CN101811965B - Process for separating and recovering butyl acetate and butyl alcohol in wastewater by using azeotropic rectification - Google Patents
Process for separating and recovering butyl acetate and butyl alcohol in wastewater by using azeotropic rectification Download PDFInfo
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- CN101811965B CN101811965B CN201010166090.3A CN201010166090A CN101811965B CN 101811965 B CN101811965 B CN 101811965B CN 201010166090 A CN201010166090 A CN 201010166090A CN 101811965 B CN101811965 B CN 101811965B
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- DKPFZGUDAPQIHT-UHFFFAOYSA-N Butyl acetate Natural products CCCCOC(C)=O DKPFZGUDAPQIHT-UHFFFAOYSA-N 0.000 title claims abstract description 70
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 title claims abstract description 37
- 239000002351 wastewater Substances 0.000 title claims abstract description 22
- 238000000034 method Methods 0.000 title abstract description 12
- FUZZWVXGSFPDMH-UHFFFAOYSA-N hexanoic acid Chemical compound CCCCCC(O)=O FUZZWVXGSFPDMH-UHFFFAOYSA-N 0.000 title abstract 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 238000011084 recovery Methods 0.000 claims abstract description 13
- -1 alcohol ester Chemical class 0.000 claims abstract description 8
- 238000001816 cooling Methods 0.000 claims abstract description 6
- 238000005516 engineering process Methods 0.000 claims description 17
- 238000000605 extraction Methods 0.000 claims description 17
- 238000010533 azeotropic distillation Methods 0.000 claims description 12
- 238000010438 heat treatment Methods 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 11
- 238000010992 reflux Methods 0.000 claims description 10
- 238000005191 phase separation Methods 0.000 claims description 7
- 238000009833 condensation Methods 0.000 claims description 5
- 230000005494 condensation Effects 0.000 claims description 5
- 238000012856 packing Methods 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 238000003860 storage Methods 0.000 claims description 3
- 241000282326 Felis catus Species 0.000 claims description 2
- 239000002904 solvent Substances 0.000 abstract description 5
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 238000004821 distillation Methods 0.000 abstract description 2
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 238000000746 purification Methods 0.000 abstract description 2
- 230000008719 thickening Effects 0.000 abstract 2
- 239000010410 layer Substances 0.000 abstract 1
- 239000012044 organic layer Substances 0.000 abstract 1
- 239000000463 material Substances 0.000 description 11
- 238000009835 boiling Methods 0.000 description 10
- 239000007788 liquid Substances 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 230000032050 esterification Effects 0.000 description 5
- 238000005886 esterification reaction Methods 0.000 description 5
- 239000003960 organic solvent Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 229930182555 Penicillin Natural products 0.000 description 1
- JGSARLDLIJGVTE-MBNYWOFBSA-N Penicillin G Chemical compound N([C@H]1[C@H]2SC([C@@H](N2C1=O)C(O)=O)(C)C)C(=O)CC1=CC=CC=C1 JGSARLDLIJGVTE-MBNYWOFBSA-N 0.000 description 1
- 238000007171 acid catalysis Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 150000002148 esters Chemical group 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 239000004922 lacquer Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 229940049954 penicillin Drugs 0.000 description 1
- 239000002304 perfume Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention relates to a process for separating and recovering butyl acetate and butyl alcohol in wastewater by using azeotropic rectification, comprising the following steps of: carrying out normal-pressure distillation and thickening on the wastewater containing the butyl alcohol, the butyl acetate, water and organic residues in a first rectifying tower T-01 to obtain pure water and the organic residues through a tower kettle; delaminating condensed steam at a tower top, flowing a water layer back, and causing an organic layer to enter a second rectifying tower T-02 for pressurization and rectification under 120-200 Kpa so that the high-purity butyl acetate is extracted by the tower kettle and the steam with the alcohol ester ratio of 3/1-9/1 is obtained at the tower top; condensing to cause one part of a condensate to back flow and one part of the condensate to enter a third rectifying tower T-03 for pressure reduction and rectification under 3-15 KPa so that the high-purity butyl alcohol is extracted by the tower kettle and the steam with the alcohol ester ratio of 1/3-1/2 is obtained at the tower top; and after condensing and cooling, causing the steam with the alcohol ester ratio of 1/3-1/2 to enter the tower from a feed inlet of the second rectifying tower T-02 for continuous thickening and purification. The process has the advantages of environmental protection, low energy consumption, investment saving, no entrainer addition, high recovery rate (above 99%) of solvents and the like.
