CN117658260A - Tetrahydrofuran waste liquid recovery system and method - Google Patents
Tetrahydrofuran waste liquid recovery system and method Download PDFInfo
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- CN117658260A CN117658260A CN202311652356.9A CN202311652356A CN117658260A CN 117658260 A CN117658260 A CN 117658260A CN 202311652356 A CN202311652356 A CN 202311652356A CN 117658260 A CN117658260 A CN 117658260A
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- tetrahydrofuran
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- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 title claims abstract description 218
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 title claims abstract description 110
- 239000007788 liquid Substances 0.000 title claims abstract description 81
- 239000002699 waste material Substances 0.000 title claims abstract description 69
- 238000011084 recovery Methods 0.000 title claims abstract description 23
- 238000000034 method Methods 0.000 title claims abstract description 16
- 239000012528 membrane Substances 0.000 claims abstract description 46
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 38
- 230000008016 vaporization Effects 0.000 claims abstract description 25
- 238000009834 vaporization Methods 0.000 claims abstract description 23
- 239000012535 impurity Substances 0.000 claims abstract description 16
- 239000000203 mixture Substances 0.000 claims abstract description 12
- 238000005373 pervaporation Methods 0.000 claims abstract description 11
- 238000010992 reflux Methods 0.000 claims description 50
- 238000000926 separation method Methods 0.000 claims description 20
- 239000012071 phase Substances 0.000 claims description 16
- 239000007791 liquid phase Substances 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 5
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims description 3
- 238000001179 sorption measurement Methods 0.000 claims description 3
- 238000005215 recombination Methods 0.000 claims 3
- 230000006798 recombination Effects 0.000 claims 3
- 238000002407 reforming Methods 0.000 claims 2
- 238000001704 evaporation Methods 0.000 claims 1
- 239000000463 material Substances 0.000 abstract description 16
- 239000000047 product Substances 0.000 description 21
- 239000007789 gas Substances 0.000 description 12
- 230000009466 transformation Effects 0.000 description 10
- 230000018044 dehydration Effects 0.000 description 6
- 238000006297 dehydration reaction Methods 0.000 description 6
- YEJRWHAVMIAJKC-UHFFFAOYSA-N 4-Butyrolactone Chemical compound O=C1CCCO1 YEJRWHAVMIAJKC-UHFFFAOYSA-N 0.000 description 5
- 239000002808 molecular sieve Substances 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 5
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 4
- JKTCBAGSMQIFNL-UHFFFAOYSA-N 2,3-dihydrofuran Chemical compound C1CC=CO1 JKTCBAGSMQIFNL-UHFFFAOYSA-N 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 3
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000007792 gaseous phase Substances 0.000 description 2
- 239000002920 hazardous waste Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- WERYXYBDKMZEQL-UHFFFAOYSA-N butane-1,4-diol Chemical compound OCCCCO WERYXYBDKMZEQL-UHFFFAOYSA-N 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 150000002170 ethers Chemical class 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- -1 heterocyclic organic compound Chemical class 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000007873 sieving Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 125000003718 tetrahydrofuranyl group Chemical group 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to the technical field of tetrahydrofuran waste liquid treatment, in particular to a tetrahydrofuran waste liquid recovery system and a tetrahydrofuran waste liquid recovery method, wherein the tetrahydrofuran waste liquid recovery system comprises a light component, a heavy component and a vaporization membrane device, the light component comprises a light component, the heavy component comprises a heavy component, the light component, the heavy component and the vaporization membrane device are connected with each other through a pipeline and a conveying pump to convey materials, and the tetrahydrofuran waste liquid recovery method comprises the following steps: s1, rectifying tetrahydrofuran waste liquid to remove light components and impurities; s2, rectifying tetrahydrofuran, water and heavy components obtained after the light component removal of the S1 to remove heavy component impurities; s3, removing water from the tetrahydrofuran and water mixture obtained after the weight removal of the S2 by pervaporation, and finally obtaining a tetrahydrofuran finished product.
Description
Technical Field
The invention relates to the technical field of tetrahydrofuran waste liquid treatment, in particular to a tetrahydrofuran waste liquid recovery system and a tetrahydrofuran waste liquid recovery method.
