WO2009084521A1 - 脱水システム及び脱水方法 - Google Patents
脱水システム及び脱水方法 Download PDFInfo
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- WO2009084521A1 WO2009084521A1 PCT/JP2008/073372 JP2008073372W WO2009084521A1 WO 2009084521 A1 WO2009084521 A1 WO 2009084521A1 JP 2008073372 W JP2008073372 W JP 2008073372W WO 2009084521 A1 WO2009084521 A1 WO 2009084521A1
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- Prior art keywords
- aqueous solution
- organic aqueous
- stage
- water separation
- separation membrane
- Prior art date
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- 238000000034 method Methods 0.000 title claims abstract description 43
- 239000007864 aqueous solution Substances 0.000 claims abstract description 268
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 210
- 238000000926 separation method Methods 0.000 claims description 161
- 239000012528 membrane Substances 0.000 claims description 144
- 230000018044 dehydration Effects 0.000 claims description 102
- 238000006297 dehydration reaction Methods 0.000 claims description 102
- 238000002156 mixing Methods 0.000 claims description 13
- 239000012466 permeate Substances 0.000 claims description 9
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 54
- 239000002994 raw material Substances 0.000 description 33
- 239000000203 mixture Substances 0.000 description 16
- 238000004064 recycling Methods 0.000 description 16
- 239000000047 product Substances 0.000 description 13
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 7
- 238000010586 diagram Methods 0.000 description 7
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 6
- 230000006837 decompression Effects 0.000 description 6
- 239000000446 fuel Substances 0.000 description 6
- 238000005373 pervaporation Methods 0.000 description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 5
- 239000002253 acid Substances 0.000 description 5
- 230000007423 decrease Effects 0.000 description 5
- 230000004907 flux Effects 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 238000004821 distillation Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000012982 microporous membrane Substances 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 238000009834 vaporization Methods 0.000 description 3
- 230000008016 vaporization Effects 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- 229910021536 Zeolite Inorganic materials 0.000 description 2
- 150000008064 anhydrides Chemical class 0.000 description 2
- 238000010533 azeotropic distillation Methods 0.000 description 2
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 2
- -1 ethanol anhydride Chemical class 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 230000010287 polarization Effects 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 239000010457 zeolite Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 240000008042 Zea mays Species 0.000 description 1
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 1
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 239000002152 aqueous-organic solution Substances 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 235000005822 corn Nutrition 0.000 description 1
- 239000012043 crude product Substances 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 125000001301 ethoxy group Chemical group [H]C([H])([H])C([H])([H])O* 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 239000011147 inorganic material Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 125000000956 methoxy group Chemical group [H]C([H])([H])O* 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000004065 semiconductor Substances 0.000 description 1
- 238000007873 sieving Methods 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 230000001629 suppression Effects 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
- B01D63/06—Tubular membrane modules
- B01D63/066—Tubular membrane modules with a porous block having membrane coated passages
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/362—Pervaporation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
- B01D63/06—Tubular membrane modules
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G33/00—Dewatering or demulsification of hydrocarbon oils
- C10G33/06—Dewatering or demulsification of hydrocarbon oils with mechanical means, e.g. by filtration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/08—Specific process operations in the concentrate stream
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/10—Temperature control
- B01D2311/103—Heating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/25—Recirculation, recycling or bypass, e.g. recirculation of concentrate into the feed
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2317/00—Membrane module arrangements within a plant or an apparatus
- B01D2317/02—Elements in series
- B01D2317/022—Reject series
Definitions
- the present invention relates to a dehydration system and a dehydration method. More specifically, the present invention relates to a dehydration system and a dehydration method that can efficiently dehydrate an organic aqueous solution such as a mixture of ethanol, propanol, and water having an azeotropic composition with water, or a mixture of acid and water.
- an organic aqueous solution such as a mixture of ethanol, propanol, and water having an azeotropic composition with water, or a mixture of acid and water.
- ⁇ ⁇ ⁇ ⁇ ⁇ ⁇ Ethanol is attracting attention as a fuel source to replace petroleum fuel, and its market size is predicted to be 55 million kiloliters in 2010.
- a crude product obtained from a bio raw material such as corn must be purified by distillation and dehydrated to at least 99.7 wt% or more.
- a dilute ethanol aqueous solution is concentrated in the distillation column to near the azeotropic point of the ethanol / water system and then dehydrated.
- Pervaporation membrane separation is a promising method for the purification of ethanol fuel and the like, but further performance is required for practical use. In particular, it is required to obtain a highly pure ethanol anhydride with higher efficiency.
- the present inventors have found that the organic aqueous solution to be treated is discharged from the inlet of the water separation membrane. It has been found that the temperature of the organic aqueous solution decreases as it goes to. This is because the latent heat when the organic aqueous solution passes through the water separation membrane and becomes a gas is taken away from the organic aqueous solution to be treated.
- FIG. 8 shows the relationship between the distance from the membrane inlet of the water separation membrane reactor and the temperature. A decrease in the temperature of the organic aqueous solution leads to a decrease in permeation flux (unit: kg / m 2 h) representing the membrane performance of the water separation membrane.
- FIG. 9 is a schematic diagram of a dehydration system in which three stages of dehydrators 100a, 100b, and 100c are provided, and the preheaters 300a, 300b, and 300c are arranged in front of each dehydrator. In this case, as shown in FIG. 10, the temperature decrease width in the second stage from the first stage and in the third stage from the second stage becomes smaller.
- the inventors of the present invention have attempted to construct a system with further water separation performance and low energy consumption for the practical use of a dehydration apparatus equipped with a water separation membrane, and have completed the present invention.
- the present invention is a dehydration system comprising a first preheater and a plurality of dehydrators connected in series to the subsequent stage of the preheater for separating water from an organic aqueous solution, the dehydrator main body, An organic aqueous solution inlet at the bottom of a water separation membrane having one or more flow paths extending vertically to pass the organic aqueous solution, an organic aqueous solution outlet at the top, and a water separation membrane portion outside the water separation membrane portion A shell portion defined by a side surface and an inner wall of the apparatus main body, and as the organic aqueous solution ascends the water separation membrane, moisture in the organic aqueous solution permeates the water separation membrane and moves to the shell portion.
- a dehydrating device for dehydrating the organic aqueous solution a returning means for returning a part of the organic aqueous solution that has passed through one or more dehydrating devices to the dehydrating device, or a dehydrating device preceding the dehydrating device, and the returning means. Preheat the aqueous organic solution returned by before supplying it to the dehydrator That comprises a second preheater.
