JP2005111319A - Method and apparatus for concentrating liquid raw material - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a new method and a new apparatus for concentrating a liquid raw material in each of which concentration efficiency can be enhanced by using the thermal energy of a heating medium to be discharged from a heating boiler with high efficiency and accelerating the evaporation rate of the liquid raw material in the heating boiler. <P>SOLUTION: After the liquid in a long pipe 11 of the heating boiler 1 is heated, the heating medium discharged from the heating boiler 1 is sent to a preheater 5 to heat the liquid raw material L0 before being supplied to an evaporator 2 through the preheater 5. The heating medium is composed of a drain D produced by condensing the vapor component S0 in the heating boiler 1 and uncondensed gas S2. As a result, the liquid raw material L0 can furthermore be heated by the latent heat to be generated when the uncondensed gas S2 heats the liquid raw materia L0 and condenses. Since the thermal energy of both of the uncondensed gas S2 and the drain D is supplied to the liquid raw material L0, the liquid raw material L0 can be heated to a high temperature. <P>COPYRIGHT: (C)2005,JPO&NCIPI

Description

  The present invention relates to an apparatus used for concentrating various seasonings, various extracts, factory waste liquids, etc., and can particularly reduce running costs and increase the evaporation rate of liquid components in a heating can. The present invention relates to a concentrating method that can be performed and an apparatus therefor.

Traditionally, various liquid substances such as herbal medicine extracts, various seasonings, animal extracts, seafood extracts, plant extracts, fermented liquor, etc., aqueous solutions such as amino acids, yeasts, proteins, etc. or various waste liquids are used as liquid raw materials. Various apparatuses are used for concentration.
This type of apparatus is roughly divided into a heat pump type concentrator C ′ using a vertical heating can 1 ′ shown in FIG. 6 and a heat pump type concentrator C using a horizontal heating can 1 ′ shown in FIG. In any type of apparatus, the solvent component of the liquid raw material L0 is evaporated in a pipe line 11 ′ provided in the heating can 1 ′, and the heating can 1 ′ is used as a heat source for this purpose. The steam component S0 discharged to the outside is heated by the compressor 7 'to be steam S1, and then passed outside the pipe 11'.

A part of the steam S1 after supplying heat to the liquid raw material L0 is discharged to the outside as an uncondensed gas S2, and a part of the steam S1 is condensed and discharged to the outside as a drain D. Therefore, it has been attempted to increase the evaporation efficiency by raising the temperature of the liquid raw material L0 by the thermal energy of the uncondensed gas S2 and the drain D and putting it in the heating can 1 ′.
Specifically, in the apparatus shown in FIG. 6, the uncondensed gas S2 discharged from the heating can 1 ′ is cooled and condensed by a preheater 5 ′ to which a vent condenser is applied. The liquid raw material L0 passing through 'is heated by receiving vapor latent heat (see Patent Document 1).
Further, in the apparatus shown in FIG. 7, the drain D condensed in the long tube 11 'is led to the preheater 5' to raise the temperature of the liquid raw material L0, and the heated liquid raw material L0 is charged into the heating can 1 '. (See Patent Document 2).

However, as described above, although an attempt has been made to preheat the liquid raw material L using either the uncondensed gas S2 or the drain D discharged from the heating can 1 ′, the heat recovery efficiency is sufficient. That wasn't true.
For this reason, the temperature of the liquid raw material L0 when entering the long pipe 11 'is low, and it takes time until the liquid raw material L0 boils in the long pipe 11'. As described above, the liquid region having a low thermal conductivity increases, which causes a reduction in the processing capacity of the heating can 1 ′.
Japanese Patent No. 3226316 (pages 3 to 4, FIG. 1) Japanese Utility Model Publication 2-39521 (pages 3-4, FIG. 1)

  The present invention has been made in view of such a background, and makes efficient use of the thermal energy of the heating medium discharged from the heating can with high efficiency and increases the evaporation rate of the liquid material in the heating can. Development of a novel liquid raw material concentration method and apparatus capable of improving the concentration efficiency is a technical issue.