Background
Tetrahydrofuran (THF), also known as oxolane, 1, 4-epoxybutane, is a heterocyclic organic compound of the formula C4H8O, belongs to ethers, is a completely hydrogenated product of furan, is a colorless transparent liquid, is dissolved in water, ethanol, diethyl ether, acetone, benzene, and the like, and is mainly used as a solvent, a chemical synthesis intermediate, an analytical reagent.
In the production of N-methylpyrrolidone (NMP), the byproducts are increased along with the improvement of the productivity of the device; tetrahydrofuran is a byproduct of gamma-butyrolactone (GBL) after light component removal, THF waste liquid is generally stored in a THF waste liquid storage tank after light component removal and then is filled into a ton barrel, and is sent out to be used as dangerous waste treatment, but the THF waste liquid treatment cost is extremely high, the operation cost of a company is increased, and the market competitiveness of the company is reduced due to the increase of the cost under the huge market competition pressure.
Disclosure of Invention
In order to solve the technical problems, the invention provides a tetrahydrofuran waste liquid recovery system and a tetrahydrofuran waste liquid recovery method, so as to achieve the purposes of recycling tetrahydrofuran waste liquid, removing impurities in the tetrahydrofuran waste liquid and improving the purity of products.
The invention is realized by the following technical scheme:
the tetrahydrofuran waste liquid recovery system comprises a light component removing component for removing light component impurities in waste liquid, a heavy component removing component for removing heavy component impurities in waste liquid and a vaporization membrane device for vaporizing and separating water in tetrahydrofuran and water mixture, wherein the light component removing component comprises a light component removing tower, the heavy component removing component comprises a light component removing tower, and the light component removing tower, the heavy component removing tower and the vaporization membrane device are connected with each other through a pipeline and a conveying pump to convey materials.
Further preferably, the light component further comprises a first-stage condenser A, a second-stage condenser A, a first reflux tank and a first reflux pump, wherein the first-stage condenser A, the first reflux tank and the first reflux pump are sequentially connected through pipelines, a feeding end of the first-stage condenser A is connected with a pipeline at the top of the light tower, an output end of the first reflux pump is connected with the pipeline at the top of the light tower, the second-stage condenser A is connected with the outer pipeline of the first-stage condenser A, and a discharging end of the second-stage condenser A is connected with the pipeline from the first-stage condenser A to the first reflux tank through a pipeline.
Further preferably, the system further comprises a light component storage tank, and a pipeline connected with the light component storage tank is further arranged on a pipeline connected with the top of the light component removal column through the first reflux pump.
Further preferably, the light component further comprises a first reboiler, and the first reboiler is connected with the bottom of the light component through an inlet and outlet pipeline.
Further preferably, the weight removing assembly further comprises a first-stage condenser B, a second reflux tank and a second reflux pump, wherein the first-stage condenser B, the second reflux tank and the second reflux pump are sequentially connected through pipelines, the feeding end of the first-stage condenser B is connected with the top pipeline of the weight removing tower, the output end of the second reflux pump is connected with the top pipeline of the weight removing tower, a pipeline connected with the feeding end of the second-stage condenser B is further arranged outside the first-stage condenser B, and the discharging end of the second-stage condenser B is connected with the pipeline from the first-stage condenser B to the second reflux tank through the pipeline.
Further preferably, the heavy component removing device further comprises a second reboiler, and the second reboiler is connected with the bottom of the heavy component removing device through an inlet and outlet pipeline.
Still preferably, the pipeline that second backwash pump and heavy-duty removal top of the tower are connected still has the conveying pipeline of being connected with vaporization membrane device, vaporization membrane device includes temporary storage tank, the pre-heater, the evaporimeter, the gas-liquid separation jar, membrane module, first order condenser C and second grade condenser C, temporary storage tank is connected with the conveying pipeline, temporary storage tank discharge end passes through the delivery pump and is connected with the pre-heater through pipeline, the pre-heater top is connected with the evaporimeter pipeline, the evaporimeter is connected with the gas-liquid separation jar pipeline, the liquid phase after the gas-liquid separation jar separation is connected with the evaporimeter through the liquid phase pipe that sets up, the gaseous phase after the gas-liquid separation jar separation is connected with the membrane module through the gaseous phase pipe that sets up, membrane module's discharge end and pre-heater pipe connection, pre-heater bottom and first order condenser C pipe connection, first order condenser C and second grade condenser C pipe connection.