- the return means is means for returning a part of the organic aqueous solution that has passed through the last-stage dehydrator to the front-stage dehydrator, It is preferable that the preheater also serves as the second preheater.
- the return means is means for returning a part of the organic aqueous solution that has passed through the last-stage dehydrator to the dehydrator after the first stage. It is preferable that the second preheater is installed in the front stage of the dehydrator after the front stage. In such an embodiment, there are three or more dehydrators connected in series.
- the return means is means for returning a part of the organic aqueous solution that has passed through the dehydrator before the last stage to the dehydrator after the first stage, It is preferable that the second preheater is installed in a front stage of the dehydrator after the foremost stage.
- the dewatering devices before the last stage are arranged at a later stage than the dewatering devices after the foremost stage.
- the dehydration system of the present invention is a preheater that preheats an organic aqueous solution, and a dehydrator that separates water from the preheated organic aqueous solution, for passing the organic aqueous solution into the dehydrator body.
- a water separation membrane portion having an organic aqueous solution inlet at the bottom of a water separation membrane having one or more channels extending vertically, an organic aqueous solution outlet at the top, an outer surface of the water separation membrane portion, and an inner wall of the apparatus main body
- the organic aqueous solution ascends the water separation membrane, the water in the organic aqueous solution passes through the water separation membrane and moves to the shell portion.
- Another aspect of the present invention is a dehydration method in which a preheated organic aqueous solution is flowed from a lower inlet to an upper outlet of a water separation membrane having one or more flow paths extending vertically to pass the organic aqueous solution.
- a water separation step of reducing the outside of the water separation membrane and allowing water in the organic aqueous solution to permeate the water separation membrane, and at least part of the organic aqueous solution that has undergone one or more water separation steps is A step of mixing with an organic aqueous solution or an untreated organic aqueous solution that has undergone fewer water separation steps than the aqueous solution, a step of preheating the mixed organic aqueous solution, and a step of subjecting the preheated organic aqueous solution to the water separation step again.
- the present invention it is possible to obtain a dewatering system with improved water separation performance and high energy efficiency as a whole. Specifically, with the above configuration of the present invention, the temperature of the organic aqueous solution in each dehydrating apparatus can be kept constant, and the flow rate of the organic aqueous solution in the apparatus can be increased. In addition, the system can be simplified.
- FIG. 1 is a conceptual diagram illustrating a first embodiment of a dehydration system according to the present invention. It is a key map explaining one embodiment of a dehydrating device concerning the present invention. It is a key map explaining one embodiment of a water separation membrane part concerning the present invention. It is a conceptual diagram explaining other embodiment of the water separation membrane part which concerns on this invention. It is a conceptual diagram explaining 2nd embodiment of the dehydration system which concerns on this invention. It is a conceptual diagram explaining 3rd embodiment of the dehydration system which concerns on this invention. It is a conceptual diagram explaining 4th embodiment of the spin-drying
- FIG. 1 shows a first embodiment of a dehydration system according to the present invention.
- the dehydrating system shown in FIG. 1 is composed of three dehydrating apparatuses 1a, 1b, 1c, a raw material pump 2, a preheater 3, a cooler 4, and a return means 6 including a recycle pump 5 as main components. Is done.
- the raw material pump 2 is arranged at the rear stage of the raw material supply apparatus (not shown), and the preheater 3 is arranged at the rear stage of the raw material pump 2.
- a first-stage dewatering device 1a is disposed at the rear stage of the preheater 3.
- the first-stage dewatering device 1a, the second-stage dewatering device 1b, and the third-stage dewatering device 1c are connected in series. There is no preheater between them.
- the pipe drawn from the third-stage dewatering device 1c is branched into two after the third-stage dewatering device 1c.
- a cooler 4 is disposed downstream of one of the tubes.
- the other tube constitutes the return means 6.
- the return means is connected to a pipe connecting the raw material pump 2 and the preheater 3.
- a recycling pump 5 is installed in the return means 6.
- All of the three dehydrators 1a, 1b, and 1c are apparatuses that separate water from an organic aqueous solution by a pervaporation method using a water separation membrane.
- the organic aqueous solution refers to a mixture of water that is mutually soluble in water and water.
- the liquid that dissolves in water include, but are not limited to, ethanol, methanol, isopropyl alcohol, acids such as acetic acid, and ketones such as acetone.
- Such dehydration apparatuses 1a, 1b, and 1c typically have an organic aqueous solution inlet at the bottom of a water separation membrane having one or more flow paths extending vertically to pass the organic aqueous solution in the main body of the dehydration apparatus.
- a water separation membrane part having an organic aqueous solution outlet at the top; a shell part defined by an outer surface of the water separation membrane part and an inner wall of the apparatus main body; and the shell part near the inlet of the organic aqueous solution Is provided with a connection port with a decompression means, and as the organic aqueous solution ascends the water separation membrane, moisture in the organic aqueous solution permeates the water separation membrane and moves to the shell portion. Dehydrated.
- FIG. 2 illustrates an example of an apparatus that can be used as the dehydrating apparatuses 1a, 1b, and 1c.
- 2A is a conceptual cross-sectional view of the dehydrating apparatus 1
- FIG. 2B is a cross-sectional view taken along AA in FIG. 1A.
- the dehydrating apparatus 1 shown in FIG. 2 includes a water separation membrane part 10, a shell part 11, and a vacuum duct 14 in the main body of the dehydrating apparatus 1 as main components, and a decompression device 13 is connected to the main body of the dehydrating apparatus. Is done.
- the water separation membrane unit 10 is composed of a water separation membrane 10d, with an organic aqueous solution inlet 10a at the lower end and an outlet 10b at the upper end, through which the organic aqueous solution passes as an organic aqueous solution channel 10c. Therefore, one or more hollow portions extending vertically are formed.
- the shell portion 11 is located around the side surface of the water separation membrane portion 10.
- a vacuum duct 14 is provided below the shell portion 11 and in the vicinity of the organic aqueous solution inlet 10a. The vacuum duct 14 is connected to the decompression device 13.
- the water separation membrane unit 10 separates the organic aqueous solution into anhydride and water.
- a water separation membrane part 10 various forms are known and are commercially available.
- a monolith type and a tubular type water separation membrane part can be used.
- FIG. 3B is a cross section taken along line BB of FIG. 3A.
- the monolith type water separation membrane part is provided with a plurality of organic aqueous solution flow paths 110c that are one or more hollow parts extending vertically to pass the organic aqueous solution through the cylindrical water separation membrane 110d.
