JP5923226B1 - Concentration apparatus and concentration method - Google Patents

Abstract

The present invention provides a concentration apparatus and a concentration method capable of stably obtaining a concentrated liquid having a predetermined concentration rate at low cost. A concentrating apparatus (1) includes a membrane distillation cell having a first chamber (10a) through which a stock solution is flowed and a second chamber (10b) separated from the first chamber (10a) by a porous membrane (11) that selectively transmits vapor. 10, the heater 20 for heating the stock solution, the cooler 40 for cooling the second chamber 10b, and the first chamber 10a and the second chamber 10b by changing the pressure in the first chamber 10a or the second chamber 10b The pressure adjustment means 70 which adjusts the pressure difference between them, and the control part 80, the control part 80 controls the heater 20 and the cooler 40 to a predetermined temperature range, and the condensate of the 2nd chamber 10b The pressure adjusting means 70 is controlled so that the amount of the pressure becomes a predetermined amount. In the concentration method, in the membrane distillation cell, the first chamber side and the second chamber side of the porous membrane are adjusted to a predetermined temperature difference so that the amount of condensate becomes a predetermined amount. Adjust the pressure difference with the chamber. [Selection] Figure 1

Description

  The present invention relates to a concentration apparatus and a concentration method based on the principle of membrane distillation.

  In various fields such as production of food and drink, waste liquid treatment, desalination treatment, and chemical industry, operations for concentrating liquids are performed. As a concentration method, an evaporation concentration method using an evaporator or a heating plate is generally used. As other methods, a membrane concentration method using a reverse osmosis (RO membrane), a freeze concentration method, and the like are also used.

  Although the evaporative concentration method is a method that can easily realize a high concentration rate, it has a disadvantage that it takes a large heating cost to evaporate the liquid. Further, the evaporation concentration method volatilizes low-boiling components such as aroma components with heating, and thus is not suitable for the production of food and drink. On the other hand, the freeze-concentration method also requires a high endothermic refrigeration capacity, and has problems such as complicated apparatus and operation and difficulty in concentrating the suspension.

  Under such circumstances, the use of the membrane concentration method is expanding as an alternative technology to replace the evaporation concentration method and the like. In the membrane concentration method, concentration is performed according to the principle of filtration or dialysis using a separation membrane. A reverse osmosis membrane (Reverse Osmosis; RO membrane) is generally used as a separation membrane when low molecules or more are to be concentrated. Conventionally, as disclosed in Patent Document 1, a technique for concentrating a saccharified solution using a reverse osmosis membrane device or a nanofiltration membrane device is known.

  The reverse osmosis method can be carried out at a relatively low cost and has the advantage that the quality of the concentrated liquid is hardly impaired because it is not necessary to volatilize low boiling components. However, in the reverse osmosis method, the concentration rate is limited due to the relationship between the operating pressure and the pressure resistance. Further, even if the reverse osmosis membrane is pretreated as described in Patent Document 1, fouling is still likely to occur. In addition, the material is often easily deteriorated by the bactericidal agent. Therefore, it is not always the best method in consideration of operation and maintenance of the apparatus.

  A membrane distillation method (MD method) is also known as a method using a separation membrane. In the membrane distillation method, a hydrophobic porous membrane is used that does not permeate liquid but permeates gas. In the concentration by the principle of membrane distillation, the liquid is separated with a phase transition to a gas, and the original liquid is concentrated. The membrane distillation method is advantageous as a method for concentrating liquids containing solutes and turbids because it is easy to operate and maintain the apparatus even in consideration of sterilization treatment and the like.

  Mass transfer in membrane distillation is driven by the vapor pressure differential across the membrane. For this reason, the concentration operation is performed by giving a temperature difference between one side of the membrane with which the stock solution is brought into contact and the opposite side of the membrane with which the vapor is emitted, and making the saturated vapor pressure different. Specific forms of the membrane distillation method include the indirect contact method in which the vapor that has permeated the membrane is cooled on a cooling surface remote from the membrane, and the cooling that has passed through the membrane on the opposite side of the membrane. There is a direct contact method in which the liquid is absorbed.

JP 2014-128213 A

  In the concentration based on the principle of membrane distillation, it is desired that the stock solution can be concentrated to a target concentration rate. However, the solute concentration of the stock solution to be concentrated is not always constant. For example, when concentrating fruit juice to obtain concentrated fruit juice, the sugar concentration of the fruit juice may not be uniform among lots due to differences in quality, variety, storage conditions, and the like. Moreover, even if the initial sugar concentration is the same, there may be a case where the concentration unevenness occurs due to the difference in specific gravity before the fruit juice is brought into contact with the membrane.

  As the solute concentration in the stock solution in contact with the membrane rises and falls, the permeation flux of the membrane also changes due to the vapor pressure drop. For this reason, the concentration rate of the resulting concentrated solution is not stable, and the concentration rate often varies depending on the solute concentration of the stock solution. On the other hand, in order to prepare the solute concentration of the stock solution in advance, the equipment cost and man-hours for pretreatment are required. That is, in the concentration based on the principle of membrane distillation, it is difficult to stably obtain a concentrate having a predetermined concentration rate at a low cost.

  Further, in the concentration based on the principle of membrane distillation, there is a demand for setting the target concentration rate freely according to the quality of the stock solution and the use of the concentrated solution. For example, for concentrated fruit juice used for fruit juice beverages, it is necessary to concentrate the sugar content or acidity of the fruit juice to about 4 to 7 times or more. On the other hand, for fruit juice used for fermented beverages such as wine, a relatively low concentration rate suitable for alcohol fermentation is sufficient.

  Since mass transfer in membrane distillation is driven by a difference in vapor pressure, conventionally, it has been necessary to sequentially change the heating temperature in order to change the setting of the target concentration rate for each concentration operation. However, switching the heating device itself according to the heating temperature is costly. In addition, if the heating temperature is changed significantly, the component quality of the concentrate will vary if the components in the stock solution are susceptible to heat. Therefore, there is a demand for means that can obtain a concentrated solution having a target concentration rate freely without cost and with stable component quality.

  Then, an object of this invention is to provide the concentration apparatus and concentration method which can obtain the concentrate of the predetermined concentration rate stably at low cost.

  In order to solve the above problems, a concentrating device according to the present invention has a first chamber through which a stock solution is flowed, and a second chamber separated from the first chamber by a porous membrane that selectively transmits vapor. A membrane distillation cell, a heater for heating the stock solution, a cooler for cooling the second chamber, and the first chamber and the second chamber by changing the pressure in the first chamber or the second chamber. A pressure adjusting means for adjusting a pressure difference between the heater, the cooler, and the pressure adjusting means, and the control section includes the heater and the cooler. The pressure adjusting means is controlled to a predetermined temperature range so that the amount of condensate produced by condensing the vapor generated in the second chamber becomes a predetermined amount.