Description
Technical field
The present invention relates to N-BUTYL ACETATE in the azeotropic distillation Separation and Recovery waste water and the technology of butanols, be called for short m-HSAD technology.
Background technology
N-BUTYL ACETATE is the important chemical basic material, is widely used in the solvent of paint class, leatheroid and plastics industry, also can be used as extraction agent, preparation lacquer thinner and is used for perfume industry etc.What the industrial production of N-BUTYL ACETATE generally adopted is traditional sulfuric acid catalysis esterification process, is divided into several process sections such as esterification, neutralization and washing, rectifying in technology.In process of production, the rectifying power consumption accounts for 40% of total energy consumption, and reducing the rectifying energy consumption is that N-BUTYL ACETATE is produced energy-conservation important channel.In the esterification technique section, product is ester and water, carries out as much as possible to the right in order to make reaction, and the water sepn that requires usually as much as possible esterification to be produced goes out, and at this moment, isolated water is called as esterification water.In addition, as the extraction agent of effective ingredient in the fermented liquid or the solvent of reaction process, N-BUTYL ACETATE and butanols often remain in the raffinate of production process discharge in medicine production, and its content is generally between 0.1-9%wt.If this trade effluent directly discharges, on the one hand, serious environment pollution; On the other hand, can cause serious waste.Therefore, need before the discharging wherein organic solvent is carried out the resource utilization recycling.
In the penicillin production process, N-BUTYL ACETATE and butanols are two kinds of solvents commonly used wherein.Because production process, these two kinds of solvents usually can appear among the waste liquid simultaneously.Therefore, they being isolated from waste liquid and they are separately re-refined into high purity product separately and recycle, is the double requirements of cleaner production and environment protection.Yet both generally can form azeotrope under normal pressure for they, adopt the conventional distillation method to be difficult to they separation and purifications.General employing azeotropic distillation means separating butanol and N-BUTYL ACETATE in the existing industrialization process, but need carry out recovery and the circulation of entrainer, energy consumption is higher.
Summary of the invention
The object of the present invention is to provide " multitower thermal coupling transformation azeotropic distillation novel process ", with the organic solvent in separating acetic acid butyl ester-butanols-water-organic detritus (or other high boiling material) system, and with its resource utilization.This technology is called for short m-HSAD technology.The present invention can reclaim obtain content at the N-BUTYL ACETATE more than 99.5% (wt) and content the butanols more than 99.5% (wt), and energy expenditure is low, technical process is short, invests less.
Comprise rectifying tower T1, T2, T3 and tower reactor reboiler, condensate cooler, interchanger and phase separation tank in the m-HSAD technology that the present invention proposes.Purpose of the present invention can realize by following technical solution.