- the flow path 110c of the organic aqueous solution inside the water separation membrane is called the primary side or supply side of the membrane, and the outside of the water separation membrane 110d is the secondary side of the membrane, or It is called the transmission side.
- the water separation membrane part 110 is preferably installed so that the direction of the flow path is parallel to the vertical direction. Then, while reducing the pressure on the permeate side of the water separation membrane 110, the organic aqueous solution is supplied from the inlet 110a on the lower side in the vertical direction, flows in the direction opposite to gravity, and is discharged from the outlet 110b on the upper side in the vertical direction. . By this operation, water in the organic aqueous solution becomes water vapor and is drawn out from the side surface of the cylindrical water separation membrane 110d to the permeate side. As a result, the organic aqueous solution recovered from the water separation membrane part outlet 110b is dehydrated.
- the illustrated monolith-type water separation membrane 110 is schematic, but as an example, a water separation membrane in which 30 holes with a diameter of 3 mm are provided for a cylindrical water separation membrane with a diameter of 30 mm. Part can be used. As another example, a water separation membrane part having 200 holes with a diameter of 2 mm can be used for a water separation membrane part with a diameter of 150 to 200 mm.
- the length of the water separation membrane portion can be appropriately determined by those skilled in the art according to the desired membrane performance, but as an example, a length of 150 mm to 1 m can be used.
- FIGS. 4A and 4B is a cross-sectional view taken along the line CC of FIG. 4A.
- the tubular water separation membrane part 210 is a tubular water separation membrane 210d in which only one flow path 210c of an organic aqueous solution is provided.
- the tubular-type water separation membrane unit 210 has the same installation mode and operational effects as the monolith-type water separation membrane unit.
- the tubular water separation membrane part one having an outer diameter of 10 mm and an inner diameter of 7 mm can be used, and as another example, one having an outer diameter of 30 mm and an inner diameter of 22 mm can be used.
- a length of 150 mm to 1 m can be used.
- a microporous membrane whose pore size is precisely controlled with an inorganic material can be used.
- the microporous membrane exhibits a molecular sieving effect that allows small molecular gases to pass through and excludes large molecular gases, and shows a behavior of activated diffusion whose permeability coefficient increases with increasing temperature.
- the microporous membrane include a carbon membrane, a silica membrane, and a zeolite membrane.
- a silica-based or zeolite-based inorganic water separation membrane having a pore diameter of 10 angstroms or less is suitable as the water separation membrane.
- an inorganic water separation membrane described in Japanese Patent No. 2808479 can be applied.
- the inorganic water separation membrane of Patent No. 2808479 is an acid-resistant composite separation obtained by supporting silica gel obtained through hydrolysis of an alkoxysilane containing an ethoxy group or a methoxy group in the pores of an inorganic porous body. It is a membrane.
- the form, size, and material of the water separation membrane can be appropriately selected by those skilled in the art according to the purpose of use.
- the shell portion 11 is a portion around the water separation membrane portion 10 and corresponds to the permeation side of the water separation membrane and serves as a flow path for the water vapor 51 discharged from the side surface of the water separation membrane portion 10.
- the shell portion 11 is a space defined by the side surface of the water separation membrane section 10 and the inner wall of the main body of the dehydrating apparatus 1.
- the shell portion 11 is configured such that an organic aqueous solution before being supplied to the water separation membrane portion 10 or an organic aqueous solution discharged from the water separation membrane portion 10 does not flow.
- a vacuum duct 14 is provided below the shell portion 11 and in the vicinity of the inlet 10a of the water separation membrane portion 10.
- the vacuum duct 14 serves as a connection port for connecting to the decompression device 13.
- the water vapor 51 released to the shell portion 11 from the vacuum duct 14 is recovered.
- the vacuum duct 14 may be provided sideways as illustrated, or may be provided vertically downward, and the direction thereof is not limited.
- the decompression device 13 is means for decompressing the shell portion 11 and sucking the water vapor released from the water separation membrane portion 10. What is necessary is just to reduce the pressure to about 10 to 100 torr (1333.22 to 13332.2 Pa), and a normal pressure reducing pump or the like can be used.
- the dehydrating apparatus 1 including one water separation membrane unit 10 is illustrated.
- the dehydrating apparatus according to the present invention includes a plurality of water separation membrane units in the main body of the dehydrating apparatus. May be connected in parallel. By providing a plurality of water separation membrane parts connected in parallel in the dehydrator main body, the amount of the organic aqueous solution to be treated at one time by one dehydrator can be increased.
- any dehydrating apparatus having the above functions can be used in the dehydrating system according to the present embodiment.
- the three dehydrating apparatuses 1a, 1b, and 1c may all be the same dehydrating apparatus or may be partially dehydrating apparatuses.
- a dehydrator provided with a tubular water separation membrane and a dehydrator provided with a monolith type water separation membrane can be alternately arranged.
- the raw material pump 2 may be, for example, a diaphragm type, a centrifugal type, or a plunger type specification, but is not limited thereto.
- the preheater 3 disposed in the front stage of the dehydrating apparatus 1a may be any one that can heat the organic aqueous solution supplied to the dehydrating apparatus 1a, and a normal heat exchanger or heater can be used.
- the organic aqueous solution 54 obtained by mixing the raw organic aqueous solution 50 and the recycled organic aqueous solution 53 has a temperature close to the azeotropic point but can be heated to a temperature equal to or lower than the azeotropic point.
- the cooler 4 disposed in the subsequent stage of the dehydrating device 1c may be any one that can cool a high-temperature organic aqueous solution with reduced moisture to room temperature through the dehydrating device 1c, and uses a normal heat exchanger. be able to.
- the return means 6 is a means for returning a part of the high-temperature organic aqueous solution that has passed through the dehydrating apparatus 1c to the front stage of the dehydrating apparatus 1c, and is typically a pipe.
- the return means 6 is connected between the raw material pump 2 and the preheater 3.
- the recycle pump 5 constitutes a part of the return means 6. The same material pump can be used.
- the dehydration system having such a configuration can efficiently separate water from the organic aqueous solution and condense the organic aqueous solution.
- an embodiment of a method for dehydrating an organic aqueous solution using such a dehydrator system according to the present embodiment will be described.
- the pre-heated organic aqueous solution flows from the lower inlet to the upper outlet of the water separation membrane having one or more flow paths extending vertically to pass the organic aqueous solution, and the water separation membrane
- the dehydration method includes a water separation step in which the water in the organic aqueous solution is permeated through the water separation membrane by decompressing the outside of the organic aqueous solution, and a portion of the organic aqueous solution that has undergone the three water separation steps is treated with untreated organic
- the organic aqueous solution that is a target of the dehydration method according to the present embodiment is generally an organic aqueous solution that is a mixture of a liquid that is mutually soluble in water and water.
