WO2015015631A1 - 固液分離装置、及びその方法 - Google Patents
固液分離装置、及びその方法 Download PDFInfo
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- WO2015015631A1 WO2015015631A1 PCT/JP2013/070962 JP2013070962W WO2015015631A1 WO 2015015631 A1 WO2015015631 A1 WO 2015015631A1 JP 2013070962 W JP2013070962 W JP 2013070962W WO 2015015631 A1 WO2015015631 A1 WO 2015015631A1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/13—Treatment of sludge; Devices therefor by de-watering, drying or thickening by heating
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D11/00—Solvent extraction
- B01D11/02—Solvent extraction of solids
- B01D11/0288—Applications, solvents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D11/00—Solvent extraction
- B01D11/02—Solvent extraction of solids
- B01D11/0292—Treatment of the solvent
- B01D11/0296—Condensation of solvent vapours
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
- B03B5/00—Washing granular, powdered or lumpy materials; Wet separating
- B03B5/48—Washing granular, powdered or lumpy materials; Wet separating by mechanical classifiers
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C1/00—Magnetic separation
- B03C1/005—Pretreatment specially adapted for magnetic separation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/15—Treatment of sludge; Devices therefor by de-watering, drying or thickening by treatment with electric, magnetic or electromagnetic fields; by treatment with ultrasonic waves
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D11/00—Solvent extraction
- B01D11/02—Solvent extraction of solids
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D12/00—Displacing liquid, e.g. from wet solids or from dispersions of liquids or from solids in liquids, by means of another liquid
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/40—Extractive distillation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
- C02F11/147—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents using organic substances
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/32—Hydrocarbons, e.g. oil
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/42—Liquid level
Definitions
- the present invention relates to a solid-liquid separator for separating a liquid and a solid, and a method thereof.
- Patent Document 1 and Patent Document 2 as conventional techniques related to the present invention.
- Patent Document 1 moisture is extracted from coal containing moisture by using a cycle of state change of a substance (hereinafter referred to as substance A) that is a gas at normal temperature and normal pressure and can dissolve water and oil in a liquefied state.
- substance A a substance that is a gas at normal temperature and normal pressure and can dissolve water and oil in a liquefied state.
- Patent Document 2 discloses a heat source used for the state change cycle of the substance A and a method for using the heat source.
- Patent Document 1 is disclosed as a solid-liquid separation method using the characteristics of the substance A.
- DME dimethyl ether
- a compressor is used to change the state of the DME, but it is necessary to select an oil-free compressor as the compressor used here.
- Oil-free compressors include turbo chillers, screw chillers, reciprocating chillers, etc., but for solid-liquid separation using substance A, the minimum throughput is too high or the maintenance interval is short. However, there is no commercially suitable compressor.
- the amount of DME circulating in the cycle needs to be maintained appropriately.
- the amount of DME in the cycle is large, a liquid phase unfavorable for heat exchange occurs in the heat exchanger.
- the amount of DME is small, a gas-liquid two-phase flow is generated at a position that should be a liquid phase in the cycle.
- the efficiency of the cycle decreases. Therefore, despite the fact that the range of the appropriate amount of efficient DME is narrow, it is necessary to comprehensively calculate it from the measured temperature, pressure, flow rate, etc. using the PH diagram, and the amount of DME in the cycle It is difficult to grasp and control accurately.
- Patent Document 2 discloses a configuration in which heat from the external environment is used to supply DME condensation heat and evaporation heat.
- the efficiency of this configuration will be significantly reduced if an external medium with a temperature suitable for the DME state change cycle cannot be obtained. Even when an external medium with an appropriate temperature is obtained, the sensible heat of each individual is used. Therefore, the heat exchange efficiency is lower than that of Patent Document 1, and the heat exchanger needs to be large. There is.
- impurities are often included. Therefore, frequent maintenance is required to reduce the heat exchange efficiency by causing dirt and blockage on the external medium side of the heat exchanger. I need it.
- the present invention provides a solid-liquid separation apparatus that can efficiently change the state of the substance A and reduce the maintenance frequency.
