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WO2016121011A1 - Appareil de distillation - Google Patents

Appareil de distillation Download PDF

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Publication number
WO2016121011A1
WO2016121011A1 PCT/JP2015/052252 JP2015052252W WO2016121011A1 WO 2016121011 A1 WO2016121011 A1 WO 2016121011A1 JP 2015052252 W JP2015052252 W JP 2015052252W WO 2016121011 A1 WO2016121011 A1 WO 2016121011A1
Authority
WO
WIPO (PCT)
Prior art keywords
substance
distillation apparatus
heat exchanger
heating
liquid
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/JP2015/052252
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English (en)
Japanese (ja)
Inventor
光宏 松澤
佐野　理志
陽子 國眼
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Hitachi Ltd
Original Assignee
Hitachi Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Hitachi Ltd filed Critical Hitachi Ltd
Priority to PCT/JP2015/052252 priority Critical patent/WO2016121011A1/fr
Publication of WO2016121011A1 publication Critical patent/WO2016121011A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/02—Crystallisation from solutions

Definitions

  • the present invention relates to a distillation apparatus.
  • Distillation is a method of separating and concentrating components having a lower boiling point by evaporation from a mixture containing a plurality of substances having different boiling points, and is used in various fields.
  • Patent Document 1 describes a distiller using mechanical vibration.
  • a wire or coil is stretched in the vicinity of the heat transfer tube, and mechanical vibration is applied thereto. And a method of vibrating the contact surface between the heat transfer tube and the liquid existing at the bottom of the tower with sound waves is disclosed.
  • An object of the present invention is to provide a distillation apparatus that can fundamentally suppress the adhesion of a substance to the surface of a heat transfer tube, suppress a decrease in heat transfer efficiency, and can be stably operated.
  • the present invention is a distillation apparatus for heating a liquid mixture containing a plurality of components to vaporize and separate one of the components, and depositing a heating unit for vaporizing the one component and other components It is characterized by having a cooling part for making it happen.
  • the heating unit and the cooling unit are arranged so as not to overlap in the vertical direction, and a partition plate is installed between the heating unit and the cooling unit. It is.
  • the present invention is characterized in that, in the distillation apparatus, the mixed solution containing the plurality of components is introduced from below the heating unit, and the heating unit is arranged in the streamline direction.
  • the present invention is characterized in that in the distillation apparatus, the cooling section is installed at the same height as the heating section or below the heating section.
  • the present invention is characterized in that, in the distillation apparatus, the heating unit is installed at a position of 3/4 or less of the liquid height of the mixed solution from the bottom.
  • the treatment apparatus and the liquid substance A are brought into contact with each other by contacting the substance to be treated with the liquid substance A, and the substance A is vaporized by the distillation apparatus.
  • the distillation apparatus in order to separate the magnetic substance while the solid mixture containing the magnetic substance is dispersed in the liquid substance A, the inside of the treatment tank or the flow path for extracting the treatment object from the treatment is used.
  • the magnetic separation device is installed in.
  • the present invention is characterized in that, in the distillation apparatus, the high temperature side of the heating unit and the low temperature side of the heat exchanger D are connected by a refrigeration cycle using a refrigerant.
  • the adhesion of the substance to the heat exchanger tube surface can be suppressed, the fall of heat transfer efficiency can be suppressed, and the distillation apparatus which can be operated stably can be provided.
  • FIG. 1 is an overview diagram showing a first embodiment of a distillation apparatus according to the present invention. It is the graph which showed the solubility curve and operation
  • FIG. 1 is a diagram showing an overview of a distillation apparatus according to this example.
  • the boiling point of substance A is smaller than the boiling point of substance B, and the density of substance A is higher than the density of substance B at the same temperature.
  • FIG. 2 is a graph showing a solubility curve of the substance B with respect to the substance A and an operation cycle in the distillation apparatus of FIG. The present invention is valid when the solubility of the substance B in the substance A increases as the temperature increases.
  • the heating heat exchanger 2 and the cooling heat exchanger 3 are installed in the same container inside the distillation apparatus 1, and between the heating heat exchanger 2 and the cooling heat exchanger 3 A partition plate 4 is installed so as to be parallel to the vertical direction. There is a gap above and below the partition plate 4 so that the liquid substance A11 in which the substance B is dissolved can flow.
  • an inflow port 5 through which the liquid material A11 in which the material B is dissolved flows in and an outflow port 6 through which the gaseous material A12 flows out are installed.