- Specific examples include a mixture of ethanol and water, a mixture of propanol and water, a mixture of isopropyl alcohol and water, or a mixture of an acid such as acetic acid and water. According to the method according to the present embodiment, these are dehydrated to 99.7% anhydride suitable for fuel applications, for example, or to 99.99% or more for semiconductor substrate cleaning applications.
- the organic aqueous solution is obtained by treating a mixture as a raw material with a distillation column or an alcohol selective membrane so that the concentration of alcohol or acid is 80 to 95 wt%.
- the organic aqueous solution to be treated may be a pressurized organic aqueous solution.
- the temperature of the organic aqueous solution can be increased without gasifying the organic aqueous solution supplied to the dehydrating apparatus 1 according to the present embodiment.
- an organic aqueous solution pressurized to 1.5 atm to 10 atm, preferably 2 to 3 atm can be used.
- the ethanol concentration in the raw material according to the present embodiment is preferably 95 wt%.
- a raw material organic aqueous solution 50 that is a mixture of 95 wt% ethanol and 5 wt% water is conveyed by a raw material pump 2 from a supply source (not shown).
- the raw organic aqueous solution 50 is mixed with the recycled organic aqueous solution 53 from the return means 6 at the front stage of the preheater 3.
- the recycle organic aqueous solution 53 is generally a mixture of about 99 to 99.7 wt% ethanol and about 0.3 to 1 wt% water, depending on the recycle ratio.
- the temperature of the recycled organic aqueous solution 53 depends on the recycle ratio, but when the recycle ratio is about 1 to 5, it is about 65 to 78 ° C.
- the recycling ratio refers to the ratio of the recycled organic aqueous solution 53 to the raw organic aqueous solution 50.
- the power of the recycle pump 5 is required.
- the recycle ratio can be appropriately determined by those skilled in the art from the desired product 52 concentration, the temperature of the organic aqueous solution at the outlet of each dehydration apparatus 1a, 1b, 1c, and the overall energy efficiency.
- the recycle ratio can be, for example, 1 to 5, but is not limited thereto.
- the mixed organic aqueous solution 54 is heated by the preheater 3.
- the temperature of the organic aqueous solution after the temperature rise is preferably from 70 ° C. to less than 80 ° C., which is close to the azeotropic point of ethanol and water but less than the azeotropic point (about 80 ° C.). This is because the higher the temperature of the organic aqueous solution, the larger the permeation flux and the higher the membrane performance.
- a temperature higher than the azeotropic point a part of the organic aqueous solution is vaporized and takes away latent heat of evaporation.
- the organic aqueous solution heated by the preheater 3 is supplied to the first-stage dehydrator 1a from the organic aqueous solution inlet of the water separation membrane unit 10.
- the shell part 11 is decompressed. At this time, it is preferable to reduce the pressure of the shell portion 11 so as to be about 10 to 100 torr (1333.22 to 13332.2 Pa). This is because the separation is promoted by the differential pressure between the supply side and the permeation side of the water separation membrane. The pressure is reduced from a vacuum duct 14 provided below the shell portion 11.
- the organic aqueous solution flows through the flow path 10 c from the bottom to the top of the water separation membrane unit 10. During this time, water in the organic aqueous solution is taken out as water vapor 51 to the shell portion 11 through the separation membrane 10d. Due to the vaporization of water, the organic aqueous solution is deprived of heat of vaporization as needed. Therefore, the temperature of the organic aqueous solution flowing out from the outlet 10b is slightly lower than that at the time of supply, and the concentration of contained water is also reduced.
- the water vapor 51 released to the shell part 11 convects from above the shell part 11 downward. This is because vacuum suction is performed from below the shell portion 11. As shown in FIG. 2B, the water vapor 51 convects toward the duct 14 and is recovered from the duct 14. The recovered water vapor 51 is condensed in a subsequent stage by a cooler such as a heat exchanger (not shown). Note that the position of vacuum suction and the direction of convection described in this embodiment are merely examples, and the present invention is not limited to such a mode. As another example, a mode in which water vapor convects from below to above and co-flows with the organic aqueous solution can be exemplified.
- the organic aqueous solution that has passed through the first stage dehydrator 1a is supplied to the second stage dehydrator 1b without passing through a preheater or the like.
- the temperature of the organic aqueous solution depends on the recycle ratio, but when the recycle ratio is about 1 to 5, the ethanol concentration in the organic aqueous solution is about 96 to 98.5% when the recycle ratio is about 1 to 5. ing.
- the second-stage dehydrating apparatus 1b as in the first-stage dehydrating apparatus 1a, the dehydration process is performed, the water 51 is discharged by the decompression apparatus, and the organic aqueous solution further dehydrated is discharged from the dehydrating apparatus 1b.
- the organic aqueous solution that has passed through the second stage dehydrator 1b is supplied to the third stage dehydrator 1c without passing through a preheater or the like.
- the temperature of the organic aqueous solution supplied to the third-stage dehydrator 1c depends on the recycle ratio, but when the cycle ratio is about 1 to 5, it is about 48 to 76 ° C., and the ethanol concentration in the organic aqueous solution is About 97.5 to 99.3%.
- the dehydration process is performed, and the organic aqueous solution further dehydrated is discharged from the dehydration apparatus 1c. .
- the temperature of the organic aqueous solution at the outlet of the third-stage dehydrator 1c depends on the recycle ratio, but when the recycle ratio is about 1 to 5, it is about 50 to 79 ° C., and the ethanol concentration in the organic aqueous solution is , Approximately 98.6-99.6%.
- Part of the organic aqueous solution discharged from the dehydrating apparatus 1 c is cooled to about 35 ° C. or less by the subsequent cooler 4 to become a product 52.
- the remainder is returned to the front stage of the preheater 3 as a recycled organic aqueous solution 53.
- the ratio of the organic aqueous solution to be the product 52 and the recycled organic aqueous solution 53 can be determined from the above-described recycling ratio.
- the recycled organic aqueous solution 53 is subjected to a water separation step in the three-stage dehydrators 1a, 1b, and 1c, and ethanol is concentrated to about 50 to 79% and the temperature is about 98.6 to 99, depending on the recycling ratio. It is 6 ° C.
- the recycle aqueous solution 53 is returned to the front stage of the preheater 3 by the pipe constituting the return means 6 and the recycle pump 5.
- the temperature and ethanol concentration at each stage described in this embodiment are examples, and the temperature and concentration vary depending on the film performance, and are not limited to these values.