  Further, the concentration method according to the present invention is a membrane distillation cell having a first chamber in which a stock solution is flowed, and a second chamber separated from the first chamber by a porous membrane that selectively permeates vapor. The temperature of the first chamber side and the second chamber side of the porous membrane is adjusted so as to have a predetermined temperature difference, and the amount of condensate produced by condensing the vapor generated in the second chamber is The pressure difference between the first chamber and the second chamber is adjusted to be a predetermined amount.

  ADVANTAGE OF THE INVENTION According to this invention, the concentrating apparatus and the concentration method which can obtain the concentrate of a predetermined | prescribed concentration rate stably stably at low cost can be provided.

It is a figure which shows schematic structure of the concentration apparatus which concerns on one Embodiment of this invention. It is a figure which shows schematic structure of the concentration apparatus which concerns on the 1st modification of this invention. It is a figure which shows schematic structure of the concentration apparatus which concerns on the 2nd modification of this invention. It is a figure which shows schematic structure of the concentration apparatus which concerns on the 3rd modification of this invention. It is a block diagram which shows schematic structure of a drink manufacturing system.

  Hereinafter, a concentration apparatus and a concentration method according to an embodiment of the present invention will be described. In addition, about the structure which is common in each following figure, the same code | symbol is attached | subjected and the overlapping description is abbreviate | omitted.

FIG. 1 is a diagram showing a schematic configuration of a concentrating device according to an embodiment of the present invention.
As shown in FIG. 1, the concentration apparatus 1 according to the present embodiment includes a membrane distillation cell 10, a heater 20, a concentrated liquid tank 30, a stock solution pump P1, a first temperature sensor T1, and a cooler 40. , Coolant tank 50, coolant pump P2, second temperature sensor T2, flow rate sensor (liquid amount measuring means) F1, condensate tank 60, decompressor (pressure adjusting means) 70, controller ( (Control part) 80, the undiluted | stock solution flow path 110, and the cooling fluid flow path 120 are provided.

  The concentration apparatus 1 is an apparatus that performs a concentration operation for increasing the concentration of a liquid based on the principle of membrane distillation. In the concentrating device 1, the stock solution as the liquid to be treated is subjected to membrane distillation in the membrane distillation cell 10. In the membrane distillation cell 10, a low-boiling component contained in the stock solution is separated, while a concentrated solution in which the original stock solution is concentrated is generated. For example, by performing membrane distillation using fruit juice, vegetable juice or the like as an undiluted solution, concentrated liquids such as concentrated fruit juice or concentrated vegetable juice that can be used as a raw material for foods and drinks are obtained.

  The membrane distillation cell 10 includes a porous membrane 11, a cooling plate (heat transfer wall) 12, a stock solution chamber (first chamber) 10a, a condensation chamber (second chamber) 10b, and a cooling chamber (third chamber) 10c. And have. As shown in FIG. 1, the inside of the membrane distillation cell 10 is partitioned into a stock solution chamber 10a, a condensing chamber 10b, and a cooling chamber 10c by a porous membrane 11 and a cooling plate 12.

  The porous membrane 11 is made of a porous material and forms part of the wall portion of the stock solution chamber 10a. The porous membrane 11 has a property of transmitting gas while not transmitting liquid, and exhibits an action of selectively transmitting vapor in the contacted stock solution. That is, the vapor evaporated from the stock solution can pass through the porous membrane 11 and move from the stock solution chamber 10a side to the condensation chamber 10b side. On the other hand, the original stock solution from which the vapor is released is concentrated in the stock solution chamber 10a without passing through the porous membrane 11.

  As the porous membrane 11, various forms such as a flat membrane, a hollow fiber membrane, and a tubular membrane are applied. The method of assembling the porous membrane 11 is not particularly limited, and various forms such as a circular tube type and a spiral type can be adopted. An example of the porous membrane 11 has an average pore diameter of 0.2 μm, an aperture ratio of 60% to 80%, and a thickness of 50 μm to 200 μm.

  A preferred material for the porous membrane 11 is a material having high hydrophobicity. As the organic material, for example, a fluorinated polyolefin such as polytetrafluoroethylene (PTFE), or a polyolefin such as polyethylene (PE) or polypropylene (PP) can be used. Moreover, as an inorganic material, hydrophobic zeolite, silica, carbon, etc. can be used, for example.

  The cooling plate 12 is made of a material having a high thermal conductivity, and forms part of each wall portion of the condensing chamber 10b and the cooling chamber 10c. The cooling plate 12 is cooled by the coolant from the cooling chamber 10c side, and condenses the vapor that has passed through the porous film 11 on the surface on the condensation chamber 10b side.

  Preferred materials for the cooling plate 12 are stainless steel, aluminum, titanium, copper, alloys thereof, synthetic resin with high thermal conductivity, and the like. A more preferable material is a material having both high thermal conductivity and corrosion resistance, such as stainless steel and titanium.

  The stock solution chamber 10a is a compartment through which the stock solution flows. From the outlet of the stock solution chamber 10a to the inlet, it communicates with the outside through piping or the like, and a stock solution flow path 110 for circulating the stock solution to the stock solution chamber 10a is formed. On the stock solution flow path 110, a heater 20, a concentrate tank 30, a stock solution pump P1 for circulating the stock solution, and a stock solution temperature sensor T1 for measuring a representative temperature of the stock solution are installed. The stock solution flow path 110 connects the outlet and the inlet of the stock solution chamber 10a via the heater 20, the concentrate tank 30 and the like, and the concentrate obtained by membrane distillation in the stock solution chamber 10a is recycled to the stock solution chamber 10a. Let it flow.

  The heater 20 heats the stock solution flowing in the pipe by heat exchange. Mass transfer in the porous membrane 11 is driven by a vapor pressure difference generated between the interface between the stock solution and the porous membrane 11 and the cooling surface of the cooling plate 12. The higher the temperature of the stock solution, the higher the saturated vapor pressure, and the higher the saturated vapor pressure, the larger the permeation flux of the porous membrane 11, and the higher the ratio of latent heat to sensible heat, and the smaller the heat loss. . Therefore, the stock solution is heated by the heater 20 to a predetermined temperature and introduced into the stock solution chamber 10a.

  The cooling chamber 10c is a section through which the coolant flows. The cooling chamber 10 c is separated from the condensing chamber 10 b by the cooling plate 12. From the outlet to the inlet of the cooling chamber 10c communicates with the outside through a pipe or the like, and a coolant channel 120 for circulating the coolant in the cooling chamber 10c is formed. On the coolant flow path 120, a cooler 40, a coolant tank 50, a coolant pump P2 for circulating the coolant, and a coolant temperature sensor T2 for measuring a representative temperature of the coolant are installed. . The coolant channel 120 connects the outlet and the inlet of the cooling chamber 10c via the cooler 40, the coolant tank 50, etc., and circulates the coolant cyclically into the cooling chamber 10c.