That is, in the method for concentrating liquid raw material according to claim 1, a circulation path is formed by connecting a heating can and an evaporator through a blow pipe and a return pipe, and after being supplied into the evaporator, The liquid flowing into the long pipe arranged in the heating can through the return pipe is boiled by heating from the vapor supplied to the outside of the long pipe to evaporate the solvent component, thereby increasing the concentration of the liquid component and the vapor. In the method of obtaining a high concentration liquid by blowing the components into the evaporator and separating the liquid component and the vapor component in the evaporator, after supplying heat to the liquid in the long pipe, The discharged heating medium is sent to a preheater, and the temperature of the liquid raw material before being supplied to the evaporator is raised in the preheater. The heating medium sent to the preheater is a vapor component in the heating can. Those comprising as a feature that is condensed with drain and uncondensed gas generated.
According to the present invention, since the uncondensed gas that has heated the liquid material releases latent heat when it condenses, the liquid material can be further heated by this latent heat. Moreover, since heat energy can be supplied with respect to a liquid raw material from both uncondensed gas and drain, a liquid raw material can be made into high temperature.

In addition to the above requirements, the liquid raw material concentration method according to claim 2 further includes a temperature sensor in front of the inlet of the heating medium in the preheater, and the amount of air in the heating medium is determined based on the detected value of the temperature sensor. Judging and adjusting the opening of the valve provided in the pipe line connecting between the preheater and the vacuum pump according to the air amount, the exhaust amount from the preheater is adjusted. is there.
According to this invention, the temperature drop of the heating medium in the preheater can be avoided.

In addition to the above requirements, the liquid raw material concentration method according to claim 3 is characterized in that the liquid raw material heated by the preheater is further heated by a second preheater and supplied to the evaporator. It consists of.
According to the present invention, it is possible to reduce the temperature drop of the liquid component caused by the liquid raw material being charged into the evaporator, and to shorten the time until the liquid component boils in the long pipe.

Further, the liquid raw material concentrating device according to claim 4 forms a circulation path by connecting between the heating can and the evaporator by a blowing pipe and a return pipe, and after being supplied into the evaporator, The liquid flowing into the long pipe arranged in the heating can through the return pipe is boiled by heating from the vapor supplied to the outside of the long pipe to evaporate the solvent component, thereby increasing the concentration of the liquid component and the vapor. In an apparatus for obtaining a high-concentration liquid by blowing the components into the evaporator and separating the liquid component and the vapor component in the evaporator, the evaporation is performed after the heating medium outlet of the heating can. The preheater is provided with a preheater for raising the temperature of the liquid raw material before being supplied to the can. The preheater has a pipe for allowing the liquid raw material to pass through the shell and is heated outside the pipe. Also let the medium pass The area below the drain outlet formed in the shell is an area where the temperature of the liquid material is raised by the drain, and the area above is an area where the temperature of the liquid material is raised by the uncondensed gas. It consists of.
According to the present invention, since the uncondensed gas that has heated the liquid material releases latent heat when it condenses, the liquid material can be further heated by this latent heat. Moreover, since heat energy can be supplied with respect to a liquid raw material from both uncondensed gas and drain, a liquid raw material can be made into high temperature.

Furthermore, in addition to the requirements of claim 4, the liquid raw material concentrating device according to claim 5 includes a temperature sensor in front of the inlet of the heating medium in the preheater, and further between the preheater and the vacuum pump. It is characterized by having a valve in the connecting pipe line.
According to this invention, by detecting a temperature drop, the amount of air in the heating medium can be detected, and a temperature drop in the preheater can be avoided.

Furthermore, the liquid raw material concentrating device according to claim 6 is a second preheater for further raising the temperature of the liquid raw material between the preheater and the evaporator in addition to the requirements of 4 or 5. It is characterized by having.
According to the present invention, it is possible to reduce the temperature drop of the liquid component caused by the liquid raw material being charged into the evaporator, and to shorten the time until the liquid component boils in the long pipe.
The above problems can be solved by using the configuration of the invention described in each of the claims as a means.