- a system and a method using a three-stage dehydrating apparatus are described.
- the present invention is not limited to a system and a method using a three-stage dehydrating apparatus.
- a dehydration system including a two-stage dehydration apparatus or a dehydration system including four to ten or more stages of dehydration apparatuses can be used.
- the flow rate is increased as compared with the case of the one-pass method, and the preheater 3.
- the amount of heat supplied to the dehydrators 1a, 1b, 1c increases. Since the increase amount of the latent heat taken away by permeation of the water separation membrane is smaller than the increase amount of the supplied heat amount, there is an advantage that the decrease in the temperature of the organic aqueous solution in the dehydrator can be suppressed. Moreover, increasing the flow rate leads to suppression of concentration polarization in the water separation membrane.
- Concentration polarization in a water separation membrane is a phenomenon in a tubular water separation membrane where the water concentration at the center of the tube is high, the water concentration is low near the separation membrane, and the permeation performance of the water separation membrane is reduced.
- the flow rate is about It can be increased from 5 times to about 10 times.
- the organic aqueous solution 54 obtained by mixing the recycled organic aqueous solution and the raw organic aqueous solution is supplied to the first-stage dehydrating apparatus, the water concentration in the solution supplied to the first-stage dehydrating apparatus is changed to the raw organic aqueous solution. Is lower than.
- the water concentration range in the organic aqueous solution supplied to each dehydrator is reduced, and the degree of deterioration of the water separation membrane of each dehydrator can be made uniform.
- the preheater does not have to be arranged in front of the second and subsequent dehydrators, and the energy efficiency of the entire system is excellent.
- the power of the recycling pump required for recycling is 5 times the recycle ratio, differential pressure 20m, and pump efficiency 50% compared to the power for supplying the same amount of heat as the recycled organic aqueous solution with the preheater in the first stage of the dehydrator. Is 1/100. Therefore, it can be said that it is excellent also in the energy efficiency of the whole system also in this point.
- FIG. 5 shows a second embodiment of the dehydration system according to the present invention.
- the dehydrating system shown in FIG. 5 has three dehydrating apparatuses 1a, 1b, 1c, a raw material pump 2, two preheaters 3a, 3b, a cooler 4, and a recycling pump 5 as main components. 6a.
- the raw material pump 2 is arranged at the rear stage of the raw material supply apparatus (not shown), and the preheater 3 a is arranged at the rear stage of the raw material pump 2.
- a first-stage dewatering device 1a is disposed at the subsequent stage of the preheater 3a.
- a second preheater 3b is disposed downstream of the first stage dewatering apparatus 1a, and a second stage dewatering apparatus 1b is disposed further downstream.
- a third-stage dewatering device 1c is connected in series to the subsequent stage of the second-stage dewatering device 1b. No preheater is disposed between the second stage dehydrator 1b and the third stage dehydrator 1c.
- the pipe drawn from the third-stage dewatering device 1c is branched into two after the third-stage dewatering device 1c.
- a cooler 4 is disposed downstream of one of the tubes.
- the other pipe is the return means 6a.
- the return means 6a is connected to a pipe connecting the first-stage dewatering device 1a and the second preheater 3b.
- a recycling pump 5 is installed in the return means 6.
- the second preheater 3b is disposed between the first-stage dewatering device 1a and the second-stage dewatering device 1b, and the return means 6a is the first-stage dewatering device. It differs from 1st embodiment by the point connected to the pipe
- the second preheater 3b may be the same as the first preheater 3a, and the same device can be used.
- a preheated organic aqueous solution flows from the lower inlet to the upper outlet of the water separation membrane having one or more flow paths extending vertically to pass the organic aqueous solution, and the water separation membrane
- the dehydration method includes a water separation step in which the water in the organic aqueous solution is allowed to permeate through the water separation membrane by reducing the outside of the organic aqueous solution.
- the organic aqueous solution as a raw material and the concentration thereof are the same as those in the first embodiment, and thus the description thereof is omitted.
- a raw material organic aqueous solution 50 that is a mixture of 95 wt% ethanol and 5 wt% water is conveyed by a raw material pump 2 from a supply source (not shown).
- the raw organic aqueous solution 50 is heated by the preheater 3a.
- the temperature of the organic aqueous solution after the temperature rise is preferably from 70 ° C. to less than 80 ° C., which is close to the azeotropic point of ethanol and water but less than the azeotropic point (about 80 ° C.).
- the organic aqueous solution heated by the preheater 3a is supplied to the first-stage dehydrator 1a from the organic aqueous solution inlet of the water separation membrane unit 10. At this time, the concentration of the organic aqueous solution is the same as that of the raw material.
- the supply flow rate of the organic aqueous solution to the water separation membrane part can be appropriately determined by those skilled in the art in relation to the permeation flux.
- the water separation step of the organic aqueous solution in the first-stage dehydration apparatus 1a is the same as that in the first embodiment, and thus the description thereof is omitted.
- the organic aqueous solution 55 that has passed through the first-stage dehydrator 1a is mixed with the recycled organic aqueous solution 53 from the supply means 6a at the front stage of the second-stage preheater 3b.
- the mixing ratio between the organic aqueous solution that has passed through the first-stage dehydrating apparatus 1a and the recycled organic aqueous solution 53 is determined by the recycling ratio.
- the recycle ratio can be appropriately determined by those skilled in the art from the desired product 52 concentration, the temperature of the organic aqueous solution at the outlet of each dehydrator 1a, 1b, 1c, and the overall energy efficiency. However, it is not limited to these.
- the mixed organic aqueous solution 56 is heated by the second stage preheater 3b.
- the organic aqueous solution heated by the second stage preheater 3b is supplied to the second stage dehydrator 1b from the organic aqueous solution inlet of the water separation membrane unit 10.
- the supply flow rate of the organic aqueous solution to the water separation membrane unit can be appropriately determined by those skilled in the art in relation to the recycle ratio and the like.
- the ethanol concentration in the organic aqueous solution supplied to the second stage dehydrator 1b is also a value that can vary depending on the recycle ratio.
- a system and method using a three-stage dehydration apparatus are described.
- the present invention is not limited to a system and method using a three-stage dehydration apparatus.
- a dehydration system including a four-stage dehydration apparatus or a dehydration system including a five-stage to ten-stage dehydration apparatus can be used.
- the organic aqueous solution at the outlet of the fourth-stage dehydration device can be returned to the second-stage dehydration device as a recycled organic aqueous solution.
- the recycled aqueous solution is preheated by the preheater before the second stage dehydrator.
