Dehydration system for organic solvent

Abstract

The utility model relates to the technical field of dehydration, in particular to an organic solvent dehydration system. The dehydration system comprises a raw material storage tank, a first-stage membrane separation unit, a second-stage membrane separation unit, a pressurizing and heating pipeline, a condensing and recycling pipeline and a return pipeline; pressurizing and heating the mixed material in the raw material storage tank, conveying to a first-stage membrane separation unit, and dehydrating for the first time; conveying a second separated substance of the first-stage membrane separation unit to a second-stage membrane separation unit for secondary dehydration; and condensing and recovering the second separated substance of the secondary membrane separation unit to obtain the low-water-content organic solvent. The system is provided with two stages of membrane separation units, and a first separated substance of the secondary membrane separation unit is mixed with a high-water-content organic solvent and then enters the membrane separation units for dehydration, so that the membrane dehydration efficiency is improved, the organic matter recovery rate of the system is improved, the sewage treatment load is reduced, and the operation cost is reduced.

Description

TECHNICAL FIELD

[0001] The utility model relates to dehydration technical field especially relates to a dehydration system of organic solvent. BACKGROUND

[0002] At present, the optimization of membrane separation technology in membrane material, membrane assembly and process flow mainly concentrates on the material of raw material side. The loss of organic solvent on the water permeation side, especially in the deep dehydration process, is less concerned. For high value-added organic solvent, its organic solvent recovery rate needs to be further improved. In addition, the high organic matter content on the water permeation side increases the sewage treatment load, resulting in the rise of production operation cost. SUMMARY

[0003] In view of the deficiencies in the prior art, the utility model provides a dehydration system of organic solvent, aiming at solving the problem of low organic solvent recovery rate.

[0004] The technical scheme provided by the utility model is:

[0005] A dehydration system of organic solvent, the dehydration system includes raw material storage tank, first stage membrane separation unit, second stage membrane separation unit, pressurized heating pipeline, condensation recovery pipeline and reflux pipeline;

[0006] The raw material storage tank is provided with raw material inlet, raw material outlet and permeate recovery port, the raw material inlet of the raw material storage tank is used for connecting with external raw material pipeline conveying high water content organic solvent, one end of the pressurized heating pipeline is connected with the raw material outlet of the raw material storage tank, the other end is connected with the material inlet of the first stage membrane separation unit, the material inlet of the second stage membrane separation unit is connected with the material outlet of the first stage membrane separation unit, one end of the condensation recovery pipeline is connected with the material outlet of the second stage membrane separation unit, one end of the reflux pipeline is connected with the vacuum outlet of the second stage membrane separation unit, the other end is connected with the permeate recovery port of the raw material storage tank, and the mixed material of the raw material storage tank includes high water content organic solvent conveyed by external raw material pipeline and the first separated material of the second stage membrane separation unit.

[0007] Further, the pressurized heating pipeline includes first pipeline, pressurized pump, preheater and heater, the pressurized pump, the preheater and the heater are sequentially arranged on the first pipeline, and the two ends of the first pipeline are connected with the raw material outlet of the raw material storage tank and the material inlet of the first stage membrane separation unit respectively.

[0008] Further, the condensing recovery pipeline comprises a second pipeline, a back pressure valve and a product condenser, the back pressure valve and the product condenser are arranged on the second pipeline, a section of the second pipeline is the hot fluid pipeline of the preheater and is located between the back pressure valve and the product condenser, one end of the second pipeline is connected with the material outlet of the secondary membrane separation unit.

[0009] Further, the reflux pipeline comprises a third pipeline, a secondary vacuum condenser and a permeate circulating pump, the secondary vacuum condenser and the permeate circulating pump are arranged on the third pipeline in sequence, two ends of the third pipeline are connected with the vacuum outlet of the secondary membrane separation unit and the permeate recovery port of the raw material storage tank respectively.

[0010] Further, the dehydration system further comprises a secondary vacuum set, a material inlet of the secondary vacuum set is connected with an outlet of the secondary vacuum condenser, for extracting uncondensed material, a material outlet of the secondary vacuum set is used for connecting a pipeline of a tail gas treatment system.

