KR20120035200A - Organic solvent recovery system - Google Patents

Abstract

An object of this invention is to provide the organic solvent collection | recovery system containing the structure which can reduce the energy used for an organic solvent collection | recovery system.
In this organic solvent recovery system 1B, the performance of the concentrator 20 is improved by lowering the concentration magnification, so that the cooling temperature of the cooler 300 increases (from 28 deg. C to 40 deg. C) and the air supply heating device 500. Increasing the temperature of introduction (33 ° C. → 70 ° C.) becomes possible, and the utility amount of the cooler 300 and the air supply heating device 500 can be reduced. As a result, it becomes possible to reduce the energy used throughout the system.

Description

Organic solvent recovery system {ORGANIC SOLVENT RECOVERY SYSTEM}

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an organic solvent recovery system for recovering an organic solvent from an exhaust gas containing an organic solvent, and more particularly to an industry containing an organic solvent discharged from various factories, research facilities, etc. (hereinafter, collectively referred to as production equipment). An organic solvent recovery system for efficiently recovering an organic solvent from exhaust gas.

As a treatment system for recovering an organic solvent from an exhaust gas containing an organic solvent, an adsorption element containing an adsorbent is known. In the treatment system using the adsorption element, the exhaust gas is brought into contact with the adsorbent to adsorb the organic solvent, and sprayed with a high temperature gas to desorb the organic solvent to recover the exhaust gas as a desorption gas containing a high concentration of the organic solvent. A processing apparatus is mentioned (refer patent document 1, 2 below).

Patent Document 1: Japanese Patent Application Laid-Open No. 01-127022 Patent Document 2: Japanese Patent Application Laid-Open No. 2007-44595

In Patent Documents 1 and 2, when the organic solvent in the exhaust gas is concentrated, cooled and condensed and recovered, energy such as heating at the time of desorption of the adsorption element containing the adsorbent and cooling to liquefy and condense the high concentration exhaust gas or desorption gas Is needed. In recent years, it has become an urgent task to efficiently recover the organic solvent in the organic solvent recovery system and to reduce (energy saving) this energy used in the organic solvent recovery system.

An object of the present invention is to provide an organic solvent recovery system and a recovery method having a configuration capable of further reducing the energy used in the organic solvent recovery system.

In the organic-solvent recovery system and collection method based on this invention, the organic-solvent collection system which collect | recovers the said organic solvent from exhaust gas whose temperature containing an organic solvent is about 50 degreeC-about 200 degreeC is organic. An adsorption section for adsorbing the organic solvent in the solvent-containing gas with an adsorption element containing an adsorbent to generate a clean gas, and allowing the exhaust gas having a higher temperature than the organic solvent-containing gas to pass through the adsorption element, A concentrating device having a desorption unit for desorbing the adsorbed organic solvent to generate desorption gas, and a cooling recovery device for cooling and condensing the desorption gas including the desorption gas or the exhaust gas to recover the organic solvent. have.

In another aspect of the organic solvent recovery system and recovery method, the exhaust gas is a gas discharged from a production facility, and the clean gas is returned to the production facility.

In another aspect of the organic solvent recovery system and the recovery method, the concentrating device includes a rotating shaft and a cylindrical adsorber as the adsorption element provided around the rotating shaft, and the cylindrical shape is formed around the rotating shaft. By rotating an adsorbent, the adsorption element which adsorbed the said organic solvent in the said organic solvent containing gas moves to the said desorption part continuously.

In another aspect of any one of the organic solvent recovery systems and recovery methods, a first temperature measuring instrument for measuring the temperature of the clean gas at the outlet side of the adsorption unit of the concentrating device, and the outlet side of the desorption unit of the concentrating device. And a second temperature measuring instrument for measuring the temperature of the desorbing gas, wherein a temperature of the clean gas measured by the first temperature measuring instrument and a temperature of the desorbing gas measured by the second temperature measuring instrument are respectively set to a predetermined temperature. The time for the organic solvent-containing gas to pass through the adsorption unit and the time for the exhaust gas to pass through the desorption unit are controlled so that the adsorption unit passes.

The organic solvent-containing gas is a gas containing the organic solvent that has not been recovered in the cooling recovery device and the recovery method, and the air flow rate that allows the exhaust gas and the desorption gas to pass through the cooling recovery device is the exhaust gas. Is 0% -50%, and the desorption gas is 50% -100%.

In another aspect of the organic solvent recovery system and the recovery method described above, the air flow rate that allows the exhaust gas and the desorption gas to pass through the cooling and recovery apparatus is 0%, and the desorption gas is 100%. to be.

In another aspect of any one of the organic solvent recovery systems and recovery methods, the organic solvent is n-methyl-2-pyrrolidone, N, N-dimethylformamide, N, N-dimethylacetamide or n- Deccan.

In another embodiment of the organic solvent recovery system and recovery method based on the present invention, the organic solvent recovery system for recovering the organic solvent from the exhaust gas of the temperature containing the organic solvent is about 50 ℃ to about 200 ℃, the organic solvent An adsorption portion for adsorbing the organic solvent in the organic solvent-containing gas containing an adsorbent with an adsorption element containing an adsorbent to generate a clean gas, and allowing the exhaust gas to pass through the exhaust gas having a higher temperature than the organic solvent-containing gas; A condensing unit having a desorption unit for desorbing the organic solvent adsorbed to the adsorption element to generate desorption gas, and a purge portion in which the desorption treatment of the adsorption element at the desorption unit is completed before the transition to the adsorption unit. And a desorber containing the desorber or the exhaust gas. By cooling and a recovery apparatus for recovering the organic solvent.

The purge part outlet gas discharged | emitted from the said purge part mixes with the said organic solvent containing gas introduce | transduced into the said adsorption part, The said organic solvent containing gas is the said adsorption part in the state heated up by receiving the heat energy of the said purge part exit gas. Is introduced.

In another aspect of the organic solvent recovery system and recovery method, part of the clean gas discharged from the adsorption unit is introduced into the purge unit.

In another aspect of any one of the organic solvent recovery systems and recovery methods, a part of the purge part outlet gas is supplied to the desorption part together with the exhaust gas and / or to the cooling recovery device together with the desorption gas. Supplied, the remainder of the purge part outlet gas is introduced into the adsorption part together with the organic solvent-containing gas, and the ratio of the air volume between the part of the purge part outlet gas and the remainder of the purge part outlet gas is adjusted. The temperature of the organic solvent-containing gas introduced into the adsorption unit is controlled.

In another aspect of any one of the organic solvent recovery systems and recovery methods described above, the volume ratio of the purge part to the adsorption part of the concentration device is about 5% to about 50%.

In another aspect of the organic solvent recovery system and the recovery method, the exhaust gas is a gas discharged from a production facility, and the remainder of the clean gas is returned to the production facility.

In another aspect of any one of the organic solvent recovery systems and recovery methods, the concentrating device includes a rotary shaft and a cylindrical adsorber as the adsorption element provided around the rotary shaft, and the cylinder is formed around the rotary shaft. By rotating the shape adsorber, the adsorption element which adsorbs the organic solvent in the organic solvent-containing gas in the adsorption part continuously moves to the purge part via the desorption part.

In another aspect of any one of the organic solvent recovery systems and recovery methods, a first temperature measuring instrument for measuring the temperature of the clean gas at the outlet side of the adsorption unit of the concentrating device, and the outlet side of the desorption unit of the concentrating device. And a second temperature measuring device for measuring the temperature of the desorption gas, and a third temperature measuring device for measuring the temperature of the adsorption unit inlet gas at the inlet side of the adsorption unit of the concentrating device, and measured by the first temperature measuring device. The organic solvent of the adsorption unit is such that the temperature of the clean gas, the temperature of the desorption gas measured by the second temperature measuring instrument, and the temperature of the adsorption unit inlet gas measured by the third temperature measuring instrument become predetermined temperatures, respectively. The time at which the containing gas passes, the time at which the exhaust gas passes through the desorption unit and the fur The time at which branch clean gas passes is controlled.

The organic solvent-containing gas is a gas containing the organic solvent that has not been recovered in the cooling recovery device and the recovery method, and the air flow rate ratio that allows the exhaust gas and the desorption gas to pass through the cooling recovery device is the exhaust gas. Is 0% -50%, and the desorption gas is 50% -100%.

In another aspect of the organic solvent recovery system and the recovery method described above, the air flow rate that allows the exhaust gas and the desorption gas to pass through the cooling and recovery apparatus is 0%, and the desorption gas is 100%. to be.