- it can also be set as the system which returns the organic aqueous solution of the 4th step
- the recycled aqueous solution is preheated by a preheater before the third stage dehydrator.
- dehydration is provided with a return means for returning the organic aqueous solution discharged from the last stage of dehydrators to the dehydrator of any stage after the second stage. It can be a system.
- the recycled organic aqueous solution that has passed through the third-stage dewatering device is returned to the front stage of the second-stage dewatering device, so that the recycled organic aqueous solution and the first-stage dewatering device Is mixed with a highly concentrated organic aqueous solution that has been dehydrated.
- This has the merit that the recycle ratio can be lowered and the power of the recycle pump 5 can be reduced.
- FIG. 6 shows a third embodiment of the dehydration system according to the present invention.
- the dehydrating system shown in FIG. 6 includes three dehydrating apparatuses 1a, 1b, and 1c, a raw material pump 2, three preheaters 3a, 3b, and 3c, a cooler 4, and a recycle pump 5 as main components. It is comprised from the sending means 6b.
- the raw material pump 2 is arranged at the rear stage of the raw material supply apparatus (not shown), and the preheater 3 a is arranged at the rear stage of the raw material pump 2.
- a first-stage dewatering device 1a is disposed at the subsequent stage of the preheater 3a.
- a second preheater 3b is disposed downstream of the first stage dewatering apparatus 1a, and a second stage dewatering apparatus 1b is disposed further downstream.
- the pipe drawn from the second-stage dewatering device 1b is branched into two after the second-stage dewatering device 1b.
- a third preheater 3c is arranged at the rear stage of one of the branched pipes, and a third stage dehydrator 1c is arranged at the subsequent stage.
- the cooler 4 is disposed at the subsequent stage of the third-stage dehydrating apparatus 1c.
- the other branched pipe is the return means 6b.
- the return means 6b is connected to a pipe connecting the first-stage dewatering device 1a and the second preheater 3b.
- a recycling pump 5 is installed in the return means 6b.
- the third preheater 3c is disposed between the second-stage dewatering device 1b and the third-stage dewatering device 1c, and the return means 6b is the second-stage dewatering device. It differs from the second embodiment in that it branches off from the subsequent stage of 1b.
- the third preheater 3c may be the same as the first preheater 3a and the second preheater 3b, and the same apparatus can be used.
- a dehydration method using the dehydration system shown in FIG. 6 will be described.
- a preheated organic aqueous solution flows from the lower inlet of the water separation membrane having one or more flow paths extending vertically to pass the organic aqueous solution toward the upper outlet, and the water separation membrane
- a dehydration method including a water separation step of depressurizing the outside and allowing water in the organic aqueous solution to permeate through a water separation membrane, wherein a part of the organic aqueous solution that has undergone two water separation steps is separated once
- a step of mixing with the organic aqueous solution that has undergone the step a step of preheating the mixed organic aqueous solution, and a step of subjecting the preheated organic aqueous solution to at least two water separation steps again.
- the organic aqueous solution as a raw material and the concentration thereof are the same as those in the first embodiment, and thus the description thereof is omitted.
- a raw material organic aqueous solution 50 that is a mixture of 95 wt% ethanol and 5 wt% water is conveyed by a raw material pump 2 from a supply source (not shown).
- the raw organic aqueous solution 50 is heated by the preheater 3a.
- the temperature of the organic aqueous solution after the temperature rise is preferably from 70 ° C. to less than 80 ° C., which is close to the azeotropic point of ethanol and water but less than the azeotropic point (about 80 ° C.).
- the organic aqueous solution heated by the preheater 3a is supplied to the first-stage dehydrator 1a from the organic aqueous solution inlet of the water separation membrane unit 10. At this time, the concentration of the organic aqueous solution is the same as that of the raw material.
- the supply flow rate of the organic aqueous solution to the water separation membrane part can be appropriately determined by those skilled in the art in relation to the permeation flux.
- the water separation step of the organic aqueous solution in the first-stage dehydration apparatus 1a is the same as that in the first embodiment, and thus the description thereof is omitted.
- the organic aqueous solution 55 that has passed through the first-stage dehydrating apparatus 1a is mixed with the recycled organic aqueous solution 53 from the supply means 6b at the front stage of the second-stage preheater 3b.
- the mixing ratio between the organic aqueous solution that has passed through the first-stage dehydrating apparatus 1a and the recycled organic aqueous solution 53 is determined by the recycling ratio.
- the recycle ratio can be appropriately determined by those skilled in the art from the desired product 52 concentration, the temperature of the organic aqueous solution at the outlet of each dehydrator 1a, 1b, 1c, and the overall energy efficiency. However, it is not limited to these.
- the mixed organic aqueous solution 57 is heated by the second stage preheater 3b.
- the organic aqueous solution heated by the second stage preheater 3b is supplied to the second stage dehydrator 1b from the organic aqueous solution inlet of the water separation membrane unit 10.
- the supply flow rate of the organic aqueous solution to the water separation membrane is appropriately determined depending on the recycle ratio.
- the ethanol concentration in the organic aqueous solution supplied to the second stage dehydrator 1b is also a value that can vary depending on the recycle ratio.
- the organic aqueous solution that has passed through the second-stage dehydration apparatus 1b is divided into a recycled organic aqueous solution 53 and an organic aqueous solution 58 that is supplied to the third-stage dehydration apparatus 1c, after the second-stage dehydration apparatus 1b.
- the ratio at this time is determined from the above-mentioned recycling ratio.
- the recycled organic aqueous solution 53 is returned to the front stage of the second stage preheater 3b by the return means 6b.
- the organic aqueous solution 58 supplied to the third-stage dehydrator 1c is heated by the third-stage preheater 3c and then supplied to the third-stage dewaterer 1c. Since the water separation step in the third-stage dehydration apparatus 1c and the organic aqueous solution 52 that is the product that has passed through the third-stage dehydration apparatus 1c are the same as those in the first embodiment, description thereof is omitted.
- a system and method using a three-stage dehydration apparatus are described.
- the present invention is not limited to a system and method using a three-stage dehydration apparatus.
- a dehydration system including a four-stage dehydration apparatus or a dehydration system including a five-stage to ten-stage dehydration apparatus can be used.
- the organic aqueous solution at the outlet of the third dehydrator can be returned to the second dehydrator as a recycled organic aqueous solution.
- the recycled aqueous solution is preheated by the preheater before the second stage dehydrator.
- the organic aqueous solution is preheated by the preheater even before the third stage dehydrator.