  According to the present invention, the thermal energy discharged from the heating can in the first preheater is efficiently used with high efficiency, and the temperature of the liquid raw material before being put into the evaporator is raised, and further in the second preheater Since the temperature of the liquid material is increased, the evaporation rate of the liquid material in the heating can can be increased. As a result, the running cost of the concentrator can be reduced and the production efficiency of the concentrate can be increased.

  Hereinafter, the liquid raw material concentration method and apparatus of the present invention will be described with reference to the drawings. First, the configuration of the liquid raw material concentration apparatus will be described, and then the liquid raw material will be combined with the operation mode of the apparatus. The concentration method of will be described.

What is indicated by a symbol C in the figure is the concentrating device of the present invention, which is formed by connecting the heating can 1 and the evaporator 2 by a blow-in conduit 3 and a return conduit 4. Then, the liquid raw material L0 introduced into the long tube 11 disposed in the heating can 1 is boiled by heating from the steam S1 supplied to the outside of the long tube 11, thereby evaporating the solvent component and increasing the concentration. In this device, the liquid component L1 and the vapor component S0 are blown into the evaporator 2, and the liquid component L1 and the vapor component S0 are separated in the evaporator 2.
In this embodiment, as the steam S1, the steam component S0 separated in the evaporator 2 is used after being heated by the compression pump 7.

Hereinafter, various members constituting the concentrating device C will be described in detail.
First, the heating can 1 will be described. The heating can 1 is provided with a plurality of long pipes 11 which are pipes made of a heat-resistant material such as metal in a casing 10 with confidentiality as shown in FIG. The lower end of the long tube 11 is in communication with the liquid supply port 12 formed in the lower portion of the casing 10, while the upper end of the long tube 11 is in communication with the discharge port 13 formed in the upper portion of the casing 10. It consists of.
Further, a steam port 14 and a drain port 15 are formed in a side peripheral portion of the housing 10. Note that the fluid flowing from both the liquid supply port 12 through the long pipe 11 to the discharge port 13 and the flow channel from the vapor port 14 to the drain port 15 do not interfere with each other. Thus, only thermal energy moves between the two flow paths.
Furthermore, a steam supply device 9 is connected to the steam port 14 formed in the heating can 1.

Next, the evaporator 2 will be described. In this case, as shown in FIG. 2, for example, an exhaust port 21 is formed in the upper part of the casing 20 which is a hollow member having a shape in which an inverted conical part is connected to the lower part of the cylindrical part. The inlet 22 is formed on the upper side of the side periphery.
A nozzle 82 is disposed in the housing 20, and the liquid material L 0 stored in the liquid supply tank 8 is ejected from the nozzle 82. The ejection amount of the liquid raw material L0 is adjusted by adjusting the opening degree of the valve 81.

And between the discharge port 13 in the heating can 1 and the inflow port 22 in the evaporator 2 is connected in a communicating state by a blow pipe 3, and the liquid supply port 12 in the heating can 1 and the lower part of the evaporator 2 Are connected to each other by a return line 4. As a result, a circulation path including the evaporator 2, the return pipe 4, the long pipe 11, and the blowing pipe 3 is formed.
The return conduit 4 is formed with a concentrate discharge port 41, and is configured so that the concentrated liquid component L1 can be discharged to the outside by opening the valve.

  Further, the exhaust port 21 in the evaporator 2 is connected to the compression pump 7 by a pipe 71, and a demister 72 is provided between the compression pump 7 and the evaporator 2 side in the pipe 71. The output side of the compression pump 7 is connected to a steam port 14 in the heating can 1.