  As the cooling liquid, an appropriate fluid having a high heat capacity and latent heat and having an appropriate viscosity and phase transition temperature is applied. For example, when an aqueous stock solution such as an aqueous solution or a water suspension is to be concentrated, cooling water such as pure water, tap water, or industrial water can be used.

  The cooler 40 is an in-line type device that cools the coolant flowing in the pipe. The cooling liquid is cooled by the cooler 40 to a temperature at which the vapor in the condensing chamber 10b can be condensed and introduced into the cooling chamber 10c.

  The condensation chamber 10b is a compartment for condensing steam. The condensation chamber 10b is separated from the stock solution chamber 10a by the porous membrane 11, and is a closed system capable of adjusting the internal pressure. The vapor evaporated from the stock solution in the stock solution chamber 10a passes through the porous membrane 11, and then moves from the porous membrane 11 to the cooling plate 12 by natural convection or diffusion. Then, the cooling plate 12 cooled by the coolant flowing in the coolant flow path 120 cools the condensation chamber 10b and condenses the vapor in the condensation chamber 10b.

  The condensing chamber 10b is connected to a drain path for discharging the condensate outside the cell and an exhaust path for exhausting the steam. A decompressor 70 is installed in the exhaust path. On the other hand, a flow rate sensor (liquid amount measuring means) F1 for measuring the amount of condensate and a condensate tank 60 are installed in the drainage passage.

  The decompressor 70 is a decompression pump that can adjust the suction force of the gas by inverter control or the like, and freely reduces the internal pressure of the condensing chamber 10b to a predetermined pressure so that it is between the stock solution chamber 10a and the condensing chamber 10b. Is adjusted to a predetermined atmospheric pressure difference. From the viewpoint of increasing the permeation flux of the porous membrane 11, it is more advantageous that the internal pressure on the condensation chamber 10b side is lower than that on the stock solution chamber 10a side. At this time, if an attempt is made to increase the vapor pressure difference by giving a temperature difference to the film, the amount of sensible heat transfer including heat conduction through the film increases, which may increase heat loss. According to the decompressor 70, the vapor pressure difference can be generated without changing the temperature difference, so that both good permeation flux and thermal efficiency can be achieved.

  The controller 80 has a function of controlling the heater 20 and the cooler 40. The controller 80 is, for example, the representative temperature of the stock solution measured by the stock solution temperature sensor T1, that is, the inlet temperature of the stock solution chamber 10a, or the representative temperature of the coolant measured by the coolant temperature sensor T2, that is, the inlet of the cooling chamber 10c. The amount of heat transferred by the heater 20 or the cooler 40 is controlled so that the temperature becomes a preset target temperature.

  The controller 80 also has a function of controlling the decompressor 70. For example, the controller 80 controls the adjustment pressure of the condensing chamber 10b by the decompressor 70 so that the total amount of condensate discharged from the condensing chamber 10b within a predetermined period becomes a preset target amount. The total amount of the condensate can be obtained, for example, by integrating the flow rate of the condensate measured by the flow rate sensor F1 for an arbitrary predetermined period.

  Next, the concentration method according to the present embodiment will be described based on a specific operation method of the concentration device 1.

  The concentration method according to the present embodiment includes a stock solution chamber (first chamber) through which the stock solution flows and a condensation chamber (second chamber) separated from the stock solution chamber by a porous membrane that selectively permeates vapor. In the membrane distillation cell, the temperature of the stock solution chamber side and the condensation chamber side is adjusted so as to have a predetermined temperature difference, and the amount of condensate produced by condensation of the vapor generated in the condensation chamber is set to a predetermined amount. This is a method of adjusting the pressure difference between the stock solution chamber and the condensing chamber, that is, the atmospheric pressure difference.

  In the concentration method according to the present embodiment, in order to generate a concentrated liquid having a predetermined concentration rate, the operation is performed so that the amount of the condensed liquid that passes through the porous membrane and is generated in the condensation chamber becomes a predetermined amount. The amount of the condensate is adjusted to match the target amount determined for each use of the concentrate. As a result, a concentrated solution concentrated to the target concentration rate is generated regardless of the solute concentration, quality, type, storage conditions, pretreatment conditions, etc. of the stock solution.

The permeation amount separated from the stock solution as vapor and permeating through the porous membrane can be regarded as being equivalent to the amount of condensate produced in the condensation chamber. Therefore, the concentration ratio (C _f ) of the concentrate is expressed as the following formula (1) from the mass balance in the membrane distillation cell, where Q _f is the amount of the stock solution and Q _p is the amount of the condensate. Can do.
_{/ C f = Q f (Q} f -Q p) ··· (1)

The amount (Q _f ) of the stock solution can be easily grasped as the amount introduced into the membrane distillation cell. For example, in the concentration apparatus 1, measurement can be performed by installing a flow sensor in the stock solution flow path 110 or installing a level sensor or a weight sensor in the concentrate tank 30. Therefore, the target amount (Q _p ) of the condensate to be generated in the condensing chamber in order to produce a concentrate having a predetermined concentration rate is determined by the target concentration rate (C _f ) set in advance and the amount of known stock solution ( Q _f ) and can be determined from equation (1).

In the concentrating device 1, the stock solution is circulated to the membrane distillation cell 10 and repeated membrane distillation, whereby the stock solution is concentrated to a predetermined target concentration rate. Therefore, a target concentration rate (C _f ) corresponding to the intermediate concentration rate is preset in the controller 80. The intermediate target condensate amount (Q _p ) corresponding to this is stored in the controller 80 as a control target value that can be referred to. The intermediate target condensate amount (Q _p ) includes the target concentration rate (C _f ) corresponding to the intermediate concentration rate and the corresponding intermediate known stock solution amount (Q _f ), that is, the batch processing solution amount From the formula (1) based on

  In the concentrating device 1, the stock solution is introduced into the stock solution channel 110 from outside the system by opening the first valve V <b> 10. And after the 1st valve | bulb V10 is closed, it is made to circulate through the stock solution flow path 110 by the stock solution pump P1, and is circulated and supplied to the stock solution chamber 10a. Further, the coolant is circulated through the coolant flow path 120 by the coolant pump P2 and is circulated and supplied to the cooling chamber 10c. At this time, the representative temperature of the stock solution is measured over time by the stock solution temperature sensor T <b> 1, and the measured value at each time point is output to the controller 80. In addition, the representative temperature of the coolant is measured over time by the coolant temperature sensor T <b> 2, and the measured value at each time point is output to the controller 80.