- the present invention uses a substance A that can dissolve water and oil, and dehydrates the water to be processed, water and solid, oil and solid, or a mixture of water, oil and solid,
- a substance B that circulates while changing its state in a closed system; a compressor that compresses the substance B; a first heat exchanger that exchanges the condensation heat of the substance B and the evaporation heat of the substance A; , Expansion means for depressurizing the condensed substance B, a second heat exchanger for exchanging heat of evaporation of the substance B and condensation heat of the substance A, and separation of water or oil by the first heat exchanger
- the substance A evaporated while being condensed in the second heat exchanger, and a treatment tank in which the condensed substance A is mixed with the object to be treated and a pump for circulating the substance A are provided. It is a feature.
- the present invention provides a solid-liquid separator, A third heat exchanger using outside air or cooling water is provided between the first heat exchanger for condensing the substance B and the expansion means to control the temperature of the substance B. It is what.
- the present invention provides a solid-liquid separator, In order to separate the magnetic substance while the solid mixture containing the magnetic substance as the object to be processed is dispersed in the substance A, which is a liquid, the magnetic material is formed inside the processing tank or on the flow path for extracting the object to be processed from the processing tank. It is characterized by installing a separation device.
- the present invention provides a solid-liquid separator,
- the first heat exchanger is of a shell and tube type, and a liquid level sensor for detecting the liquid level of the water layer or oil layer deposited at the lower part of the shell is provided.
- the present invention provides a solid-liquid separator
- the second heat exchanger is a shell and tube type, and a liquid level sensor for detecting the liquid level of the substance A deposited at the lower part of the shell is provided.
- the present invention uses a substance A that can dissolve water and oil, from the object to be treated, which is water and solid, oil and solid, or a mixture of water, oil and solid.
- a substance A that can dissolve water and oil, from the object to be treated, which is water and solid, oil and solid, or a mixture of water, oil and solid.
- Circulating the substance B causing the state change in the closed system, compressing the substance B, and exchanging the heat of condensation of the substance B and the heat of evaporation of the substance A by the first heat exchanger means , Depressurizing the condensed substance B, exchanging heat of evaporation of the substance B and condensation heat of the substance A by the second heat exchange means, separating the water or oil from the first heat exchanger
- the evaporated substance A is condensed by the second heat exchanging means, and the condensed substance A is mixed with the object to be processed.
- the present invention provides a solid-liquid separation method
- a third heat exchange means that uses outside air or cooling water is provided between the first heat exchange means and the expansion means.
- the present invention provides a solid-liquid separation method, On the flow path after the substance A is condensed by the second heat exchange means in order to separate the magnetic substance while the solid mixture containing the magnetic substance as the object to be processed is dispersed in the liquid substance A Is provided with magnetic separation means.
- the present invention provides a solid-liquid separation method, A shell and tube type heat exchanger is adopted as the first heat exchange means, and a liquid level sensor means for detecting the liquid level of the water layer or oil layer deposited at the lower part of the shell of the heat exchanger is installed. It is a feature.
- the present invention provides a solid-liquid separation method, A shell and tube type heat exchanger is adopted as the second heat exchange means, and a liquid level sensor means for detecting the liquid level of the substance A deposited at the lower part of the shell of the heat exchanger is installed. It is what.
- the state change of the substance can be performed with an appropriate throughput. It is possible to provide a solid-liquid separation apparatus and method that can extend the maintenance interval of the apparatus, and that can easily grasp and control the amount of the substance A in the cycle and that can be operated efficiently.
- TH diagram temperature-enthalpy diagram showing the state change of two substances used in the present invention. It is another example of the block diagram of the solid-liquid separator of this invention.
- the solid-liquid separation apparatus and method of the present invention can separate a solid, water, and oil mixture into solid, water, and oil, respectively.
- the solid-liquid separation device and the method of the present invention can be used for a combination of solid and water and a combination of solid and oil. Specifically, water, oil and solids of sludge generated by water treatment, purification of soil contaminated with oil, dehydration and deoiling from plankton, desorption of impurities adsorbed on activated carbon used for water treatment, etc. It can be applied to solid-liquid separation.
