JP5806489B2 - Concentrating device provided with centrifugal thin film vacuum evaporator and method of operating the same - Google Patents

Description

  The present invention relates to a centrifugal thin film vacuum evaporator, and more particularly to a concentrating device provided with a centrifugal thin film vacuum evaporator capable of realizing an operation with energy saving and an operation method thereof.

As a concentration device for various solutions, a single-effect can-type concentration device, a multi-effect can-type concentration device, a vapor compression concentration device, and the like are widely used. The thermal efficiency of these devices is about 0.8 to 0.9 for the single effect can type concentrator, about 1.4 for the multi effect can type concentrator, and about 4 to 7 for the vapor compression type concentrator.
By the way, in a heating operation such as evaporation and concentration of a substance susceptible to thermal denaturation, it is necessary to perform a desired operation by applying a predetermined amount of heat at a low temperature in a short time (see, for example, Non-Patent Document 1). The effect can type concentrator and the vapor compression type concentrator cannot be used.
First, the multi-effect can-type concentrator has a high processing temperature of 70 ° C. or higher, and the residence time of the concentrated liquid in the machine becomes long from 4 minutes to several hours. Cannot be used.
In addition, when handling chemicals, foods, etc., it is required that the apparatus has a high detergency. However, in the case of a multi-effect can type concentrator, the configuration of the apparatus is complicated, which is not suitable.

In addition, although the vapor compression type concentrator is a heat-efficient and energy-saving system, the energy consumption of the compressor increases in proportion to the compression ratio (discharge pressure / suction pressure), and suction is performed from a lower pressure environment. Even in this case, energy consumption becomes large. The operation of such a vapor compression type concentrator is usually performed with a suction pressure of 20 to 70 kPa (abs) and a temperature-converted compression ratio of 5 to 15 ° C. (the temperature of the discharge gas with respect to the temperature of the suction gas). Is raised at 5 to 15 ° C.), the temperature of the concentrate becomes as high as 60 to 90 ° C., and the residence time in the apparatus becomes as long as 10 to 60 minutes.
For the reasons described above, a vapor compression concentrator cannot be used when handling a substance that is susceptible to thermal denaturation.

Therefore, an apparatus for concentrating a substance susceptible to thermal denaturation has been put into practical use, and even the present applicant provides the market with a centrifugal thin film vacuum evaporator 1 as shown in FIG. For example, see Patent Document 1). In this apparatus, a rotating body 3 having a mortar-shaped evaporation plate 31 is provided in a casing 2 in which an internal space can be evacuated. Then, the evaporation plate 31 is heated by supplying the steam S to the heating unit 40, and the raw material liquid L0 supplied to the center of the evaporation plate 31 is moved toward the outer periphery by centrifugal force for about one second. A volatile component evaporates at a concentrated liquid temperature of 50 ° C. or lower to obtain a concentrated liquid L1. For this reason, in order to keep the concentrated liquid temperature at 50 ° C. or lower (12 kPa (abs) or lower), cooling water at 40 ° C. or lower flows through the condenser 8 connected to the casing 2.
In addition, the casing 2 is configured to be split at the connection portion 25, and is excellent in cleanability and maintainability.
However, the centrifugal thin-film vacuum evaporator 1 as described above is classified as a single-effect can as the structure, so that the thermal efficiency is low, and there is room for improvement in this respect, but the centrifugal thin-film vacuum evaporator 1 In order to generate high-temperature steam that satisfies the conditions required for the above, an apparatus such as a boiler is required, and it has been recognized that there is a limit to improving thermal efficiency.

"<Food Engineering Basic Account> 6 Concentration and Drying, Kozo Co., Ltd., August 31, 1989, P26, 27" Utility Model Registration No. 2590568

  The present invention has been made in view of such a background. In particular, high-temperature steam satisfying the conditions required for a centrifugal thin film vacuum evaporator is heated by the heat discharged from the centrifugal thin film vacuum evaporator. As a technical problem, the development of a concentrating device equipped with a novel centrifugal thin-film vacuum evaporation device capable of improving the thermal efficiency and realizing an energy-saving operation by using the above-mentioned method and its operating method was made a technical problem.

That is, the concentrating device provided with the centrifugal thin film vacuum evaporator according to claim 1 is provided with a rotating body having a mortar-shaped evaporation plate in a casing, and a raw material supply formed near the rotation center of the evaporation plate On the surface, a raw material liquid supply pipe is provided with its tip facing, and a weir plate is provided near the outermost periphery of the evaporation plate, and a condensate discharge pairing tube is provided near the tip of the evaporating plate. And a heating part for supplying steam to the back side of the evaporation plate is formed, and the raw material liquid supplied to the raw material supply surface generates heat from the evaporation plate in the process of moving on the evaporation plate. In the concentrating device provided with the centrifugal thin film vacuum evaporator configured to evaporate and concentrate the volatile component by evaporation, and then discharge the concentrated liquid to the outside by the pairing tube, Thin film vacuum The heat discharged from the source device, by taking the heat medium, the configured so that it can serve as a heat source for the steam generator for generating steam to be supplied to the heating unit made by, and the steam generator In addition, a preheater for preheating water before becoming steam with a refrigerant of the heat pump is provided between the condenser and the expansion valve in the heat pump. It is characterized in that it is configured to generate steam at 120 ° C. by using carbon dioxide as a refrigerant .

  In addition to the requirement of claim 1, the concentrating device provided with the centrifugal thin film vacuum evaporator according to claim 2 has a heat provided as a heat source when generating steam supplied to the heating unit, The heat is contained in the vapor component evaporated from the raw material liquid.

  Furthermore, the concentrating device provided with the centrifugal thin film vacuum evaporator according to claim 3 is provided as a heat source when generating the steam supplied to the heating unit in addition to the requirements of claim 1 or 2. This heat is the heat contained in the gas or liquid mixture of drain or drain and steam discharged from the heating unit.

Furthermore, the concentrating device provided with the centrifugal thin film vacuum evaporator according to claim 4 adds auxiliary steam to the steam generated by the steam generator in addition to the requirements of claim 1, 2, or 3. It is characterized by being configured to be able to.