In another aspect of any one of the organic solvent recovery systems and recovery methods, the organic solvent is n-methyl-2-pyrrolidone, N, N-dimethylformamide, N, N-dimethylacetamide or n- Deccan.

According to the organic solvent recovery system and recovery method based on this invention, it becomes possible to reduce the energy used for an organic solvent recovery system more.

1 is a conceptual diagram showing the structure of an organic solvent recovery system in a reference technique.
2 is a conceptual diagram showing the structure of the organic solvent recovery system in the present embodiment.
3 is a schematic view showing the structure of a concentration apparatus employed in an organic solvent recovery system according to the present embodiment.
It is a figure which shows the comparison of the utility amount of a reference technique and the organic-solvent collection system in this embodiment.
It is a figure which shows the comparison of the running cost of a reference technique and the organic-solvent collection system in this embodiment.
It is a figure which shows the contrast of NMP density | concentration of the reference technique and the organic-solvent collection system in this embodiment.
7 is a conceptual diagram illustrating a structure of an organic solvent recovery system in an embodiment.
It is a schematic diagram which shows the structure of the concentration apparatus employ | adopted for the organic solvent collection | recovery system in embodiment.
It is a conceptual diagram which shows the structure of the organic-solvent collection system in the other structure of embodiment.

EMBODIMENT OF THE INVENTION Hereinafter, embodiment of this invention is described in detail with reference to drawings. In the embodiment shown below, the same code | symbol is attached | subjected in the figure about the same or corresponding part, and the description may not be repeated. In addition, when referring to the number, quantity, etc. in embodiment described below, the range of this invention is not necessarily limited to the number, quantity, etc. unless there is a special description.

(Reference technology: organic solvent recovery system (1A))

First, with reference to FIG. 1, the reference technique with respect to the organic-solvent collection system of this invention is demonstrated. The organic solvent recovery system 1A in the reference technology is an organic solvent recovery system for recovering an organic solvent from the exhaust gas G1 discharged from the production facility 1000, and includes a concentrator 200, a regeneration heater 100, The cooler 300, the recovery tank 400, and the air supply heating device 500 are provided.

(Concentrator 200)

The concentrating device 200 has a desorption part (desorption zone) 21 and an adsorption part (adsorption zone) 22. The organic solvent containing gas G2 containing the organic solvent is introduced into the adsorption part 22. By contacting the adsorbent with the organic solvent-containing gas G2, the organic solvent contained in the organic solvent-containing gas G2 is adsorbed by the adsorbent. As a result, the organic solvent-containing gas G2 is purified and discharged as the clean gas G3.

Clean gas G3 which is hotter than organic solvent containing gas G2 is introduced into desorption part 21. The organic solvent is desorbed from the adsorbent, whereby the clean gas G3 is discharged as the desorption gas G4 containing the organic solvent.

Piping lines L2 and L3 are connected to the adsorption | suction part 22 of the concentrating apparatus 200. As shown in FIG. The piping line L2 introduces the organic solvent containing gas G2 into the adsorption part 22. The piping line L3 derives the clean gas G3 from the adsorption part 22. The piping line L7 branched to the regeneration heater 100 is connected to the piping line L3.

In the piping line L3, a valve V101 for adjusting the flow rate of the clean gas G3 to the air supply heating device 500 is installed, and the flow rate of the clean gas G3 to the regeneration heater 100 is adjusted in the pipe line L7. The valve V102 is provided.

Piping lines L8 and L5 are connected to the detachable part 21. The piping line L8 introduces high temperature clean gas G3 into the detachable part 21. The piping line L5 leads the desorption gas G4 from the desorption part 21.

(Regeneration heater 100)

The regeneration heater 100 puts the clean gas G3 in a high temperature state. Piping lines L7 and L8 are connected to the regeneration heater 100. The piping line L7 introduces a clean gas G3, and the piping line L8 directs the hot clean gas G3 to the desorption portion 21 of the concentrator 20.

(Cooler 300 and Recovery Tank 400)

The separator 300 is configured by the cooler 300 and the recovery tank 400. The cooler 300 condenses the desorption gas G4 or the like using cooling water. The cooler 300 separates desorption gas G4 and the like into a recovery liquid containing an organic solvent at a high concentration, and an organic solvent-containing gas G2 containing a low concentration of an organic solvent. The recovery liquid containing the organic solvent at a high concentration is recovered to the recovery tank 400.

Piping lines L1, L2, and L6 are connected to the cooler 300. As shown in FIG. The piping line L5 joins the piping line L1. The piping line L1 introduces the exhaust gas G1 and the desorption gas G4 into the cooler 300, and the piping line L2 concentrates the organic solvent-containing gas G2 containing a low concentration of the separated organic solvent. It is led to the adsorption part 22 of the apparatus 200, and the piping line L6 leads the separated recovery liquid to the recovery tank 400. FIG.

(Air supply heating device 500)

The air supply heating device 500 heats up the temperature of the clean gas G3 to a predetermined temperature, and supplies the clean gas G3 to the production facility 1000. Piping lines L3 and L4 are connected to the air supply heating device 500. The pipe line L3 introduces a clean gas G3 sent out from the adsorption unit 22 of the concentrator 200, and the pipe line L4 is heated to the production facility 1000 to a predetermined temperature. (G3) is derived.

(Collection of collection)

By using the organic solvent recovery system 1A including the above structure, the organic solvent [NMP (n-methyl-2-pyrrolidone)] used in the lithium ion battery manufacturing facility is recovered as the production facility 1000. The system will be described below.

The exhaust gas G1 discharged from the production facility 1000 has a flow rate of about 770 NCMM, an organic solvent concentration of about 1000 ppm, and a temperature of about 110 ° C. The cooler 300 is introduced in a state in which the exhaust gas G1 discharged from the production facility 1000 and the desorption gas G4 desorbed from the concentrator 20 are mixed. The desorption gas G4 has a flow rate of about 110 NCMM, an organic solvent concentration of about 2581 ppm, and a temperature of about 73 ° C. The mixed gas of the exhaust gas G1 and the desorption gas G4 introduced into the cooler 300 has a flow rate of about 880 NCMM, an organic solvent concentration of about 1198 ppm, and a temperature of about 105 ° C.

The mixed gas of the exhaust gas G1 and the desorption gas G4 is separated by the cooler 300 into a recovery liquid containing a high concentration of an organic solvent and an organic solvent containing gas G2 containing a low concentration of an organic solvent. The recovery liquid containing the organic solvent at a high concentration is recovered to the recovery tank 400. The concentration of organic solvent [NMP] is about 78 wt%. The organic solvent-containing gas G2 containing the organic solvent at a low concentration has an organic solvent concentration of about 343 ppm and a temperature of about 28 ° C. The organic solvent containing gas G2 is led to the adsorption part 22 of the concentrating device 200 by the piping line L2.

The clean gas G3 derived by the adsorption unit 22, the flow rate is about 770 NCMM, the organic solvent concentration is about 20 ppm, and the temperature is about 33 ° C. A part of the clean gas G3 is led to the air supply heating device 500 through the pipe line L3, and the remainder is led to the regeneration heater 100 through the pipe line L7. The flow rate of the clean gas G3 to be supplied to the air supply heating device 500 and the regeneration heater 100, respectively, is appropriately controlled by the valve V101 and the valve V102.

The clean gas G3 led to the regeneration heater 100 is led to the desorption unit 21 of the concentrating device 200 through the pipe line L8 after the temperature is heated to about 130 ° C. The clean gas G3 introduced to the desorption unit 21 desorbs the organic solvent from the adsorbent and is led to the cooler 300 through the pipe lines L5 and L1 as the desorption gas G4 containing the organic solvent. .

The clean gas G3 drawn to the air supply heating device 500 is led to the production facility 1000 through the pipe line L4 after the temperature is heated to about 70 ° C.

(Embodiment: Organic Solvent Recovery System 1B)

Next, with reference to FIG. 2, the organic-solvent collection | recovery system 1B in embodiment based on this invention is demonstrated. The organic solvent recovery system 1B according to the present embodiment is also an organic solvent recovery system for recovering the organic solvent from the exhaust gas G1 discharged from the production facility 1000, similarly to the organic solvent recovery system 1A described above. And a concentrator 200, a regeneration heater 100, a cooler 300, a recovery tank 400, and an air supply heating device 500.