- the solid-liquid separation device of the present invention and the mode for carrying out the method will be described by taking the activated carbon regeneration device as an example, but the applied product of the present invention is limited to the activated carbon regeneration device and the method thereof. is not.
- FIG. 1 is used to explain the configuration of an activated carbon regenerator that is one of the application targets of the present invention.
- dimethyl ether (DME) is used as the substance A that can dissolve water and oil
- chlorofluorocarbon is used as a substance that circulates while changing its state in a closed system (hereinafter referred to as a substance B).
- two heat exchangers use a shell and tube type, and both show an example in which DME is passed through the shell side.
- liquefied DME is sent from the pump 1 through the pipe 11 to the treatment tank 2 filled with used activated carbon.
- the impurities such as oil adhering to the activated carbon are dissolved in DME together with moisture adhering thereto.
- Impurities and water are sent to the first heat exchanger 3 through the pipe 12 while being dissolved in the liquefied DME. Since the first heat exchanger 3 is continuously supplied with chlorofluorocarbon having a temperature higher than that of liquefied DME, it is heated above the boiling point of DME by the latent heat and sensible heat of chlorofluorocarbon, and the liquefied DME is discharged as DME gas. Is done.
- the discharged high-purity DME gas is sent to the second heat exchanger 4 via the pipe 13. Since the second heat exchanger 4 is continuously supplied with chlorofluorocarbon lower than liquefied DME, it is cooled below the boiling point of DME by the latent heat and sensible heat of chlorofluorocarbon, and the DME gas is discharged as liquefied DME. Is done.
- the discharged liquefied DME is sent to the pump 1 via the pipe 14 to form a cycle for changing the state of the DME.
- the concentration of water and impurities gradually increases, and for example, substances such as water that do not mix completely start to precipitate.
- the amount of precipitation increases a lot immediately after operation, but the amount of precipitation gradually approaches zero as the removal rate from the activated carbon increases. Therefore, by continuously measuring the water level with the liquid level sensor 7, it is possible to determine the end of the cleaning of the activated carbon.
- the liquid level sensor 8a is installed to detect the liquid level of DME.
- a liquid level sensor 8b is installed to detect the liquid level of DME.
- the liquid level of liquefied DME is higher than the DME gas outlet and lower than the low temperature side pipe (tube) of the heat exchanger, so that the outflow of two-phase flow is suppressed and high heat exchange is achieved. Efficiency can be maintained.
- the liquid level can be adjusted by changing the operating speed of the pump 1 or the compressor 5. However, if the amount of DME in the cycle is excessive or insufficient, a tank installed outside the cycle (not shown) To adjust with a pump or a valve.
- the amount of water in the treatment tank 2 is reduced, so that the amount of DME in the cycle for maintaining efficient operation gradually becomes insufficient.
- the liquid phase formation is confirmed using the PH diagram from the temperature and pressure at the outlet of the condensed part after compression. The amount cannot be confirmed.
- the DME cycle in the conventional method improves the operating efficiency as the temperature difference between the evaporation section and the condensation section decreases.
- the degree of supercooling after condensation decreases, so it is discharged as a two-phase flow. Therefore, it is difficult to continue proper operation considering the error of the measuring equipment.
- the chlorofluorocarbon that supplies heat and cold to the DME is discharged from the compressor 5 as a high-temperature and high-pressure gas and is sent to the first heat exchanger 3 via the pipe 21.
- the high-temperature chlorofluorocarbon condenses and transmits the heat of condensation to the DME side, and the liquefied DME uses the supplied heat as the evaporation heat to become DME gas.
- the liquefied chlorofluorocarbon passes through the pipe 22 and is depressurized by the expansion valve 6, so that the temperature and pressure are reduced, and the two-phase flow is sent to the second heat exchanger 4 through the pipe 23.
- the high-temperature DME gas condenses the heat of condensation while condensing it, and the low-temperature freon uses the supplied heat as the evaporation heat to become a fluorocarbon gas.
- the chlorofluorocarbon gas that has become gas is sent to the compressor 5 via the pipe 24 to form a refrigeration cycle.