The liquid raw material L0 supplied into the evaporator 2 is configured to be heated by the first preheater 5 and the second preheater 6.
The preheater 5 will now be described. As shown in FIG. 3, the preheater 5 includes a pipe 51 for allowing the liquid raw material L0 to pass through a hollow shell 50, and a heating medium outside the pipe 51. The liquid raw material L0 introduced into the raw material liquid inlet 52 receives thermal energy from the heating medium in the process of passing through the pipe 51, and is discharged from the raw material liquid outlet 53 in a heated state. The
Further, the preheater 5 includes a portion where the temperature of the liquid raw material L0 is increased by the uncondensed gas S2 which is a heating medium discharged from the evaporator 2, and a liquid raw material which is also drained as a heating medium discharged from the evaporator 2. A portion where the temperature of L0 is raised is formed, and an area E1 where the temperature of the liquid raw material L0 is raised by the drain D is lower than the discharge port 56 formed in the side wall portion of the shell 20. The area E2 above the outlet 56 is an area E2 where the temperature of the liquid raw material L0 is increased by the uncondensed gas S2.
That is, the heat medium supplied into the shell 50 from the heat medium inlet 54 formed in the upper part of the shell 50 is uncondensed gas S2 and drain D, and the drain D is discharged from the outlet 56 by the vacuum pump P. Therefore, a portion above the discharge port 56 is a space where the uncondensed gas S2 is accumulated. A valve 57 is provided between the discharge port 56 and the vacuum pump P. Further, a temperature sensor T is provided in a pipe line connecting the drain port 15 in the heating can 1 and the heat medium inlet 54 in the preheater 5.

Furthermore, the deaeration port 55 formed in the upper part of the shell 50 is connected to the vacuum pump P by an appropriate pipe line, and this pipe line is branched into two paths on the way. A valve 58 and a valve 59 are provided.
As shown in FIG. 1, a second preheater 6 to which an electric heater is applied is provided between the first preheater 5 and the evaporator 2 as an example.

  As shown in FIG. 4, a pipe line can be positioned in the shell 50, and the tip of this pipe line can be used as the discharge port 56.

The concentration apparatus C of the present invention is configured as described above as an example, and the liquid raw material concentration method of the present invention will be described below together with the operation mode of this apparatus.
[Initial operation]
First, the vacuum pump P is activated to reduce the pressure in the system of the concentrating device C, and the valves 57, 58 and 59 are operated as appropriate to connect the evaporator 2, the heating can 1 and the preheater 5 to each other. The inside is depressurized.
Next, steam is supplied from the steam supply device 9 into the heating can 1, and the steam that has passed through the outside of the long tube 11 aggregates to become a drain D, is discharged from the drain port 15, and reaches the preheater 5.

In this state, by opening the valve 81, various liquid substances such as herbal medicine extracts, various seasonings, animal extracts, seafood extracts, plant extracts, fermentation liquids, aqueous solutions such as amino acids, yeasts, proteins, or various waste liquids And the like as a liquid raw material L0, and the liquid raw material L0 is heated when passing through the first preheater 5 and the second preheater 6. The principle of raising the temperature of the liquid raw material L0 by the preheater 5 will be described in detail later.
The liquid raw material L0 supplied into the evaporator 2 from the nozzle 82 is supplied into the long can 11 in the heating can 1 via the return pipe 4, and boils inside the long tube 11 by the heat conducted from the steam. Then, when the generated vapor component S0 rises in the long pipe 11, the liquid component L1 is pulled up. The vapor component S0 and the liquid component L1 ascend in the long pipe 11 to reach the discharge port 13 and enter the blow-in pipe 3 from there, and then flow into the housing 20 from the inlet 22 in the evaporator 2. .

Then, the vapor component S0 and the liquid component L1 are separated in the housing 20, and the vapor component S0 reaches the compression pump 7 from the exhaust port 21, where the temperature is raised to become the vapor S1, and the heating can 1 is supplied to the steam port 14 in FIG. At this time, mist, dust and the like contained in the vapor component S0 are removed by the demister 72.
On the other hand, the liquid component L1 accumulates in the lower part of the housing 20 and is supplied from here through the return line 4 to the liquid supply port 12 in the evaporator 1.
By continuing such operation, the concentrated liquid component L1 is again located in the long tube 11 in the heating can 1 with the new liquid raw material L0 supplied from the nozzle 82, and further concentrated. Is done.

  Eventually, when the temperature in the system sufficiently rises, the steam supply device 9 is stopped, the valves 58 and 59 are closed, and a steady operation is started.