(Concentrator 200)

The concentrating device 200 has a desorption part (desorption zone) 21 and an adsorption part (adsorption zone) 22. The organic solvent-containing gas G2 containing the unrecovered organic solvent from the cooler 300 is introduced into the adsorption unit 22, whereby the organic solvent-containing gas G2 comes into contact with the adsorption material, and the organic solvent-containing gas G2 is introduced. The organic solvent contained in) is adsorbed by the adsorbent.

As a result, the organic solvent-containing gas G2 is purified and discharged as the clean gas G3. In the desorption part 21, organic solvent is desorbed from an adsorption material by introduce | transducing exhaust gas G1 of higher temperature than organic solvent containing gas G2 to an adsorption material, and exhaust gas G1 is desorption gas containing organic solvent by this. It is discharged as (G4).

Piping lines L2 and L3 are connected to the adsorption | suction part 22 of the concentrating apparatus 200. As shown in FIG. The piping line L2 introduces the organic solvent containing gas G2 into the adsorption part 22. The piping line L3 derives the clean gas G3 from the adsorption part 22. On the outlet side of the adsorption part 22, the 1st temperature measuring device T1 which measures the temperature of the clean gas G3 is provided.

Piping lines L8 and L5 are connected to the detachable part 21. The piping line L8 introduces the exhaust gas G1 from the production facility 1000. The piping line L5 leads the desorption gas G4 from the desorption part 21. On the outlet side of the desorption part 21, the 2nd temperature measuring device T2 which measures the temperature of desorption gas G4 is provided.

With reference to FIG. 3, the specific structure of the concentration apparatus 200 is demonstrated. This concentrating device 200 has shown the case where the cylindrical cylindrical adsorption body 210 was used. As shown in the figure, in the case of using the cylindrical adsorbent 210 having a cylindrical outer shape, the rotary shaft 211 is provided at the center of the axis of the cylindrical adsorbent 210 configured to allow gas to flow in the axial direction. This rotation shaft 211 is driven to rotate by an actuator or the like.

As the adsorbent, activated alumina, silica gel, activated carbon material and zeolite are widely used for the cylindrical adsorbent 210, and among them, activated carbon and hydrophobic zeolite are particularly suitably used. Activated carbon and hydrophobic zeolite have excellent functions of adsorbing and desorbing low concentration organic compounds, and have been used in various apparatuses as adsorbents since ancient times.

Piping lines L2, L3, L5, and L8 (see FIG. 2), which are not specifically shown in FIG. A part of 210 is used as the adsorption part 22 for adsorption treatment, and another part of the adsorption part 22 is used as desorption part 21 for desorption treatment.

The organic-solvent containing gas G2 is introduce | transduced into the adsorption | suction part 22 of the cylindrical adsorption body 210 from one side of an axial direction, and the clean gas G3 is guide | induced from the other side of an axial direction. The high temperature exhaust gas G1 is introduced into the desorption part 21 of the cylindrical adsorption body 210, and desorption gas G4 is guide | induced from the other side of an axial direction.

In this concentrating device 200, the cylindrical adsorption body 210 rotates at a predetermined speed in the direction of arrow A in the figure with the rotating shaft 211 as the rotation center. As a result, the portion where the adsorption treatment of the cylindrical adsorbent 210 is completed is moved to the zone where the desorption treatment is performed, and the portion where the desorption treatment of the cylindrical adsorbent 210 is completed is moved to the zone where the adsorption treatment is performed. Therefore, in this concentrating apparatus 200, a adsorption process and a desorption process are performed simultaneously, and it becomes possible to perform a cleaning process continuously.

By the rotational speed of the concentrating device 200, the time of an adsorption process and the time of a desorption process are controlled. In addition, the concentrating device (the temperature of the clean gas G3 measured by the 1st temperature measuring device T1 and the temperature of the desorption gas G4 measured by the 2nd temperature measuring device T2 become a predetermined temperature, respectively. The rotational speed of 200 controls the time of the adsorption process and the time of the desorption process. In particular, as a method of setting the temperature of the clean gas G3 and the desorption gas G4 to a predetermined temperature, it is also possible to introduce a heat exchanger such as aluminum into the front and rear of the adsorption element of the concentrator 200 and the adsorption element itself. Do.

(Regeneration heater 100)

Referring again to FIG. 2, the regeneration heater 100 is provided between the piping line L1 and the piping line L8 extending from the production facility 1000. When the temperature of the exhaust gas G1 discharged from the production facility 1000 is sufficiently high, the regeneration heater 100 is not used. However, when the production equipment 1000 is in an operation initial state and the temperature of the exhaust gas G1 does not reach a predetermined temperature, it is used to heat the exhaust gas G1 to a predetermined temperature.

In the piping line L1 extended from the production facility 1000, the piping line L9 branched from the piping line L1 and passing through the piping line L5 is provided. In the exhaust gas G1 discharged from the production facility 1000, the desorption unit 21 of the concentrating device 20 is sent out through the pipe line L1, the regeneration heater 100, and the pipe line L8, but a part thereof is partially discharged. Exhaust gas G1 enables direct extraction to cooler 300 via piping line L9. The amount of the exhaust gas G1 sent to the desorption portion 21 and the amount directly sent to the cooler 300 are respectively provided by the valve V111 provided in the pipe line L1 and the valve V112 provided in the pipe line L9. Controlled.

(Cooler 300 and Recovery Tank 400)

The separator 300 is configured by the cooler 300 and the recovery tank 400. The cooler 300 is an apparatus which separates the desorption gas G4 etc. using cooling water etc., and isolate | separates into the recovery liquid containing organic solvent in high concentration, and the organic solvent containing gas G2 containing an organic solvent. The recovery liquid containing the organic solvent at a high concentration is recovered to the recovery tank 400.

Piping lines L2, L5, and L6 are connected to the cooler 300. As shown in FIG. The piping line L2 directs the organic solvent containing gas G2 containing the separated organic solvent to the adsorption part 22 of the concentrator 200, and the piping line L5 is desorbed from the desorption part 21. The gas G4 is introduced, and the pipe line L6 draws the separated recovery liquid into the recovery tank 400.

(Air supply heating device 500)

The air supply heating device 500 heats up the temperature of the clean gas G3 to a predetermined temperature, and supplies the clean gas G3 to the production facility 1000. Piping lines L3 and L4 are connected to the air supply heating device 500. The pipe line L3 introduces a clean gas G3 sent out from the adsorption unit 22 of the concentrator 200, and the pipe line L4 is heated to the production facility 1000 to a predetermined temperature. (G3) is derived. In this embodiment, since the temperature of the clean gas G3 guide | induced from the desorption part 21 adsorption part 22 is a high temperature state, it is not necessary to heat clean gas G3 by the air supply heating apparatus 500. FIG.

(Collection of organic solvent)

In the organic solvent recovery system 1B including the above structure, similarly to the organic solvent recovery system 1A described in the reference technique, the organic solvent [NMP (n-methyl) used in the lithium ion battery manufacturing facility as the production facility 1000 is described. -2-pyrrolidone)] will be described below.

The exhaust gas G1 discharged from the production facility 1000 has a flow rate of about 770 NCMM, an organic solvent concentration of about 1000 ppm, and a temperature of about 110 ° C. With the valve V111 in the fully open state and the valve V112 in the closed state, the exhaust gas G1 discharged from the production facility 1000 is introduced into the 100% desorption portion 21. Since the temperature of the exhaust gas G1 is sufficiently high, the heating of the exhaust gas G1 by the regeneration heater 100 is not performed here.

The desorption gas G4 discharged from the desorption unit 21 has a flow rate of about 770 NCMM, an organic solvent concentration of about 2122 ppm, and a temperature of about 80 ° C. Since the valve V112 is closed and 100% of the exhaust gas G1 discharged from the production facility 1000 is introduced into the desorption unit 21, the gas introduced into the cooler 300 is desorbed gas ( G4) is 100% and the exhaust gas G1 introduced directly is 0%.

The desorption gas G4 is separated in the cooler 300 into a recovery liquid containing an organic solvent at a high concentration and an organic solvent-containing gas G2 containing an organic solvent. The recovery liquid containing the organic solvent at a high concentration is recovered to the recovery tank 400. The concentration of organic solvent [NMP] is about 91 wt%. The organic solvent-containing gas G2 containing the organic solvent has an organic solvent concentration of about 1142 ppm and a temperature of about 40 ° C. This organic solvent containing gas G2 is guide | induced to the adsorption | suction part 22 of the concentrator 200 by piping line L2.