  The controller 80 includes the heater 20 and the cooler 40 so that the temperature difference between the stock solution flowing through the stock solution chamber 10a and the cooling plate 12 of the condensing chamber 10b is constant while the stock solution and the coolant are being circulated. Are controlled at a constant temperature within a predetermined temperature range. For example, the controller 80 feedback-controls the heater 20 and the cooler 40 based on the measured temperature, and adjusts the liquid temperature of the stock solution and the liquid temperature of the cooling liquid so as to be a predetermined constant temperature.

The temperature difference between the stock solution side and the cooling side is set to a temperature at which an appropriate vapor pressure difference is secured for the porous membrane 11 according to the target concentration rate (C _f ). The target temperature for heating by the heater 20 can be less than 90 ° C. when an aqueous stock solution is to be concentrated. On the other hand, the target temperature for cooling by the cooler 40 may be set in consideration of the amount of movement of sensible heat or latent heat. In the concentrating device 1, pressure adjustment is performed together with temperature adjustment, so that it is not necessary to cause an excessive temperature difference, and heat loss due to the movement of sensible heat can be reduced.

  In the stock solution chamber 10a of the membrane distillation cell 10, the low boiling point components evaporate from the heated stock solution, and the vapor passes through the porous membrane 11 and is cooled on the cooling plate 12 to become a condensate. It is discharged from the chamber 10b. The flow rate of the discharged condensate is measured over time by the flow rate sensor F <b> 1, and the measured value at each time point is output to the controller 80.

The controller 80 controls the decompressor 70 so that the amount of the condensate produced by condensing the steam generated in the condensing chamber 10b becomes the target amount (Q _p ) while the stock solution is circulated and supplied. . For example, the target concentration factor (C _f) with the amount of known stock (Q _f) to the target condensate weight determined on the basis of the reference to the (Q _p), the target condensate amount (Q _p) of the flow rate sensor F1 Is compared with the integrated value of the flow rate measured by the predetermined period. As a result, the controller 80 feedback-controls the decompressor 70 to make the amount of condensate generated in the condensing chamber 10b coincide with the target condensate amount (Q _p ).

The adjustment pressure targeted by the decompressor 70 is adjusted to a range in which steam can be condensed on the cooling plate 12. The temperature difference between the stock solution side and the cooling side is set according to the target concentration rate (C _f ), and an approximate vapor pressure difference is ensured by the temperature difference. Therefore, even if a vapor pressure drop occurs in the stock solution, it is highly responsive. And the concentration rate can be adjusted precisely.

In the membrane distillation cell 10, the concentrated solution concentrated to the target concentration rate (C _f ) corresponding to the intermediate concentration rate passes through the stock solution flow path 110 and flows again into the stock solution chamber 10 a to be further concentrated. The concentrated solution is circulated and supplied to the stock solution chamber 10a until the final concentration rate is reached. Thereafter, the stock solution pump P1 is stopped, the closed second valve V20 and third valve V30 are opened, and the concentrated solution concentrated to the target concentration rate is recovered.

  According to the concentrating device and the concentrating method according to the above embodiment, the amount of condensate that permeates through the porous membrane and is generated in the condensing chamber can be freely adjusted. It can be obtained stably. Specifically, even if an unexpected change occurs in the heating temperature, the cooling temperature, or the solute concentration of the stock solution, a concentrated solution that is concentrated according to the target concentration rate can be obtained reliably.

  Moreover, according to the concentration apparatus and the concentration method according to the above embodiment, pretreatment for preparing the solute concentration of the stock solution in advance is not necessarily required, and the apparatus / equipment is provided for each stock solution having a different target concentration rate. Since switching is not required, a concentrated solution concentrated to a predetermined concentration rate can be obtained at low cost.

  Further, according to the concentrating device and the concentrating method according to the above-described embodiment, it is sufficient to adjust the temperature of the stock solution chamber and the condensing chamber to a constant temperature in order to obtain a concentrated solution concentrated to a predetermined concentration rate. The heat history given to can be easily aligned between lots. In other words, since the heating temperature of the stock solution is kept constant for each concentration operation, the different concentrated operations can be given to each concentrated solution as long as the heating temperature value and the heating time value are managed. The heat history can be made uniform. Therefore, even when the components in the stock solution are easily affected by heat, it is possible to obtain concentrates with the same concentration ratio or concentrates with different concentration ratios with a constant component quality and less variation. It is.

  Next, the concentration apparatus and concentration method according to the first modification will be described.

FIG. 2 is a diagram showing a schematic configuration of the concentrating device according to the first modified example of the present invention.
The concentrating device according to the embodiment may be a concentrating device (concentrating device according to a first modification) of a form provided in association with an external heat source.

  As shown in FIG. 2, the concentration device 2 according to the first modified example is similar to the concentration device 1 described above, the membrane distillation cell 10, the heater 20, the concentrated liquid tank 30, the stock solution pump P <b> 1, 1 temperature sensor T1, cooler 40, coolant tank 50, coolant pump P2, second temperature sensor T2, flow rate sensor (liquid amount measuring means) F1, condensate tank 60, decompressor ( (Pressure adjusting means) 70, a controller (control unit) 80, a stock solution channel 110, and a coolant channel 120.

  Further, the concentrating device 2 has the same configuration as the concentrating device 1 described above, an external heat source (heat source) (H1, H2,... Hn), a heat medium pipe 130, and an on-off valve (heat source switching means). (V1, V2,... Vn), a heat medium pump (flow rate adjusting means) P3, and a heat exchanger 90 are further provided. The concentration apparatus 2 according to the first modification is an apparatus that performs a concentration operation for increasing the concentration of a liquid based on the principle of membrane distillation in the same manner as the concentration apparatus 1 described above.

  The external heat sources (H1, H2,... Hn) have heat energy that can be used for heating the stock solution. There are a plurality of external heat sources (H1, H2,... Hn), and a heat medium pipe 130 is connected to each. Each of the external heat sources (H1, H2,... Hn) has heat energy independently of each other, and each heat energy is applied to the heat medium flowing through the heat medium pipe.

  The external heat sources (H1, H2,... Hn) can supply heat energy to the heater 20 as shown in FIG. That is, the plurality of heat medium tubes 130 connect between the external heat sources (H1, H2,... Hn) and the heater 20, and the heaters are connected from the external heat sources (H1, H2,... Hn). A heat medium can flow toward 20. A heat exchanger 90 is installed between the external heat source (H1, H2,... Hn) and the heater 20, and heat energy is relayed by the heat exchanger 90. .

  As the external heat sources (H1, H2,... Hn), appropriate types of heat sources are used. However, a preferable form is a waste heat source using, for example, exhaust heat from factories, business establishments, power plants, incineration facilities, etc., geothermal sources, hot spring sources, or the like. The heating performance of the heater 20 is sufficient to adjust the temperature of the stock solution to a predetermined constant temperature, and there is no need to perform variable temperature control. For this reason, as the external heat sources (H1, H2,... Hn), appropriate types of heat sources can be used, including waste heat sources and the like having an unstable amount of exhaust heat.