Furthermore, the concentrating device provided with the centrifugal thin film vacuum evaporator according to claim 5 is a cooling device for cooling the heat medium supplied to the evaporator in the heat pump in addition to the requirements of claim 1 or 4. It is characterized by having a vessel.

Furthermore, the concentrating device provided with the centrifugal thin film vacuum evaporator according to claim 6 is for heating the heat medium supplied to the evaporator in the heat pump in addition to the requirements of claim 1, 4 or 5. It is characterized by comprising a preheater.

According to a seventh aspect of the present invention, there is provided a method of operating a concentrating device provided with a centrifugal thin film vacuum evaporator, wherein a rotating body having a mortar-shaped evaporation plate is provided in a casing, and is formed near the rotation center of the evaporation plate. The raw material supply surface is provided with a raw material liquid supply pipe facing the tip, and a barrier plate is provided near the outermost periphery of the evaporation plate, and a condensate discharge pairing tube is provided near the barrier plate. Is formed with a heating portion to which steam is supplied on the back side of the evaporation plate, and the raw material liquid supplied to the raw material supply surface moves in the process of moving on the evaporation plate. Operation of an apparatus provided with a centrifugal thin film vacuum evaporator configured to evaporate and concentrate volatile components by receiving heat from the liquid, and then discharge the concentrated liquid to the outside through the pairing tube In the centrifugal type The heat discharged from the membrane vacuum evaporator, by taking the heat medium is intended to serve as a heat source of the steam generator for generating steam to be supplied to the heating unit, as the steam generator, steam generator In addition, a preheater is provided between the condenser and the expansion valve in this heat pump to preheat water before it becomes steam with the refrigerant of the heat pump. In addition, by using carbon dioxide as a refrigerant, an apparatus configured to generate steam at 120 ° C. is used .

Furthermore, the operation method of the concentrating device provided with the centrifugal thin film vacuum evaporator according to claim 8 is used as a heat source when generating the steam supplied to the heating unit in addition to the requirements of claim 7. The heat to be generated is heat contained in the vapor component evaporated from the raw material liquid.

Furthermore, the operation method of the concentrating device provided with the centrifugal thin film vacuum evaporator according to claim 9 is the heat source for generating the steam supplied to the heating unit in addition to the requirements of claim 7 or 8. The heat provided as is characterized in that it is the heat contained in the drain or the gas-liquid mixture of drain and steam discharged from the heating section.

Furthermore, the operation method of the concentrating device provided with the centrifugal thin film vacuum evaporator according to claim 10 is not limited to the requirement of claim 7 , and is an auxiliary device for generating steam to be supplied to the heating unit. It is characterized by adding steam.

Furthermore the method of operating or claim 11 concentrator centrifugal thin-film vacuum evaporator was equipped according, in addition to the requirements of the claims 7 or 10, wherein cooling the heat medium supplied to the evaporator in the heat pump It is characterized by this.

Furthermore, the operation method of the concentrating device provided with the centrifugal thin film vacuum evaporator according to claim 12 is the requirement of claim 11 , and the cooling of the heat medium is performed by a cooler to which a heat exchanger is applied. The temperature of the circulating recooled water supplied to the cooler is set to 40 ° C. or lower.

Furthermore, the operation method of the concentrating device provided with the centrifugal thin film vacuum evaporator according to claim 13 is a heat pump discharged from a condenser connected to the casing in addition to the requirements of claim 7, 11 or 12. The heating medium supplied to the evaporator is heated.
The above-described problems can be solved by using the requirements described in these claims as means.

First, according to the first aspect of the present invention, the heat discharged from the centrifugal thin film vacuum evaporator is transferred to the heat medium, and then used as a heat source when generating steam to be supplied to the centrifugal thin film vacuum evaporator. Since it is used, the energy efficiency of the entire apparatus can be improved. At this time, the state of the vapor can be made suitable for a centrifugal thin film vacuum evaporator.
In addition, the characteristics of the centrifugal centrifugal thin film vacuum evaporator (prone to thermal degradation) due to the device composed of a novel combination of a centrifugal thin film vacuum evaporator and a steam generating heat pump, which is not found in existing concentrators It is possible to concentrate the liquid to be treated, and it can be operated with energy saving while taking advantage of the ability to handle foods and pharmaceuticals.
Furthermore, since the water supplied to the steam generator is supplied to the condenser in a preheated state by the refrigerant discharged from the condenser, the temperature of the steam generated in the condenser can be increased. The energy saving property can be further improved.

  Further, according to the invention described in claim 2, since the temperature of the heat medium serving as the heat source of the steam generating device can be raised by the heat contained in the vapor component evaporated from the raw material liquid, energy saving can be improved.

  Furthermore, according to the third aspect of the present invention, the heat medium serving as the heat source of the steam generator can be heated by the heat contained in the drain or the gas-liquid mixture of the drain and the steam. Can be increased.

Furthermore, according to the invention described in claim 4 , even when the total amount of heat in the vapor component discharged from the centrifugal thin film vacuum evaporator is reduced and the efficiency of the steam generator using this heat as a heat source is reduced, the centrifugal component is centrifuged. The conditions of the vapor supplied to the thin film thin film vacuum evaporator can be kept constant.

Furthermore, according to the invention described in claim 5, the amount of heat taken into the heat medium fluctuates or is excessive when the concentration and flow rate of the raw material liquid fluctuate for some reason when the concentrator is started up or in operation. For this reason, the temperature of the heat medium may not be stabilized at a constant value, but even in such a case, the temperature of the heat medium can be maintained at a constant value.

Furthermore, according to the invention described in claim 6, the amount of heat taken into the heat medium is insufficient or fluctuates when the concentration and flow rate of the raw material liquid fluctuate for some reason when the concentrator is started up or in operation. For this reason, there may occur a situation where the temperature of the heat medium is not stabilized at a constant value. Even in such a case, the temperature of the heat medium can be maintained at a constant value.

