CN103007565B - Method and device for triple-effect separation of methylbenzene and polyethylene - Google Patents
Method and device for triple-effect separation of methylbenzene and polyethylene Download PDFInfo
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- CN103007565B CN103007565B CN201310010361.XA CN201310010361A CN103007565B CN 103007565 B CN103007565 B CN 103007565B CN 201310010361 A CN201310010361 A CN 201310010361A CN 103007565 B CN103007565 B CN 103007565B
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Abstract
The invention relates to a method for the triple-effect separation of methylbenzene and polyethylene and a device used for the method. The method comprises the following step: separating a polyethylene-containing methylbenzene waste liquid sequentially through primary reduced-pressure distillation, primary normal-pressure distillation and primary positive-pressure distillation, wherein methylbenzene steam serves as a heat source which is used repeatedly. The device comprises a waste liquid preheater, a negative-pressure evaporator, a methylbenzene condenser, a decanter, a tail gas condenser, a normal-pressure evaporator, a positive-pressure evaporator, a positive-pressure methylbenzene intermediate tank, a methylbenzene residue storage tank and a residue evaporation tank. The device provided by the invention is an energy-saving and emission-reducing device. According to the method provided by the invention, based on the distillation range difference of one liquid under different pressures, the material is concentrated by using secondary steam, thereby greatly saving the production cost.
Description
Technical field
The present invention relates to a kind of triple effect separation of methylbenzene and poly method, and the device that the method is used.
Technical background
Microfiber synthetic leather manufacturing works are using toluene as solvent in the manufacture process of non-woven fabrics, dissolve the polyethylene in wash-out base cloth.As eluting solvent, production line production capacity is directly proportional with toluene consumption within the specific limits, and the retracting device as enterprise's production line first Benzene and Toluene is synchronous operated.
Toluene waste liquid in microfiber synthetic leather production process derives from production line to be extracted groove out and finds out groove, and the polyethylene concentration in waste liquid is about about 2%.Using water seal as the seal approach entering cloth in production process, so also with part water in the waste liquid of toluene, because toluene is insoluble in water, in the process deposited in waste tank, water is separated with toluene, water is discharged in treatment tank, therefore in recovery system, moisture is less.
At the single-action treatment technology that super fine toluene recovery technique is in the past Japan, its energy consumption is higher, and because of making still-process easily produce bumping containing moisture, affects recovery toluene quality.Along with the expansion of production scale of enterprise, the consumption of toluene increases thereupon, and therefore the yield of toluene governs the production capacity of microfiber synthetic leather, and the recovery process of economic benefits and social benefits also no longer meets the demand of producing and expanding.
Summary of the invention
The object of this invention is to provide a kind of energy consumption low, shorten residue treatment time avoid the triple effect separation of methylbenzene of boiling explosion phenomenon and poly method.
Another object of the present invention is to provide the device that the method uses.
The technical solution used in the present invention:
A kind of triple effect separation of methylbenzene and poly method, it is separated containing poly toluene waste liquid through one-level decompression distillation, one-level air-distillation, the distillation of one-level malleation successively, and toluene vapor reuses as thermal source; Specifically comprise the steps: that after preheating, first entering vacuum evaporator containing poly toluene waste liquid carries out decompression distillation concentrate, toluene vapor is separated through the laggard decanter of condenser condenses; Toluene waste liquid through decompression distillation enters atmospheric evaporation device again and carries out air-distillation concentrate, atmospheric evaporation device top toluene vapor is separated through the laggard decanter of heat exchange condensation, toluene waste liquid after air-distillation enters malleation evaporimeter and continues distillation concentrate, top toluene vapor after normal pressure evaporator heat exchange flash distillation to vacuum evaporator, the laggard decanter of condensation is separated, and malleation evaporimeter waste liquid enters residue evaporation boiler and continues concentrate evaporation.
Using low pressure steam as a thermal source in described malleation evaporimeter, atmospheric evaporation device with the toluene vapor of malleation evaporimeter for thermal source, vacuum evaporator with the toluene vapor steamed in atmospheric evaporation device for thermal source.
