CN107913525B - Recovery device and recovery method for low boiling point substance - Google Patents
Recovery device and recovery method for low boiling point substance Download PDFInfo
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- CN107913525B CN107913525B CN201710416334.0A CN201710416334A CN107913525B CN 107913525 B CN107913525 B CN 107913525B CN 201710416334 A CN201710416334 A CN 201710416334A CN 107913525 B CN107913525 B CN 107913525B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/02—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in boilers or stills
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/28—Evaporating with vapour compression
- B01D1/2803—Special features relating to the vapour to be compressed
Abstract
The invention provides a low boiling point substance recovery device and a recovery method, which can recover low boiling point substances with high concentration and can realize energy saving. An ammonia recovery device (1) is provided with: a distillation column (2) into which steam for heating is blown and which is subjected to stripping; an evaporator (3) for evaporating water by heat exchange between the vapor containing ammonia discharged from the top of the distillation column and water; a compression device (4) which compresses and raises the temperature of the water vapor discharged from the evaporator and discharges the water vapor to the distillation tower as heating water vapor; a concentration tower (5) for introducing the ammonia-containing vapor concentrated by the evaporator, cooling the vapor to remove moisture, and increasing the concentration of the ammonia-containing vapor to a high concentration (for example, 20 wt% or more); a first absorption tower (6) for absorbing moisture from the ammonia-containing vapor from the concentration tower to produce recovered ammonia water having a predetermined concentration; and a second absorption tower (7) which prevents the uncondensed ammonia-containing vapor in the first absorption tower from being discharged to the outside.
Description
Technical Field
The present invention relates to a recovery apparatus and a recovery method for separating and recovering a low boiling point substance such as ammonia from a wastewater containing the low boiling point substance.
Background
As a method for separating and removing ammonia-containing wastewater, a stripping method is known. A typical ammonia recovery apparatus using this stripping method includes a distillation column for performing stripping, and the ammonia-containing vapor discharged from the top of the distillation column is subjected to fractional condensation by a condenser, and the condensed water is returned to the top of the distillation column as a reflux liquid, and the remaining concentrated ammonia-containing vapor is supplied to an absorption column, absorbed by water, and discharged as recovered ammonia water.
However, the stripping method used in such an ammonia recovery apparatus is a method of blowing steam directly to the bottom of the distillation column, and since a large amount of steam is used, the running cost is high and the treatment cost needs to be reduced. On the other hand, in this method, ammonia-containing vapor is generated in an amount substantially equal to the amount of vapor to be charged, but in order to obtain a reflux liquid flowing to the column top of the distillation column and a recovered ammonia liquid, cooling by a heat exchanger (condenser) provided at the column top is required, and energy is used once.
In order to solve such a problem, it has been proposed that the vapor discharged from the top of the distillation column is compressed by a vapor compressor and heat is recovered by a reboiler to reduce the amount of the vapor (see patent document 1 below). In addition, the following structure is proposed: the method is characterized in that make-up water is supplied to a condenser for segregating ammonia-containing vapor discharged from the top of a distillation column, the make-up water and the ammonia-containing vapor are evaporated by heat exchange, and the evaporated make-up water is introduced into a vapor compressor, compressed, heated, and reused as vapor (see patent document 2 below).
Prior art documents
Patent document
Patent document 1: japanese laid-open patent publication No. 2002-28637
Patent document 2: japanese laid-open patent publication No. 2004-114029
Problems to be solved by the invention
The conventional examples disclosed in patent documents 1 and 2 described above effectively utilize the heat of the ammonia-containing vapor discharged from the top of the distillation column to save energy and reduce the running cost.
However, in the structure of the conventional example including at least a distillation column, a heat exchanger (a reboiler or a condenser, which corresponds to the evaporator of the present application) and a vapor compressor, if it is intended to recover ammonia at a high concentration of, for example, 20 wt% or more, the following problems occur. That is, if an attempt is made to increase the concentration to a high concentration only by the heat exchanger (corresponding to the evaporator of the present application), the temperature difference between the inlet and the outlet of the ammonia-containing vapor in the heat exchanger becomes large, and accordingly, the load on the vapor compressor becomes too large, which is contrary to the demand for energy saving by the use of the vapor compressor. The above-described problems are not limited to the recovery apparatus containing ammonia, but are widely common to recovery apparatuses containing low boiling point substances.