The clean gas G3 in which the organic solvent is adsorbed by the adsorption unit 22 of the concentrating device 200 is led to the air supply heating device 500 through the pipe line L3. The clean gas G3 derived from the adsorption unit 22 has a flow rate of about 770 NCMM, an organic solvent concentration of about 20 ppm, and a temperature of about 70 ° C.

The clean gas G3 derived from the air supply heating device 500 is not heated by the air supply heating device 500, and the clean gas G3 having a temperature of about 70 ° C. is directly produced through the piping line L4. Is derived at 1000.

(Action, effect)

The effect of the organic solvent recovery system 1B having the above-described configuration will be described when compared with the organic solvent recovery system 1A described as a reference technique.

(The rise of the cooling temperature required for the cooler 300 is possible 28 ° C → 40 ° C)

According to the organic-solvent collection system 1B in this embodiment, organic-solvent collection | recovery is sent by sending the exhaust gas G12 of the high temperature state discharged | emitted from the production facility 1000 to the desorption part 21 of the concentrator 200. The use of the regeneration heater 100 in the system 1A becomes unnecessary, and it becomes possible to suppress the increase in the utility usage amount.

Specifically, in 1 A of organic solvent recovery systems, it was necessary to heat the clean gas G3 led to the desorption part 21 by the regeneration heater 100 from 33 degreeC to 130 degreeC. However, according to the organic-solvent recovery system 1B in this embodiment, since the exhaust gas G21 of a high temperature state is sent to the desorption part 21 of the concentrator 200 in a high temperature state, it is sent to the desorption part 21. There is no need to heat the resulting gas. As a result, it becomes possible to reduce the concentration magnification (adsorption air volume / desorption air volume) in the concentrator 200. In the desorption part 21, since desorption operation by the exhaust gas G2 containing high concentration of NMP is performed, desorption operation can be improved by using the adsorption material with high desorption efficiency.

As described above, in the organic solvent recovery system 1B according to the present embodiment, compared with the organic solvent recovery system 1A, it is possible to improve the performance of the concentrating device 200 by economically lowering the concentration magnification. As a result, the cooling temperature of the cooler 300 can be increased (from 28 ° C. to 40 ° C.) (see FIG. 4), thereby enabling a reduction in the amount of utility used by the cooler 300.

(Reduction of introduction gas temperature into the cooler 300 is possible. 105 ° C. → 80 ° C.)

Moreover, by sending the exhaust gas G12 of the high temperature state discharged | emitted from the production facility 1000 to the desorption part 21 of the concentrator 200, heat exchange by an adsorption material is performed and it introduce | transduces into the cooler 300. It is possible to reduce (105 ° C. to 80 ° C.) the previous gas temperature (see FIG. 4), thereby enabling the reduction of the utility usage of the cooler 300.

(The rise of the introduction temperature of the air supply heating device 500 is possible 33 ° C → 70 ° C)

Moreover, by sending the exhaust gas G12 of the high temperature state discharged | emitted from the production facility 1000 to the desorption part 21 of the concentrator 200, heat exchange by an adsorption material is performed, and the air supply heating apparatus 500 is performed. It is possible to raise the gas temperature before introduction of the furnace (33 ° C. to 70 ° C.) (see FIG. 4), thereby enabling the reduction of the utility amount of the air supply heating device 500.

As described above, according to the organic solvent recovery system 1B of the present embodiment, the high-temperature exhaust gas G21 discharged from the production facility 1000 is sent to the desorption unit 21 of the concentrating device 200. The utility usage of the cooler 300 and the air supply heating device 500 can be reduced. As a result, as shown in FIG. 5, the overall running cost of the system can be significantly reduced in the organic solvent recovery system 1A as compared with the case.

(Concentration improvement of NMP recovery solution 78 wt% → 91 wt%)

In addition, according to the organic solvent recovery system 1B of the present embodiment, since the temperature of the cooler 300 can be increased in the organic solvent recovery system 1A as compared with the case, the amount of condensation of water is reduced and NMP in the recovery liquid is reduced. It is possible to improve the concentration (78 wt% to 91 wt%) (see Fig. 6).

In the organic solvent recovery system 1B according to the above embodiment, a case where 110 degrees is assumed as an example of the temperature of the exhaust gas G1 is shown. However, the temperature of the exhaust gas G1 discharged from the production equipment is 50 ° C. 200 ° C is assumed. Therefore, when the temperature of exhaust gas does not reach predetermined temperature, the exhaust gas G1 is heated using the regeneration heater 100 as needed.

Moreover, although the case where the exhaust gas G1 discharged | emitted from the production facility 1000 is led to the 100% desorption part 21 and the desorption gas G4 is led to the 100% cooler 300 is demonstrated, A part of the exhaust gas G1 discharged from a facility can also be led to the cooler 300 directly via the piping line L9. The assumed air flow rate ratio of the gas passing through the cooler 300 is about 0% to 50% for the exhaust gas G1 and about 50% to 100% for the desorption gas G4.

In addition, although the case where the purified gas is returned to the production facility 1000 using the gas discharged from the production facility 1000 as the exhaust gas G1 is described, the production facility 1000 is used as the exhaust gas G1. It is not necessary to directly use the gas discharged from), and as long as it is exhaust gas G1 which has the same property, it is possible to collect | recover high concentration organic solvent using the organic-solvent collection system 1B in this embodiment. Moreover, it is not necessary to return the purified gas to the production facility 1000, and it is also possible to use the purified gas for other uses.

Moreover, although the case where [NMP (n-methyl- 2-pyrrolidone)] is collect | recovered as an organic solvent is demonstrated, it is not limited to this organic solvent, It can liquefy and collect | recover by cooling at 1 degreeC-50 degreeC. Any organic solvent may be used. That is, the organic solvent is, for example, N, N-dimethylformamide, N, N-dimethylacetamide or n-decane. Also about the collection | recovery of the organic solvent which has the same characteristic as NMP, it is possible to use the organic-solvent collection | recovery system 1B based on this invention.

(Embodiment: Organic Solvent Recovery System 1C)

Next, with reference to FIG. 7, the organic solvent recovery system 1C in embodiment based on this invention is demonstrated. The organic solvent recovery system 1C according to the embodiment is also an organic solvent recovery system for recovering the organic solvent from the exhaust gas G1 discharged from the production facility 1000, similarly to the organic solvent recovery system 1A described above. The organic solvent recovery system 1C includes a concentrator 200, a regeneration heater 100, a cooler 300, a recovery tank 400, and a heat exchanger 600.

(Concentrator 200)

The concentrating device 200 includes an adsorption element, and has a desorption part 21, an adsorption part 22, and a purge part 23. The adsorption element adsorbs the organic solvent in the gas by bringing the gas containing the organic solvent into contact with the adsorption element of the concentrating device 200. The adsorption element desorbs the adsorbed organic solvent by bringing a gas higher in temperature than the gas containing the organic solvent into this adsorption element that adsorbs the organic solvent.

In the concentrating device 200, the adsorption element is sequentially transferred to the adsorption unit 22 (adsorption state), the desorption unit 21 (desorption state), and the purge unit 23 (purge state), and the purge unit 23 After the (purge state), the process returns to the adsorption unit 22 (adsorption state). That is, the purge part 23 is comprised after the desorption part 21 (desorption state), and before the adsorption part 22 (adsorption state).

These transitions are realized by rotation of an adsorption element (cylindrical adsorption body), for example, if it is a rotor type concentrating device (refer to FIG. 8, and mention later for details). If these transitions are, for example, a batch type concentrating device, the adsorption element is moved to the adsorption unit 22 (adsorption state), the desorption unit 21 (desorption state) and the purge unit 23 by damper (and valve) operation. Is realized by shifting to a (purge state).

In the adsorption part 22 of the condenser 200, the organic-solvent containing gas G2 containing the organic solvent unrecovered from the cooler 300, and the purge part exit gas G6 discharged | emitted from the purge part 23 are shown. Mixed gas (hereinafter referred to as adsorption unit inlet gas G5) is introduced. The adsorption part inlet gas G5 contacts the adsorption material in the adsorption part 22, and the organic solvent contained in the adsorption part inlet gas G5 is adsorb | sucked by an adsorption material. As a result, the adsorption unit inlet gas G5 is purified and discharged as the clean gas G3.