The toluene vapor flash distillation after pans of described malleation evaporimeter top, to vacuum evaporator, carries out Btu utilization again.
Described residue evaporation boiler adopts negative pressure intermittent operation.
Implement a device for said method, comprise waste liquid preheater, vacuum evaporator, Toluene condenser, decanter, tail gas condenser, atmospheric evaporation device, malleation evaporimeter, malleation toluene pans, toluene residue storage tank and residue evaporation boiler;
Described waste liquid preheater is connected with the top of vacuum evaporator, and the entrance of Toluene condenser connects the toluene vapor outlet on vacuum evaporator top, and the outlet of Toluene condenser connects decanter, and the gas vent of decanter connects tail gas condenser; The bottom of vacuum evaporator is connected through the bottom of pump with atmospheric evaporation device; The toluene vapor outlet on atmospheric evaporation device top connects the top of vacuum evaporator; The bottom of atmospheric evaporation device is connected with malleation evaporimeter through pump; The toluene vapor outlet on malleation evaporimeter top connects the upper inlet of atmospheric evaporation device, and the toluene condensate outlet bottom atmospheric evaporation device 2 is connected with the top of vacuum evaporator 1 through malleation toluene pans; The toluene outlet on malleation evaporimeter top connects toluene residue storage tank, and the outlet at bottom of toluene residue storage tank connects residue evaporation boiler.
Heat(ing) coil is provided with in described residue evaporation boiler.
The present invention reclaims to be separated on basis in original single-action and adds one-level vacuum evaporator, one-level malleation evaporimeter.By the waste liquid after preheating in vacuum evaporator its top feed, due to toluene and water azeotropic, and azeotropic point reduces, and has partial material immediately flash vaporized, thus because the proportion of water is comparatively large when avoiding atmospheric evaporation, and the lower generation boiling explosion phenomenon of boiling point; Negative pressure discharging is to atmospheric evaporation device, and the toluene vapor of atmospheric evaporation device is used for the heating source of vacuum evaporator; Normal pressure discharging to malleation evaporimeter, the toluene vapor of malleation evaporimeter first for the heating source of atmospheric evaporation device, then as the thermal source of vacuum evaporator after the flash distillation of malleation toluene pans; After malleation evaporation, the polyvinyl-toluene solution that concentration is higher is delivered to residue evaporation boiler and is continued concentrate evaporation, because concentration increases, poly mobility reduces, slowly, simple jacket type evaporimeter heating effect is undesirable in its heat transfer, increases heat(ing) coil in residue evaporation boiler, heat transfer in pot is made evenly, to reduce concentration time.
Accompanying drawing explanation
Fig. 1 is the process principle figure of the inventive method.
In FIG: 1 vacuum evaporator, 2 atmospheric evaporation devices, 3 malleation toluene evaporates devices, 4 Toluene condenser, 5 decanters, 6 tail gas condensers, 7 toluene residue storage tanks, 8 residue evaporation boilers, 8-1 heat(ing) coil, 9 malleation toluene pans, 10 waste liquid preheaters.
Detailed description of the invention
As shown in Figure 1, the device of the present embodiment comprises waste liquid preheater 10, vacuum evaporator 1, Toluene condenser 4, decanter 5, tail gas condenser 6, atmospheric evaporation device 2, malleation toluene evaporates device 3, malleation toluene pans 9, toluene residue storage tank 7 and residue evaporation boiler 8;
Described waste liquid preheater 10 is connected with the top of vacuum evaporator 1, and the entrance of Toluene condenser 4 connects the toluene vapor outlet on vacuum evaporator 1 top, and the outlet of Toluene condenser 4 connects decanter 5, and the gas vent of decanter 5 connects tail gas condenser 6; The bottom of vacuum evaporator 1 is connected through the bottom of pump with atmospheric evaporation device 2; The toluene vapor outlet on atmospheric evaporation device 2 top connects the top of vacuum evaporator 1; The bottom of atmospheric evaporation device 2 is connected with malleation evaporimeter 3 through pump; The toluene vapor outlet on malleation evaporimeter 3 top connects the upper inlet of atmospheric evaporation device 2, and the toluene condensate outlet bottom atmospheric evaporation device 2 is connected with the top of vacuum evaporator 1 through malleation toluene pans 9; The toluene outlet on malleation evaporimeter 3 top connects toluene residue storage tank 7, and the outlet at bottom of toluene residue storage tank 7 connects residue evaporation boiler 8.Heat(ing) coil 8-1 is provided with in described residue evaporation boiler 8.