Therefore, a low boiling point substance recovery apparatus capable of recovering ammonia at a high concentration and realizing energy saving has been demanded.
Disclosure of Invention
The present invention has been made in view of the above problems, and an object of the present invention is to provide a low boiling point substance recovery apparatus and a recovery method that can recover a low boiling point substance at a high concentration and can achieve energy saving.
Means for solving the problems
In order to achieve the above object, the present invention according to claim 1 provides an apparatus for recovering a low boiling point substance, comprising: a distillation column in which a raw liquid containing a low boiling point substance is brought into contact with heating steam, the low boiling point substance is separated from the raw liquid and vaporized, the vapor is discharged from the top of the column as a vapor containing the low boiling point substance, and treated water obtained by removing the low boiling point substance from the raw liquid is stored in the bottom of the column; an evaporator that condenses the vapor containing the low boiling point substance by segregating the vapor containing the low boiling point substance by heat exchange with water, and evaporates and discharges the water as water vapor, the vapor being discharged from the top of the distillation column; a compression device for compressing and raising the temperature of the steam discharged from the evaporator, guiding the compressed and raised temperature steam to the distillation column, and using the steam as heating steam used in the distillation column; and a concentration tower for introducing the vapor containing the low boiling point substance that has been fractionated by the evaporator, and cooling the vapor to remove moisture, thereby further concentrating the vapor containing the low boiling point substance.
According to the above configuration, the evaporator and the concentration column disposed after the evaporator are provided, and the vapor containing ammonia discharged from the distillation column can be concentrated in two stages by the evaporator and the concentration column, thereby generating a vapor containing a low boiling point substance at a predetermined high concentration (for example, 20 wt% or more). According to such a configuration, the load on the compression device can be prevented from becoming excessively large as compared with a configuration in which the compression is performed only to a predetermined high concentration (for example, 20 wt% or more) by the evaporator. As a result, a recovery apparatus capable of saving energy and generating a high-concentration (for example, 20 wt% or more) vapor containing a low boiling point substance can be obtained.
Examples of the "low boiling point substance" include alcohols such as ammonia and methanol, ketones such as acetone, and esters such as methyl acetate.
As the "water", pure water, soft water, ion-exchanged water, etc. can be used.
The apparatus for recovering a low boiling point substance according to claim 2 is based on the apparatus for recovering a low boiling point substance according to claim 1, and is characterized by comprising a preheater provided in a middle of a discharge line for discharging the treated water stored in the bottom of the distillation column to the outside, the preheater being configured to heat the water used in the evaporator by exchanging heat between the water used in the evaporator and the treated water in advance.
According to the above configuration, energy saving during heat exchange in the evaporator can be achieved by preheating the water used in the evaporator.
According to the above configuration, the opening degree of the control valve is controlled based on the detection result of the temperature sensor, and the flow rate of the cooling water passing through the heat exchanger is adjusted. Thus, the ammonia-containing vapor having a predetermined high concentration (for example, 20 wt% or more) can be produced by cooling the stock solution (condensate of the vapor containing the low boiling point substance) stored in the bottom of the concentration column to a predetermined temperature and spraying the cooled stock solution.
Technical solution 6 relates to a method for recovering a low boiling point substance, which is characterized by comprising: a first step of blowing heating steam into a distillation column, bringing a raw liquid containing a low boiling point substance into contact with the heating steam, separating and vaporizing the low boiling point substance from the raw liquid, discharging the vaporized low boiling point substance as steam containing the low boiling point substance from the top of the distillation column, and storing treated water obtained by removing the low boiling point substance from the raw liquid in the bottom of the distillation column; a second step of condensing the vapor containing the low boiling point substance by heat exchange between the vapor containing the low boiling point substance discharged from the top of the distillation column and water, and evaporating and discharging the water as vapor; a third step of compressing and raising the temperature of the steam discharged from the evaporator, and guiding the steam after compression and raising the temperature to the distillation column to use the steam as heating steam used in the distillation column; and a fourth step of introducing the vapor containing the low boiling point substance that has been segregated by the evaporator, and cooling the vapor to remove moisture, thereby further concentrating the vapor containing the low boiling point substance.
According to the above configuration, a method for recovering a low boiling point substance can be configured, which can recover a low boiling point substance at a high concentration and can save energy.