Piping lines L2 and L3 are connected to the suction part 22. The piping line L2 introduces an adsorption | suction part inlet gas G5 into the adsorption | suction part 22. As shown in FIG. The piping line L3 derives the clean gas G3 from the adsorption part 22. On the outlet side of the adsorption part 22, the 1st temperature measuring device T1 which measures the temperature of the clean gas G3 is provided. At the inlet side of the adsorption unit 22, a third temperature measuring device T3 for measuring the temperature of the adsorption unit inlet gas G5 is provided.

The piping line L11 branched to the purge part 23 is connected to the piping line L3. The pipe line L3 is provided with a valve V113 for adjusting the flow rate of the clean gas G3 to the heat exchanger 600, and the flow rate of the clean gas G3 to the purge 23 is provided at the pipe line L11. The regulating valve V114 is provided.

Piping lines 23 are connected to piping lines L11 and L12. The piping line L11 introduces a part of the clean gas G3 into the purge part 23. The piping line L12 derives the purge part outlet gas G6 from the purge part 23. The piping line L12 joins the piping line L2.

In the desorption part 21, the organic solvent is desorbed from an adsorption material by introduce | transducing the exhaust gas G1 whose temperature is higher than the adsorption | suction part inlet gas G5 to an adsorbent, and exhaust gas G1 contains the organic solvent by this. It is discharged as (G4).

Piping lines L8 and L5 are connected to the detachable part 21. The piping line L8 introduces the exhaust gas G1 from the production facility 1000. The piping line L5 leads the desorption gas G4 from the desorption part 21. On the outlet side of the desorption part 21, the 2nd temperature measuring device T2 which measures the temperature of desorption gas G4 is provided.

Here, with reference to FIG. 8, the specific structure of the concentration apparatus 200 is demonstrated. As an example, this concentrating device 200 is a rotor type and uses the cylindrical cylindrical adsorbent 210. As shown in the figure, in the case of using the cylindrical adsorbent 210 having a cylindrical outer shape, the rotary shaft 211 is provided at the center of the axis of the cylindrical adsorbent 210 configured to allow gas to flow in the axial direction. This rotation shaft 211 is driven to rotate by an actuator or the like.

As the adsorbent, activated alumina, silica gel, activated carbon material and zeolite are widely used for the cylindrical adsorbent 210, and among them, activated carbon and hydrophobic zeolite are particularly suitably used. Activated carbon and hydrophobic zeolite have excellent functions of adsorbing and desorbing low concentration organic compounds, and have been used in various apparatuses as adsorbents since ancient times.

Piping lines L2, L3, L5, L8, L11, and L12 (see FIG. 7) which are not specifically shown in FIG. 8 are connected so that the end surface of the cylindrical adsorption body 210 may approach both end surfaces. A part of the cylindrical adsorbent 210 is used as the adsorption unit 22 for performing the adsorption treatment, and the other part of the cylindrical adsorbent 210 is used as the desorption unit 21 for performing the desorption treatment. The other part of the cylindrical adsorption body 210 is used as the purge part 23 for performing a purge process.

The adsorption | suction part inlet gas G5 is introduce | transduced into the adsorption part 22 of the cylindrical adsorption body 210 from one side of an axial direction, and the clean gas G3 is guide | induced from the other side of an axial direction. The high temperature exhaust gas G1 is introduced into the desorption part 21 of the cylindrical adsorption body 210, and desorption gas G4 is guide | induced from the other side of an axial direction. A part of the clean gas G3 is introduce | transduced into the purge part 23 of the cylindrical adsorption body 210 from one side of an axial direction, and the purge part exit gas G6 is derived from the other side of an axial direction.

In this concentrating device 200, the cylindrical adsorption body 210 rotates at a predetermined speed in the direction of arrow A in the figure with the rotating shaft 211 as the rotation center. Accordingly, the portion where the adsorption treatment of the cylindrical adsorber 210 is completed is moved to the desorption portion 21 for desorption treatment, and the portion where the desorption treatment of the cylindrical adsorption body 210 is completed is a purge portion for performing the purge treatment. It moves to 23, and the part to which the purge process is completed moves to the adsorption part 22 which performs an adsorption process. In this concentrating apparatus 200, adsorption treatment, desorption treatment, and purge treatment are performed at the same time, and it becomes possible to perform the purifying treatment continuously.

For example, suppose that the purge part 23 is not formed in the concentrator 200. In this case, since the adsorption element is still high temperature immediately after the desorption treatment, that is, at the beginning of the adsorption treatment, the adsorption performance as the adsorption material is low. Moreover, adsorption performance may fall by carrying in of the organic solvent at the time of rotationally shifting from the desorption part which performs a desorption process to the adsorption part which performs an adsorption process.

In the concentrating device 200 of this embodiment, the purge part 23 is comprised after the desorption part 21 and before the adsorption part 22. A part of clean gas G3 is introduce | transduced into the purge part 23, and the adsorption element in the purge part 23 is cooled. Since the adsorption element is cooled by the clean gas G3, the cooling efficiency of the adsorption element is high.

The clean gas G3 introduced into the purge part 23 is introduced into the adsorption part 22 again as the adsorption part inlet gas G5 together with the organic solvent-containing gas G2 as the purge part outlet gas G6. By this cycle, the concentrating device 200 can increase the removal rate of the organic solvent in the adsorption part 22. The volume ratio of the purge part 23 to the adsorption part 22 is preferably about 5% to about 50%. If this ratio is less than about 5%, the desired purge effect cannot be obtained. If this ratio exceeds about 50%, the economy becomes worse.

Moreover, the clean gas G3 which heat-exchanged with the adsorption element in the purge part 23 is heated up and is taken out from the purge part 23 as purge part exit gas G6. The purge part outlet gas G6 which is in a temperature rising state is heated with the organic solvent containing gas G2 derived from the cooler 300 (refer FIG. 2), and it raises the temperature of the organic solvent containing gas G2. Here, when the organic solvent is n-methyl-2-pyrrolidone or the like, part of the organic solvent-containing gas G2 derived from the cooler 300 may be in a mist state.

The organic solvent-containing gas G2 in the mist state needs to be in a gas state by being heated before being introduced into the adsorption portion 22. In the organic solvent recovery system 1C, the organic solvent-containing gas G2 in the mist state can be heated up by utilizing the purge part outlet gas G6 in the elevated temperature derived from the purge part 23. By heating up the organic-solvent containing gas G2 of the mist state by the purge part outlet gas G6, it becomes possible to reduce the usage-amount of energy in the other heating means (not shown) required for the temperature rising.

By the rotational speed of the concentrating device 200, the time of an adsorption process, the time of a desorption process, and the time of a purge process are controlled. The temperature of the clean gas G3 measured by the first temperature measuring device T1, the temperature of the desorbed gas G4 measured by the second temperature measuring device T2, and the adsorption measured by the third temperature measuring device T3. The time of the adsorption process, the time of the desorption process, and the time of the purge process are controlled by the rotational speed of the concentrating device 200 so that the temperature of the sub inlet gas G5 becomes a predetermined temperature, respectively. In particular, as a method of setting the temperature of the clean gas G3, the desorption gas G4, or the adsorption unit inlet gas G5 to a predetermined temperature, aluminum or the like is provided before or after the adsorption element of the concentrating device 200 or on the adsorption element itself. It is also possible to introduce a heat exchanger.

(Regeneration heater 100)

Referring again to FIG. 7, the regeneration heater 100 is provided between the piping line L1 and the piping line L8 extending from the production facility 1000. When the temperature of the exhaust gas G1 discharged from the production facility 1000 is sufficiently high, the regeneration heater 100 is not used. However, when the production facility 1000 is in an operation initial state and the temperature of the exhaust gas G1 does not reach a predetermined temperature, the regeneration heater 100 is used to heat the exhaust gas G1 to a predetermined temperature. do.

In the piping line L1 extended from the production facility 1000, the piping line L9 branched from the piping line L1 and passing through the piping line L5 is provided. A part of the exhaust gas G1 discharged | emitted from the production facility 1000 is sent to the desorption part 21 of the concentrating apparatus 200 via the piping line L1, the regeneration heater 100, and the piping line L8. .

The remainder of the exhaust gas G1 discharged from the production facility 1000 can be sent directly to the cooler 300 via the piping line L9. The delivery amount to the desorption part 21 of the exhaust gas G1 and the delivery amount to the cooler 300 are respectively controlled by the valve V111 provided in the piping line L1 and the valve V112 provided in the piping line L9. .

(Cooler 300 and Recovery Tank 400)

The cooler 300 and the recovery tank 400 constitute a cooling recovery device. The cooler 300 condenses the desorption gas G4 or the like with cooling water or the like to separate the recovery liquid containing the organic solvent at a high concentration and the organic solvent-containing gas G2 containing the organic solvent. The recovery liquid containing the organic solvent at a high concentration is recovered to the recovery tank 400.