[0011] Further, the dehydration system further comprises a primary vacuum condenser, a hot material inlet of the primary vacuum condenser is connected with a vacuum outlet of the primary membrane separation unit, a condensed material outlet of the primary vacuum condenser is used for connecting a sewage treatment system.

[0012] Further, the dehydration system further comprises a primary vacuum set, a material inlet of the primary vacuum set is connected with an outlet of the primary vacuum condenser, a material outlet of the primary vacuum set is used for connecting a pipeline of a tail gas treatment system.

[0013] Further, the reflux pipeline comprises a third pipeline, a secondary vacuum condenser, a permeate circulating pump, a first switch valve, a fourth pipeline, a secondary vacuum set, a tail condenser and a second switch valve.

[0014] The secondary vacuum condenser, the first switch valve and the permeate circulating pump are arranged on the third pipeline in sequence, two ends of the third pipeline are connected with the vacuum outlet of the secondary membrane separation unit and the permeate recovery port of the raw material storage tank respectively.

[0015] The secondary vacuum set, the tail condenser and the second switch valve are arranged on the fourth pipeline in sequence, two ends of the fourth pipeline are connected with the outlet of the secondary vacuum condenser and a branch port of the third pipeline respectively, the branch port of the third pipeline is located between the first switch valve and the permeate circulating pump.

[0016] Further, the reflux pipeline has a first reflux mode, in the first reflux mode, the first switch valve is closed and the second switch valve is opened.

[0017] Further, the reflux pipeline has a second reflux mode, in which the first switch valve is opened, and the second switch valve is opened.

[0018] According to the technical scheme, the utility model has the beneficial effects: the utility model has two-stage membrane separation units, the first-stage membrane separation unit can complete the first dehydration, the second-stage membrane separation unit further dehydrates the second separated material of the first-stage membrane separation unit, that is, the second dehydration is performed, so that deep dehydration is achieved, the first separated material of the second-stage membrane separation unit is returned to the raw material storage tank, the first separated material of the second-stage membrane separation unit is mixed with the high-water-content organic solvent and then enters the membrane separation unit for dehydration, the organic matter recovery rate of the system is improved, the sewage treatment load is reduced, and the operation cost is reduced. BRIEF DESCRIPTION OF DRAWINGS

[0019] Figure 1 is a structural schematic block diagram of the organic solvent dehydration system provided by the utility model embodiment;

[0020] Figure 2 is a structural schematic block diagram of the organic solvent dehydration system provided by another utility model embodiment. DETAILED DESCRIPTION

[0021] In order to make the purpose, technical scheme and advantages of the utility model more clear, the utility model is further described in detail below in combination with the drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain the utility model, and are not used to limit the utility model.

[0022] As shown in the drawings, Figure 1 An organic solvent dehydration system is provided by the utility model embodiment, and the dehydration system comprises a raw material storage tank 21, a first-stage membrane separation unit 31, a second-stage membrane separation unit 32, a pressurized and heated pipeline, a condensation and recovery pipeline and a reflux pipeline.

[0023] The raw material storage tank 21 is provided with a raw material inlet, a raw material outlet and a permeate recovery port, the raw material inlet of the raw material storage tank 21 is used to be connected with an external raw material pipeline conveying a high-water-content organic solvent, one end of the pressurized and heated pipeline is connected with the raw material outlet of the raw material storage tank 21, the other end is connected with a material inlet of the first-stage membrane separation unit 31, a material inlet of the second-stage membrane separation unit 32 is connected with a material outlet of the first-stage membrane separation unit 31, one end of the condensation and recovery pipeline is connected with a material outlet of the second-stage membrane separation unit 32, one end of the reflux pipeline is connected with a vacuum outlet of the second-stage membrane separation unit 32, and the other end is connected with the permeate recovery port of the raw material storage tank 21, and the mixed material of the raw material storage tank comprises the high-water-content organic solvent conveyed by the external raw material pipeline and the first separated material of the second-stage membrane separation unit 32.