- FIG. 2 is a diagram showing the relationship between a D-ME and a TH diagram describing the cycle of Freon used in the present invention.
- CFCs follow the process of compression, condensation, expansion, and evaporation in the same way as a normal refrigeration cycle. Among these, a large amount of latent heat is generated in the condensation process, so it is transmitted to the DME at a lower temperature and used as the evaporation heat of the DME. In addition, since the latent heat of vaporization is required in the process of chlorofluorocarbon, it receives the heat of condensation of higher temperature DME gas. The pressure of DME at this time is always almost constant except for the pressure loss during circulation.
- the present invention uses a temperature change rather than a pressure change, so there is no need to use an expensive dedicated compressor for organic gas, and an inexpensive chemical pump can be used. It is possible to cycle the DME state change cycle.
- most of the amount of heat transferred between the first heat exchanger 3 and the second heat exchanger 4 is such that both DME and Freon occupy most of the latent heat instead of sensible heat, that is, preferably both of the latent heats.
- the refrigeration cycle of CFCs under these conditions can reduce the temperature difference unlike the air conditioner for air conditioning, the temperature of the condensation process is slightly higher than the boiling point of DME, and the temperature of the evaporation process is that of DME. It is only necessary to make it slightly lower than the boiling point. Therefore, the loss during compression required for the circulation of Freon can be suppressed to a small level.
- the pressure loss generated when the cycle is circulated only needs to be compensated by the pump. The state change can be efficiently performed.
- the DME state change cycle is circulated a plurality of times. This is because the solubility in liquefied DME varies depending on the substance, and there are substances that do not completely mix with liquefied DME. In order to sufficiently dissolve even a substance with low solubility, high-purity DME is supplied by circulating DME. Continuing, the removal rate of impurities is improved.
- the pump is used in the DME state change cycle.
- a compressor as in the prior art, it is necessary to select an oil-free compressor.
- oil for the purpose of compressor lubrication is mixed with refrigerant, but in a cycle that changes the state of DME, the oil is separated during the evaporation of DME and stays in the middle of the cycle. Therefore, it cannot be used in the present invention.
- turbo chillers, screw chillers, reciprocating chillers, etc. as the types of oil-free compressors, but the former two models can be operated because there is a gap between the high-pressure and low-pressure partition walls and leakage occurs.
- the lower limit processing amount is large, the latter has a problem that the maintenance frequency is high due to wear because there is a sealant in the sliding part, and there is no commercially suitable compressor.
- the DME pump used in the present invention can use an ordinary chemical pump, the configuration of the present invention can be easily implemented.
- DME is used as an example of a regeneration solvent for activated carbon, but the same object can be achieved with substances such as ethyl methyl ether, formaldehyde, ketene, and acetaldehyde.
- refrigeration cycle on the heat source side used in the present invention is chlorofluorocarbon
- refrigerants such as ammonia and isobutane
- temperature and pressure described in the figure are examples described for explanation, and the present invention is not limited to these values because it varies depending on the operating conditions.
- the operation of the activated carbon regenerator may be stopped and performed in an open state, but the activated carbon packed tower installed in the water treatment line is disconnected from the water treatment line with a valve or the like and connected to the DME circulation line. And may be used as an alternative to the treatment tank 2.
- the sludge targeted in this embodiment is a mixture composed of magnetic powder, oil, silt, and water, which is generated when oily water mixed with oil is purified by the coagulation magnetic separation method.
- sludge generated by water treatment is treated as industrial waste, it is dehydrated using a mechanical dehydrator such as a belt press to reduce disposal costs.
- a mechanical dehydrator such as a belt press to reduce disposal costs.
- the proportion of water after dehydration is about 70%, and water accounts for most of the dehydrated sludge.
- magnetic powder is mixed in the sludge because magnetic powder is added for water purification. Therefore, if the magnetic powder can be recovered without being discarded, the running cost can be reduced through reuse and sludge reduction.
- sludge reduction apparatus of the present invention by collecting water and oil in sludge by liquefied DME, it becomes possible to individually obtain magnetic powder and silt with significantly reduced moisture and oil adhesion amount, and sludge treatment Costs and running costs can be reduced.