  • the heating heat exchanger 2 and the cooling heat exchanger 3 are installed so as to be completely immersed in the liquid substance A11.
  • a storage tank 9, in which the substance B13 is stored, a discharge port 7, and a valve 8 are installed below the cooling heat exchanger 3, a storage tank 9, in which the substance B13 is stored, a discharge port 7, and a valve 8 are installed.
  • the substance A in which the substance B is dissolved is introduced into the distillation apparatus 1 from the inlet 5 and joins with the liquid substance A11 circulating in the distillation apparatus 1 (state a in FIGS. 1 and 2). Then, it is heated by the heat exchanger 2 for heating and the temperature rises (state b). A part of the heated liquid substance A11 reaches the boiling point and then vaporizes, and the remaining part remains liquid (state c). Therefore, in the state c, the concentration of the substance B in the substance A is high. Since the vaporized substance A has a lower density than the liquid substance A, it floats above the heat exchanger 2 for heating.
  • the volume of the vaporized substance A is usually several thousand times the volume of the substance A when liquid. Therefore, the substance A that has become larger in volume and vaporized and floats above the heat exchanger 2 for heating becomes a driving force, and the liquid substance A11 circulates in the distillation apparatus 1 as indicated by the arrow 10 in FIG. .
  • the vaporized substance A12 passes through the outlet 6 and flows out of the distillation apparatus 1. Then, of the liquid substance A heated by the heating heat exchanger 2, the liquid substance A that has not been vaporized passes over the partition plate 4, reaches the cooling heat exchanger 3, and is cooled (state) d).
  • the concentration of the substance B has a high concentration close to saturation solubility.
  • the temperature decreases along the solubility curve, and the dissolved substance B is deposited (from the state d to the state e). Change).
  • the substance B having a density higher than that of the substance A settles below the cooling heat exchanger 3 due to gravity and accumulates in the storage tank 9.
  • the substance B accumulated in the storage tank 9 is discharged from the discharge port 7 by opening the discharge valve 8 as appropriate.
  • the cooled liquid substance A passes under the partition plate 4 and mixes with the liquid substance A in which the new substance B introduced from the inlet 5 is dissolved (state a), and again heats for heating Heated by the exchanger 2, the above cycle is repeated.
  • the distillation apparatus in the heat exchanger 2 for heating, since the process from the state e to the state c in FIG. 2 is performed, the substance A is only vaporized and the substance B is not precipitated.
  • the cooling heat exchanger 3 since the process from the state d to the state e in FIG. That is, in the distillation apparatus in the present embodiment, the part where the substance A is vaporized and the part where the substance B dissolved in the substance A is separated can be separated, and impurities are present on the surface of the heat exchanger 2 for heating. An excellent function of maintaining high-efficiency heat exchange performance without adhering is exhibited. Further, by using the change in density and volume when the substance A is vaporized as a driving force, the liquid substance A11 can be circulated in the distillation apparatus 1 without requiring a special liquid feeding system.
  • the liquid substance A is heated by the heating heat exchanger 2 and vaporized.
  • the concentration of substance B in substance A reaches saturation solubility.
  • the substance B dissolved in the substance A is deposited on the surface of the heating heat exchanger 2, and gradually adheres to and accumulates on the surface of the heating heat exchanger 2.
  • the heat exchanger 2 for heating is precisely designed in terms of surface area, material, diameter, etc. so that a desired amount of heat can be exchanged.
  • the inlet 5 is installed below the heating heat exchanger 2, and the heating heat exchanger 2 is installed at the destination of the liquid substance A flowing in from the inlet 5. Is desirable. According to this configuration, in addition to the driving force for circulating the liquid substance A by the vaporized substance A described above, the flow of the liquid substance A flowing in from the inlet 5 can be used, so that the distillation apparatus 1 is better. It becomes easy to circulate the liquid substance A inside.
  • the partition plate 4 is not provided, the minimum purpose is achieved, but it is preferable that it is installed. Due to the partition plate 4, an upward flow is generated on one side where the heat exchanger 2 for heating is installed, and a downward flow is generated on the other side where the heat exchanger 3 for cooling is installed.
  • the circulation of the substance A is rectified, the substance A is vaporized in the heat exchanger 2 for heating, and the substance B is precipitated in the heat exchanger 3 for cooling, and the action can be more effectively separated.
