polysulfonates, Merlon, polyester, cellulose acetate, celluloid, cellulose and acrylic acid for described group, the aperture of described perforated membrane is in the scope of 0.001 μ to 1 μ, and the thickness of described film is in the scope of 0.005mm to 3mm.
29. the system of claim 28, the aperture of wherein said perforated membrane is in the scope of 0.1 μ to 0.2 μ, and the thickness of described film is in the scope of 0.2mm to 0.6mm.
30. the system of claim 18, the hole substantial symmetry of wherein said perforated membrane.
31. the system of claim 18, wherein said dense gas is selected from methane, ethane, propane, butane, iso-butane, ethene, propylene, fluorohydrocarbon, tetrafluoromethane, F-22, carbon dioxide, nitrous oxide, sulfur hexafluoride, ammonia and chloromethane.
32. the system of claim 18, wherein said fluorohydrocarbon is selected from partially fluorinated methane, ethane and propane.
33. the system of claim 18, wherein said dense gas is a carbon dioxide.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 95196162 CN1162929A (en) | 1994-09-09 | 1995-01-17 | Method and system for extracting a solute from a fluid using dense gas and a porous membrane |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US08/303,445 | 1994-09-09 | ||
| CN 95196162 CN1162929A (en) | 1994-09-09 | 1995-01-17 | Method and system for extracting a solute from a fluid using dense gas and a porous membrane |
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| Publication Number | Publication Date |
|---|---|
| CN1162929A true CN1162929A (en) | 1997-10-22 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 95196162 Pending CN1162929A (en) | 1994-09-09 | 1995-01-17 | Method and system for extracting a solute from a fluid using dense gas and a porous membrane |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102658030A (en) * | 2012-05-14 | 2012-09-12 | 刘宁生 | Liquid and membrane non-contact barrel-shaped membrane distiller |
| CN105408310A (en) * | 2013-09-04 | 2016-03-16 | 出光兴产株式会社 | Carbazole derivative, material for organic electroluminescent element using carbazole derivative, and organic electroluminescent element and electronic device using carbazole derivative |
-
1995
- 1995-01-17 CN CN 95196162 patent/CN1162929A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102658030A (en) * | 2012-05-14 | 2012-09-12 | 刘宁生 | Liquid and membrane non-contact barrel-shaped membrane distiller |
| CN105408310A (en) * | 2013-09-04 | 2016-03-16 | 出光兴产株式会社 | Carbazole derivative, material for organic electroluminescent element using carbazole derivative, and organic electroluminescent element and electronic device using carbazole derivative |
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