[0024] The pressurized heating pipeline transports the mixed material in the raw material storage tank 21 to the primary membrane separation unit 31 for the first dehydration under pressure and heating. The raw material storage tank 21 is provided with a raw material inlet for connecting to an external raw material pipeline. The raw material storage tank 21 is provided with a permeate recovery port for connecting to the outlet of the permeate circulation pump 63. The raw material storage tank 21 is provided with a raw material outlet for connecting to the pressure pump 22.

[0025] The primary membrane separation unit 31 is composed of one or more membrane modules connected in series. The material inlet of the first membrane module is connected to the outlet of the heater 24, and the material outlet of the last membrane module is connected to the inlet of the secondary membrane separation unit. A vacuum pipeline is provided on one side of each membrane module and is connected to the inlet of the primary vacuum condenser 41.

[0026] The second separated product of the primary membrane separation unit is transported to the secondary membrane separation unit for a second dehydration. The secondary membrane separation unit 32 is composed of one or more membrane modules connected in series. The material inlet of the first membrane module is connected to the outlet of the primary membrane separation unit 31, and the material outlet of the last membrane module is connected to the inlet of the back pressure valve 51. A vacuum pipeline is installed on one side of each membrane module and is connected to the inlet of the secondary vacuum condenser 61.

[0027] The condensation recovery pipeline condenses and recovers the second separation product of the secondary membrane separation unit 32 to obtain a low-water-content organic solvent.

[0028] The reflux pipeline returns the first separation product of the secondary membrane separation unit 32 to the raw material storage tank 21 .

[0029] The utility model is provided with a two-stage membrane separation unit. The first-stage membrane separation unit 31 can complete the first dehydration, and the second-stage membrane separation unit 32 further dehydrates the second separation of the first-stage membrane separation unit 31, that is, performs a second dehydration to achieve deep dehydration, and returns the first separation of the second-stage membrane separation unit 32 to the raw material storage tank 21. The first separation of the second-stage membrane separation unit 32 is mixed with a high-water-content organic solvent and then enters the membrane separation unit for dehydration, thereby improving the organic matter recovery rate of the system, reducing the sewage treatment load, and reducing operating costs.

[0030] In this embodiment, the first separated product is the permeate and the second separated product is the retentate.

[0031] In this embodiment, the pressurized heating pipeline includes a first pipeline, a pressure pump 22, a preheater 23 and a heater 24. The pressure pump 22, the preheater 23 and the heater 24 are arranged in sequence on the first pipeline, and the two ends of the first pipeline are respectively connected to the raw material outlet of the raw material storage tank 21 and the material inlet of the first membrane separation unit 31.

[0032] The mixture in the raw material tank 21 is sequentially pressurized by the pressurizing pump 22, preheated by the preheater 23, and heated to operating temperature by the heater 24, and then enters the first membrane separation unit 31 for the first dehydration.

[0033] The pressurizing pump 22 is used to impart energy to the raw material and transport the material, and the inlet and outlet thereof are respectively connected with the raw material tank 21 and the preheater 23.

[0034] The preheater 23 is used to recover part of the heat and reduce the cost, and the cold material is the mixture in the raw material tank, and the hot material is the second separated material of the second membrane separation unit 32.

[0035] The heater 23 can be a liquid heater, and can also be a vaporizer, which is used to further heat the mixture in the raw material tank 21 to operating temperature, and the phase of the mixture in the raw material tank 21 in the first and second membrane separation units can be vapor phase or liquid phase. If it is liquid phase, the heater is a liquid heater; if it is vapor phase, the heater is a vaporizer.

[0036] In the embodiment, the condensation recovery pipeline comprises a second pipeline, a back pressure valve 51 and a product condenser 52, the back pressure valve 52 and the product condenser 52 are arranged on the second pipeline, one section of the second pipeline is the hot fluid pipeline of the preheater 23, and is located between the back pressure valve 52 and the product condenser 52, and one end of the second pipeline is connected with the material outlet of the second membrane separation unit 32.