  • Heating heat exchanger 2 should be installed near the center of the liquid level of liquid substance A11, and cooling heat exchanger 3 should be installed at the same height as or below heat exchanger 2 for heating. Is desirable. According to this configuration, the substance B precipitated in the cooling heat exchanger 3 is unlikely to flow out in the direction of the heating heat exchanger 2 and easily collects in the storage tank 9 and is easy to collect. Also, if the heat exchanger 2 for heating and the heat exchanger 3 for cooling are too close to each other, it is difficult to make a temperature difference, and the substance B does not easily precipitate in the heat exchanger 3 for cooling. It is more preferable that the heat exchanger 3 for use is separated to some extent in the vertical direction.
  • the heating heat exchanger 2 is installed at a height near the liquid level of the liquid substance A11, the driving force for circulation by the vaporized substance A may be weakened. Therefore, it is preferable that the heat exchanger 2 for heating is installed at a position of 3/4 or less, more preferably 1/2 of the liquid height of the liquid substance A11 from the bottom surface. Further, when the partition plate 4 is made of a heat insulating material having a low thermal conductivity, the heating heat exchanger 2 and the cooling heat exchanger 3 may have the same height, and the cooling heat exchanger 3 is higher. It may be installed at a position.
  • the heat exchanger 2 for heating and the heat exchanger 3 for cooling may be installed at the same height, or may be installed near the bottom surface of the distillation apparatus 1. According to this configuration, the driving force for circulating the liquid substance A by the vaporized substance A described above becomes larger and can be easily circulated.
  • the heating heat exchanger 2 may be a multi-tube type, a flat plate type, or any other type, but preferably has a shape that allows the liquid substance A to easily flow between the heating heat exchangers 2.
  • a tubular heat exchanger is preferred.
  • the cooling heat exchanger 3 may be installed on the wall surface of the storage tank 9 as shown in FIG. According to this configuration, the substance B13 can be easily cooled even after being deposited. Therefore, even after deposition, it is difficult to redissolve in the liquid substance A11, and the substance B13 is easily kept in a deposited state.
  • the heat exchanger 2 for heating and the heat exchanger 3 for cooling may be provided in separate containers and connected by a pipe 101 and a pipe 102. According to this configuration, the heating unit and the cooling unit can be further separated, the cooling unit can be more easily cooled, and the substance B precipitated in the cooling heat exchanger 3 can be easily recovered. If the heating unit and the cooling unit are configured to be detachable from each other, maintenance such as cleaning or replacement of only one of the heating unit and the cooling unit is facilitated.
  • FIG. 5 is a configuration diagram of an activated carbon regenerator using the distillation apparatus described in the first embodiment.
  • the activated carbon regenerator will be described as an example, but the application target of the present invention is not limited to the activated carbon regenerator.
  • the activated carbon regenerator in the present embodiment is composed of the distillation apparatus 1, the heat exchanger D22, the pump 23, the treatment tank 21, the compressor 24, and the expansion valve 25 described in the first embodiment.
  • substance A in Example 1 is dimethyl ether (DME)
  • substance B is water and oil.
  • 5 indicates the flow of the substance C
  • the substance C is a refrigerant flon (R410A).
  • the substance A is assumed to be dimethyl ether (DME), but any liquid that can dissolve water and oil can be used.
  • DME dimethyl ether
  • ethyl methyl ether, formaldehyde, ketene, acetaldehyde, etc. can be used.
  • refrigerant of the substance C ammonia, isobutane, HFO1234yf, R143a, R32, etc. can be used in addition to R410A.
  • liquefied DME is sent from the pump 23 to the treatment tank 21 filled with used activated carbon.
  • water or oil adhering to the activated carbon is dissolved in DME.
  • the DME in which the water and oil are dissolved passes through the inlet 5 and flows into the distillation apparatus 1.
  • the heat exchanger 2 for heating in the distillation apparatus 1 is continuously supplied with chlorofluorocarbon having a temperature higher than that of the liquefied DME, and the liquefied DME introduced into the distillation apparatus 1 by the latent heat and sensible heat of the chlorofluorocarbon is higher than the boiling point. It is heated and vaporizes.
  • the subsequent operation and action in the distillation apparatus 1 are the same as those described in the first embodiment.
  • the vaporized DME passes through the outlet 6 and is sent to the heat exchanger D22. Since low-temperature chlorofluorocarbon is continuously supplied to the heat exchanger D22, the vaporized DME is cooled below the boiling point of the DME by the heat exchanger D and becomes liquefied DME. This liquefied DME is sent again to the pump 23, and a cycle of changing the state of the DME is formed.
  • the chlorofluorocarbon that supplies heat and cold to the DME is discharged from the compressor 24 as a high-temperature and high-pressure gas and supplied to the heating heat exchanger 2 in the distillation apparatus 1.
  • the high-temperature chlorofluorocarbon is condensed and becomes a liquid, and the condensation heat at that time is transmitted to the liquefied DME 11, and the liquefied DME 11 uses the supplied heat as the evaporation heat to become the vaporized DME 12.