According to the seventh aspect of the present invention, the heat contained in the vapor component evaporated from the raw material liquid is transferred to the heat medium in the condenser, and then the vapor supplied to the centrifugal thin film vacuum evaporator is generated. Since it is used as a heat source at the time, the energy efficiency of the entire apparatus can be improved. At this time, the state of the vapor can be made suitable for a centrifugal thin film vacuum evaporator.
In addition, the characteristics of the centrifugal centrifugal thin film vacuum evaporator (prone to thermal degradation) due to the device composed of a novel combination of a centrifugal thin film vacuum evaporator and a steam generating heat pump, which is not found in existing concentrators It is possible to concentrate the liquid to be treated, and it can be operated with energy saving while taking advantage of the ability to handle foods and pharmaceuticals.
Furthermore, since the water supplied to the steam generator is supplied to the condenser in a preheated state by the refrigerant discharged from the condenser, the temperature of the steam generated in the condenser can be increased. The energy saving property can be further improved.

According to the eighth aspect of the present invention, the temperature of the heat medium serving as the heat source of the steam generator can be raised by the heat contained in the vapor component evaporated from the raw material liquid, so that energy saving can be improved.

Furthermore, according to the ninth aspect of the present invention, the temperature of the heat medium serving as the heat source of the steam generator can be raised by the heat contained in the drain or the gas-liquid mixture of drain and steam. Can be increased.

Furthermore, according to the invention described in claim 10 , even when the total amount of heat in the steam component discharged from the centrifugal thin film vacuum evaporator is reduced and the efficiency of the steam generator using this heat as a heat source is lowered, the centrifugal component is reduced. The conditions of the vapor supplied to the thin film thin film vacuum evaporator can be kept constant.

Furthermore, according to the invention described in claim 11, the amount of heat taken into the heat medium fluctuates or is excessive when the concentration and flow rate of the raw material liquid fluctuate for some reason when the concentrator is started up or in operation. For this reason, the temperature of the heat medium may not be stabilized at a constant value, but even in such a case, the temperature of the heat medium can be maintained at a constant value.

Furthermore, according to the invention described in claim 12, in the case of foods and pharmaceuticals that need to be concentrated in a short time of about 1 second at a processing temperature of 50 ° C. or lower, the processing temperature can be maintained at 50 ° C. or lower, that is, by centrifugation. The cooling capacity of the condenser for maintaining the vacuum pressure in the casing of the thin film vacuum drying apparatus can be maintained.

Furthermore, according to the invention described in claim 13, the amount of heat taken into the heat medium is insufficient or fluctuates when the concentration and flow rate of the raw material liquid fluctuate for some reason when the concentrator is started up or in operation. For this reason, there may occur a situation where the temperature of the heat medium is not stabilized at a constant value. Even in such a case, the temperature of the heat medium can be maintained at a constant value.

It is a block diagram which shows the concentration apparatus of this invention demonstrated as Example 1. FIG. It is the cross-sectional view and longitudinal cross-sectional view which show the rotary body accommodated in the casing and the casing. It is a block diagram which shows the concentration apparatus of this invention demonstrated as Example 2. FIG. It is a block diagram which shows the concentration apparatus of this invention demonstrated as Example 3. FIG. Is a block diagram showing an enrichment device you described as reference example 4. Is a block diagram showing an enrichment device you described as Reference Example 5. It is a block diagram which shows the concentration apparatus of this invention demonstrated as Example 6. FIG. Examples 1 , 2, 3 and 6 and the operating conditions of the concentrator described as Reference Examples 4 and 5 ; P. It is a table | surface which shows the thermal efficiency of COP, power consumption and thermal efficiency, and another concentrating apparatus.

  Hereinafter, the “concentrating device provided with the centrifugal thin film vacuum evaporator and the operation method thereof” of the present invention will be described first with respect to the centrifugal thin film vacuum evaporator 1 and peripheral devices constituting the concentrating device E. The operation method of the present invention will be described together with the operation mode.

As shown in FIG. 1, the centrifugal thin film vacuum evaporator 1 includes a rotating body 3 having an evaporation plate 31 in a casing 2 in which an internal space can be evacuated. Then, the evaporation plate 31 is heated by the steam S, and the volatile component evaporates in about one second during which the raw material liquid L0 supplied near the rotation center of the evaporation plate 31 moves toward the outer peripheral portion by centrifugal force. Concentration of the raw material liquid L0 is performed.
The concentration device E of the present invention can treat substances that are susceptible to heat denaturation, such as medicines, foods, etc., and can be used for antibiotic solutions, enzyme solutions, amino acid seasoning solutions, green tea, tea, fruit juice, etc. It can be handled as the raw material liquid L0.
Hereinafter, the components of the centrifugal thin film vacuum evaporator 1 will be described in detail with reference to FIG.

First, the casing 2 has a hollow cylindrical container in a laid-down state. An exhaust pipe 21 is connected to an appropriate upper portion, and a drain port 24 is formed at an appropriate lower portion. Is.
Further, the casing 2 is configured to be divided at the connection portion 25 for maintenance and the like, and further includes an inspection window 26 through which the inside can be visually observed.

  Next, the rotating body 3 will be described. In this structure, a mortar-shaped evaporation plate 31 is provided on a rotating shaft 30 that is rotationally driven by a motor M provided outside the casing 2.

Further, the deepest portion of the mortar-shaped evaporation plate 31 is formed so as to be orthogonal to the axial direction of the rotary shaft 30 to be a raw material supply surface 31a, and the raw material is disposed so that the discharge port faces the raw material supply surface 31a. A liquid supply pipe 5 is provided. In this embodiment, the raw material liquid supply pipe 5 is configured to be provided at two places, and the respective connection systems will be described later. When distinguishing the raw material liquid supply pipes 5 provided at two places, the respective reference numerals are handled differently from the raw material liquid supply pipe 51 and the raw material liquid supply pipe 52.
Further, a scattering prevention plate 32 is provided in the vicinity of the discharge port of the raw material liquid supply pipe 5.
Furthermore, a dam plate 33 is provided at the open end of the evaporation plate 31 over the entire circumference, and the liquid suction port 60 can face a connecting portion between the dam plate 33 and the evaporation plate 31. A pairing tube 6 is rotatably provided.

Further, the outer cover plate 4 is provided in a jacket shape on the back side of the evaporation plate 31, and a heating unit 40 is formed between the evaporation plate 31 and the outer cover plate 4. By adopting such a configuration, when the steam S is supplied from the steam supply port 41 to the heating unit 40 (the back side of the evaporation plate 4), the evaporation plate 31 is heated.
The heating unit 40 is provided with a condensate recovery pipe 7 so that the liquid suction port 70 faces the boundary between the evaporation plate 31 and the outer cover plate 4. The condensate recovery pipe 7 is provided with a drain. Connected to the mouth 42.