- the DME circulation cycle and the Freon circulation cycle in the sludge reduction device are equivalent to the activated carbon regeneration device of the above-described embodiment, except that the object filled in the treatment tank 2 is not used activated carbon but sludge.
- the magnet or the electromagnet is installed outside the processing tank 2 here, it can be separated by discharging the liquefied DME and silt while holding the magnetic powder magnetically. Is possible.
- the expansion valve is depressurized in the evaporation path of liquefied DME, the water and oil that precipitate when passing through the expansion valve tend to be fine droplets, resulting in an emulsion. Once an emulsion is formed, it is difficult to perform gravity separation of water and oil.
- the liquefied DME is evaporated by applying heat in the first heat exchanger 3, the evaporation proceeds in a milder state as compared with the evaporation due to the pressure drop. And water can be separated easily.
- the temperature in the cycle gradually increases due to the loss in the refrigeration cycle of Freon. Therefore, it is preferable to install a heat exchanger using outside air or cooling water in order to remove the temperature in the cycle.
- a heat exchanger using outside air or cooling water in order to remove the temperature in the cycle.
- a liquid having a relatively high temperature and good heat transfer coefficient can be used as the high temperature side medium in the apparatus. Can be exchanged.
- this invention is not limited to the above-mentioned 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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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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Abstract
Description
閉じられた系内で状態変化を起こしながら循環する物質Bと,前記物質Bを圧縮する圧縮機と,前記物質Bの凝縮熱と前記物質Aの蒸発熱を交換する第1の熱交換器と,凝縮した前記物質Bを減圧する膨張手段と,前記物質Bの蒸発熱と前記物質Aの凝縮熱を交換する第2の熱交換器と,前記第1の熱交換器で水もしくは油と分離しながら蒸発した前記物質Aが前記第2の熱交換器で凝縮し,凝縮した前記物質Aが被処理物とを混合する処理槽と,前記物質Aを循環させるポンプと,を備えたことを特徴とするものである。
前記物質Bを凝縮する前記第1の熱交換器と前記膨張手段との間に,前記物質Bの温度を制御するために外気もしくは冷却水を用いる第三の熱交換器を設けたことを特徴とするものである。
前記被処理物として磁性物質を含んだ固体の混合物を液体の前記物質Aに分散させたまま磁性物質を分離するために,処理槽の内部もしくは処理槽から前記被処理物を抜き出す流路上に磁気分離装置を設置したことを特徴とするものである。
前記第1の熱交換器がシェルアンドチューブ型であり,シェルの下部に析出する水層もしくは油層の液面を検知する液面センサーを設置したことを特徴とするものである。