Effects of the invention
According to the present invention, low boiling point substances can be recovered at a high concentration, and energy saving can be achieved.
Drawings
Fig. 1 is an overall configuration diagram of an ammonia recovery apparatus according to an embodiment.
Fig. 2 is an enlarged view of the vicinity of the evaporator.
Fig. 3 is an enlarged view of the vicinity of the concentration tower.
Description of reference numerals:
1: an ammonia recovery unit;
2: a distillation column;
3: an evaporator;
4: a compression device;
5: a concentration tower;
6: a first absorption tower;
7: a second absorption tower;
18. 19: a vapor compressor.
Detailed Description
The present invention will be described in detail below based on embodiments. In the following embodiments, an ammonia recovery apparatus that uses ammonia-containing wastewater as a raw liquid and separates and removes ammonia from the ammonia-containing wastewater to recover the ammonia is exemplified as a low boiling point substance recovery apparatus. The low boiling point substance may be used in addition to ammonia, for example, alcohols such as methanol, ketones such as acetone, and esters such as methyl acetate.
(embodiment mode)
Fig. 1 is an overall configuration diagram of an ammonia recovery apparatus according to an embodiment. The ammonia recovery device (corresponding to the low boiling point substance recovery device of the present invention) 1 includes: a distillation column 2 into which heating steam is blown and which is subjected to steam stripping; an evaporator 3 for evaporating water by heat exchange between the vapor containing ammonia discharged from the top of the distillation column 2 and water; a compression device 4 for compressing and heating the steam discharged from the evaporator 3 to turn the steam into heating steam and discharging the steam to the distillation column 2; a concentration tower 5 for introducing the ammonia-containing vapor concentrated by the evaporator 3, cooling the vapor to remove moisture, and increasing the concentration of the ammonia-containing vapor to a high concentration (for example, 20 wt% or more); a first absorption tower 6 for absorbing moisture in the ammonia-containing vapor from the concentration tower 5 to produce a recovered ammonia water having a predetermined concentration; and a second absorption tower 7 which prevents the uncondensed ammonia-containing vapor in the first absorption tower from being discharged to the outside. Here, in order to explain the features of the ammonia recovery apparatus 1 according to embodiment 1, the evaporator 3 and the concentration column 5 disposed after the evaporator 3 are provided, and ammonia water having a predetermined high concentration (for example, 20 wt% or more) can be recovered from the ammonia-containing vapor discharged from the distillation column 2 by two-stage concentration performed by the evaporator 3 and the concentration column 5.
Hereinafter, a specific configuration of the ammonia recovery device 1 will be described including the above-described characteristic configurations. The distillation column 2 may be a multi-stage distillation column 2, and the distillation column 2 is not limited thereto, and may be a non-multi-stage distillation column 2. That is, a plate column or a packed column can be used as the distillation column 2. The raw liquid (ammonia-containing waste water) was supplied to the top of the distillation column 2 through a raw liquid supply line L1. The stock solution may be subjected to pH adjustment in advance.
The heating steam from the steam ejector 10 is supplied to the bottom of the distillation column 2 through the heating steam supply pipe L3. The bottom of the distillation column 2 is connected to the heat recovery tank 11 via a pipe L4, and the stock solution (low-concentration ammonia water) at the bottom of the column is supplied to the heat recovery tank 11 via a pipe L4. The vapor injector 10 is a vapor compression mechanism that performs suction and compression of vapor, and a vapor supply pipe L5 through which vapor supplied from a high-pressure vapor source (not shown) such as a boiler flows and a vapor reuse pipe L6 extending from the heat recovery tank 11 are connected to the vapor suction side 10 a. With such a configuration, the stock solution in the heat recovery tank 11 is flash evaporated, sucked and compressed by the vapor ejector 10, mixed with the vapor from the vapor supply pipe L5, and blown into the bottom of the distillation column 2 as heating vapor. The stock solution in the heat recovery tank 11 is flash evaporated and reused as a part of the heating vapor, thereby recovering heat.