The device of use the present embodiment carries out triple effect separation of methylbenzene and poly process is as follows:
Containing poly toluene waste liquid through waste liquid preheater 10 preheating laggard vacuum evaporator 1 initial concentration, negative pressure toluene vapor is through Toluene condenser 4 condensation laggard decanter 5 standing separation water, toluene, vacuum evaporator 1 discharging through pump to atmospheric evaporation device 2 further concentrate steam toluene, the toluene vapor of atmospheric evaporation device 2 as the thermal source of vacuum evaporator 1, through the laggard decanter 5 of heat exchange condensation, atmospheric evaporation device 2 discharging continues concentrate through pump to malleation evaporimeter 3 and steams toluene, the toluene vapor of malleation evaporimeter 3 is first as the thermal source of atmospheric evaporation device 2, through heat exchange condensation laggard malleation toluene pans 9, malleation toluene pans 9 after non-return valve flash distillation again as the thermal source of vacuum evaporator 1, through the polyvinyl-toluene solution overflow of malleation evaporimeter 3 concentrate to toluene residue storage tank 7, to ensure the continued operation of evaporization process, polyethylene is discharged after being delivered to residue evaporation boiler 8 engler distillations by toluene residue storage tank 7, heat(ing) coil is increased in the cylindrical shell of residue evaporation boiler 8, make heat transfer in pot even, reduce concentration time.Present invention process is malleation, normal pressure, the distillation of negative pressure triple effect, and because the vapor partial pressure of toluene is higher, increase tail gas condenser 6 and uncooled for isolated for decanter 5 part toluene vapor condensation reclaimed, water is discharged through pump.
Triple effect separation of methylbenzene of the present invention and poly device are a kind of energy-saving emission-reducing apparatus, and this device utilizes the boiling range difference of same liquid under different pressures, utilizes indirect steam concentrate material, thus greatly saves production cost.
The consumption of this covering device primary steam is compared with traditional toluene evaporates device steam consumption, and unit toluene vapor consumption lowers 55%.According to investigations, traditional toluene evaporates device steam consumption is 0.17 ton of steam/ton crude cresylic acid, and using this process unit to lower is 0.08 ton of steam/ton crude cresylic acid.
With production line producing days by 300 days, 24 hours every days counted:
Crude cresylic acid treating capacity per hour 30 cubic metres, every cubic metre of steam saving 0.09 ton, steam in 180 yuan/per ton:
Every day can save: 0.09*30*24*180=11664 unit,
Can save every year: 11664*300=349.92 ten thousand yuan.
Claims (6)
1. triple effect separation of methylbenzene and a poly method, is characterized in that: be separated through one-level decompression distillation, one-level air-distillation, the distillation of one-level malleation successively containing poly toluene waste liquid, toluene vapor reuses as thermal source; Detailed process is: after preheating, first enter vacuum evaporator containing poly toluene waste liquid and carry out decompression distillation concentrate, and toluene vapor is separated through the laggard decanter of condenser condenses; Toluene waste liquid through decompression distillation enters atmospheric evaporation device again and carries out air-distillation concentrate, atmospheric evaporation device top toluene vapor is separated through the laggard decanter of heat exchange condensation, toluene waste liquid after air-distillation enters malleation evaporimeter and continues distillation concentrate, top toluene vapor after normal pressure evaporator heat exchange flash distillation to vacuum evaporator, the laggard decanter of condensation is separated, and malleation evaporimeter waste liquid enters residue evaporation boiler and continues concentrate evaporation.