前記第2の熱交換器がシェルアンドチューブ型であり,シェルの下部に析出する前記物質Aの液面を検知する液面センサーを設置したことを特徴とするものである。
閉じられた系内で状態変化を起こす物質Bを循環すること,前記物質Bを圧縮すること,第1の熱交換器手段により前記物質Bの凝縮熱と前記物質Aの蒸発熱を交換すること,凝縮した前記物質Bを減圧すること、第2の熱交換手段により前記物質Bの蒸発熱と前記物質Aの凝縮熱を交換すること,前記第1の熱交換器で水もしくは油と分離しながら蒸発した前記物質Aが前記第2の熱交換手段で凝縮し,凝縮した前記物質Aが前記被処理物と混合すること、を備えたことを特徴とするものである。
前記第1の熱交換手段と前記膨張手段との間に,前記物質Bの温度を制御するために外気もしくは冷却水を用いる第三の熱交換手段を設けたことを特徴とするものである。
前記被処理物として磁性物質を含んだ固体の混合物を液体の前記物質Aに分散させたまま磁性物質を分離するために,前記物質Aが前記第2の熱交換手段で凝縮した後の流路上に磁気分離手段を設けたことを特徴とするものである。
前記第1の熱交換手段としてシェルアンドチューブ型の熱交換器を採用し、該熱交換器のシェルの下部に析出する水層もしくは油層の液面を検知する液面センサー手段を設置したことを特徴とするものである。
前記第2の熱交換手段としてシェルアンドチューブ型の熱交換器を採用し,該熱交換器のシェルの下部に析出する前記物質Aの液面を検知する液面センサー手段を設置したことを特徴とするものである。
2 処理槽
3 第1の熱交換器
4 第2の熱交換器
5 圧縮機
6 膨張弁
31 磁気分離装置
33 回収タンク
Claims (10)
- 水と油を溶解できる物質Aを用い,被処理物である水と固体,油と固体,もしくは水と油と固体の混合物の被処理物から脱水,脱油を行う固液分離装置において,
閉じられた系内で状態変化を起こしながら循環する物質Bと,
前記物質Bを圧縮する圧縮機と,
前記物質Bの凝縮熱と前記物質Aの蒸発熱を交換する第1の熱交換器と,
凝縮した前記物質Bを減圧する膨張手段と,
前記物質Bの蒸発熱と前記物質Aの凝縮熱を交換する第2の熱交換器と,
前記第1の熱交換器で水もしくは油と分離しながら蒸発した前記物質Aが前記第2の熱交換器で凝縮し,凝縮した前記物質Aが被処理物とを混合する処理槽と,
前記物質Aを循環させるポンプと,
を備えたことを特徴とする固液分離装置。
- 請求項1の固液分離装置において、
前記物質Bを凝縮する前記第1の熱交換器と前記膨張手段との間に,前記物質Bの温度を制御するために外気もしくは冷却水を用いる第三の熱交換器を設けたことを特徴とする固液分離装置。
- 請求項1の固液分離装置において、
前記被処理物として磁性物質を含んだ固体の混合物を液体の前記物質Aに分散させたまま磁性物質を分離するために,処理槽の内部もしくは処理槽から前記被処理物を抜き出す流路上に磁気分離装置を設置したことを特徴とする固液分離装置
- 請求項1の固液分離装置において、
前記第1の熱交換器がシェルアンドチューブ型であり,シェルの下部に析出する水層もしくは油層の液面を検知する液面センサーを設置したことを特徴とする
固液分離装置
- 請求項1の固液分離装置において、
前記第2の熱交換器がシェルアンドチューブ型であり,シェルの下部に析出する前記物質Aの液面を検知する液面センサーを設置したことを特徴とする
固液分離装置
- 水と油を溶解できる物質Aを用い,被処理物である水と固体,油と固体,もしくは水と油と固体の混合物の被処理物から脱水,脱油を行う固液分離方法において,
閉じられた系内で状態変化を起こす物質Bを循環すること,
前記物質Bを圧縮すること,
第1の熱交換器手段により前記物質Bの凝縮熱と前記物質Aの蒸発熱を交換すること,
凝縮した前記物質Bを減圧すること、
第2の熱交換手段により前記物質Bの蒸発熱と前記物質Aの凝縮熱を交換すること,
前記第1の熱交換器で水もしくは油と分離しながら蒸発した前記物質Aが前記第2の熱交換手段で凝縮し,凝縮した前記物質Aが前記被処理物と混合すること、
を備えたことを特徴とする固液分離方法。
- 請求項6の固液分離方法において、
前記第1の熱交換手段と前記膨張手段との間に,前記物質Bの温度を制御するために外気もしくは冷却水を用いる第三の熱交換手段を設けたことを特徴とする固液分離方法。
- 請求項6の固液分離方法において、
前記被処理物として磁性物質を含んだ固体の混合物を液体の前記物質Aに分散させたまま磁性物質を分離するために,前記物質Aが前記第2の熱交換手段で凝縮した後の流路上に磁気分離手段を設けたことを特徴とする固液分離方法。
- 請求項6の固液分離方法において、
前記第1の熱交換手段としてシェルアンドチューブ型の熱交換器を採用し、該熱交換器のシェルの下部に析出する水層もしくは油層の液面を検知する液面センサー手段を設置したことを特徴とする固液分離方法。
- 請求項6の固液分離装置において、
前記第2の熱交換手段としてシェルアンドチューブ型の熱交換器を採用し,該熱交換器のシェルの下部に析出する前記物質Aの液面を検知する液面センサー手段を設置したことを特徴とする固液分離方法。
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