A tetrahydrofuran waste liquid recovery method comprises the following steps:
s1, rectifying tetrahydrofuran waste liquid to remove light components and impurities;
s2, rectifying tetrahydrofuran, water and heavy components obtained after the light component removal of the S1 to remove heavy component impurities;
s3, removing water from the tetrahydrofuran and water mixture obtained after the weight removal of the S2 through pervaporation, and finally obtaining a tetrahydrofuran finished product.
Further preferably, S2 is rectified in a heavy-duty removal tower to remove heavy weight, gas phase in the heavy-duty removal tower is subjected to two-stage deep condensation and separation, part of condensate is returned to the heavy-duty removal tower, and part of condensate is extracted to be vaporized to remove water.
Further preferably, in the step S3, the tetrahydrofuran and water mixture is preheated, evaporated and vaporized, vapor and liquid are separated, the separated liquid phase is returned to be vaporized again, the separated gas phase is subjected to heat exchange and adsorption to remove water molecules, and the product is obtained after condensation.
The invention has the beneficial effects that:
1) The invention removes light component impurities such as 2, 3-dihydrofuran in the tetrahydrofuran waste liquid through the light component removing tower, removes heavy component impurities in the tetrahydrofuran waste liquid through the heavy component removing tower, and then the water in the mixture of tetrahydrofuran and water is separated through vaporization of the vaporization membrane device, finally the high-purity tetrahydrofuran finished product is obtained, and the purity of the product is more than 99.5%.
2) The invention adopts the pervaporation molecular sieve membrane to realize molecular sieving dehydration under the azeotropic system of tetrahydrofuran and water, and the water content of the tetrahydrofuran is less than 0.1wt.% after the dehydration of the pervaporation molecular sieve membrane.
3) The invention changes waste tetrahydrofuran liquid into qualified tetrahydrofuran product, fully utilizes material resources, saves cost for treating the waste tetrahydrofuran liquid, creates economic benefit and improves the market competitiveness of companies.
The following describes the embodiments of the present invention in further detail with reference to the drawings.
Drawings
The accompanying drawings are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate the invention and together with the description serve to explain, without limitation, the invention. In the drawings:
FIG. 1 is a schematic diagram of a tetrahydrofuran waste liquid recovery system of the present invention.
1-waste liquid storage tank, 2-delivery pump, 3-delivery pipe, 100-light component, 110-light component removal tower, 120-first reboiler, 130-first-stage condenser A, 140-second-stage condenser A, 150-first reflux tank, 160-first reflux pump, 170-light component storage tank, 200-heavy component removal component, 210-heavy component removal tower, 220-second reboiler, 230-first-stage condenser B, 240-second-stage condenser B, 250-second reflux tank, 260-second reflux pump, 270-heavy component storage tank, 280-bottom pump, 300-vaporization membrane device, 310-temporary storage tank, 320-preheater, 330-evaporator, 340-gas-liquid separation tank, 350-membrane component, 360-first-stage condenser C, 370-second-stage condenser C, 380-liquid phase pipe, 390-gas phase pipe.
Detailed Description
Embodiments of the present invention are described in detail below, examples of which are illustrated in the accompanying drawings, wherein the same or similar reference numerals refer to the same or similar elements or elements having the same or similar functions throughout. The embodiments described below by referring to the drawings are exemplary only for explaining the present invention and are not to be construed as limiting the present invention.
In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more of the described features. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.
In the description of the present invention, it should be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically connected, electrically connected or can be communicated with each other; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
In the present invention, unless expressly stated or limited otherwise, a first feature "above" or "below" a second feature may include both the first and second features being in direct contact, as well as the first and second features not being in direct contact but being in contact with each other through additional features therebetween. Moreover, a first feature being "above," "over" and "on" a second feature includes the first feature being directly above and obliquely above the second feature, or simply indicating that the first feature is higher in level than the second feature. The first feature being "under", "below" and "beneath" the second feature includes the first feature being directly under and obliquely below the second feature, or simply means that the first feature is less level than the second feature.
The following disclosure provides many different embodiments, or examples, for implementing different features of the invention. In order to simplify the present disclosure, components and arrangements of specific examples are described below. They are, of course, merely examples and are not intended to limit the invention. Furthermore, the present invention may repeat reference numerals and/or letters in the various examples, which are for the purpose of brevity and clarity, and which do not themselves indicate the relationship between the various embodiments and/or arrangements discussed. In addition, the present invention provides examples of various specific processes and materials, but one of ordinary skill in the art will recognize the application of other processes and/or the use of other materials.