  By adopting the configuration as described above, the steam supplied to the heating unit 40 during about one second when the raw material liquid L0 supplied to the center of the evaporation plate 31 moves toward the outer peripheral part by centrifugal force. The volatile component of the raw material liquid L0 is evaporated and concentrated by the heat of S.

  Next, other peripheral devices constituting the concentrating device E and their connection modes will be described. Here, the peripheral devices and their connection modes in the first embodiment shown in FIG. 1 and the second embodiment shown in FIG. 3 will be described, and the peripheral devices and their connection modes in the third to sixth embodiments will be described. The explanation will be given as needed when explaining the examples.

First, as shown in FIG. 1, a raw material liquid tank T0 for containing the raw material liquid L0 is connected to the raw material liquid supply pipe 51 via a raw material liquid supply pump P0.
Further, a concentrate tank T1 is connected to the pairing tube 6 with a concentrate discharge pump P1 interposed therebetween.
The conduit connecting the concentrated liquid discharge pump P1 and the concentrated liquid tank T1 is branched, and this branched path is connected to the raw material liquid tank T0. A concentration sensor 53 is provided between the branch point and the concentrate discharge pump P1, and a valve V4 is provided between the branch point and the concentrate tank T1, and further, the branch point and the raw material liquid tank T0. Between the two, a valve V3 is provided.
Further, the drainage port 24 of the raw material liquid L0 scattered in the casing 2 and the raw material liquid supply pipe 52 are connected by an appropriate pipe line, and a return pump P5 is provided in this pipe line.
Furthermore, a vacuum pump P3 and a separator 9 are connected to the drain port.

Further, the exhaust pipe 21 is connected to the introduction port 81 of the capacitor 8, and the distillate discharge pump P <b> 2 and the distillate tank T <b> 2 are connected to the discharge port 82. The condenser 8 is a device for condensing the vapor component supplied to the introduction port 81, and for this reason, the cooling water C is configured to pass through an appropriate pipe line inside the condenser 8.
The evaporator 103 in the steam generator 10 is connected to the cooling water supply port 83 and the cooling water discharge port 84, and a heat medium that circulates in the closed circuit by the heat source water pump P6 is used as the cooling water C.
A vacuum pump P4 is connected to the vent 85 in the capacitor 8.

Here, the steam generator 10 will be described. This is configured by combining the heat pump 100 and the preheater 110 as an example.
The heat pump 100 includes a condenser 101, an expansion valve 102, an evaporator 103, and a compressor 104 to form a heat pump cycle. As an example, one using carbon dioxide as a refrigerant is employed. In addition, the temperature of the water W heated by the heat pump 100 can be increased by using carbon dioxide as the refrigerant. In the future, when a heat pump 100 having an equivalent performance using other refrigerants is put into practical use, this can be adopted.
A preheater 110 to which a heat exchanger or the like is applied is disposed between the condenser 101 and the expansion valve 102, and the water W supplied from the outside exchanges heat with the refrigerant in the preheater 110. Is supplied to the condenser 101 in a state where the temperature is raised (preheated). Next, in the condenser 101, the water W is further heated by heat exchange with the refrigerant to become steam S, and is supplied to the steam supply port 41 in the centrifugal thin film vacuum evaporator 1.

In addition, a pipe line provided with valves V1 and V2 is connected to a pipe line connecting the condenser 101 and the steam supply port 41 with respect to the steam S generated by the condenser 101. and excess steam generated in the device, which consists, as may be incorporated an auxiliary steam S1, generated by another appropriate device. In Examples 4 and 5 to be described later, the auxiliary steam S1 is not used, so the illustration of the supply mechanism of the auxiliary steam S1 (FIGS. 5 and 6) is omitted, but the auxiliary steam S1 is used. Such a supply mechanism shall be provided.

In addition, when the concentrator E is started up or in operation, or when the concentration and flow rate of the raw material liquid L0 fluctuate for some reason, the amount of exchange heat in the condenser 8 may be insufficient, fluctuate, or become excessive. is there. At this time, since the temperature of the cooling water C1 is not stabilized at a constant value, in order to stabilize, the cooling for cooling the cooling water C1 between the heat source water pump P6 and the evaporator 103 (path of the cooling water C1). Any one or both of the heater 120 and the preheater 121 for heating the cooling water C1 shall be provided.
In this embodiment, a heat exchanger is adopted as the cooler 120 and the preheater 121, and a temperature sensor 105 is provided in the vicinity of the inlet of the cooling water C1 in the evaporator 103, and detection of the temperature sensor 105 is performed. Based on the value, the amount of circulating re-cooled water W1 flowing to the cooler 120 or the amount of auxiliary steam S2 flowing to the preheater 121 can be controlled to stabilize the temperature of the cooling water C1 at a predetermined value.
Moreover, about the said cooler 120 and the preheater 121, a Peltier device, an electric heater, etc. can also be used besides the heat exchanger mentioned above.

Although not shown in the drawings, the steam generator 10 may be configured to generate hot air by the heat pump 100 and generate steam S by heating the water W using the hot air.
In addition, the preheater 110 may not be provided depending on conditions such as the performance of the heat pump 100 and the temperature of the water W (for example, Examples 4 and 5 described later).

The concentrator E (E1, E2) shown in Examples 1 and 2 is configured as described above, and the operation method of the concentrator E will be described below.
In the operation of the concentrator E, a method of making the gas-liquid mixture of the steam S and the drain D discharged from the heating unit 40 one-pass and a method of circulating use are selected. A method of using one pass will be described as Examples 1 to 3, and a method of circulating use will be described as Examples 4 to 6.