Piping lines L2, L6, and L10 are connected to the cooler 300. As shown in FIG. The piping line L2 draws out the organic-solvent containing gas G2 containing the separated organic solvent to the adsorption | suction part 22 of the concentrating apparatus 200. As shown in FIG. The piping line L6 leads the separated recovery liquid to the recovery tank 400. Desorption gas G4 is introduce | transduced into piping line L10 from the desorption part 21 through piping line L5 and the heat exchanger 600 demonstrated below.

(Heat exchanger 600)

The heat exchanger 600 is located between the piping line L3 and the piping line L4, and this heat exchanger 600 is also located between the piping line L5 and the piping line L10. Although two heat exchangers 600 are shown apart in FIG. 7, the heat exchanger 600 can exchange heat energy between the pipe lines L3 and L4 and heat energy between the pipe lines L5 and L10.

The heat exchanger 600 heats up the clean gas G3 derived from the adsorption part 22 by heat exchange, and then sends it to the production facility 1000. The heat exchanger 600 cools the desorption gas G4 derived from the desorption part 21 by heat exchange, and then sends it to the cooler 300. By heat exchange of the heat exchanger 600, it becomes possible to reduce the usage amount of the other energy for making clean gas G3 sent to a production facility into predetermined temperature. By the heat exchange of the heat exchanger 600, it becomes possible to reduce the usage-amount of other energy for making desorption gas G4 sent to the cooler 300 into a predetermined temperature.

(Collection of organic solvent)

In the organic solvent recovery system 1C having the above structure, similarly to the organic solvent recovery system 1A described in the reference technology, the organic solvent [NMP (n-methyl) used in the lithium ion battery manufacturing facility as the production facility 1000 is described. -2-pyrrolidone)] will be described below.

The exhaust gas G1 discharged from the production facility 1000 has a flow rate of about 770 NCMM, an organic solvent concentration of about 1000 ppm, and a temperature of about 110 ° C. With the valve V111 in the fully open state and the valve V112 in the closed state, the exhaust gas G1 discharged from the production facility 1000 is introduced into the 100% desorption portion 21. Here, since the temperature of the exhaust gas G1 is sufficiently high, the heating of the exhaust gas G1 by the regeneration heater 100 is not performed.

The desorption gas G4 discharged from the desorption unit 21 has a flow rate of about 770 NCMM, an organic solvent concentration of about 1803 ppm, and a temperature of about 93 ° C. Since the valve V112 is closed and 100% of the exhaust gas G1 discharged from the production facility 1000 is introduced into the desorption unit 21, the gas introduced into the cooler 300 is desorbed gas ( G4) is 100% and the exhaust gas G1 introduced directly is 0%.

The desorption gas G4 is separated in the cooler 300 into a recovery liquid containing an organic solvent at a high concentration and an organic solvent-containing gas G2 containing an organic solvent. The recovery liquid containing the organic solvent at a high concentration is recovered to the recovery tank 400. The concentration of organic solvent [NMP] is about 89 wt%. The organic solvent-containing gas G2 containing the organic solvent has a flow rate of about 770 NCMM, an organic solvent concentration of about 857 ppm, and a temperature of about 37 ° C.

The purge part exit gas G6 is mixed with this organic solvent containing gas G2 by the piping line L12 connected to the piping line L2. The purge part outlet gas G6 has a flow rate of about 100 NCMM, an organic solvent concentration of about 386 ppm, and a temperature of about 100 ° C. The adsorption | suction part inlet gas G5 which consists of mixing organic solvent containing gas G2 and purge part outlet gas G6 has a flow volume of about 870 NCMM, an organic solvent concentration of about 803 ppm, and a temperature of about 44 degreeC. The adsorption part inlet gas G5 is led to the adsorption part 22 of the concentrating device 200.

The clean gas G3 in which the organic solvent is adsorbed by the adsorption unit 22 of the concentrator 200 has a flow rate of about 770 NCMM, an organic solvent concentration of about 12 ppm, and a temperature of about 53 ° C. A part of the clean gas G3 is led to the purge part 23 through the piping line L11. The remainder of the clean gas G3 is led to the heat exchanger 600 via the piping line L3.

The clean gas G3 derived from the purge part 23 cools the adsorption element in the purge part 23 and is led from the purge part 23 in a state of being heated up as the purge part outlet gas G6. The clean gas G3 derived from the heat exchanger 600 is heat-exchanged with the desorption gas G4 sent out from the desorption unit 21 to the cooler 300, and is produced from the heat exchanger 600 in a heated state. Drawn to facility 1000.

(Action, effect)

The effect of the organic solvent recovery system 1C having the above configuration will be described when compared with the organic solvent recovery system 1A described as a reference technique.

According to the organic-solvent recovery system 1C in this embodiment, the purge part 23 is comprised after the desorption part 21 and before the adsorption part 22. As shown in FIG. A part of the clean gas G3 is introduced into the purge part 23, and the adsorption element in the purge part 23 is cooled. Since the adsorption element is cooled by the clean gas G3, the cooling efficiency of the adsorption element is high.

The clean gas G3 introduced into the purge part 23 is introduced into the adsorption part 22 again as the adsorption part inlet gas G5 together with the organic solvent-containing gas G2 as the purge part outlet gas G6. By this cycle, the concentrating device 200 can increase the removal rate of the organic solvent in the adsorption part 22.

(The rise of the cooling temperature required for the cooler 300 is possible 28 ° C → 37 ° C)

According to the organic-solvent recovery system 1C in this embodiment, organic-solvent collection | recovery is sent by sending the exhaust gas G12 of the high temperature state discharged | emitted from the production facility 1000 to the desorption part 21 of the concentrator 200. The use of the regeneration heater 100 in the system 1A becomes unnecessary, and it becomes possible to suppress the increase in the utility usage amount.

Specifically, in 1 A of organic solvent recovery systems, it was necessary to heat the clean gas G3 led to the desorption part 21 by the regeneration heater 100 from 33 degreeC to 130 degreeC. However, according to the organic-solvent recovery system 1C of this embodiment, since the exhaust gas G12 of a high temperature state is sent to the desorption part 21 of the concentrator 200 in a high temperature state, it is sent to the desorption part 21. It is not necessary to heat the gas to be drawn. As a result, it becomes possible to reduce the concentration magnification (adsorption air volume / desorption air volume) in the concentrator 200. In the desorption part 21, since desorption operation by the exhaust gas G12 containing NMP high concentration is performed, desorption operation can be improved by using the adsorption material with high desorption efficiency.

As described above, in the organic solvent recovery system 1C according to the present embodiment, it is possible to improve the performance of the concentrating device 200 by economically lowering the concentration magnification as compared with the organic solvent recovery system 1A. As a result, the cooling temperature of the cooler 300 can be increased (from 28 ° C. to 37 ° C.), thereby reducing the utility usage of the cooler 300.

In addition, when the organic solvent is n-methyl-2-pyrrolidone or the like, part of the organic solvent-containing gas G2 derived from the cooler 300 is in a mist state. The organic solvent-containing gas G2 in the mist state needs to be in a gas state by being heated up before being introduced into the adsorption portion 22. By utilizing the purge part outlet gas G6 in the temperature increase state derived from the purge part 23, the organic-solvent containing gas G2 in the mist state can be heated up. By heating up the organic-solvent containing gas G2 of the mist state by the purge part outlet gas G6, it becomes possible to reduce the usage-amount of energy in the other heating means (not shown) required for the temperature rising.

(Reduction of the introduction gas temperature into the cooler 300 is possible 105 ° C → 73 ° C)

Moreover, by sending the exhaust gas G1 of the high temperature state discharged | emitted from the production facility 1000 to the desorption part 21 of the concentrator 200, heat exchange by an adsorption material is performed and it introduce | transduces into the cooler 300. It is possible to reduce the previous gas temperature (105 ° C. to 73 ° C.), thereby enabling the reduction of the utility amount of the cooler 300.

In addition, since the heat exchanger 600 capable of heat exchange between the piping lines L3 and L4 is provided between the piping lines L5 and L10, the cooler 300 is exchanged by the heat exchanger 600. It is possible to reduce the amount of other energy used for setting the desorption gas G4 to be sent to the predetermined temperature.