[0037] The second separated material of the second membrane separation unit 32 is sequentially condensed by the back pressure valve 52, the hot fluid pipeline of the preheater 23 and the product condenser 52, and a low-water organic solvent is obtained, wherein the pipeline of the preheater 23 through which the mixture in the raw material tank 21 passes is a cold fluid pipeline.

[0038] The back pressure valve 51 is used to assist in imparting pressure to the raw material side material of the first and second membrane separation units, the back pressure valve 51 is provided with an inlet for being connected with the material outlet of the second membrane separation unit 32, and the back pressure valve 51 is provided with an outlet for being connected with the material inlet of the preheater 23.

[0039] The product condenser 52 is used for product cooling, and the hot material is a low-water-content product cooled by waste heat recovery, and the cold material is circulating water.

[0040] In the embodiment, the reflux pipeline comprises a third pipeline, a second vacuum condenser 61 and a permeate circulating pump 63, the second vacuum condenser 61 and the permeate circulating pump 63 are sequentially arranged on the third pipeline, and two ends of the third pipeline are respectively connected with the vacuum outlet of the second membrane separation unit 32 and the permeate recovery port of the raw material tank 21.

[0041] The first separated material of the secondary membrane separation unit 32 is sequentially condensed by the secondary vacuum condenser 61, and the permeate circulation pump 63 returns to the raw material storage tank 21.

[0042] The secondary vacuum condenser 61 is used to condense the first separated material of the secondary membrane separation unit 32, and the hot material inlet of the secondary vacuum condenser 61 is connected with the vacuum outlet header of the secondary membrane separation unit 32. The condensed material is connected to the secondary water permeation side organic matter content condensate pipeline, and then discharged to the inlet of the permeate circulation pump 63. The uncondensed material is connected to the inlet of the secondary vacuum unit.

[0043] The permeate circulation pump 63 is used to realize the recovery of the first separated material of the secondary membrane separation unit 32, and the inlet of the permeate circulation pump 63 is connected with the condensed material outlet of the secondary vacuum condenser 61. The outlet of the permeate circulation pump 63 is connected with the inlet of the raw material storage tank 21.

[0044] In this embodiment, the dehydration system further comprises a secondary vacuum unit 66, the material inlet of the secondary vacuum unit 66 is connected with the outlet of the secondary vacuum condenser 61, and the uncondensed material is extracted. The material outlet of the secondary vacuum unit 66 is used to connect the tail gas treatment system pipeline.

[0045] The uncondensed material in the secondary vacuum condenser 61 is transported to the tail gas treatment system pipeline through the secondary vacuum unit 66.

[0046] The secondary vacuum unit 66 is used to give the water permeation side of the secondary membrane separation unit a vacuum degree and extract the uncondensed material. The material inlet of the secondary vacuum unit 66 is connected with the outlet of the secondary vacuum condenser 61. The material outlet of the secondary vacuum unit 66 is connected with the tail gas treatment system pipeline.

[0047] In this embodiment, the dehydration system further comprises a primary vacuum condenser 41, the hot material inlet of the primary vacuum condenser 41 is connected with the vacuum outlet of the primary membrane separation unit 31, and the condensed material outlet of the primary vacuum condenser 41 is connected with the sewage treatment system.

[0048] The first separated material of the primary membrane separation unit 31 is sequentially condensed by the primary vacuum condenser 41 and then discharged to the sewage treatment system.

[0049] The primary vacuum condenser 41 is used to condense the first separated material of the primary membrane separation unit 31, and the hot material inlet is connected with the vacuum outlet header of the primary membrane separation unit 31. The condensed material is connected to the primary water permeation side high water content condensate pipeline and then discharged to the sewage treatment system. The uncondensed material is connected to the inlet of the primary vacuum unit 42.

[0050] In this embodiment, the dehydration system further includes a first-stage vacuum unit 42, the material inlet of the first-stage vacuum unit 42 is connected to the outlet of the first-stage vacuum condenser 41, and the material outlet of the first-stage vacuum unit 42 is used to connect to the exhaust gas treatment system pipeline.

[0051] The uncondensed material in the first-stage vacuum condenser 41 is transported to the tail gas treatment system pipeline via the first-stage vacuum unit 42 .