[Example 1] (See FIG. 1, C1: 37 ° C., C2: 32 ° C., with auxiliary steam S1, without auxiliary steam S2, without circulating recooled water W1, treatment temperature 50 ° C., L0: amino acid seasoning solution)
(1) [Startup operation]
First, the inside of the casing 2 is evacuated, and the vacuum pump P4 is activated to discharge the air in the casing 2 to 12.3 kPa (abs) as an example.
Next, the motor M is started to rotate the rotating body 3 (400 to 1500 rpm).
Further, the heat source water pump P6 is started to circulate the cooling water C1 as a heat medium, and the auxiliary steam S2 is supplied to the preheater 121, and the temperature of the cooling water C1 is set to a desired value (37 ° C. in this embodiment). And

(2) [Generation and supply of steam]
On the other hand, the steam generator 10 generates steam S. When the compressor 104 is started and the refrigerant is circulated, the refrigerant heats the cooling water C1 (37 ° C. in this embodiment) in the evaporator 103. At the same time, heat is transferred to the water W in the preheater 110 and the condenser 101. At this time, the temperature of the cooling water C2 after transferring the heat is 32 ° C.
And the water W becomes the vapor | steam S (120 degreeC 0.1MPaG 900kg / h) suitable for supplying to the centrifugal thin film vacuum evaporation apparatus 1 in the condenser 101, and the vapor | steam supply port in the centrifugal thin film vacuum evaporation apparatus 1 41.
In this embodiment, by adding auxiliary steam S1 (120 ° C., 0.1 MPaG, 100 kg / h) to steam S, the amount of steam supplied to centrifugal thin film vacuum evaporator 1 becomes 1000 kg / h. I did it.
Then, the steam S supplied to the steam supply port 41 reaches the inside of the heating unit 40 and is condensed after the evaporation plate 31 is heated to become the drain D. Through the condensate recovery pipe 7 by the suction action of the vacuum pump P3. The gas-liquid mixture sent to the separator 9 is divided into air A and drain D and discharged to the outside. A part of the steam S is discharged from the drain port 42 together with the drain D without condensing.

(3) [Supply and concentration of raw material solution]
Then, the raw material liquid supply pump P0 is activated to supply the raw material liquid L0 from the raw material supply pipe 51 to the raw material supply surface 31a. The raw material liquid L0 moves on the evaporation plate 31 toward the outer peripheral portion by centrifugal force. In about 1 second, it reaches the weir plate 33. During this time, it is heated by the evaporation plate 31, and the volatile component evaporates to become the concentrated liquid L1.
The concentrated liquid L1 is blocked by the dam plate 33, and is sent from the pairing tube 6 to the concentrated liquid tank T1 by the suction action of the concentrated liquid discharge pump P1 (valve V3 closed, valve V4 opened).
In this embodiment, the pressure in the space to which the raw material liquid L0 is supplied in the casing 2 is 12.3 kPa (abs), that is, the processing temperature is 50 ° C.

(4) [Heat recovery from exhausted steam component to coolant]
On the other hand, the vapor component evaporated from the raw material liquid L0 is taken into the condenser 8 from the exhaust pipe 21 by the suction action of the vacuum pump P4. Here, heat exchange is performed with the cooling water C2 (32 ° C.). While the cooling water C2 is heated to become the cooling water C1 (37 ° C.), the vapor component becomes the distillate L2, and is stored in the distillate tank T2 by the distillate discharge pump P2.
In this embodiment, since the supply of the raw material liquid L0 from the raw material liquid supply pipe 5 to the evaporation plate 31 is a one-pass method, the steam S supplied from the steam generator 10 to the centrifugal thin film vacuum evaporator 1 is always the same. Since the amount of heat taken into the cooling water C2 in the condenser 8 is always constant, stable operation can be performed.

[Example 2] (See FIG. 3, C1: 52 ° C., C2: 47 ° C., no auxiliary steam S1, no auxiliary steam S2, no circulating re-cooled water W1, processing temperature 65 ° C., L0: green tea)
Next, Example 2 shown in FIG. 3 will be described. The concentrator E2 shown in the second embodiment and the concentrator E1 shown in the first embodiment have the same device configuration, and the second embodiment is an embodiment in which the operating conditions are different. Specifically, the steam S generated by the steam generator 10 is in a state (120 ° C., 0.1 MPaG, 1000 kg / h) suitable for supplying to the centrifugal thin film vacuum evaporator 1, The auxiliary steam S1 was not mixed.
The temperature of the cooling water C1 is 52 ° C., the temperature of the cooling water C2 is 47 ° C., and the pressure of the space in the casing 2 to which the raw material liquid L0 is supplied is 25.0 kPa (abs), that is, the processing temperature. Was set to 65 ° C.

[Example 3] (See FIG. 4, C1: 55 ° C., C2: 50 ° C., no auxiliary steam S1, no auxiliary steam S2, no circulating re-cooled water W1, processing temperature 50 ° C., L0: fruit juice)
Next, Example 3 shown in FIG. 4 will be described. The difference between the concentrator E3 shown in the third embodiment and the concentrator E2 shown in the second embodiment (the same applies to the concentrator E1) is that the temperature of the cooling water C1 heated by the condenser 8 in the second embodiment is 52. On the other hand, in Example 3, the heat of the gas-liquid mixture of the steam S and the drain D discharged from the drain port 42 in the centrifugal thin film vacuum evaporator 1 is cooled by the heating device 111 in the cooling water C2. In this way, the temperature of the cooling water C1 is set to 55 ° C. For this reason, in Example 3, the separator 91 is connected to the exhaust pipe 21 of the centrifugal thin film vacuum evaporator 1 with the vacuum pump P4 interposed therebetween, and the condenser 8 and the distillate discharge pump P2 are not used. did.
In Example 3, the steam S generated by the steam generator 10 is in a state (120 ° C., 0.1 MPaG, 1000 kg / h) suitable for supplying to the centrifugal thin film vacuum evaporator 1, and the steam S The auxiliary steam S1 was not mixed into the tank.
In addition, the temperature of the cooling water C2 was set to 50 ° C., and the pressure in the space in the casing 2 to which the raw material liquid L0 was supplied was 12.3 kPa (abs), that is, the processing temperature was set to 50 ° C.
In addition, although only the drain D may be discharged | emitted from the said drain port 42, the heat | fever of the drain D can be taken in into the cooling water C2 by the temperature rising device 111 also in this case.