(The rise of the introduction temperature of the heat exchanger 600 air supply heating apparatus 500 is possible 33 degreeC → 53 degreeC)

Moreover, by sending the exhaust gas G1 of the high temperature state discharged | emitted from the production facility 1000 to the desorption part 21 of the concentrator 200, heat exchange by an adsorption material is performed, and the heat exchanger 600 is carried out. It becomes possible to raise the gas temperature before introduction (33 degreeC-53 degreeC). Since the heat exchanger 600 which can exchange heat between piping lines L5 and L10 is installed between piping lines L3 and L4, the cleanness which is sent to a production facility by the heat exchange of the heat exchanger 600 is carried out. It is possible to reduce the amount of other energy used to bring the gas G3 to a predetermined temperature.

As described above, according to the organic solvent recovery system 1C according to the present embodiment, the high-temperature exhaust gas G1 discharged from the production facility 1000 is sent to the desorption unit 21 of the concentrating device 200. The overall running cost of the system can be greatly reduced as compared with the case of the organic solvent recovery system 1A.

(Concentration improvement of NMP recovery solution 78 wt% → 89 wt%)

In addition, according to the organic solvent recovery system 1C of the present embodiment, since the temperature of the cooler 300 can be increased as compared with the case of the organic solvent recovery system 1A, the amount of condensation of water is reduced and the NMP in the recovery liquid is reduced. It is possible to improve the concentration (78 wt% to 89 wt%).

In the organic solvent recovery system 1C according to the embodiment, 110 ° C is assumed as an example of the temperature of the exhaust gas G1. However, the temperature of the exhaust gas G1 discharged from the production equipment is 50 ° C. 200 ° C is assumed. Therefore, when the temperature of exhaust gas does not reach predetermined temperature, the exhaust gas G1 is heated using the regeneration heater 100 as needed.

Moreover, although the case where the exhaust gas G1 discharged | emitted from the production facility 1000 is led to the 100% desorption part 21 and the desorption gas G4 is led to the 100% cooler 300 is demonstrated, A part of the exhaust gas G1 discharged from a facility can also be led to the cooler 300 directly via the piping line L9. The assumed air flow rate ratio of the gas passing through the cooler 300 is about 0% to 50% for the exhaust gas G1 and about 50% to 100% for the desorption gas G4.

In addition, although the case where the purified gas is returned to the production facility 1000 using the gas discharged from the production facility 1000 as the exhaust gas G1 is described, the production facility 1000 is used as the exhaust gas G1. It is not necessary to directly use the gas discharged from), and as long as it is exhaust gas G1 which has the same property, it is possible to collect | recover high concentration organic solvent using the organic-solvent collection system 1C in this embodiment. Moreover, it is not necessary to return the purified gas to the production facility 1000, and it is also possible to use the purified gas for other uses.

Moreover, although the case where [NMP (n-methyl- 2-pyrrolidone)] is collect | recovered as an organic solvent is demonstrated, it is not limited to this organic solvent, It can liquefy and collect | recover by cooling at 1 degreeC-50 degreeC. Any organic solvent may be used. That is, the organic solvent is, for example, N, N-dimethylformamide, N, N-dimethylacetamide or n-decane. Also about the collection | recovery of these organic solvents which have the same characteristic as NMP, it is possible to use the organic-solvent collection system 1C based on this invention.

Moreover, in 1 C of organic solvent collection | recovery systems in the said embodiment, each time of an adsorption process, a desorption process, and a purge process is controlled by the rotational speed of the concentrating apparatus 200. FIG. Each time of the adsorption process, the desorption process, and the purge process by the rotational speed of the concentrating device 200 so that the temperatures of the clean gas G3, the desorption gas G4, and the adsorption unit inlet gas G5 become predetermined temperatures, respectively. The case where this is controlled is explained.

Like the organic solvent recovery system 1D shown in FIG. 9, each temperature of the clean gas G3, the desorption gas G4, and the adsorption part inlet gas G5 is a part of the purge part outlet gas G6 that is desorbed gas. It may adjust by introducing into the cooler 300 in the state mixed with (G4). In this case, the piping line L13 branched from the piping line L12 and connected to the piping line L5 is provided. The air volume of the purge part outlet gas G6 in the piping line L13 may be adjusted by the valve V115.

Moreover, each temperature of the clean gas G3, the desorption gas G4, and the adsorption | suction part inlet gas G5 is a desorption part 21 in the state which mixed a part of purge part outlet gas G6 with exhaust gas G1. It may be adjusted by introducing into). In this case, the piping line L14 branched from the piping line L12 and connected to the piping line L8 is provided. The air volume of the purge part outlet gas G6 in the piping line L14 may be adjusted by the valve V116. In order to adjust each temperature of the clean gas G3, the desorption gas G4, and the adsorption | suction part inlet gas G5, two piping lines L13 and L14 may be provided.

As described above, each of the above-described embodiments is exemplary in all respects and is not restrictive. The technical scope of the present invention is defined by the claims, and includes all modifications within the meaning and range equivalent to the description of the claims.

1A, 1B: organic solvent recovery system 20, 200: concentration device
21: desorption part (desorption zone) 22: adsorption part (adsorption zone)
100: regeneration heater 210: cylindrical adsorbent
211: rotating shaft 300: cooler
400: recovery tank 500: air supply heating device
600: heat exchanger 1000: production equipment
G1: exhaust gas G2: gas containing organic solvent
G3: clean gas G4: desorption gas
G5: adsorption part inlet gas G6: purge part outlet gas
L1? L13: Piping line T1? T3: Temperature gauge
V101, V102, V110-V116: Valve

Claims (34)