  Open / close valves (V1, V2,... Vn) are installed in the respective heat medium tubes 130 connected to the external heat sources (H1, H2,... Hn). Each of the plurality of on-off valves (V1, V2,... Vn) independently opens and closes the heat medium pipe 130 and supplies a heat source that gives thermal energy to the heater 20 as a plurality of external heat sources (H1, H2,. .. can be selectively switched among Hn).

  A heat medium pump P3 is installed in the heat medium pipe 130 connected to the external heat sources (H1, H2,... Hn). The heat medium pump P3 causes the heat medium to flow from the external heat sources (H1, H2,... Hn) toward the heater 20, and adjusts the flow rate of the heat medium flowing through the heat medium pipe 130 to an appropriate amount.

  Next, based on the operation method of the concentration apparatus 2, the concentration method according to the first modification will be described.

  The concentration method according to the first modification includes a stock solution chamber (first chamber) through which a stock solution is flowed, and a condensing chamber (second chamber) separated from the stock solution chamber by a porous membrane that selectively transmits vapor. In the membrane distillation cell, the amount of heat given to the stock solution is changed to a constant heat amount by switching the heat source among the plurality of heat sources and adjusting the flow rate of the heat medium from the heat source, and the stock solution chamber side and the condensation chamber side are set to a predetermined temperature. Adjust the temperature difference so that there is a difference, and adjust the pressure difference between the stock solution chamber and the condensing chamber, that is, the atmospheric pressure difference, so that the amount of condensate produced by condensing the vapor generated in the condensing chamber becomes a predetermined amount It is a method to do.

In the concentrator 2, as with the concentrator 1, the target concentration rate (C _f ) is set in advance, and the target condensate amount (Q _p ) to be generated in the condensing chamber is a control target value that can be referred to. It is stored in the controller 80. Moreover, the target exchange heat amount required in the heater 20 is calculated | required based on the target temperature of the heating of stock solution, and is memorize | stored in the controller 80 as a control target value which can be referred. Then, the stock solution is circulated through the stock solution channel 110, and the coolant is circulated through the coolant channel 120.

  The controller 80 grasps the exchange heat quantity in each of the external heat sources (H1, H2,... Hn) while the stock solution is circulated and supplied. The amount of exchange heat can be adjusted to the temperature and heat medium flow rate by installing a flow sensor for measuring the heat medium flow rate or installing a temperature sensor in each external heat source (H1, H2,... Hn), for example. It can be grasped on the basis.

  The controller 80 controls the amount of heat that the heater 20 gives to the stock solution while the stock solution is being circulated by switching the heat source among the plurality of external heat sources (H1, H2,... Hn). For example, on the basis of the exchange heat quantity measured in each of the external heat sources (H1, H2,... Hn), an optimal heat source that gives heat to the heater 20 is selected, and the corresponding on-off valves (V1, V2,. Open only Vn).

  As a heat source for opening the on-off valves (V1, V2,... Vn), only a single heat source may be selected as long as it exceeds the target exchange heat amount required in the heater 20. However, a combination of a plurality of heat sources may be selected. It is preferable in that the waste heat can be reduced if the heat exchange that the heater 20 gives to the undiluted solution exceeds the target exchange heat amount required by the heater 20 and the heat source that becomes the minimum is selected.

  After the opening / closing valves (V1, V2,... Vn) are opened, the controller 80 controls the amount of heat that the heater 20 gives to the stock solution by adjusting the flow rate of the heating medium. For example, based on the exchange heat quantity measured by each of the external heat sources (H1, H2,... Hn) and the target exchange heat quantity required in the heater 20, the heat medium is eliminated so that the difference between these heat quantities is eliminated. The flow rate of the heat medium flowing through the tube 130 is decreased. Then, the stock solution adjusted to a constant temperature by the heater 20 is concentrated while adjusting the pressure difference between the stock solution chamber 10a and the condensing chamber 10b.

  According to the concentrating apparatus and the concentrating method according to the first modification described above, the heat source that supplies thermal energy to the heater that heats the stock solution can be switched among the plurality of heat sources, so that the heating of the stock solution can be performed stably and stably. Can be done. For example, even if a heat source that does not sustain the supply of heat energy is used as the heat source of the heater, it is possible to use other heat sources while the supply of heat energy is interrupted. The concentration operation can be performed continuously.

  Moreover, according to the concentration apparatus and concentration method which concern on the above 1st modification, since the flow volume of the heat medium from the heat source supplied to a heater is adjusted, the energy efficiency at the time of heating a undiluted | stock solution can be improved. it can. For example, even when a heat source with excessive heat energy is used as a heat source for the heater, a certain amount of exchange heat for the heater is ensured, while excess heat energy is exhausted and recovered for use in other applications. It becomes possible.

  In addition, in the concentration apparatus 2 according to the first modified example described above, the amount of heat given to the stock solution is changed to a constant heat amount by switching the heat source among a plurality of heat sources and adjusting the flow rate of the heat medium from the heat source. Has been. However, instead of this, only switching of the heat source or adjustment of the flow rate of the heat medium may be performed. That is, only one of the flow rate adjusting unit and the heat source switching unit may be provided to perform concentration by membrane distillation. When the heat source is not switched, the heat source may be single. Various devices such as on-off valves and pumps may be used as appropriate as the flow rate adjusting means and the heat source switching means.

  Next, a concentration apparatus and a concentration method according to the second modification will be described.

FIG. 3 is a diagram showing a schematic configuration of a concentrating device according to a second modification of the present invention.
The concentrating device according to the above embodiment can be a concentrating device (concentrating device according to the second modified example) configured to pressurize the internal pressure of the stock solution chamber.

  As shown in FIG. 3, the concentration device 3 according to the second modified example is similar to the concentration device 1 described above, the membrane distillation cell 10, the heater 20, the concentrated liquid tank 30, the stock solution pump P <b> 1, 1 temperature sensor T1, cooler 40, coolant tank 50, coolant pump P2, second temperature sensor T2, flow rate sensor (liquid amount measuring means) F1, condensate tank 60, controller ( (Control part) 80, the undiluted | stock solution flow path 110, and the cooling fluid flow path 120 are provided.

  The concentrator 3 is different from the concentrator 1 in that a concentrator 3 (pressure adjusting means) V40 and a relief valve (pressure adjusting means) V50 are provided instead of the decompressor (pressure adjusting means) 70. Is a point. The concentration apparatus 3 according to the second modification is an apparatus that performs a concentration operation for increasing the concentration of a liquid based on the principle of membrane distillation in the same manner as the concentration apparatus 1 described above.