2. method according to claim 1, it is characterized in that in described malleation evaporimeter using low pressure steam as a thermal source, atmospheric evaporation device with the toluene vapor of malleation evaporimeter for thermal source, vacuum evaporator with the toluene vapor steamed in atmospheric evaporation device for thermal source.
3. method according to claim 1, is characterized in that the toluene vapor flash distillation after pans of described malleation evaporimeter top, to vacuum evaporator, carries out Btu utilization again.
4. method according to claim 1, is characterized in that described residue evaporation boiler adopts negative pressure intermittent operation.
5. implement the claims a device for method described in any one of 1-4, it is characterized in that comprising waste liquid preheater (10), vacuum evaporator (1), Toluene condenser (4), decanter (5), tail gas condenser (6), atmospheric evaporation device (2), malleation evaporimeter (3), malleation toluene pans (9), toluene residue storage tank (7) and residue evaporation boiler (8);
Described waste liquid preheater (10) is connected with the top of vacuum evaporator (1), the entrance of Toluene condenser (4) connects the toluene vapor outlet on vacuum evaporator (1) top, the outlet of Toluene condenser (4) connects decanter (5), and the gas vent of decanter (5) connects tail gas condenser (6); The bottom of vacuum evaporator (1) is connected through the bottom of pump with atmospheric evaporation device (2); The toluene vapor outlet on atmospheric evaporation device (2) top connects the top of vacuum evaporator (1); The bottom of atmospheric evaporation device (2) is connected with malleation evaporimeter (3) bottom through pump; The toluene vapor outlet on malleation evaporimeter (3) top connects the upper inlet of atmospheric evaporation device (2), and the toluene condensate outlet of atmospheric evaporation device (2) bottom is connected through the top of malleation toluene pans (9) with vacuum evaporator (1); The toluene outlet on malleation evaporimeter (3) top connects toluene residue storage tank (7), and the outlet at bottom of toluene residue storage tank (7) connects residue evaporation boiler (8).
6. device according to claim 5, is characterized in that being provided with heat(ing) coil (8-1) in described residue evaporation boiler (8).
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| Application Number | Priority Date | Filing Date | Title |
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| CN201310010361.XA CN103007565B (en) | 2013-01-11 | 2013-01-11 | Method and device for triple-effect separation of methylbenzene and polyethylene |
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| CN201310010361.XA CN103007565B (en) | 2013-01-11 | 2013-01-11 | Method and device for triple-effect separation of methylbenzene and polyethylene |
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| CN103007565B true CN103007565B (en) | 2015-01-21 |
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Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104557421B (en) * | 2013-10-16 | 2016-05-18 | 禾欣可乐丽超纤皮(嘉兴)有限公司 | Triple effect toluene recovery technology |
| CN110746258A (en) * | 2019-10-31 | 2020-02-04 | 上海聚友化工有限公司 | Method for separating toluene and polyethylene |
| CN113277538B (en) * | 2021-06-18 | 2023-04-18 | 沈阳铝镁设计研究院有限公司 | Method for reducing consumption of new steam in alumina production |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102126920A (en) * | 2010-01-13 | 2011-07-20 | 中国石油化工集团公司 | Method for preparing azeotropic ethanol through three-tower triple-effect differential pressure heat integration |
| CN102211992A (en) * | 2011-04-18 | 2011-10-12 | 湖南百利工程科技有限公司 | Process for reclaiming dibasic acid from adipic acid production waste solution |
| CN102824751A (en) * | 2012-08-31 | 2012-12-19 | 烟台东洁环保机械工程有限公司 | Distillation separation and recovery method for toluene-polyethylene mixed solution and used equipment |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102126920A (en) * | 2010-01-13 | 2011-07-20 | 中国石油化工集团公司 | Method for preparing azeotropic ethanol through three-tower triple-effect differential pressure heat integration |
| CN102211992A (en) * | 2011-04-18 | 2011-10-12 | 湖南百利工程科技有限公司 | Process for reclaiming dibasic acid from adipic acid production waste solution |
| CN102824751A (en) * | 2012-08-31 | 2012-12-19 | 烟台东洁环保机械工程有限公司 | Distillation separation and recovery method for toluene-polyethylene mixed solution and used equipment |
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