[0052] The first-level vacuum unit 42 is used to provide vacuum on the water permeation side of the first-level membrane separation unit and to produce uncondensed materials. The first-level vacuum unit 42 is provided with a material inlet for connecting to the outlet of the first-level vacuum condenser 41. The first-level vacuum unit 42 is provided with a material outlet for connecting to the tail gas treatment system pipeline.

[0053] like Figure 2 As shown, in some embodiments, the reflux line includes a third pipeline, a secondary vacuum condenser 61, a permeate circulation pump 63, a first switch valve 62, a fourth pipeline, a secondary vacuum unit 66, a tail cooler 64 and a second switch valve 65;

[0054] The secondary vacuum condenser 61, the first switch valve 62 and the permeate circulation pump 63 are sequentially arranged on the third pipeline, and the two ends of the third pipeline are respectively connected to the vacuum outlet of the secondary membrane separation unit 32 and the permeate recovery port of the raw material storage tank 21;

[0055] The secondary vacuum unit 66, the tail cooler 64 and the second switch valve 65 are sequentially arranged on the fourth pipeline. The two ends of the fourth pipeline are respectively connected to the outlet of the secondary vacuum condenser 61 and the branch port of the third pipeline. The branch port of the third pipeline is located between the first switch valve 62 and the permeate circulation pump 63.

[0056] The reflux line has a first reflux mode. In the first reflux mode, the first switch valve 62 is closed and the second switch valve 65 is open.

[0057] Control the second switch valve 65 to open; the first separation of the secondary membrane separation unit 32 is sequentially condensed through the secondary vacuum condenser 61 for the first time, the secondary vacuum unit 66, the tail cooler 64 for the second condensation, and the permeate circulation pump 63 is refluxed to the raw material storage tank 21.

[0058] In the embodiment of the utility model, mainly applied to low boiling point organic solvent, namely the organic solvent with boiling point below 100 DEG C. The second switch valve 65 opens, the first switch valve 62 closes, the first separated object of two stage membrane separation unit 32 is sequentially condensed in two stage vacuum condenser 61, is condensed in two stage vacuum unit 66, tail cooler 64 second time, and is sequentially condensed in permeate circulating pump 63, is then transported to raw material storage tank 21 by the outlet of permeate circulating pump 63.

[0059] In some embodiments, the return line has a second return mode in which the first switch valve 62 is open and the second switch valve 65 is open.

[0060] The first switch valve 62 and the second switch valve 65 are opened, the first separated object of the two stage membrane separation unit 32 is sequentially condensed in the two stage vacuum condenser 61, and is returned to the raw material storage tank 21 by the permeate circulating pump 63; the uncondensed material in the two stage vacuum condenser 61 is sequentially condensed in the two stage vacuum unit 66 and the tail cooler 64, and is returned to the raw material storage tank 21 by the permeate circulating pump 63.

[0061] In the embodiment of the utility model, mainly applied to high boiling point organic solvent, namely the organic solvent with boiling point above 100 DEG C, realize two times recovery to high water content organic solvent. The second switch valve 65 opens, the first switch valve 62 opens, the first separated object of two stage membrane separation unit 32 is sequentially condensed in two stage vacuum condenser 61 and enters the inlet of permeate circulating pump 63; the uncondensed material in two stage vacuum condenser 61 is sequentially condensed in two stage vacuum unit 66 and tail cooler 64 and enters the inlet of permeate circulating pump 63; then is transported to raw material storage tank 21 by the outlet of permeate circulating pump 63.

[0062] The above only is the preferred embodiment of the utility model, and does not use to limit the utility model, any modification, equivalent replacement and improvement etc. that are made within the spirit and principle of the utility model should be included in the protection scope of the utility model.