  The pressurizer V40 is installed on the stock solution flow path 110 at the exit of the stock solution chamber 10a. The pressurizer V40 is a pressure adjusting valve that opens and closes the stock solution flow path 110, closes the stock solution flow path 110, and freely pressurizes the internal pressure of the stock solution chamber 10a to a predetermined pressure. In the concentrating device 3, the stock solution flow path 110 is a closed system capable of adjusting the internal pressure.

  The relief valve V50 is installed on the exhaust path connected to the condensation chamber 10b. The relief valve V50 is a back pressure valve that can adjust the internal pressure on the primary side, and freely reduces the internal pressure in the condensing chamber 10b to a predetermined pressure. Therefore, the pressure difference between the stock solution chamber 10a and the condensing chamber 10b is adjusted to a predetermined value by the pressurizer V40 and the relief valve V50.

  Next, based on the operation method of the concentration apparatus 3, the concentration method according to the second modification will be described.

  The concentration method according to the second modification includes a stock solution chamber (first chamber) through which a stock solution is flowed, and a condensing chamber (second chamber) separated from the stock solution chamber by a porous membrane that selectively transmits vapor. In the membrane distillation cell, the temperature of the stock solution chamber side and the condensation chamber side is adjusted so as to have a predetermined temperature difference, and the amount of condensate produced by condensation of the vapor generated in the condensation chamber is set to a predetermined amount. In this method, the stock solution chamber is pressurized and the condensing chamber is decompressed to adjust the pressure difference between the stock solution chamber and the condensing chamber, that is, the atmospheric pressure difference.

  In the concentrating device 3, the stock solution is concentrated by membrane distillation batchwise. The stock solution is introduced from outside the system into the stock solution flow path 110 by opening the first valve V10, and after the first valve V10 is closed, the stock solution is pressurized by the stock solution pump P1 and introduced into the stock solution chamber 10a. . Further, the coolant is caused to flow through the coolant channel 120 by the coolant pump P2.

  When the undiluted solution is supplied to the membrane distillation cell 10, the controller 80 is configured so that the temperature difference between the undiluted solution flowing in the undiluted solution chamber 10a and the cooling plate 12 of the condensing chamber 10b is constant. 40 is controlled at a constant temperature within a predetermined temperature range. For example, the controller 80 feedback-controls the heater 20 and the cooler 40 based on the measured temperature, and adjusts the liquid temperature of the stock solution and the liquid temperature of the cooling liquid so as to be a predetermined constant temperature.

  The controller 80 closes the pressurizer V40 when the stock solution reaches a predetermined target heating temperature. The stock solution flows into the stock solution chamber 10a while generating steam in a state where the pressurizer V40 is closed, and the internal pressure of the stock solution chamber 10a is pressurized.

The controller 80 controls the pressurizer V40 and the relief valve V50 so that the amount of condensate generated in the condensation chamber 10b becomes the target amount (Q _p ). For example, referring to the target condensate amount (Q _p ) obtained based on the target concentration rate (C _f ) and the known stock solution amount (Q _f ), the amount of condensate generated in the condensing chamber 10 b is the target condensate amount. condensate amount (Q _p) and so as to control the opening of the pressurizer V40 and relief valve V50, to match the amount of condensate produced in condensing chamber 10b to the target condensate amount (Q _p). Then, the concentrated liquid concentrated to the target concentration rate (C _f ) is collected by opening the closed second valve V20 and third valve V30.

  According to the concentrating apparatus and the concentrating method according to the second modification described above, since the stock solution chamber is pressurized and the stock solution is subjected to membrane distillation, the concentration rate is set higher than in the case where only the decompression chamber is decompressed. be able to. In addition, since the stock solution is batch-distilled, it is easy to stabilize the amount of vapor that permeates the porous membrane, and a concentrated solution having a more accurate concentration rate can be obtained.

  Next, a concentration apparatus and a concentration method according to the third modification will be described.

FIG. 4 is a diagram showing a schematic configuration of a concentrating device according to a third modification of the present invention.
The concentration device according to the above embodiment can be a one-pass type concentration device (concentration device according to the third modification) in which the stock solution is simply charged into the membrane distillation cell.

  As shown in FIG. 4, the concentrating device 4 according to the third modified example, like the concentrating device 1, includes a membrane distillation cell 10, a heater 20, a stock solution pump P <b> 1, a first temperature sensor T <b> 1, A cooler 40, a coolant tank 50, a coolant pump P 2, a second temperature sensor T 2, a flow rate sensor (liquid amount measuring means) F 1, a condensate tank 60, and a decompressor (pressure adjusting means) 70 , A controller (control unit) 80 and a coolant flow path 120 are provided.

  The concentrating device 4 is different from the concentrating device 1 described above in that the concentrating liquid obtained by membrane distillation in the concentrating liquid chamber 10a is used instead of the concentrating liquid flow path 110 for re-inflowing into the concentrating liquid chamber 10a. It is the point provided with the concentrate feeding path 150 and the concentrated liquid collection path 160 for discharging the concentrated liquid out of the cell. The concentration apparatus 4 according to the third modification is an apparatus that performs a concentration operation for increasing the concentration of a liquid based on the principle of membrane distillation in the same manner as the concentration apparatus 1 described above.

  The stock solution input path 150 is connected to the inlet of the stock solution chamber 10a. The undiluted solution introduction path 150 is constituted by piping or the like, and forms a flow path for introducing undiluted solution from outside the system into the undiluted solution chamber 10a. A heater 20, a stock solution pump P1, and a stock solution temperature sensor T1 are installed on the stock solution feeding path 150, and the stock solution heated by the heater 20 is fed into the stock solution chamber 10a. .

  The concentrated liquid recovery path 160 is connected to the outlet of the stock solution chamber 10a. The concentrated liquid recovery path 160 is constituted by piping or the like, and forms a flow path for discharging and recovering the concentrated liquid from the stock solution chamber 10a to the outside of the system. On the concentrate recovery path 160, a concentrate tank 31 for receiving the concentrate concentrated in the stock solution chamber 10a is installed.

  Next, a specific operation method of the concentrating device 4 will be described.

In the concentrator 4, the stock solution is concentrated by membrane distillation batchwise. That is, the target concentration rate (C _f ) corresponding to the final concentration rate is preset, and the target condensate amount (Q _p ) to be generated in the condensing chamber corresponding to this is set as a control target value that can be referred to. 80. The stock solution is heated to a predetermined temperature by the heater 20 and is introduced into the stock solution chamber 10 a through the stock solution charging path 150. In addition, the coolant flows through the coolant channel 120.