(Steady operation)
Hereinafter, the operation mode of the concentrating device C when in a steady operation will be described.
First, the liquid raw material L0 (temperature 20 ° C.) stored in the liquid supply tank 8 is supplied to the raw material liquid inlet 52 in the preheater 5 and is heated to about 70 ° C. when passing through the pipe 51. It will be discharged | emitted from the raw material liquid outlet 53. FIG.
Here, the principle of sound rise of the liquid raw material L0 by the preheater 5 will be described. Inside the shell 50, as shown in FIG. 3, the drain D is stored up to about half the height, and the upper part is filled with the uncondensed gas S2. It has become. That is, the vacuum pump P is connected to the discharge port 56 provided in the side wall portion of the shell 50, and the drain D is discharged by the action of the vacuum pump P. Therefore, the position of the discharge port 56 is the upper limit level of the drain D. The area below the discharge port 56 is an area E1 where the temperature of the liquid material L0 is raised by the drain D, while the area above the discharge port 56 is the area where the temperature of the liquid material L0 is raised by the uncondensed gas S2. E2.
In the process of passing through the pipe 51, the liquid material L0 is first heated by receiving heat energy from the drain D, and then further heated by receiving heat energy from the uncondensed gas S2.

In the area E2, since the latent heat is released when the uncondensed gas S2 that has heated the liquid material L0 in the long tube 11 is condensed in the heating can 1, the liquid material L0 is further heated by the latent heat. Become. Further, since the uncondensed gas S2 is condensed to become the drain D, this further heats the liquid raw material L0 in the long tube 11 in the area E1.
The ratio of the drain D discharged from the drain port 15 in the heating can 1 and taken into the preheater 5 to the uncondensed gas S2 is about 95: 5, and both the drain D and the uncondensed gas S2 are used as heat sources. By doing so, about twice as much heat as that obtained when only the drain D is used as a heat source can be obtained.
Further, since the liquid raw material L0 contains air and further leaks of the apparatus itself, the drain D and the uncondensed gas S2 discharged from the drain port 15 contain air. As the amount increases, the detection value of the temperature sensor T decreases. Therefore, the opening degree of the valve 57 is adjusted in accordance with the detected value, and the valve 58 is further opened to release the air in the shell 50 from the deaeration port 55 to the outside. By such an operation, a temperature drop of the heating medium in the shell 50 is avoided.

Subsequently, the liquid raw material L0 heated to about 70 ° C. by the first preheater 5 is heated to 80 to 85 ° C. by the second preheater 6 and then charged into the evaporator 2 from the nozzle 82. The
The liquid raw material L0 is mixed with the concentrated liquid component L1 at the bottom of the evaporator 2, and then reaches the long tube 11 in the heating can 1 where the solvent evaporates. At this time, the liquid raw material L0 is concentrated with the liquid raw material L0. Since the mixed liquid with the liquid component L1 can maintain a high temperature state of 80 to 85 ° C., it immediately boils in the long tube 11. For this reason, as shown in FIG. 5, the liquid region having a low thermal conductivity is slightly reduced, the evaporation rate is increased, and the processing capacity of the heating can 1 is increased.
The temperatures of the heating medium discharged from the heating can 1, that is, the uncondensed gas S2 and the drain D are 100 ° C. and 70 ° C., respectively.

The operation as described above is continued, and when the liquid component L1 reaches a desired concentration, the valve 42 is opened, and the concentrated liquid component L1 is discharged to the outside.
As described above, according to the present invention, the uncondensed gas S2 that has heated the liquid raw material L0 in the preheater 5 releases latent heat when condensed, so that the liquid raw material L0 can be further heated by this latent heat. Moreover, since heat energy can be supplied with respect to the liquid raw material L0 from both the uncondensed gas S2 and the drain D, the liquid raw material L0 can be made high temperature.
Further, by detecting a temperature drop, an abnormal increase in air can be detected, and a temperature drop of the heating medium in the preheater 5 can be avoided.
Furthermore, the temperature drop of the liquid component L1 caused by the liquid raw material L0 being charged into the evaporator 2 can be reduced, and the time until the liquid component L1 boils in the long tube 11 can be shortened.