Although not shown in the drawing, the configuration using the condenser 8 and the distillate discharge pump P2 can be adopted as in the first and second embodiments described so far. In this case, the evaporator 103 and the cooling water supply are used. What is necessary is just to connect the cooling water discharge port 84 and the temperature rising device 111 with a pipe line while connecting the port 83 with a pipe line.
Although illustration is omitted, a configuration using the cooler 120 and the preheater 121 can be adopted as in the first and second embodiments described so far. In this case, the heater 111 and the evaporator 103 are used. A cooler 120 and a preheater 121 may be provided in a pipe line connecting the two.

[ Reference Example 4] (See FIG. 5, C1: 16 ° C, C2: 8.7 ° C, no auxiliary steam S1, no auxiliary steam S2, circulating re-cooled water W1, treatment temperature 20 ° C, L0: antibiotic solution)
Next, Reference Example 4 shown in FIG. 5 will be described. The concentrating device E4 shown in the reference example 4 has the same basic configuration as the concentrating device E1 and the concentrating device E2, but the difference is that the steam S discharged from the heating unit 40 and the drain D are different. The point is that the gas-liquid mixture is recycled.
Therefore, a water tank 130 is provided between the steam supply port 41 and the drain port 42 and the condenser 101, and a separator 131 is further provided between the water tank 130 and the drain port 42.
A water pump P7 is provided between the water tank 130 and the condenser 101, and a liquid pump P8 is provided between the water tank 130 and the separator 131. Furthermore, an exhaust pipe is connected to the separator 131, and a valve V5 and a vacuum pump P9 are provided in this pipe.

By adopting such a configuration, the water tank 130 is filled with water W, and this water W is sent to the condenser 101 as circulating water W2 to form hot water W3. Further, this hot water W3 is supplied to the water tank 130. Supplying steam S is generated. And after this vapor | steam S is supplied to the heating part 40 and the evaporation plate 31 is heated, a part is condensed and it becomes the drain D, and the gas-liquid mixture of the vapor | steam S and the drain D passes through the separator 131, and is a water tank. While being returned to 130, it will be provided again as circulating water W2. In Example 4 and Example 5 described later, the water tank 130 is also a constituent element of the steam generator 10. It is assumed that water W is appropriately supplied into the water tank 130.
A cushion tank 140 and a heat source water pump P6 are provided between the preheater 121 and the evaporator 103.
In Reference Example 4, as an example, the temperature of the circulating water W2 is set to 80 ° C., and the temperature of the hot water W3 is set to 90 ° C.
Moreover, in this reference example 4, it is set as the state (80 degreeC, 47 kPa (abs), 900 kg / h) suitable for supplying the vapor | steam S produced | generated in the water tank 130 to the centrifugal thin film vacuum evaporation apparatus 1. FIG.
Since the auxiliary steam S1 is not mixed into the steam S, the description of the pipes provided with the valves V1 and V2 is omitted in FIG.
Further, since the temperature of the cooling water C1 discharged from the condenser 8 has reached 18.7 ° C., the temperature of the cooling water C1 at the time when it is supplied to the evaporator 103 is increased by supplying the circulating re-cooling water W1 to the cooler 120. It was set to 16.0 degreeC. The circulating re-cooled water W1 is generated by a chiller (not shown), and the power consumption of this chiller is 46 kW.
Further, the temperature of the cooling water C2 is set to 8.7 ° C., and the pressure of the space in the casing 2 to which the raw material liquid L0 is supplied is 2.3 kPa (abs), that is, the processing temperature is set to 20 ° C. did.

[ Reference Example 5] (See FIG. 6, C1: 37 ° C., C2: 30 ° C., no auxiliary steam S1, no auxiliary steam S2, circulating recooled water W1, treatment temperature 40 ° C., L0: enzyme solution)
Next, Reference Example 5 shown in FIG. 6 will be described. The concentrating device E5 shown in the reference example 5 has the same basic configuration as the concentrating device E4, except that the cooler 120 is omitted and the evaporator 103 and the cooling water supply port 83 are different. It is the point comprised so that the circulating re-cooling water W1 can be supplied to the pipe line which connects between.
And in this reference example 5 , let the vapor | steam S produced | generated in the water tank 130 be a state (80 degreeC, 47 kPa (abs), 600 kg / h) suitable for supplying to the centrifugal thin film vacuum evaporation apparatus 1. FIG.
Since the auxiliary steam S1 is not mixed into the steam S, the description of the pipes provided with the valves V1 and V2 is omitted in FIG.
Further, the temperature of the cooling water C2 was set to 30 ° C., and the circulating re-cooled water W1 of 32 ° C. was mixed in the cooling water C2 at 179 L / min so as to obtain the cooling water C3 of 30.5 ° C.
Further, the pressure of the space in the casing 2 to which the raw material liquid L0 is supplied is set to 7.3 kPa (abs), that is, the processing temperature is set to 40 ° C.
Furthermore, the temperature of the circulating water W2 was set to 80 ° C., and the temperature of the hot water W3 was set to 90 ° C.

[Example 6] (See FIG. 7, C1: 55 ° C., C2: 50 ° C., no auxiliary steam S1, no auxiliary steam S2, no circulating re-cooled water W1, treatment temperature 50 ° C., L0: green tea)
Next, Example 6 shown in FIG. 7 will be described. The concentrator E6 shown in the sixth embodiment has the same basic configuration as the concentrator E3 shown in the third embodiment, except that the steam S and the drain D discharged from the heating unit 40 are different. And the gas-liquid mixture.
For this reason, a water tank 130 is provided between the drain port 42 and the preheater 110. Further, a water pump P7 is provided between the water tank 130 and the preheater 110, and a liquid pump P8 is provided between the water tank 130 and the temperature raising device 111.
By adopting such a configuration, the water tank 130 is filled with water W, and this water W is sent to the condenser 101 as circulating water W2 to generate steam S. The steam S is heated by the heating unit 40. After the evaporation plate 31 is heated, a part is condensed to become drain D, and the gas-liquid mixture of steam S and drain D is returned to the water tank 130 via the temperature riser 111, It will be provided again as circulating water W2.
In Example 6, the steam S generated by the steam generator 10 is in a state suitable for supplying to the centrifugal thin film vacuum evaporator 1 (120 ° C., 0.1 MPaG, 1000 kg / h). The auxiliary steam S1 was not mixed into the tank.
In addition, the temperature of the cooling water C2 was set to 50 ° C., and the pressure in the space in the casing 2 to which the raw material liquid L0 was supplied was 12.3 kPa (abs), that is, the processing temperature was set to 50 ° C.