When the undiluted solution is supplied to the membrane distillation cell 10, the controller 80 controls the heater 20 and the cooler 40 at a constant temperature within a predetermined temperature range in the same manner as in the concentration device 1 described above. At the same time, the decompressor 70 is controlled so that the amount of the condensate produced by condensing the vapor generated in the condensing chamber 10b becomes the target amount (Q _p ). Then, the concentrated liquid concentrated to the target concentration rate (C _f ) is discharged out of the system through the concentrated liquid recovery path 160 and recovered.

  According to the concentration apparatus according to the third modified example, the stock solution can be concentrated batchwise. Compared to the case where the concentrate is circulated and concentrated, fluctuations in vapor pressure become more dynamic, and specifications such as membrane distillation cell dimensions, porous membrane area, and the flow rate of the concentrate tend to be restricted. On the other hand, it is possible to simplify the control for heating and cooling to a constant temperature, the apparatus constituent members, and the like.

  The concentration device 1 according to the embodiment, the concentration device 2 according to the first modification, the concentration device 3 according to the second modification, and the concentration device 4 according to the third modification are as follows. It can also be.

  For example, in the concentration apparatus 1 according to the above-described embodiment, the concentration apparatus 2 according to the first modification, the concentration apparatus 3 according to the second modification, and the concentration apparatus 4 according to the third modification, the heater 20 is It is provided outside the membrane distillation cell 10, and the stock solution flowing through the stock solution channel 110 and the stock solution input channel 150 is heated. However, instead of this, the heater 20 may be installed in the stock solution chamber 10a and the stock solution may be heated inside the stock solution chamber 10a.

  Further, in the concentration apparatus 1 according to the above-described embodiment, the concentration apparatus 2 according to the first modification, the concentration apparatus 3 according to the second modification, and the concentration apparatus 4 according to the third modification, the membrane distillation cell 10 However, it is an indirect contact type that cools the vapor that has permeated through the porous film 11 on the cooling plate 12 that is separated to the opposite side of the porous film 11. However, instead of this, it is also possible to adopt a direct contact type in which the vapor that has permeated through the porous membrane 11 is absorbed by the coolant flowing on the opposite side of the porous membrane 11. That is, the membrane distillation cell has a two-part configuration of a stock solution chamber (first chamber) and a condensing chamber (second chamber), and the stock solution chamber and the condensing chamber are separated by a porous membrane, and the outlet of the condensing chamber and the condensing chamber You may provide the cooling fluid flow path which connects between inlets by piping etc. In other words, the coolant channel can circulate the coolant in the condensation chamber, and the coolant flowing in the condensation chamber can cool the vapor generated in the condensation chamber. In the direct contact type, the pressure of the condensate may be determined by adjusting the pressure in the condensing chamber through which the coolant flows, and subtracting the initial amount of coolant from the amount of coolant after film distillation.

  Further, in the concentrating device 1 according to the embodiment, the concentrating device 2 according to the first modified example, the concentrating device 3 according to the second modified example, and the concentrating device 4 according to the third modified example, the condensing chamber 10b includes A flow rate sensor F1 for measuring the amount of condensate is installed in the connected drainage path. However, the amount of condensate may be measured based on changes in liquid level and liquid weight in addition to the flow rate. In addition to the drainage path, a liquid level measuring means for measuring the amount of condensate is installed in the exhaust path, the vapor exhausted from the exhaust path is condensed to measure the liquid level, and the condensation discharged from the drainage path You may make it grasp | ascertain the total amount of condensate by adding the quantity of liquid and the quantity discharged | emitted from an exhaust passage.

  Further, in the concentrating device 1 according to the embodiment, the concentrating device 2 according to the first modified example, and the concentrating device 4 according to the third modified example, the pressure difference between the stock solution chamber 10a and the condensing chamber 10b is adjusted. Therefore, a decompression pump is provided as the decompressor 70. However, instead of this, a vacuum pressure reducing system may be provided on the exhaust side, and a back pressure valve capable of adjusting the pressure may be installed and used.

  In addition, the concentrating device 3 according to the second modification includes a pressurizer V40 and a relief valve V50 in order to adjust the pressure difference between the stock solution side and the cooling side. However, instead of this, even if the pressure difference between the stock solution chamber 10a and the condensing chamber 10b is adjusted by installing only the pressurizer V40 capable of pressurizing the pressure of the stock solution chamber and controlling only the pressurizer V40. Good. Further, a pressure adjusting pump may be used in place of the pressurizer V40 using the pressure adjusting valve and the relief valve V50.

  Further, in the concentrating device 4 according to the third modified example, the single membrane distillation cell 10 is provided, and the concentrated liquid is discharged out of the system through the concentrated liquid recovery path 160. However, instead of this, it is also possible to connect a plurality of membrane distillation cells 10 in series and connect the concentrate recovery path 160 to the stock solution input path 150 of the next apparatus. In this case, each condensing chamber 10b may be individually regulated.

  Next, a beverage production system using a concentrating device will be described.

  The concentration apparatus 1 according to the above embodiment, the concentration apparatus 2 according to the first modification, the concentration apparatus 3 according to the second modification, and the concentration apparatus 4 according to the third modification are other apparatuses for beverage production. -It can be set as the drink manufacturing system which manufactures concentrated fruit juice and fermented drinks using fruit as a raw material by organizing with an apparatus.

FIG. 5 is a block diagram showing a schematic configuration of the beverage production system.
As shown in FIG. 5, the beverage production system 200 includes a press machine 201, a pre-filter 202, a concentrator 203, a hot water regulator 204, a heat exchanger 205, a heat source 206, a sterilizer 207, and a fermentation A tank 208, a filter 209, a storage tank 210, a filter 211, and a filling machine 212 are provided.

  In the beverage production system 200, fruits such as grapes and apples are squeezed by a squeezing machine 201, and juice that is a raw material for concentrated fruit juice and fermented beverages is squeezed. The fruit juice is then removed from the skin, flesh, and other foreign matters by the pre-filter 202, and then fed into the concentrator 203. The pre-filter 202 can be combined with a filter that removes particles of 2 microns (μm) or less that may pass through the membrane of the concentrator or cause clogging.

  The concentrator 203 is provided to remove moisture and increase the concentration of fruit juice. As the concentrating device 203, the concentrating device according to the above-described embodiment or the concentrating device according to the modification is applied. The concentrator 203 heats the fruit juice to a predetermined temperature of less than 90 ° C. using warm water in order to evaporate the water in the fruit juice and perform film distillation. The hot water is heated in the heat exchanger 205 using the thermal energy supplied from the heat source 206, and is supplied from the hot water regulator 204 to the heater (20) of the concentrating device 203.

  When producing concentrated fruit juice, the fruit juice is concentrated to the concentration ratio with a target concentration ratio set so that the sugar content and acidity are not less than specified. The fruit juice concentrated in the concentrator 203 is pasteurized by the sterilizer 207 and then filled into various containers. The concentrated fruit juice produced in this way is transported, stored, etc., and then diluted and reduced with water to become a fruit drink.