A discharge pipe L7 for discharging the treated water (for example, low-concentration ammonia water of 30ppm or less) is connected to the bottom of the heat recovery tank 11, and a treated water discharge pump P1 and three heat exchangers H1, H2, and H3 are provided in the discharge pipe L7. The heat exchanger H1 is a water heater that heats water by exchanging heat between the water and the treated water. The water heated by the heat exchanger H1 is supplied to the bottom of the evaporator 3 through a water supply pipe L8. The heat exchanger H2 is a raw liquid preheater for preheating the raw liquid by exchanging heat between the raw liquid and the treated water. The raw liquid preheated by the heat exchanger H2 is supplied to the top of the distillation column 2 through a raw liquid supply pipe L1. The heat exchanger H3 is a cooler that cools the treated water by exchanging heat between the cooling water and the treated water. The treated water cooled by the heat exchanger H3 is discharged to the outside of the system through a discharge pipe L7.
The heat exchangers H1, H2, and H3 are located on the discharge pipe L7 downstream of the treated water discharge pump P1, and are provided in the following order. That is, in discharge pipe L7, heat exchanger H1 is provided upstream of heat exchanger H2. By arranging in this order, the amount of heat given from the treated water to the water is maximized, and therefore energy saving can be achieved in the evaporator 3 that heats the water. The heat exchanger H3 is provided for the purpose of cooling the treated water, and therefore the heat exchanger H3 is provided downstream of the heat exchangers H1 and H2.
The evaporator 3 is composed of a horizontal tube-type evaporator tank 12, and includes a sprinkler 13 and an indirect heater 14. The evaporator is not limited to the horizontal tube type, and for example, a thin film flow (vertical tube) type evaporator may be used. As shown in fig. 2, the indirect heater 14 includes a heat transfer tube group 15 including one or more horizontal heat transfer tubes, and a pair of left and right header members 16A and 16B. The bottom of the evaporation tank 12 serves as a reservoir 17 for storing the water supplied through the pipe L8. The stock solution (water) in the reservoir 17 is configured to circulate: the water is supplied to the sprayer 13 provided in the upper part of the evaporation tank 12 through the pipe L9 by the circulation pump P2, and after being sprayed from the sprayer 13 toward the outer surface of the heat guide pipe group 15, the water flows down to the reservoir 17 in the lower part of the evaporation tank 12.
The header 16B is connected to the column top of the distillation column 2 via a vapor supply pipe L10, and the overhead vapor (vapor containing ammonia) discharged from the column top of the distillation column 2 passes through the vapor supply pipe L10, is guided to the header 16B, and then flows through the heat transfer tube group 15. Here, the evaporator 3 is set to a pressure lower than the pressure of the vapor at the top of the tower, and therefore the circulating liquid (water) sprayed by the sprayer 13 is subjected to thin-film evaporation on the surface of the heat transfer tube group 15, thereby generating the vapor. The water vapor is supplied to the compression device 4. Here, the principle of evaporating water in the evaporator 3 will be described in more detail, and in the evaporator 3, the pressure outside the heat transfer pipe of the heated water is lower than the pressure of the tower top vapor (inside the heat transfer pipe) that becomes the heating source, and therefore the water evaporates. The pressure difference is generated by the compression device 4 (specifically, the vapor compressors 18 and 19). This is because the pressure outside the evaporator heat transfer tube connected to the suction side of the compression device 4 is low, and the pressure of the vapor in the distillation column 2 and the overhead vapor connected to the discharge side of the compression device 4 is high. The pressure in the distillation column 2 also rises due to the steam supplied from the steam injector 10, and this causes evaporation of water in the evaporator 3.
The condensed water (low-concentration ammonia water) that has flowed and condensed through the heat exchanger tube group 15 is stored in the header 16A, and is returned to the top of the distillation column 2 as reflux liquid via the pipe L11 by driving the condensed water pump P3. The remaining residual vapor (condensed ammonia-containing vapor) is discharged to the top of the condensation column 5 via a pipe L12.
The compression device 4 includes two vapor compressors 18 and 19, and these vapor compressors 18 and 19 are configured to connect the bottom of the distillation column 2 and the upper part of the evaporation tank 12 in parallel. That is, the inlet side 18a of the vapor compressor 18 is connected to the upper part of the evaporation tank 12 via a pipe L15, and the outlet side 18b of the vapor compressor 18 is connected to the bottom part of the distillation column 2 via a pipe L16. The inlet side 19a of the vapor compressor 19 is connected to the upper part of the evaporation tank 12 via a branch pipe L17 branched from a pipe L5, and the outlet side 19b of the vapor compressor 19 is connected to the bottom part of the distillation column 2 via a pipe L18.