Although illustration is omitted, a configuration using the condenser 8 and the distillate discharge pump P2 can also be adopted as in Examples 1 and 2 and Reference Examples 4 and 5 described so far. In this case, evaporation is performed. The cooler 103 and the cooling water supply port 83 may be connected by a pipe, and the cooling water discharge port 84 and the temperature raising device 111 may be connected by a pipe.
Although illustration is omitted, a configuration using the cooler 120 and the preheater 121 can be adopted as in Examples 1 and 2 and Reference Examples 4 and 5 described so far. A cooler 120 and a preheater 121 may be provided in a pipe line connecting the condenser 111 and the evaporator 103.

[Comparison of COP and power consumption]
The operating conditions of Examples 1 , 2, 3 and 6 and Reference Examples 4 and 5 described above and P. COP, power consumption and thermal efficiency are compared using the table shown in FIG. Here H. P. COP means COP in the steam generator 10. The thermal efficiency means a value obtained by dividing energy used for evaporation by energy input to the concentrator E.

First, in the operation method of the first embodiment, H.P. P. It is COP2.5, thermal efficiency 1.96, thermal efficiency 0.8-0.9 of single-effect can type concentrator, higher efficiency than thermal efficiency 1.4 of multi-effect can type concentrator I can confirm.
Examples 2 , 3 and 6 and Reference Examples 4 and 5 deal with a raw material liquid L0 different from Example 1, but here, for reference, the power consumption and the like based on Example 1 Make a comparison.
First, in Example 2 where the temperature of the cooling water C1 that was 37 ° C. in the operation method of Example 1 was 52 ° C., H.P. P. It can be confirmed that the COP is 3.0 and the thermal efficiency is 3.0, and the power consumption is −44 kW (−16.7%) as compared with the first embodiment.
Further, in Example 3, H.P. P. It is COP3.1 and thermal efficiency 3.1, and it can be confirmed that it is -51 kW (-19.4%) as compared with Example 1.
In Reference Example 4, H.P. P. COP 2.8, thermal efficiency 2.80 (power consumption of the chiller is not included), and further, it can be confirmed that the power consumption is -61 kW (-23.2%) than the first embodiment. .
In Reference Example 5, H.P. P. COP3.4 and thermal efficiency are 3.40, and it can be confirmed that the power consumption is −151 kW (−57.4%) as compared with the first embodiment.
In Cited Example 6, H.P. P. It can be confirmed that the COP is 3.0 and the thermal efficiency is 3.00, and the power consumption is −59 kW (−22.4%) as compared with the first embodiment.

The above-described Examples 1 , 2, 3 and 6 and Reference Examples 4 and 5 are examples in which the supply of the raw material liquid L0 from the raw material liquid supply pipe 5 to the evaporation plate 31 is a one-pass method. Since the evaporation conditions in the above are always constant, the steam S supplied from the steam generator 10 to the centrifugal thin film vacuum evaporator 1 can always be set to the same condition and is recovered from the condenser 8. Since the amount of heat is always constant, stable operation can be performed.

[Other Examples]
Next, an embodiment in which the supply of the raw material liquid L0 from the raw material liquid supply pipe 5 to the evaporation plate 31 is a circulation system will be described.
Specifically, the supply of the raw material liquid L0 from the raw material liquid supply pipe 51 to the evaporation plate 31 is a circulation system, and the raw material liquid L0 supplied from the raw material liquid supply pipe 51 to the evaporation plate 31 is evaporated. It is heated when moving on the plate 31 toward the outer peripheral portion, and the volatile components are evaporated to become the concentrated liquid L1. Next, the concentrated liquid L1 is sucked from the pairing tube 6 and the concentration thereof is measured by the concentration sensor 53. When the measured concentration is lower than the desired concentration, the valve V4 is closed, The valve V3 is opened and returned to the raw material liquid tank T0. Then, the concentrated liquid L1 returned to the raw material liquid tank T0 is mixed with the raw material liquid L0 and supplied again to the evaporation plate 31 as the raw material liquid L0.
When such circulation is repeated, the concentration of the concentrate L1 eventually reaches a desired concentration, and when the measured value of the concentration sensor 53 reaches a desired value, the valve V3 is closed, and further the valve V4 is By being opened, the concentrate L1 is accumulated in the concentrate tank T1.

During operation in such a circulation system, the concentration of the raw material liquid L0 supplied from the raw material liquid supply pipe 51 to the evaporation plate 31 increases as the processing proceeds, and the vapor component sent to the condenser 8 and this vapor component The total amount of heat inside will decrease.
In this case, since the temperature of the cooling water C1 does not rise sufficiently, the auxiliary steam S2 is supplied to the preheater 121, and the temperature of the cooling water C1 is raised and then supplied to the evaporator 103, thereby improving the efficiency of the heat pump 100. Can be avoided.

  Further, during the operation in the circulation system as described above, the concentration of the raw material liquid L0 supplied from the raw material liquid supply pipe 51 to the evaporation plate 31 becomes higher as the processing proceeds, and the vapor component sent to the condenser 8 and this The total amount of heat in the steam component will decrease, and if the auxiliary steam S2 is not supplied to the preheater 121, the temperature of the cooling water C1 will not rise sufficiently, and the efficiency of the heat pump 100 using this heat as a heat source will decrease. End up. In that case, as in the first embodiment, the valves V1 and V2 are appropriately opened, and the auxiliary steam S1 is appropriately added to the steam S generated by the steam generator 10, thereby reducing the efficiency of the heat pump 100. However, the conditions of the steam S supplied to the centrifugal thin film vacuum evaporator 1 can be kept constant.