  On the other hand, when producing a fermented beverage, the fruit juice is concentrated to the concentration rate with a target concentration rate set so as to have a sugar content suitable for alcohol fermentation. For example, for grape juice, the sugar content is concentrated in the range of about 15-30. The fruit juice concentrated in the concentrator 203 is subjected to alcohol fermentation with yeast or the like in the fermenter 208. After the fermentation, the filter is removed by the filter 209, and the storage tank 210 further stores and matures the liquor. Then, it is clarified by the filter 211 and bottled by the filling machine 212 to obtain a fermented beverage such as wine.

  According to the above beverage production system, since the concentrating device 203 is provided, the concentrated fruit juice concentrated to a predetermined concentration rate or a predetermined sugar content is obtained regardless of the quality of fruit, variety, storage conditions after harvesting, etc. A fermented fermented beverage can be obtained. That is, even if the use of the concentrated fruit juice is any of concentrated fruit juice for concentration and reduction, fermented beverages, etc., the fruit juice stably concentrated to the target concentration rate is obtained in the single concentrator 203. be able to.

  In the beverage manufacturing system 200 described above, the concentrating device 203 is provided in the front stage of the fermenter 208 to remove moisture from the fruit juice. However, the concentrator 203 may be provided in the subsequent stage of the fermenter 208 to remove the alcohol content of the post-fermentation liquid. In the concentrator 203, the alcohol content can be concentrated to a predetermined concentration rate, and therefore, a non-alcoholic beverage or a beverage with a high alcohol content can be produced freely.

DESCRIPTION OF SYMBOLS 1 Concentrator 2 Concentrator 3 Concentrator 4 Concentrator 10 Membrane distillation cell 10a Stock solution chamber (first chamber)
10b Condensing chamber (second chamber)
10c Cooling room (third room)
11 Porous membrane 12 Cooling plate (heat transfer wall)
20 Heater 30 Concentrated liquid tank 40 Cooler 50 Cooling liquid tank 60 Condensed liquid tank 70 Depressurizer (pressure adjusting means)
80 Controller (control unit)
90 heat exchanger 110 undiluted liquid flow path 120 cooling liquid flow path 130 heat medium pipe 150 undiluted liquid input path 160 concentrated liquid recovery path F1 flow rate sensors H1, H2,... Hn heat source P1 undiluted liquid pump P2 cooling liquid pump P3 heat medium pump ( Flow rate adjustment means)
T1 Stock solution temperature sensor T2 Coolant temperature sensors V1, V2,... Vn On-off valve (heat source switching means)
V10 1st valve V20 2nd valve V30 3rd valve V40 Pressurizer (pressure adjusting means)
V50 Relief valve (pressure adjusting means)

Claims (10)

A membrane distillation cell having a first chamber through which the stock solution is flowed, and a second chamber separated from the first chamber by a porous membrane that selectively permeates vapor;
A heater for heating the stock solution;
A cooler for cooling the second chamber;
Pressure adjusting means for adjusting the pressure difference between the first chamber and the second chamber by changing the pressure of the first chamber or the second chamber;
A controller that controls the heater, the cooler, and the pressure adjusting means,
The control unit controls the heater and the cooler to a predetermined temperature range, and adjusts the pressure so that the amount of condensate produced by condensing the vapor generated in the second chamber becomes a predetermined amount. A concentrating device characterized by controlling the means.   The control unit refers to a target amount of the condensate obtained based on a preset target concentration rate and the amount of the stock solution flowing into the first chamber, and the condensate generated in the second chamber The concentration apparatus according to claim 1, wherein the pressure adjusting unit is controlled so that the amount becomes the target amount. A third chamber separated from the second chamber by a heat transfer wall;
A cooling liquid flow path connecting the outlet of the third chamber and the inlet of the third chamber and circulating a cooling liquid in the third chamber;
The cooler cools the coolant flowing through the coolant flow path;
The concentrator according to claim 1 or 2, wherein the heat transfer wall cooled by the coolant flowing through the third chamber cools the steam generated in the second chamber. A cooling liquid flow path for connecting the outlet of the second chamber and the inlet of the second chamber and circulating the cooling liquid in the second chamber;
The cooler cools the coolant flowing through the coolant flow path;
The concentrating apparatus according to claim 1 or 2, wherein the cooling liquid flowing through the second chamber cools the vapor generated in the second chamber.   The pressure adjusting means is a decompressor capable of depressurizing the pressure in the second chamber, a pressurizer capable of depressurizing the pressure in the first chamber, or both the depressurizer and the pressurizer. The concentration apparatus according to any one of claims 1 to 4.   The apparatus further comprises a concentrate flow path that connects between the outlet of the first chamber and the inlet of the first chamber and reflows the concentrated solution in which the concentrate is concentrated into the first chamber. The concentrating device according to any one of claims 1 to 5. A heat source capable of supplying thermal energy to the heater;
A flow rate adjusting means for adjusting a flow rate of the heat medium that mediates the thermal energy, and
The concentrator according to any one of claims 1 to 6, wherein the controller controls the amount of heat given to the stock solution by the heater by adjusting a flow rate of the heat medium. A plurality of heat sources capable of supplying thermal energy to the heater;
Heat source switching means for switching a heat source that gives the heat energy to the heater among the plurality of heat sources, and
The concentration according to any one of claims 1 to 7, wherein the control unit controls the amount of heat given to the stock solution by the heater by switching the heat source among the plurality of heat sources. apparatus. The first chamber through which the stock solution flows, the second chamber separated from the first chamber by a porous membrane that selectively permeates vapor, and the heat transfer wall that condenses the vapor that has permeated the porous membrane. A membrane distillation cell having a third chamber, which is separated from the two chambers and into which the cooling liquid is allowed to flow;
A heater for heating the stock solution;
A cooler for cooling the coolant;
Pressure adjusting means for adjusting the pressure difference between the first chamber and the second chamber by reducing the pressure in the second chamber;
A controller that controls the heater, the cooler, and the pressure adjusting means,
The control unit controls the heater and the cooler to a predetermined temperature range, and adjusts the pressure so that the amount of condensate produced by condensing the vapor generated in the second chamber becomes a predetermined amount. A concentrating device characterized by controlling the means. In a membrane distillation cell having a first chamber through which a stock solution is flowed and a second chamber separated from the first chamber by a porous membrane that selectively transmits vapor,
The temperature of the first chamber side and the second chamber side of the porous membrane is adjusted so as to have a predetermined temperature difference, and the amount of condensate produced by condensing the vapor generated in the second chamber is A concentration method comprising adjusting a pressure difference between the first chamber and the second chamber so as to be a predetermined amount.

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