Here, roots-type vapor compressors having a large maximum pressure difference are used as the vapor compressors 18 and 19. However, in the present invention, the present invention is not limited to the roots-type vapor compressor, and any one of a turbine-type vapor compressor, a screw-type vapor compressor, a vane-type vapor compressor, and another vapor compressor may be used. Although the compression device 4 is configured by two vapor compressors 18 and 19 in the present embodiment, it may be configured by one vapor compressor or three or more vapor compressors.
The concentrating tower 5 is constituted by a spray type scrubber. The storage liquid (condensate) stored in the bottom of the concentration tower 5 flows in the spray pipe (equivalent to the circulation line of the present invention) L20, is guided to the top of the tower, and is sprayed toward the inside of the top of the tower. A circulation pump P4 and a heat exchanger H4 are provided in the middle of the spray pipe L20. The reservoir liquid flowing through the spray pipe L20 is cooled by heat exchange with cooling water in the heat exchanger H4. As shown in fig. 3, a control valve V1 is provided in a pipe L21 through which cooling water flows, and the opening degree is controlled by a temperature sensor T that detects the temperature of the stock solution stored at the bottom of the concentration tower 5. That is, the opening degree of the control valve V1 is controlled based on the detection result of the temperature sensor T, and the flow rate of the cooling water passing through the heat exchanger H4 is adjusted. By cooling the storage liquid (condensate) to a predetermined temperature and spraying the cooled storage liquid, ammonia-containing vapor having a predetermined high concentration (for example, 20 wt% or more) can be produced.
Further, as shown in fig. 3, the spray pipe L20 branches at an intermediate point, and the branched branch pipe L22 is connected to the top of the distillation column 2. A control valve V2 is provided midway in the branch pipe L22. As shown in fig. 3, the concentration tower 5 is provided with a liquid level sensor S1 for detecting the liquid level of the stock solution. The liquid level sensor S has a position switch S1a that detects an upper limit set position and a position switch S1b that detects a lower limit set position. The opening degree of the control valve V2 is controlled by the liquid level sensor S1 so that the stock solution is maintained at a predetermined liquid level and the stock solution exceeding the predetermined liquid level is refluxed to the top of the distillation column 2.
First absorption tower 6 is composed of a spray type scrubber similar to that of concentrating tower 5, and a circulation pump P5 and a heat exchanger H5 are provided in spray pipe L23 through which the stock solution of first absorption tower 6 circulates. In the heat exchanger H5, the reservoir liquid flowing through the spray pipe L23 exchanges heat with the cooling water, and the reservoir liquid is cooled. The cooled storage liquid is sprayed in the form of mist of ammonia-containing vapor of high concentration (for example, 20 wt% or more) introduced from the concentration tower 5 through the pipe L24, whereby the ammonia-containing vapor is condensed and recovered, thereby producing recovered ammonia water. The spray pipe L23 branches off halfway, and the collected ammonia water is discharged to the outside of the system through the branched branch pipe L25.
Second absorption tower 7 is composed of a spray type scrubber similar to first absorption tower 6, water is supplied to the bottom of second absorption tower 7 through pipe L30, and the water stored in the bottom of the tower is sprayed from the top of the tower through spray pipe L31 by driving of circulation pump P6. Between the first absorption column 6 and the second absorption column 7, a pipe L32 for guiding the uncondensed ammonia-containing vapor in the first absorption column 6 to the top of the second absorption column 7 and a pipe L33 for returning the condensed water in the second absorption column 7 to the first absorption column 6 are provided. Further, an exhaust pipe L34 for discharging vapor from which ammonia has been removed is provided at the top of the second absorption tower 7.
In fig. 1 to 3, L40 denotes a cooling water supply pipe, L41 denotes a pipe branched from cooling water supply pipe L40, L21 denotes a pipe branched from cooling water supply pipe L40, cooling water supply pipe L40 is provided with heat exchanger H5, pipe L41 is provided with heat exchanger H3, and pipe L21 is provided with heat exchanger H4.