E Concentrator E1 Concentrator E2 Concentrator E3 Concentrator E4 Concentrator E5 Concentrator E6 Concentrator 1 Centrifugal Thin Film Vacuum Evaporator 2 Casing 21 Exhaust Pipe 24 Drainage Port 25 Connection Portion 26 Inspection Window 3 Rotating Body 30 Rotating Shaft 31 Evaporating plate 31a Raw material supply surface 32 Spattering prevention plate 33 Dam plate 4 Outer plate 40 Heating part 41 Steam supply port 42 Drain port 5 Raw material liquid supply pipe 51 Raw material liquid supply pipe 52 Raw material liquid supply pipe 53 Concentration sensor 6 Pairing tube 60 Liquid suction port 7 Condensate recovery pipe 70 Liquid suction port 8 Capacitor 81 Inlet port 82 Discharge port 83 Cooling water supply port 84 Cooling water discharge port 85 Venting port 9 Separator 91 Separator 10 Steam generator 100 Heat pump 101 Condenser 102 Expansion valve 103 Evaporator 104 Compressor 105 Temperature Sensor 110 Preheater 111 Temperature Increase DESCRIPTION OF SYMBOLS 120 Cooler 121 Preheater 130 Water tank 131 Separator 140 Cushion tank A Air D Drain L0 Raw material liquid L1 Concentrated liquid L2 Distilled liquid C Cooling water C1 Cooling water C2 Cooling water C3 Cooling water M Motor P0 Raw material liquid supply pump P1 Concentrated liquid discharge Pump P2 Distillate discharge pump P3 Vacuum pump P4 Vacuum pump P5 Return pump P6 Heat source water pump P7 Water pump P8 Liquid pump P9 Vacuum pump S Steam S1 Auxiliary steam S2 Auxiliary steam T0 Raw material tank T1 Concentrate tank T2 Distillate tank V1 Valve V2 valve V3 valve V4 valve V5 valve V6 needle valve W water W1 circulating re-cooled water W2 circulating water W3 hot water

Claims (13)

A rotating body having a mortar-shaped evaporation plate is provided in the casing, and a raw material supply surface formed near the rotation center of the evaporation plate is provided with a raw material liquid supply pipe facing its tip. A dam plate is provided near the outermost periphery of the evaporation plate, and a pairing tube for discharging the concentrate is provided in the vicinity of the dam plate so that the tip of the tube is faced, and steam is supplied to the back side of the evaporation plate. Part is formed, and the raw material liquid supplied to the raw material supply surface receives heat from the evaporation plate in the process of moving on the evaporation plate, thereby evaporating and concentrating the volatile components. In a concentrating device provided with a centrifugal thin film vacuum evaporator configured to be discharged to the outside by a pairing tube,
The heat exhausted from the centrifugal thin film vacuum evaporator is configured to be used as a heat source of a steam generator that generates steam supplied to the heating unit by taking in heat medium , and The steam generator includes a steam generation type heat pump, and further preheats water before becoming steam with a refrigerant of the heat pump between a condenser and an expansion valve in the heat pump. And a centrifugal thin film vacuum evaporator characterized by being able to generate steam at 120 ° C. by using carbon dioxide as a refrigerant. Concentrator.
The centrifugal thin-film vacuum evaporation according to claim 1, wherein the heat provided as a heat source when generating the steam supplied to the heating unit is heat contained in a vapor component evaporated from the raw material liquid. A concentrating device equipped with a device.
The heat provided as a heat source when generating the steam supplied to the heating unit is heat contained in a drain or a gas-liquid mixture of drain and steam discharged from the heating unit. A concentrator provided with the centrifugal thin film vacuum evaporator according to claim 1.
The concentration provided with the centrifugal thin-film vacuum evaporator according to claim 1, 2 or 3 , wherein auxiliary steam can be added to the steam generated by the steam generator. apparatus.
A centrifugal thin-film vacuum evaporator is equipped was concentrator according to claim 1 or 4, wherein in that it comprises a cooler for cooling the heat medium supplied to the evaporator in the heat pump.
A centrifugal thin-film vacuum evaporator was equipped concentrator of claim 1, 4 or 5, wherein in that it comprises a preheater for heating the heat medium supplied to the evaporator in the heat pump.
A rotating body having a mortar-shaped evaporation plate is provided in the casing, and a raw material supply surface formed near the rotation center of the evaporation plate is provided with a raw material liquid supply pipe facing its tip. A dam plate is provided near the outermost periphery of the evaporation plate, and a pairing tube for discharging the concentrate is provided in the vicinity of the dam plate so that the tip of the tube is faced, and steam is supplied to the back side of the evaporation plate. Part is formed, and the raw material liquid supplied to the raw material supply surface receives heat from the evaporation plate in the process of moving on the evaporation plate, thereby evaporating and concentrating the volatile components. In operation of a device comprising a centrifugal thin film vacuum evaporator configured to be discharged to the outside by a pairing tube,
The heat discharged from the centrifugal thin film vacuum evaporator is taken into a heat medium , and serves as a heat source of a steam generator for generating steam supplied to the heating unit ,
The steam generator is configured to include a steam generation type heat pump, and water before becoming steam is preheated by a refrigerant of the heat pump between the condenser and the expansion valve in the heat pump. A centrifugal thin film vacuum evaporator characterized by using a device configured to generate 120 ° C. vapor by employing carbon dioxide as a refrigerant. Operation method of the provided concentrator.
The centrifugal thin film vacuum evaporation according to claim 7 , wherein the heat provided as a heat source when generating the steam supplied to the heating unit is heat contained in a vapor component evaporated from the raw material liquid. A method of operating a concentrator concentrator provided with the apparatus.
The heat provided as a heat source when generating the steam supplied to the heating unit is heat contained in a drain or a gas-liquid mixture of drain and steam discharged from the heating unit. A method for operating a concentrator provided with the centrifugal thin film vacuum evaporator according to claim 7 or 8 .
The operation method of the concentrating device provided with the centrifugal thin film vacuum evaporator according to claim 7 , wherein auxiliary steam is added when generating steam to be supplied to the heating unit.
The operation method of the concentrating device provided with the centrifugal thin film vacuum evaporator according to claim 7 or 10, wherein a heat medium supplied to an evaporator in the heat pump is cooled.
The centrifuge according to claim 11, wherein the cooling of the heat medium is performed by a cooler to which a heat exchanger is applied, and a temperature of circulating recooled water supplied to the cooler is set to 40 ° C or less. Method of operating a concentrator equipped with a thin-film vacuum evaporator.
13. The concentrating device provided with the centrifugal thin film vacuum evaporator according to claim 7, 11 or 12, wherein a heat medium discharged from a condenser connected to the casing and supplied to an evaporator in a heat pump is heated. Driving method.

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