Referring to fig. 1, fig. 1 is a schematic diagram of a tetrahydrofuran waste liquid recovery system according to the present invention.
The utility model provides a tetrahydrofuran waste liquid recovery system, includes rectifier unit and vaporization membrane device 300, and rectifier unit includes light component 100 and takes off recombinant 200, and tetrahydrofuran waste liquid is through light component 100, heavy component 200 and vaporization membrane device 300 of taking off in proper order and is formed the tetrahydrofuran product finally, and light component 100 includes light component 110, and heavy component 200 of taking off includes heavy component 210, takes off between light component 110, heavy component 210 and the vaporization membrane device 300 through pipeline and delivery pump 2 connection conveying material.
The tetrahydrofuran waste liquid is treated by a tetrahydrofuran rectifying device and a vaporization membrane device 300 to form a tetrahydrofuran product; the tetrahydrofuran rectifying device has two packed rectifying columns: a light ends removal column 110 and a heavy ends removal column 210; the main functions of the light ends column 110 are: light component impurities such as 2, 3-dihydrofuran and the like are removed from the tower top, and the main functions of the heavy component removal tower 210 are as follows: and (3) utilizing tetrahydrofuran to azeotropy with water, extracting high-concentration tetrahydrofuran products from the top of the tower, and removing water, BDO, GBL, butanol and other heavy components from the bottom of the tower.
Specifically, the light component removal assembly 100 further includes a first reboiler 120, a first-stage condenser a130, a second-stage condenser a140, a first reflux tank 150 and a first reflux pump 160, the first reboiler 120 is connected to the bottom of the light component removal column 110 through an inlet pipe and an outlet pipe, the first-stage condenser a130, the first reflux tank 150 and the first reflux pump 160 are sequentially connected through pipes, a feed end of the first-stage condenser a130 is connected to a top pipe of the light component removal column 110, an output end of the first reflux pump 160 is connected to the top pipe of the light component removal column 110, a pipe connected to the light component storage tank 170 is further arranged on a connecting pipe between the first reflux pump 160 and the top of the light component removal column 110, a pipe connected to a feed end of the second-stage condenser a140 is further arranged outside the first-stage condenser a130, a discharge end of the second-stage condenser a140 is connected to a pipe between the first-stage condenser a130 and the first reflux tank 150 through a pipe, and a transfer pump 2 at the bottom of the light component removal column 110 transfers tetrahydrofuran, water and heavy components to the heavy component removal column 210.
The heavy component removal assembly 200 further comprises a second reboiler 220, a first-stage condenser B230, a second-stage condenser B240, a second reflux tank 250 and a second reflux pump 260, wherein the second reboiler 220 is connected with the bottom of the heavy component removal tower 210 through an inlet pipeline and an outlet pipeline, the first-stage condenser B230, the second reflux tank 250 and the second reflux pump 260 are sequentially connected through pipelines, the feeding end of the first-stage condenser B230 is connected with the pipeline at the top of the heavy component removal tower 210, the output end of the second reflux pump 260 is connected with the pipeline at the top of the heavy component removal tower 210, a conveying pipe 3 connected with the vaporization membrane device 300 is further arranged on the pipeline connected with the top of the heavy component removal tower 210, a pipeline connected with the feeding end of the second-stage condenser B240 is further arranged outside the first-stage condenser B230, the discharging end of the second-stage condenser B240 is connected with the pipeline from the first-stage condenser B230 to the second reflux tank 250, a bottom pump 280 is arranged at the bottom of the heavy component removal tower 210, and the bottom of the bottom pump 280 conveys heavy component at the bottom of the heavy component removal tower 210 to the heavy component storage tank 270.