Next, the processing operation of the ammonia recovery device 1 configured as described above will be described. Steam for heating is blown into the distillation column 2 to perform stripping. That is, in the distillation column 2, the raw liquid is brought into contact with steam for heating, ammonia is separated from the raw liquid and vaporized, and the ammonia is discharged from the top of the column as steam containing ammonia, and low-concentration ammonia water (for example, 30ppm or less) from which ammonia has been removed from the raw liquid is stored as treated water in the bottom of the column.
The vapor containing ammonia discharged from the top of the distillation column 2 is guided to the header 16B through the vapor supply pipe L10 and then flows through the heat transfer tube group 15, whereby the circulating liquid (water) sprayed by the spray device 13 is subjected to thin film evaporation on the surface of the heat transfer tube group 15 to generate vapor. The steam is supplied to the vapor compressors 18 and 19. On the other hand, condensed water (low-concentration ammonia water) which has flowed and condensed through the heat transfer tube group 15 is stored in the header 16A, and is returned as reflux liquid to the top of the distillation column 2 via a pipe L11, and the remaining excess vapor (concentrated ammonia-containing vapor) is supplied to the concentration column 5 via a pipe L12.
The vapor compressors 18 and 19 compress the supplied water vapor to raise the temperature thereof, and introduce the water vapor as heating water vapor into the bottom of the distillation column 2. This can reduce the amount of heating steam supplied from the heating steam supply pipe L3, thereby saving energy.
On the other hand, in the concentration tower 5, the opening degree of the control valve V1 is controlled based on the detection result of the temperature sensor T, and the flow rate of the cooling water passing through the heat exchanger H4 is adjusted. Thereby, the storage liquid (condensate) cooled to a predetermined temperature is sprayed from the top of the concentration tower 5, and the ammonia-containing vapor is segregated, thereby generating ammonia-containing vapor having a predetermined high concentration (for example, 20 wt% or more). The condensate is entirely returned to the top of the distillation column 2 as a reflux liquid. In this way, by introducing the ammonia-containing vapor that has been segregated by the evaporator 3 into the concentration tower 5, removing water, and further concentrating the vapor containing ammonia, it is possible to prevent the load on the vapor compressors 18 and 19 from becoming excessively large, as compared with a configuration in which the vapor is concentrated only to a predetermined high concentration (for example, 20 wt% or more) by the evaporator 3. As a result, energy saving can be achieved, and ammonia-containing vapor having a high concentration (for example, 20 wt% or more) can be generated.
Next, in the first absorption tower 6, the stock solution at the bottom of the tower is sprayed from the top of the tower through the spray pipe L23, and with such a configuration, the ammonia-containing vapor introduced from the concentration tower 5 through the pipe L24 is condensed to produce ammonia-recovered water (recovered ammonia water) containing high-concentration ammonia. In the second absorption tower 7, the uncondensed ammonia gas slightly remaining in the first absorption tower 6 is guided through the pipe L32, and the water supplied from the outside of the system is sprayed from the tower top through the spray pipe L31, whereby the uncondensed ammonia gas is absorbed. The water after ammonia absorption is returned to the condensate of the first absorption tower 6. As a result, the uncondensed ammonia gas can be prevented from being discharged to the outside. The ammonia-removed gas is discharged from the exhaust pipe L34.
(other items)
(1) In the above embodiment, the description has been given of the configuration in which "water" is supplied to the evaporator 3 and the second absorption tower 7, but the "water" may specifically be pure water, soft water, ion-exchanged water, or the like.
(2) For reference, in the case of a configuration in which vapor in a distillation column is directly compressed and used as a heat source of the distillation column (for example, patent document 1 and the like), there is a possibility that the vapor in the distillation column is directly compressed, and corrosion due to a substance contained therein, corrosion in a sealed portion, and leakage may occur. In contrast, in the case of a structure in which water is evaporated by an evaporator and directly used in a distillation column as in the present invention, since steam (water vapor) directly used in the distillation column does not contain a content substance, it is possible to prevent corrosion and leakage caused by the content substance.
Industrial applicability
The present invention is applicable to a recovery apparatus and a recovery method for separating and recovering a low boiling point substance from a wastewater containing the low boiling point substance such as ammonia.