Claims

1. An organic solvent dehydration system characterized by, The dehydration system comprises a raw material storage tank, a first membrane separation unit, a second membrane separation unit, a pressurized heating pipeline, a condensation recovery pipeline and a reflux pipeline; The raw material storage tank is provided with a raw material inlet, a raw material outlet and a permeate recovery port, the raw material inlet of the raw material storage tank is used to be connected with an external raw material pipeline conveying the high-water-content organic solvent, one end of the pressurized heating pipeline is connected with the raw material outlet of the raw material storage tank, the other end is connected with a material inlet of the first membrane separation unit, a material inlet of the second membrane separation unit is connected with a material outlet of the first membrane separation unit, one end of the condensation recovery pipeline is connected with a material outlet of the second membrane separation unit, one end of the reflux pipeline is connected with a vacuum outlet of the second membrane separation unit, the other end is connected with the permeate recovery port of the raw material storage tank, and the mixed material of the raw material storage tank comprises the high-water-content organic solvent conveyed by the external raw material pipeline and the first separated material of the second membrane separation unit.

2. The organic solvent dehydration system of claim 1, wherein, The pressurized heating pipeline comprises a first pipeline, a pressurized pump, a preheater and a heater, the pressurized pump, the preheater and the heater are sequentially arranged on the first pipeline, and two ends of the first pipeline are respectively connected with the raw material outlet of the raw material storage tank and the material inlet of the first membrane separation unit.

3. The organic solvent dehydrating system according to claim 2, wherein The condensation recovery pipeline comprises a second pipeline, a back pressure valve and a product condenser, the back pressure valve and the product condenser are arranged on the second pipeline, a section of the second pipeline is a hot fluid pipeline of the preheater and is located between the back pressure valve and the product condenser, and one end of the second pipeline is connected with the material outlet of the second membrane separation unit.

4. The organic solvent dehydration system of claim 1, wherein The reflux pipeline comprises a third pipeline, a second vacuum condenser and a permeate circulating pump, the second vacuum condenser and the permeate circulating pump are sequentially arranged on the third pipeline, and two ends of the third pipeline are respectively connected with the vacuum outlet of the second membrane separation unit and the permeate recovery port of the raw material storage tank.

5. The organic solvent dehydrating system according to claim 4, wherein The dehydration system further comprises a second vacuum unit, a material inlet of the second vacuum unit is connected with an outlet of the second vacuum condenser, and the second vacuum unit is used to extract uncondensed material, and a material outlet of the second vacuum unit is used to be connected with a tail gas treatment system pipeline.

6. The organic solvent dehydrating system according to claim 1, wherein The dehydration system further comprises a first vacuum condenser, a hot material inlet of the first vacuum condenser is connected with a vacuum outlet of the first membrane separation unit, and a condensed material outlet of the first vacuum condenser is used to be connected with a sewage treatment system.

7. The organic solvent dehydrating system according to claim 6, wherein The dehydration system further comprises a first vacuum unit, a material inlet of the first vacuum unit is connected with an outlet of the first vacuum condenser, and a material outlet of the first vacuum unit is used to be connected with a tail gas treatment system pipeline.

8. The organic solvent dehydration system of claim 1, wherein, The reflux pipeline comprises a third pipeline, a second vacuum condenser, a permeate circulating pump, a first switch valve, a fourth pipeline, a second vacuum unit, a tail condenser and a second switch valve; The second vacuum condenser, the first switch valve and the permeate circulating pump are sequentially arranged on the third pipeline, and two ends of the third pipeline are respectively connected with the vacuum outlet of the second membrane separation unit and the permeate recovery port of the raw material storage tank. The second vacuum unit, the fourth pipeline, the tail condenser and the second switch valve are sequentially arranged on the fourth pipeline, and two ends of the fourth pipeline are respectively connected with the material outlet of the first vacuum unit and the material inlet of the second vacuum unit. The secondary vacuum unit, the tail cooler and the second switch valve are sequentially arranged on the fourth pipeline, two ends of the fourth pipeline are connected with an outlet of the secondary vacuum condenser and a branch of the third pipeline respectively, and the branch of the third pipeline is located between the first switch valve and the permeate circulating pump.

9. The organic solvent dehydrating system according to claim 8, wherein The return pipeline has a first return mode, in which the first switch valve is closed and the second switch valve is opened.

10. The organic solvent dehydration system of claim 8, wherein, The return pipeline has a second return mode, in which the first switch valve is opened and the second switch valve is opened.

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