The vaporization membrane device 300 comprises a temporary storage tank 310, a preheater 320, an evaporator 330, a gas-liquid separation tank 340, a membrane assembly 350, a primary condenser C360 and a secondary condenser C370, wherein the temporary storage tank 310 is connected with a conveying pipe 3, the discharge end of the temporary storage tank 310 is connected with the preheater 320 through a conveying pump 2 and a pipeline, the top of the preheater 320 is connected with the evaporator 330 through a pipeline, the evaporator 330 is connected with the gas-liquid separation tank 340 through a pipeline, a liquid phase separated by the gas-liquid separation tank 340 flows back to the evaporator 330 through a liquid phase pipe 380, a gas phase separated by the gas-liquid separation tank 340 is connected with the membrane assembly 350 through a gas phase pipe 390, the discharge end of the membrane assembly 350 is connected with the preheater 320, the bottom of the preheater 320 is connected with the primary condenser C360 through a pipeline, and the primary condenser C360 is connected with the secondary condenser C370 through a pipeline.
Example 1
The tetrahydrofuran waste liquid in the tetrahydrofuran waste liquid storage tank 1 enters the light component removal tower 110 through a conveying pump 2 in front of the light component removal tower 110 under the control of a flow regulating valve, the light component removal tower 110 is provided with two feed inlets, a proper feed inlet is selected according to actual operation conditions, and the tetrahydrofuran waste liquid is subjected to normal pressure rectification in the light component removal tower 110; the heat source of the light component removal tower 110 is low-pressure steam, the pressure is 5bar, the tower bottom material is heated by a first reboiler 120 of the light component removal tower 110, the rectification heat of the system is maintained, light component impurities such as 2, 3-dihydrofuran in the tetrahydrofuran waste liquid are separated from the tower top, the light component impurities are condensed and separated by a first-stage condenser A130 at the top of the light component removal tower 110, condensate enters a first reflux tank 150 of the light component removal tower 110, then part of condensate flows back into the light component removal tower 110 by a first reflux pump 160 of the light component removal tower 110, the reflux quantity is controlled by a flow regulating valve, and part of condensate is extracted into a tetrahydrofuran light component storage tank 170 and the extraction quantity is controlled by a regulating valve; the gas phase in the first condenser A130 is deeply condensed by the second condenser A140 of the light component removal tower 110, condensate enters the first reflux tank 150 of the light component removal tower 110, and noncondensable gas enters the tail gas system for treatment. Tetrahydrofuran, water and heavy components at the bottom of the light ends removal column 110 are conveyed to the heavy ends removal column 210 through a conveying pump 2 at the bottom of the column.
The material is rectified in the heavy-removal tower 210 under normal pressure, the heat source of the tower kettle is low-pressure steam, the pressure is 5bar, under the heating of the second reboiler 220 at the bottom of the heavy-removal tower 210, the tetrahydrofuran product in the gas-phase rectifying section is cooled by the first condenser B230 at the top of the tower, the condensate enters the second reflux tank 250 at the top of the tower, part of the condensate flows back into the heavy-removal tower 210, part of the condensate is extracted to the tetrahydrofuran temporary storage tank 310, and the bottom of the temporary storage tank 310 is extracted to the conveying pump 2 of the vaporization membrane device 300; the gas phase of the first condenser B230 is deeply condensed by the second condenser B240 of the de-weight tower 210, the condensate enters the second reflux tank 250 of the de-weight tower 210, and the non-condensable gas enters the tail gas system for treatment. Heavy components at the bottom of the heavy component removal tower 210 are conveyed to a heavy component storage tank 270 through a tower kettle bottom pump 280.
The delivery pump 2 of the vaporization membrane device 300 delivers the rectifying section product to the vaporization membrane device 300, and delivers the material to the preheater 320, wherein the heat source of the preheater 320 is the hot material at the outlet of the membrane module 350; the preheated material enters the evaporator 330, the heat source of the evaporator 330 is low-pressure steam, tetrahydrofuran is heated and vaporized in the evaporator 330, the tetrahydrofuran steam enters the gas-liquid separation tank 340, the liquid phase in the gas-liquid separation tank 340 returns to the evaporator 330 to be evaporated again, the gas phase enters the membrane assembly 350, the membrane assembly 350 is in series operation, the membrane assembly 350 is continuously heated by the low-pressure steam, the tetrahydrofuran is cooled by the preheater 320 after passing through the membrane assembly 350, and then a qualified product is formed after passing through the product primary condenser C360 and the product secondary condenser C370.