Claims (5)
1. An apparatus for recovering a low boiling point substance, comprising:
a distillation column in which a raw liquid containing a low boiling point substance is brought into contact with heating steam, the low boiling point substance is separated from the raw liquid and vaporized, the vapor is discharged from the top of the column as a vapor containing the low boiling point substance, and treated water obtained by removing the low boiling point substance from the raw liquid is stored in the bottom of the column;
an evaporator that condenses the vapor containing the low boiling point substance by segregating the vapor containing the low boiling point substance by heat exchange with water, and evaporates and discharges the water as water vapor, the vapor being discharged from the top of the distillation column;
a compression device for compressing and raising the temperature of the steam discharged from the evaporator, guiding the compressed and raised temperature steam to the distillation column, and using the steam as heating steam used in the distillation column;
a concentration tower that introduces the vapor containing the low boiling point substance that has been condensed by the evaporator, cools the vapor to remove moisture, and further concentrates the vapor containing the low boiling point substance; and
and a preheater provided in a middle of a discharge line for discharging the treated water stored at the bottom of the distillation column to the outside, the preheater being configured to heat the water used in the evaporator by exchanging the treated water with the water in advance.
2. The recovery apparatus of low boiling point substance according to claim 1,
the device for recovering a low boiling point substance comprises:
a heat exchanger which is provided in the middle of a circulation line for guiding the storage liquid stored in the bottom of the concentration tower to the top of the tower, and which cools the storage liquid by exchanging heat between the storage liquid flowing through the circulation line and cooling water;
a temperature sensor that detects a temperature of the storage liquid stored at the bottom of the concentration tower; and
and a control valve for adjusting the flow rate of the cooling water passing through the heat exchanger according to the detection result of the temperature sensor.
3. The recovery apparatus of low boiling point substance according to claim 1,
the compression device is configured by connecting a plurality of vapor compressors in parallel.
4. The recovery apparatus of low boiling point substances according to any one of claims 1 to 3,
the low boiling point substance is ammonia.
5. A method for recovering low boiling point substances, comprising:
a first step of blowing heating steam into a distillation column, bringing a raw liquid containing a low boiling point substance into contact with the heating steam, separating and vaporizing the low boiling point substance from the raw liquid, discharging the vaporized low boiling point substance as steam containing the low boiling point substance from the top of the distillation column, and storing treated water obtained by removing the low boiling point substance from the raw liquid in the bottom of the distillation column;
a second step of condensing the vapor containing the low boiling point substance by heat exchange between the vapor containing the low boiling point substance discharged from the top of the distillation column and water by an evaporator to condense the vapor containing the low boiling point substance, and evaporating and discharging the water as vapor;
a third step of compressing and raising the temperature of the steam discharged from the evaporator, and guiding the steam after compression and raising the temperature to the distillation column to use the steam as heating steam used in the distillation column; and
a fourth step of introducing the vapor containing the low boiling point substance that has been condensed by the evaporator, cooling the vapor to remove moisture, thereby further concentrating the vapor containing the low boiling point substance,
the water used in the evaporator is heated by a preheater provided in the middle of a discharge line for discharging the treated water stored in the bottom of the distillation column to the outside, by exchanging heat between the water used in the evaporator and the treated water in advance.
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| JP2016197083A JP6780188B2 (en) | 2016-10-05 | 2016-10-05 | Low boiling point substance recovery device and recovery method |
| JP2016-197083 | 2016-10-05 |
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| JP7086815B2 (en) * | 2018-10-22 | 2022-06-20 | 木村化工機株式会社 | Energy saving system for distillation equipment |
| JP7378129B2 (en) * | 2019-11-29 | 2023-11-13 | 株式会社ササクラ | Separation device and method for low boiling point substances |
| CN112499710B (en) * | 2020-10-20 | 2023-01-24 | 阮氏化工（常熟）有限公司 | Device and method for purifying ammonia water by using ammonia-containing wastewater |
| CN113144656B (en) * | 2021-05-13 | 2022-04-22 | 湖南文理学院 | Device and method for extracting crocin from gardenia based on evaporation concentration |
| CN113750556A (en) * | 2021-09-24 | 2021-12-07 | 李媛 | Efficient distillation system and distillation method |
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| Publication number | Publication date |
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| JP6780188B2 (en) | 2020-11-04 |
| TW201813702A (en) | 2018-04-16 |
| JP2018058025A (en) | 2018-04-12 |
| CN107913525A (en) | 2018-04-17 |
| TW202112424A (en) | 2021-04-01 |
| TWI758987B (en) | 2022-03-21 |
| TWI732870B (en) | 2021-07-11 |
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