It is a side view which shows the whole concentration apparatus of this invention skeletally. It is a side view which shows a heating can and an evaporating can partially partially. FIG. 3 is a side view showing a part of the first preheater. It is a side view seeing through and showing the 1st preheater which provided the discharge port in the shell. It is a side view seeing through the long tube in an evaporator. It is a side view which shows the whole existing concentration apparatus skeleton. It is a side view which shows the whole existing concentration apparatus skeleton.

Explanation of symbols

C Concentrator 1 Heating Can 10 Case 11 Long Pipe 12 Supply Port 13 Discharge Port 14 Steam Port 15 Drain Port 2 Evaporator 20 Case 21 Exhaust Port 22 Inlet 3 Blow-in Line 31 Duct 4 Return Line 41 Concentrated Liquid Outlet 42 Valve 5 Preheater (first)
50 Shell 51 Pipe line 52 Raw material liquid inlet 53 Raw material liquid outlet 54 Heat medium inlet 55 Deaeration port 56 Outlet port 57 Valve 58 Valve 59 Valve 6 Preheater (second)
7 Compression pump 71 Pipe line 72 Demister 8 Supply tank 81 Valve 82 Nozzle 9 Steam supply device D Drain E1 Area E2 Area L0 Liquid raw material L1 Liquid component P Vacuum pump S0 Steam component S1 Steam S2 Uncondensed gas

Claims (6)

  A circulation path is formed by connecting the heating can and the evaporator through a blow pipe and a return pipe, and after being supplied into the evaporator, the inside of the long pipe disposed in the heating can through the return pipe The liquid that has flowed into the tube is boiled by heating from the vapor supplied to the outside of the long pipe to evaporate the solvent component, and the liquid component and vapor component having increased concentrations are blown into the evaporator, and the evaporator In the method of obtaining a high concentration liquid by separating the liquid component and the vapor component inside, after supplying heat to the liquid in the long tube, the heating medium discharged from the heating can is sent to the preheater, and this preheating is performed. The temperature of the liquid raw material before being supplied to the evaporator in the vessel is raised, and the heating medium fed into the preheater is composed of drain and uncondensed gas generated by condensing vapor components in the heater. Ah The method of concentrating the liquid material, characterized in that.   A temperature sensor is provided in front of the inlet of the heating medium in the preheater, and the amount of air in the heating medium is determined based on the detected value of the temperature sensor, and the space between the preheater and the vacuum pump is determined according to the amount of air. 2. The method for concentrating liquid raw material according to claim 1, wherein the amount of exhaust from the preheater is adjusted by adjusting the opening of a valve provided in the connecting pipe line.   3. The liquid raw material concentration method according to claim 1, wherein the liquid raw material heated by the preheater is further heated by a second preheater and supplied to the evaporator.   A circulation path is formed by connecting the heating can and the evaporator through a blow pipe and a return pipe, and after being supplied into the evaporator, the inside of the long pipe disposed in the heating can through the return pipe The liquid that has flowed into the tube is boiled by heating from the vapor supplied to the outside of the long pipe to evaporate the solvent component, and the liquid component and vapor component having increased concentrations are blown into the evaporator, and the evaporator In the apparatus for separating the liquid component and the vapor component in the inside to obtain a high-concentration liquid, the temperature of the liquid raw material before being supplied to the evaporator can be increased after the heating medium outlet of the heating can. The preheater comprises a pipe for passing the liquid raw material in the shell, and allows the heating medium to pass outside the pipe, and is formed in the shell. Drain The lower than the outlet, the liquid material and the area of heating by the drain, whereas, concentrator of the liquid material, characterized in that the area for raising the temperature of the liquid material upwardly by uncondensed gas.   5. The liquid raw material concentrating device according to claim 4, further comprising: a temperature sensor provided in front of the inlet of the heating medium in the preheater, and a valve provided in a pipe line connecting the preheater and the vacuum pump.   6. The liquid raw material concentrating device according to claim 4, further comprising a second preheater for further raising the temperature of the liquid raw material between the preheater and the evaporator.

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