An organic solvent recovery system for recovering the organic solvent from an exhaust gas containing an organic solvent,
An adsorption portion for adsorbing the organic solvent in the organic solvent-containing gas containing the organic solvent with an adsorption element containing an adsorbent to generate a clean gas, and the exhaust gas having a higher temperature than the organic solvent-containing gas in the adsorption element. A concentrating device having a desorption unit passing through and desorbing the organic solvent adsorbed to the adsorption element to generate desorption gas;
Cooling and recovery device for cooling the desorption gas containing the desorption gas or the exhaust gas to condense to recover the organic solvent
And
The organic solvent-containing gas is a gas containing the organic solvent not recovered in the cooling recovery device. The method of claim 1, wherein the exhaust gas is a gas discharged from the production facility,
An organic solvent recovery system for returning the clean gas to the production facility. The organic solvent recovery system according to claim 1 or 2, wherein the exhaust gas has a temperature of 50 ° C to 200 ° C. The said concentration apparatus as described in any one of Claims 1-3,
Rotation axis,
A cylindrical adsorbent as the adsorption element provided around the rotating shaft,
The organic solvent recovery system of the said adsorption part, the said adsorption element which adsorbed the said organic solvent in the said organic solvent containing gas continuously moves to the said desorption part by rotating the said cylindrical adsorption body around the said rotating shaft. The said 1st temperature measuring device of any one of Claims 1-4 which measures the temperature of the said clean gas in the exit side of the said adsorption part of the said concentrating device,
And a second temperature measuring device for measuring the temperature of the desorption gas at the outlet side of the desorption unit of the concentrating device,
A time for the organic solvent-containing gas to pass through the adsorption unit such that the temperature of the clean gas measured by the first temperature measuring instrument and the temperature of the desorption gas measured by the second temperature measuring instrument become predetermined temperatures; and The organic solvent recovery system wherein the time for the exhaust gas passes through the desorption portion is controlled. The air flow rate ratio according to any one of claims 1 to 5, wherein the exhaust gas and the desorption gas pass through the cooling and recovery apparatus are 0% to 50%, and the desorption gas is 50%. 100% organic solvent recovery system. The organic-solvent recovery system of Claim 6 whose air volume ratio which makes the said exhaust gas and the said desorption gas pass through the said cooling recovery apparatus is 0% and said desorption gas is 100%. The organic solvent according to any one of claims 1 to 7, wherein the organic solvent is selected from n-methyl-2-pyrrolidone, N, N-dimethylformamide, N, N-dimethylacetamide or n-decane. Organic solvent recovery system which is one or more kinds. An organic solvent recovery system for recovering the organic solvent from an exhaust gas containing an organic solvent,
And an adsorption element for adsorbing the organic solvent by contacting the organic solvent-containing gas containing the organic solvent and desorbing the organic solvent adsorbed by contacting the exhaust gas having a higher temperature than the organic solvent gas. An organic solvent-containing gas is introduced to adsorb the organic solvent to the adsorption element to discharge clean gas, and the exhaust gas is introduced to the adsorption element to desorb the organic solvent from the adsorption element to form the organic solvent. A concentrating device having a desorption unit for discharging desorption gas to be contained, a purge unit in which a desorption process of the desorption element of the desorption unit in the desorption unit is completed before the transition to the adsorption unit;
Cooling and recovery device for cooling the desorption gas containing the desorption gas or the exhaust gas to condense to recover the organic solvent
And
The organic solvent-containing gas is a gas containing the organic solvent not recovered in the cooling recovery device,
The purge part outlet gas discharged | emitted from the said purge part mixes with the said organic solvent containing gas introduce | transduced into the said adsorption part,
And the organic solvent-containing gas is introduced into the adsorption unit in a state in which the organic solvent-containing gas is heated in response to the heat energy of the purge part outlet gas. The organic solvent recovery system according to claim 9, wherein a part of the clean gas discharged from the adsorption unit is introduced into the purge unit. The part of the said purge part outlet gas is supplied to the said desorption part with the said exhaust gas, and / or is supplied to the said cooling collection | recovery apparatus with the said desorption gas,
Remainder of the said purge part exit gas is introduce | transduced into the said adsorption part with the said organic solvent containing gas,
An organic solvent recovery system in which the temperature of the organic solvent-containing gas introduced into the adsorption unit is controlled by controlling the ratio of the air volume between the part of the purge unit outlet gas and the remainder of the purge unit outlet gas. The organic-solvent recovery system in any one of Claims 9-11 whose volume ratio with respect to the said adsorption part of the said purge part in the said concentration apparatus is 5%-50%. The exhaust gas according to any one of claims 9 to 12, wherein the exhaust gas is a gas discharged from a production facility,
And the remainder of the clean gas is returned to the production facility. The organic solvent recovery system according to any one of claims 9 to 13, wherein the exhaust gas has a temperature of 50 ° C to 200 ° C. The said concentration apparatus as described in any one of Claims 9-14,
Rotation axis,
Cylindrical adsorber as said adsorption element provided around said rotating shaft
And
Organic solvent recovery which the said adsorption element which adsorb | sucked the said organic solvent in the said organic solvent containing gas in the said adsorption part continuously transfers to the said purge part through the said desorption part by rotating the said cylindrical adsorption body around the said rotating shaft system. The first temperature measuring device according to any one of claims 10 to 15, wherein the first temperature measuring device measures a temperature of the clean gas at an outlet side of the adsorption part of the concentrating device,
A second temperature measuring device for measuring the temperature of the desorption gas at the outlet side of the desorption unit of the concentrating device;
And a third temperature measuring device for measuring the temperature of the adsorption part inlet gas at the inlet side of the adsorption part of the concentrating device,
The temperature of the clean gas measured by the first temperature measuring instrument, the temperature of the desorbed gas measured by the second temperature measuring instrument, and the temperature of the adsorption part inlet gas measured by the third temperature measuring instrument are respectively predetermined. Temperature,
And a time at which the organic solvent-containing gas passes through the adsorption unit, a time at which the exhaust gas passes through the desorption unit, and a time at which the clean gas passes through the purge unit. The air flow rate ratio according to any one of claims 9 to 16, wherein the exhaust gas and the desorption gas pass through the cooling and recovery apparatus are 0% to 50%, and the desorption gas is 50%. 100% organic solvent recovery system. The organic-solvent recovery system of Claim 17 whose air volume ratio which makes the said exhaust gas and the said desorption gas pass through the said cooling recovery apparatus is 0% and said desorption gas is 100%. The organic solvent according to any one of claims 9 to 18, wherein the organic solvent is selected from n-methyl-2-pyrrolidone, N, N-dimethylformamide, N, N-dimethylacetamide or n-decane. Organic solvent recovery system which is one or more kinds. An organic solvent recovery method for recovering the organic solvent from an exhaust gas containing an organic solvent,
An adsorption step of adsorbing the organic solvent in the organic solvent-containing gas containing the organic solvent by an adsorption element containing an adsorbent to generate a clean gas, and the exhaust gas having a higher temperature than the organic solvent-containing gas in the adsorption element. A concentration step including a desorption step of passing and desorbing the organic solvent adsorbed to the adsorption element to generate a desorption gas;
A cooling recovery step of cooling the desorption gas including the desorption gas or the exhaust gas to condense and recover the organic solvent
Including;
The organic solvent-containing gas is a gas containing the organic solvent not recovered in the cooling recovery step. The method of claim 20, wherein the exhaust gas is a gas discharged from the production facility,
An organic solvent recovery method for returning the clean gas to the production facility. The organic solvent recovery method according to claim 20 or 21, wherein the exhaust gas has a temperature of 50 ° C to 200 ° C. The organic solvent recovery method according to any one of claims 20 to 22, wherein the time of the adsorption step and the time of the desorption step are controlled such that the temperature of the clean gas and the temperature of the desorption gas are respectively a predetermined temperature. . The air flow rate ratio according to any one of claims 20 to 23, wherein the exhaust gas and the desorption gas pass through the cooling recovery step are 0% to 50%, and the desorption gas is 50%. 100% organic solvent recovery method. The organic-solvent recovery method of Claim 24 whose air volume ratio which makes the said exhaust gas and the said desorption gas pass through the said cooling recovery process is 0% and said desorption gas is 100%. The organic solvent according to any one of claims 20 to 25, wherein the organic solvent is selected from n-methyl-2-pyrrolidone, N, N-dimethylformamide, N, N-dimethylacetamide or n-decane. The organic solvent recovery method which is 1 or more types. An organic solvent recovery method for recovering the organic solvent from an exhaust gas containing an organic solvent,
And an adsorption element for adsorbing the organic solvent by contacting the organic solvent-containing gas containing the organic solvent and desorbing the organic solvent adsorbed by contacting the exhaust gas having a higher temperature than the organic solvent gas. An adsorption step of adsorbing the organic solvent to the adsorption element by introducing an organic solvent-containing gas and discharging a clean gas; and introducing the exhaust gas into the adsorption element to desorb the organic solvent from the adsorption element to obtain the organic solvent. A concentration step including a desorption step of discharging the desorption gas contained therein; and a purge step of purging the adsorption device by introducing a portion of the clean gas discharged from the adsorption step into the adsorption device;
A cooling recovery step of cooling the desorption gas including the desorption gas or the exhaust gas to condense and recover the organic solvent
Including;
The organic solvent-containing gas is a gas containing the organic solvent not recovered in the cooling recovery step,
The purge part outlet gas discharged | emitted from the said purge process mixes with the said organic solvent containing gas introduce | transduced into the said adsorption process,
And the organic solvent-containing gas is introduced into the adsorption step in a state in which the organic solvent-containing gas is heated in response to the thermal energy of the purge part outlet gas. A part of the said purge part outlet gas is supplied to the said desorption process with the said exhaust gas, and / or is supplied to the said cooling recovery process with the said desorption gas,
Remainder of the said purge part exit gas is introduce | transduced into the said adsorption process with the said organic solvent containing gas,
An organic solvent recovery method in which the temperature of the organic solvent-containing gas introduced into the adsorption step is controlled by controlling the ratio of the air volume between the part of the purge part outlet gas and the remainder of the purge part outlet gas. The exhaust gas according to claim 27 or 28, wherein the exhaust gas is a gas discharged from a production facility,
And the remainder of the clean gas is returned to the production facility. The organic solvent recovery method according to any one of claims 27 to 29, wherein the exhaust gas has a temperature of 50 ° C to 200 ° C. The temperature of the said clean gas, the temperature of the said desorption gas, and the temperature of the said organic-solvent containing gas introduce | transduced into the said adsorption process become predetermined temperature, respectively,
The organic solvent recovery method in which the time of the said adsorption process, the time of the said desorption process, and the time of the said purge process are controlled. 32. The air flow rate ratio according to any one of claims 27 to 31, wherein the exhaust gas passes through the exhaust gas and the desorption gas in the cooling recovery step is 0% to 50%, and the desorption gas is 50%. 100% organic solvent recovery method. The organic-solvent recovery method of Claim 32 whose air volume ratio which makes the said exhaust gas and the said desorption gas pass through the said cooling recovery process is 0% and said desorption gas is 100%. The organic solvent according to any one of claims 27 to 33, wherein the organic solvent is selected from n-methyl-2-pyrrolidone, N, N-dimethylformamide, N, N-dimethylacetamide or n-decane. The organic solvent recovery method which is 1 or more types.

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