  • the liquefied fluorocarbon is depressurized by the expansion valve 25, so that the temperature and the pressure are reduced, and the two-phase flow is sent to the heat exchanger D22.
  • the high-temperature vaporized DME condenses and transmits the heat of condensation to the chlorofluorocarbon side, and the low-temperature chlorofluorocarbon uses the supplied heat as evaporation heat to become chlorofluorocarbon gas.
  • the chlorofluorocarbon gas that has become a gas is sent again to the compressor 24 to form a refrigeration cycle.
  • the water and organic matter adhering to the activated carbon in the treatment tank 21 are dissolved in DME, and then the heating heat exchanger 2 and the cooling heat exchanger 3 are used in the distillation apparatus 1.
  • DME and water or oil can be efficiently separated, and DME can be separated with high purity.
  • the circulation of DME can be formed, and the high-purity DME can be continuously supplied to the treatment tank 21, so that the solubility in DME is low.
  • Even substances can be efficiently removed from the activated carbon, and the regeneration efficiency of the activated carbon can be improved.
  • water and oil do not adhere to the heat exchanger 2 for heating, it is possible to continue supplying DME with high purity stably and stable operation of the entire system is possible.
  • chlorofluorocarbon is used as a heat medium for the heat exchanger 2 for heating and the heat exchanger D22, and both are connected by a refrigeration cycle of chlorofluorocarbon.
  • the temperature of the chlorofluorocarbon only needs to be adjusted to a temperature slightly higher than the boiling point of DME in the condensation process in the heat exchanger 2 for heating and slightly lower than the boiling point of DME in the evaporation process in the heat exchanger D22.
  • the temperature difference of the chlorofluorocarbon in the cycle can be reduced, and the loss during compression necessary for the circulation of the chlorofluorocarbon can be suppressed to a low level.
  • the circulation of DME it is only necessary to compensate for the pressure loss generated when the DME is circulated by the pump 23. Therefore, it is possible to efficiently implement the state change of the substance A as a whole device, and in this embodiment, DME with less power.
  • FIG. 6 is a diagram showing the configuration of the sludge reduction apparatus.
  • the sludge targeted in this embodiment is a mixture composed of magnetic powder, oil, silt (crushed material), and water, which is generated when oily water mixed with oil is purified by the coagulation magnetic separation method.
  • sludge generated in water treatment is treated as industrial waste, it is dehydrated using a mechanical dehydrator such as a belt press in order to reduce disposal costs.
  • a mechanical dehydrator such as a belt press
  • the proportion of water after dehydration is about 70%, and water accounts for most of the dehydrated sludge.
  • magnetic powder is added to purify water, and therefore magnetic powder is mixed in sludge. If the magnetic powder can be recovered without being discarded, the running cost can be reduced by reusing the magnetic powder and reducing sludge.
  • the configuration of the sludge reduction device will be described below with reference to FIG.
  • the circulation cycle of DME and the refrigeration cycle of Freon in the sludge reduction device are the same as the activated carbon regeneration device described in Example 2, and the treatment object filled in the treatment tank 21 is sludge instead of used activated carbon. The point is different.
  • the magnetic generator 34 is installed outside the processing tank 21, but it is installed inside the processing tank 21 and separated by discharging the liquefied DME and silt while holding the magnetic powder magnetically. Is also possible.
  • the sludge reduction device of this example by collecting the water and oil in the sludge by liquefied DME, it becomes possible to individually obtain magnetic powder and silt with a significantly reduced amount of moisture and oil attached, and sludge Processing costs and running costs can be reduced. Further, as in Example 2, it is possible to efficiently separate DME from water and oil and to separate DME with high purity. Then, by supplying the separated high-purity DME to the treatment tank 21 again, the circulation of DME can be formed, and the high-purity DME can be continuously supplied to the treatment tank 21, so that the solubility in DME is low. Even substances can be efficiently removed from sludge, and sludge regeneration efficiency can be improved. Further, since water and oil do not adhere to the heat exchanger 2 for heating, it is possible to continue supplying DME with high purity stably and stable operation of the entire system is possible.
  • this invention is not limited to an above-described Example, Various modifications are included.
  • the above-described embodiments have been described in detail for easy understanding of the present invention, and are not necessarily limited to those having all the configurations described.
  • a part of the configuration of one embodiment can be replaced with the configuration of another embodiment, and the configuration of another embodiment can be added to the configuration of one embodiment.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