- the recycled aqueous solution is preheated by a preheater before the third stage dehydrator.
- the organic aqueous solution is preheated by the preheater even before the fourth stage dehydrator.
- a dehydration system that includes five or more stages of dehydrators, return the dehydrator from any stage before the fourth stage to the dehydrator from any stage before the fourth stage and after the second stage. It is possible to provide a dehydration system provided with a simple return means.
- the third embodiment it is possible to improve the dewatering efficiency by returning the recycled organic aqueous solution that has passed through the second-stage dewatering device 3b to the previous stage of the second-stage dewatering device 3b.
- FIG. 7 shows a fourth embodiment of the dehydration system according to the present invention.
- the dehydrating system shown in FIG. 7 includes a dehydrating apparatus 1d, a raw material pump 2, a single preheater 3, a cooler 4, and a return means 6c including a recycle pump 5 as main components. .
- the dehydration system according to the present embodiment is different from the dehydration systems of the first to third embodiments in that only one dehydration device is provided and a multistage dehydration device is not provided.
- the dehydrating apparatus 1d used in the present embodiment is a large dehydrating apparatus as compared with the dehydrating apparatuses used in the first to third embodiments.
- the large dehydrating device means a dehydrating device having a membrane length comparable to that of a normally used dehydrating device of about 10 to 20 stages connected in series.
- the return means 6c branches at the subsequent stage of the dehydrating apparatus 1d and is connected between the raw material pump 2 and the preheater 3. Since the raw material pump 2, the preheater 3, the cooler 4, and the recycle pump 5 are the same as those in the other embodiments, description thereof is omitted.
- an organic aqueous solution preheated from the lower inlet to the upper outlet of the water separation membrane having one or more flow paths extending vertically to pass the organic aqueous solution flows, and the water A dehydration method including a water separation step of reducing the outside of the separation membrane and allowing water in the organic aqueous solution to permeate the water separation membrane, wherein at least a part of the organic aqueous solution that has undergone a single water separation step is not yet removed.
- the raw organic aqueous solution 50 is mixed with the recycled organic aqueous solution 53, heated by the preheater 3, and supplied to the dehydrator 1d.
- the mixing ratio between the raw organic aqueous solution 50 and the recycled organic aqueous solution 53 is determined by the recycle ratio.
- the recycle ratio can be appropriately determined by those skilled in the art based on the desired product 52 concentration, the temperature of the organic aqueous solution at the outlet of the dehydrating apparatus 1d, and the overall energy efficiency, and can be set to 1 to 5, for example. It is not limited to.
- the mixed organic aqueous solution 54 is supplied to the dehydrating apparatus 1d and dehydrated. A part of the organic aqueous solution discharged from the dehydrator is cooled to become a product 52. The remainder is returned as a recycled organic aqueous solution 53 to the front stage of the preheater 3 by the return means 6c.
- the amount of heat that can be supplied to the dehydrating apparatus 1d is increased by mixing the recycled organic aqueous solution 53 with the raw organic aqueous solution 50 by the return means 6c. For this reason, even if a large dehydrating apparatus is used, since the latent heat at the time of water separation is small with respect to the amount of heat to be supplied, it is possible to prevent a temperature drop at the latter stage of the water separation membrane. In other words, by recycling the organic aqueous solution, the amount of heat supplied to the dehydrating device can be made sufficiently larger than the latent heat of vaporization by water separation, and the dehydrating device itself can be enlarged.
- an effect that simplification of piping and reduction of equipment such as a heat exchanger can be achieved by using a plurality of dehydrating apparatuses as one large dehydrating apparatus.
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Abstract
Description
2 原料ポンプ
3 予熱器
4 冷却器
5 リサイクルポンプ
6 返送手段
10、110、210 水分離膜部
10a、110a、210a 有機水溶液の入口
10b、110b、210b 有機水溶液の出口
10c、110c、210c 流路
10d、110d、210d 水分離膜
11 シェル部
13 減圧装置
14 ダクト
19 熱交換器
50 有機水溶液
51 水蒸気
52 製品
53 リサイクル有機水溶液