The process principle is as follows: tetrahydrofuran, water, n-butanol and gamma-butyrolactone are contained in the tetrahydrofuran waste liquid, tetrahydrofuran and water are azeotroped, the azeotropy temperature is 63.3 ℃, the azeotropy composition tetrahydrofuran content is 95%, a continuous rectification process is utilized, a mixture of tetrahydrofuran and water is obtained from the top of a rectification tower, the mixture is approximate to the azeotropy proportion, and the mixture is further subjected to a pervaporation membrane to remove water, so that a tetrahydrofuran finished product is obtained.
Because tetrahydrofuran and water are azeotropy, common rectification can not completely separate the tetrahydrofuran and the water, the azeotrope adopts a pervaporation molecular sieve membrane to realize molecular sieve dehydration under an azeotropic system, and the water content of the tetrahydrofuran is less than 0.1wt.% after the dehydration of the pervaporation molecular sieve membrane. Pervaporation dehydration membrane: the pervaporation dehydration membrane is a pressurized operation. The raw materials enter the evaporator 330 after heat exchange with the gas-phase product, are fully vaporized into saturated gas-phase materials in the evaporator 330, enter the pervaporation membrane assembly 350, and are separated after selective adsorption, dissolution, diffusion and desorption of water molecules through the membranes when flowing through the surfaces of the membranes, thereby achieving the purpose of separating tetrahydrofuran/water azeotrope and water
The improvement condition of the invention is as follows:
(1) Capacity improvement aspect:
before transformation, the company has no capacity of treating tetrahydrofuran, and tetrahydrofuran waste liquid can only be barreled and then sent out for dangerous waste treatment; after transformation; the company has a tetrahydrofuran treatment process, changes waste tetrahydrofuran liquid into valuable and changes the waste tetrahydrofuran liquid into qualified tetrahydrofuran products.
(2) Tetrahydrofuran treatment aspect:
(1) before transformation, tetrahydrofuran waste liquid is stored by adopting a ton barrel, and the stock pressure is increased; after transformation, the tetrahydrofuran waste liquid is changed into a qualified tetrahydrofuran product, and a special storage tank is used for storage.
(2) Before transformation, tetrahydrofuran waste liquid is treated as hazardous waste, and the hazardous waste treatment pressure and cost are increased; after transformation, the tetrahydrofuran waste liquid becomes a product, thereby creating economic benefits for companies.
(3) Before transformation, tetrahydrofuran waste liquid is used as dangerous waste, so that material resource waste is formed; after transformation, the tetrahydrofuran waste liquid changes waste into valuable, and the material resource is fully utilized.
(3) Economic benefit aspect:
before transformation, the tetrahydrofuran waste liquid is treated as dangerous waste, and the company spends money in treating the tetrahydrofuran waste liquid; after transformation, the tetrahydrofuran waste liquid is changed into a qualified tetrahydrofuran product, which creates income for the company, and the annual profit of the company is about: 600 tens of thousands/year.
In the description of the present specification, reference to the terms "one embodiment," "certain embodiments," "illustrative embodiments," "examples," "specific examples," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the invention. In this specification, schematic representations of the above terms do not necessarily refer to the same embodiments or examples. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
In summary, although the present invention has been described in terms of the preferred embodiments, the preferred embodiments are not limited to the above embodiments, and various modifications and changes can be made by one skilled in the art without departing from the spirit and scope of the invention, and the scope of the invention is defined by the appended claims.
Claims (10)
1. A tetrahydrofuran waste liquid recovery system which characterized in that: the device comprises a light component removing component (100) for removing light component impurities in waste liquid, a heavy component removing component (200) for removing heavy component impurities in the waste liquid and a vaporization membrane device (300) for vaporizing and separating water in a tetrahydrofuran and water mixture, wherein the light component removing component (100) comprises a light component removing tower (110), the light component removing component (200) comprises a heavy component removing tower (210), and the light component removing tower (110) and the vaporization membrane device (300) are connected with each other through a pipeline and a conveying pump (2) arranged between the heavy component removing tower (210) and the vaporization membrane device (300).
2. The tetrahydrofuran waste liquid recovery system according to claim 1, wherein: the light component (100) further comprises a first-stage condenser A (130), a second-stage condenser A (140), a first reflux tank (150) and a first reflux pump (160), wherein the first-stage condenser A (130), the first reflux tank (150) and the first reflux pump (160) are sequentially connected through pipelines, a feeding end of the first-stage condenser A (130) is connected with the top pipeline of the light component removing tower (110), an output end of the first reflux pump (160) is connected with the top pipeline of the light component removing tower (110), the second-stage condenser A (140) is connected with an outer pipeline of the first-stage condenser A (130), and a discharging end of the second-stage condenser A (140) is connected with the pipeline of the first reflux tank (150) through the pipeline.