La présente invention concerne un appareil de distillation, qui supprime l'adhérence d'impuretés sur une surface de tube de transfert thermique, et est capable de supprimer la dégradation de l'efficacité de transfert thermique, et d'effectuer des opérations stables. Cet appareil de distillation chauffe un liquide mixte contenant une pluralité de composants, et sépare un composant des autres composants. L'appareil de distillation est caractérisé en ce qu'il est pourvu de : une section de chauffage qui vaporise ledit un composant ; et une sélection de refroidissement pour précipiter les autres composants.
PCT/JP2015/052252 2015-01-28 2015-01-28 Appareil de distillation Ceased WO2016121011A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/JP2015/052252 WO2016121011A1 (fr) 2015-01-28 2015-01-28 Appareil de distillation

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/JP2015/052252 WO2016121011A1 (fr) 2015-01-28 2015-01-28 Appareil de distillation

Publications (1)

Publication Number Publication Date
WO2016121011A1 true WO2016121011A1 (fr) 2016-08-04

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ID=56542668

Family Applications (1)

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PCT/JP2015/052252 Ceased WO2016121011A1 (fr) 2015-01-28 2015-01-28 Appareil de distillation

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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3775065A (en) * 1968-12-27 1973-11-27 Daido Namarikakoki Co Ltd Grain control in continuous crystallization
JPH01203093A (ja) * 1988-02-10 1989-08-15 Fuji Photo Film Co Ltd 写真処理廃液の処理方法及び装置
JPH11147708A (ja) * 1997-11-04 1999-06-02 Korea Atom Energ Res Inst 有機溶媒抽出方法による使用された添着活性炭の湿式再活用方法
WO2007018203A1 (fr) * 2005-08-11 2007-02-15 Toagosei Co., Ltd. Procédé de production de potasse caustique de grande pureté

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3775065A (en) * 1968-12-27 1973-11-27 Daido Namarikakoki Co Ltd Grain control in continuous crystallization
JPH01203093A (ja) * 1988-02-10 1989-08-15 Fuji Photo Film Co Ltd 写真処理廃液の処理方法及び装置
JPH11147708A (ja) * 1997-11-04 1999-06-02 Korea Atom Energ Res Inst 有機溶媒抽出方法による使用された添着活性炭の湿式再活用方法
WO2007018203A1 (fr) * 2005-08-11 2007-02-15 Toagosei Co., Ltd. Procédé de production de potasse caustique de grande pureté

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