図1に示す脱水システムは、主たる構成要素として、三つの脱水装置1a、1b、1cと、原料ポンプ2と、予熱器3と、冷却器4と、リサイクルポンプ5を備える返送手段6とから構成される。
また、本実施の形態においては、三段の脱水装置を用いたシステム及び方法について記載したが、本発明は、三段の脱水装置を用いたシステム及び方法に限定されるものではない。所望の製品濃度に応じて、例えば、二段の脱水装置を含む脱水システムとすることもできるし、四段から十段、あるいはそれ以上の段数の脱水装置を含む脱水システムとすることもできる。
また、流速を増加させることは、水分離膜内での濃度分極の抑制につながる。水分離膜内での濃度分極とは、管状の水分離膜内で、管の中心部分の水分濃度が高く、分離膜近傍では水分濃度が低くなり、水分離膜の透過性能が低下する現象をいう。本実施形態にかかる脱水システムによれば、処理済の有機水溶液のリサイクルをおこなわずにワンパス方式で有機水溶液を流したときと比較して、リサイクル比が約4から約9の場合、流速を約5倍から約10倍にまで上げることができる。
さらに、リサイクル有機水溶液と原料の有機水溶液を混合した有機水溶液54を、第一段の脱水装置に供給するため、第一段の脱水装置に供給される溶液中の水分濃度が、原料の有機水溶液よりも低くなっている。この場合、各脱水装置に供給される有機水溶液中の水分濃度幅が小さくなり、各脱水装置の水分離膜の劣化度合いを均一化することができるという利点がある。
さらにまた、予熱器を第二段以降の脱水装置の前段に配置しなくてもよく、システム全体のエネルギー効率に優れているという利点がある。
また、リサイクルに要するリサイクルポンプの動力は、リサイクル有機水溶液と同様の熱量を脱水装置前段の予熱器で供給するための動力と比較して、リサイクル比が5倍、差圧20m、ポンプ効率50%で計算した場合、1/100である。よって、この点においてもシステム全体のエネルギー効率に優れていると言える。
図5に示す脱水システムは、主たる構成要素として、三つの脱水装置1a、1b、1cと、原料ポンプ2と、二つの予熱器3a、3bと、冷却器4と、リサイクルポンプ5を備える返送手段6aとから構成される。
五段以上の脱水装置を含む脱水システムにおいても、同様に最後段の脱水装置から排出される有機水溶液を、二段目以降の任意の段の脱水装置に返送するような返送手段を設けた脱水システムとすることができる。
図6に示す脱水システムは、主たる構成要素として、三つの脱水装置1a、1b、1cと、原料ポンプ2と、三つの予熱器3a、3b、3cと、冷却器4と、リサイクルポンプ5を備える送手段6bとから構成される。
五段以上の脱水装置を含む脱水システムにおいても、同様に四段目以前の任意の段の脱水装置を、四段目以前であって二段目以降の任意の段の脱水装置に返送するような返送手段を設けた脱水システムとすることができる。
図7に示す脱水システムは、主たる構成要素として、一つの脱水装置1dと、原料ポンプ2と、一つの予熱器3と、冷却器4と、リサイクルポンプ5を備える返送手段6cとから構成される。
Claims (6)
- 第一の予熱器と、
該予熱器の後段に直列に接続された、有機水溶液から水を分離する複数の脱水装置であって、脱水装置本体内に、有機水溶液を通すための上下に延びる一以上の流路を有する水分離膜の下部に有機水溶液入口を、上部に有機水溶液出口を有してなる水分離膜部と、該水分離膜部の外側面と、装置本体内壁とで規定されるシェル部とを備え、該有機水溶液が該水分離膜を上昇するにつれて、該有機水溶液中の水分が、該水分離膜を透過してシェル部に移動し、該有機水溶液が脱水される脱水装置と、
一以上の脱水装置を経た有機水溶液の一部を、該脱水装置、または該脱水装置の前段の脱水装置に返送する返送手段と、
該返送手段により返送された有機水溶液を脱水装置に供給する前に予熱する第二の予熱器と
を含んでなる脱水システム。 - 前記返送手段が、最後段の脱水装置を経た有機水溶液の一部を、最前段の脱水装置に返送する手段であり、前記第一の予熱器が前記第二の予熱器を兼ねる、請求項1に記載の脱水システム。
- 前記直列に接続される脱水装置が三以上であり、前記返送手段が、最後段の脱水装置を経た有機水溶液の一部を、最前段以降の脱水装置に返送する手段であり、前記第二の予熱器が、該最前段以降の脱水装置の前段に設置されている、請求項1に記載の脱水システム。
- 前記直列に接続される脱水装置が三以上であり、前記返送手段が、最後段以前の脱水装置を経た有機水溶液の一部を、最前段以降の脱水装置に返送する手段であり、前記第二の予熱器が、該最前段以降の脱水装置の前段に設置されており、かつ、前記最後段以前の脱水装置が、前記最前段以降の脱水装置よりも後段にある、請求項1に記載の脱水システム。
- 有機水溶液を予熱する予熱器と、
予熱された有機水溶液から水を分離する脱水装置であって、脱水装置本体内に、有機水溶液を通すための上下に延びる一以上の流路を有する水分離膜の下部に有機水溶液入口を、上部に有機水溶液出口を有してなる水分離膜部と、該水分離膜部の外側面と、装置本体内壁とで規定されるシェル部とを備え、該有機水溶液が該水分離膜を上昇するにつれて、該有機水溶液中の水分が、該水分離膜を透過してシェル部に移動し、該有機水溶液が脱水される脱水装置と、
該脱水装置を経た有機水溶液の一部を、該予熱器の前段に返送する返送手段と
を含んでなる脱水システム。 - 有機水溶液を通すための上下に延びる一以上の流路を有する水分離膜の下部入口から上部出口に向けて予熱された有機水溶液を流し、該水分離膜の外側を減圧して、該有機水溶液中の水分を水分離膜に透過させる水分離工程を含む脱水方法であって、
一回以上の水分離工程を経た有機水溶液の少なくとも一部を、該有機水溶液より少ない回数の水分離工程を経た有機水溶液又は未処理の有機水溶液と混合する工程と、
混合された有機水溶液を予熱する工程と、
予熱された有機水溶液を再度水分離工程に供する工程と
を含む脱水方法。
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US12/677,168 US20110011725A1 (en) | 2007-12-28 | 2008-12-24 | Dehydrating system and dehydrating method |
BRPI0817723 BRPI0817723A2 (pt) | 2007-12-28 | 2008-12-24 | Sistema e método de desidratação |
EP08868721.5A EP2226113A4 (en) | 2007-12-28 | 2008-12-24 | DEHYDRATION SYSTEM AND METHOD |
CA2697863A CA2697863A1 (en) | 2007-12-28 | 2008-12-24 | Dehydrating system and dehydrating method |
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JP2007339132A JP5325418B2 (ja) | 2007-12-28 | 2007-12-28 | 脱水システム及び脱水方法 |
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EP (1) | EP2226113A4 (ja) |
JP (1) | JP5325418B2 (ja) |
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WO2011122059A1 (ja) * | 2010-03-31 | 2011-10-06 | 日本碍子株式会社 | 炭素膜構造体及びその製造方法 |
WO2012032994A1 (ja) * | 2010-09-09 | 2012-03-15 | 三菱重工業株式会社 | 脱水装置 |
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JP2011131148A (ja) * | 2009-12-24 | 2011-07-07 | Kyocera Corp | 分離膜装置 |
US8637698B2 (en) * | 2010-11-19 | 2014-01-28 | Celanese International Corporation | Production of acetic acid with an increased production rate |
KR101282237B1 (ko) * | 2012-03-21 | 2013-07-10 | 한국에너지기술연구원 | NaA 제올라이트 분리막을 이용한 물/에탄올 분리 방법 |
DE102013215004A1 (de) | 2013-07-31 | 2015-02-05 | Evonik Industries Ag | Membrankaskade mit sinkender Trenntemperatur |
US10582806B2 (en) * | 2013-11-12 | 2020-03-10 | Henny Penny Corporation | Pressure assist feature for pressure fryer |
JP6440156B2 (ja) * | 2014-07-29 | 2018-12-19 | オルガノ株式会社 | 有機溶剤精製システム及び方法 |
US10314320B2 (en) * | 2015-03-20 | 2019-06-11 | Meltz, LLC | Systems for controlled liquid food or beverage product creation |
CN109999669A (zh) * | 2019-04-26 | 2019-07-12 | 广州汉至蓝能源与环境技术有限公司 | 一种快速高效灵活的渗透汽化脱水系统及基于该系统的脱水提纯方法 |
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EP2226113A1 (en) | 2010-09-08 |
CA2697863A1 (en) | 2009-07-09 |
EP2226113A4 (en) | 2013-12-04 |
JP2009160482A (ja) | 2009-07-23 |
US20110011725A1 (en) | 2011-01-20 |
JP5325418B2 (ja) | 2013-10-23 |
BRPI0817723A2 (pt) | 2015-03-31 |
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