3. The tetrahydrofuran waste liquid recovery system according to claim 2, wherein: the system further comprises a light component storage tank (170), and a pipeline connected with the light component storage tank (170) is further arranged on a pipeline connected with the top of the light component removal tower (110) through the first reflux pump (160).
4. The tetrahydrofuran waste liquid recovery system according to claim 2, wherein: the light component (100) further comprises a first reboiler (120), and the first reboiler (120) is connected with the bottom of the light tower (110) through an inlet and outlet pipeline.
5. The tetrahydrofuran waste liquid recovery system according to claim 1, wherein: the stripping and recombination piece (200) further comprises a first-stage condenser B (230), a second-stage condenser B (240), a second reflux tank (250) and a second reflux pump (260), wherein the first-stage condenser B (230), the second reflux tank (250) and the second reflux pump (260) are sequentially connected through pipelines, the feeding end of the first-stage condenser B (230) is connected with the top pipeline of the stripping and recombination tower (210), the output end of the second reflux pump (260) is connected with the top pipeline of the stripping and recombination tower (210), a pipeline connected with the feeding end of the second-stage condenser B (240) is further arranged outside the first-stage condenser B (230), and the discharging end of the second-stage condenser B (240) is connected with the pipeline of the first-stage condenser B (230) to the second reflux tank (250) through a pipeline.
6. The tetrahydrofuran waste liquid recovery system according to claim 5, wherein: the de-reforming component (200) further comprises a second reboiler (220), and the second reboiler (220) is connected with the bottom of the de-reforming tower (210) through an inlet and outlet pipeline.
7. The tetrahydrofuran waste liquid recovery system according to claim 5, wherein: the second reflux pump (260) is further provided with a conveying pipe (3) connected with the vaporization membrane device (300) on a pipeline connected with the top of the de-weight tower (210), the vaporization membrane device (300) comprises a temporary storage tank (310), a preheater (320), an evaporator (330), a gas-liquid separation tank (340), a membrane component (350), a primary condenser C (360) and a secondary condenser C (370), the temporary storage tank (310) is connected with the conveying pipe (3), the discharge end of the temporary storage tank (310) is connected with the preheater (320) through a conveying pump (2) and a pipeline, the top of the preheater (320) is connected with the evaporator (330) through a pipeline, the evaporator (330) is connected with the gas-liquid separation tank (340) through a liquid phase pipe (380) arranged, the gas phase separated by the gas-liquid separation tank (340) is connected with the preheater (330) through a gas phase pipe (390) arranged, the gas phase separated by the gas-liquid separation tank (340) is connected with the membrane component (350) through the pipeline (360), the discharge end of the preheater (320) is connected with the bottom of the evaporator (320), the primary condenser C (360) is connected with the secondary condenser C (370) through a pipeline.
8. A tetrahydrofuran waste liquid recovery method is characterized in that: the method comprises the following steps:
s1, rectifying tetrahydrofuran waste liquid to remove light components and impurities;
s2, rectifying tetrahydrofuran, water and heavy components obtained after the light component removal of the S1 to remove heavy component impurities;
s3, removing water from the tetrahydrofuran and water mixture obtained after the weight removal of the S2 through pervaporation, and finally obtaining a tetrahydrofuran finished product.
9. The method for recycling waste tetrahydrofuran liquid according to claim 8, wherein: s2, rectifying and removing the weight in a weight removing tower (210), and after gas phase in the weight removing tower (210) is subjected to two-stage deep condensation and separation, part of condensate flows back into the weight removing tower (210), and part of condensate is extracted and gasified in S3 to remove water.
10. The method for recycling waste tetrahydrofuran liquid according to claim 8, wherein: and S3, preheating the tetrahydrofuran and water mixture, evaporating and vaporizing, carrying out gas-liquid separation on vaporized steam, returning the separated liquid phase to vaporize again, removing water molecules from the separated gas phase through heat exchange adsorption, and condensing to obtain the product.
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