N-BUTYL ACETATE in a kind of azeotropic distillation Separation and Recovery waste water and the technology of butanols, its technical process as shown in Figure 1, it mainly may further comprise the steps:
Step 1. will contain butanols 0.1～7% (wt), N-BUTYL ACETATE 1～5% (wt), water 85～96% (wt) and organic detritus (or other high boiling material) 1～3% (wt) from storage tank G-01 waste water is transported to interchanger H-01 heat exchange to 30～50 ℃ by pipeline 1, heating medium is the first rectifying tower T-01 tower reactor discharging, then waste water is transported to interchanger H-02 and the first rectifying tower T-01 overhead vapours heat exchange, after further being preheated to 80～90 ℃, enter in the tower from the opening for feed of the first rectifying tower T-01, carry out enrichment and purify;
The step 2. first rectifying tower T-01 working pressure is normal pressure, and tower reactor adopts steam heating, and the phlegma of rectifying tower T-01 overhead vapours after heat exchange enters phase separation tank S-01, and heavy phase is water, gently is butanols and N-BUTYL ACETATE mixture mutually, and heavy phase refluxes; Light phase extraction enters in the tower from the opening for feed of rectifying tower T-02, and 85～95 ℃ of rectifying tower T-01 tower top temperatures, 100～105 ℃ of tower reactor temperature, tower reactor obtain pure water and organic detritus (or other high boiling material);
The step 3. second rectifying tower T-02 working pressure is 120～200KPa, tower reactor adopts steam heating, 120～140 ℃ of tower top temperatures, 130～155 ℃ of tower reactor temperature, tower reactor extraction N-BUTYL ACETATE, cat head are that alcohol ester is than the steam that is 3/1～9/1, rectifying tower T-02 overhead vapours is as the thermal source of rectifying tower T-03 reboiler H-03, phlegma after heat exchange enters return tank V1, and a part refluxes, and a part enters in the tower from the opening for feed of rectifying tower T-03;
N-BUTYL ACETATE in the above-mentioned azeotropic distillation Separation and Recovery waste water and the technology of butanols, the described first rectifying tower T-01 of step 2 adopts tray column.Owing to have organic detritus (or other high boiling material) in the waste water, cause liquid flooding in order to be difficult for blocking, preferably adopt tray column.
N-BUTYL ACETATE in the above-mentioned azeotropic distillation Separation and Recovery waste water and the technology of butanols, the described second rectifying tower T-02 of step 3 preferably feed plate epimere is that rectifying section adopts packing tower (mass-transfer efficiency height), and the feed plate hypomere is that stripping section adopts tray column (be difficult for blocking and avoid causing liquid flooding).
N-BUTYL ACETATE in the above-mentioned azeotropic distillation Separation and Recovery waste water and the technology of butanols, described the 3rd rectifying tower T-03 of step 4 preferably adopts packing tower, to obtain higher mass-transfer efficiency.
The present invention utilizes under different pressures, N-BUTYL ACETATE, butanols, water can form the ternary of different azeotropic compositions, the characteristics of binary azeotrope are separated, need not introduce entrainer or other chemical substance, carry out three towers and produce continuously, can be respectively obtain water, high purity N-BUTYL ACETATE and butanols from the tower reactor of three towers.
The present invention has the following advantages: (1) has taken full advantage of used heat (low-quality heat) at the bottom of heat in the overhead vapours and the tower, realizes the purpose that cuts down the consumption of energy; (2) by transformation technology, obtain highly purified N-BUTYL ACETATE and butanols; (3) need not introduce entrainer or other chemical substance, environmental protection.(4) operational path is short, reduced investment, and the Recovery of Organic Solvent in the waste water and resource utilization rate can be up to more than 99%.
Description of drawings
Fig. 1 is schematic flow sheet of the present invention.Wherein:
G-01 is raw material feed liquid storage tank, T-01, T-02, T-03 are first, second, third rectifying tower, and H-01, H-02, H-03 are interchanger, and V-01 is return tank, S-01 is phase separation tank, and 1,2,3,4,5,6,7,8,9,10,11,12,13,14,15,16 is pipeline.
Embodiment
Further specify the present invention by the following examples.
Embodiment 1:
To contain butanols 0.1% (wt), N-BUTYL ACETATE 1% (wt), water 97.9% (wt), the flow of organic detritus (or other high boiling material) 1% (wt) is 0.125 ton/hour waste water, be preheated to 45 ℃ through interchanger H-01, enter the first rectifying tower T-01 after being heated to 80 ℃ by interchanger H-02 again, the first rectifying tower T-01 theoretical plate number is 28,0.3 meter of tower diameter, working pressure is normal pressure, tower reactor adopts steam heating, the phlegma of the first rectifying tower T-01 overhead vapours after heat exchange, enter phase separation tank S1, heavy phase refluxes, 85 ℃ of the first rectifying tower T-01 tower top temperatures, 100 ℃ of tower reactor temperature, tower reactor obtain pure water and organic detritus (or other high boiling material).Light phase extraction enters the second rectifying tower T-02, and the second rectifying tower T-02 theoretical plate number is 38,0.2 meter of tower diameter, working pressure is 120KPa, and tower reactor adopts steam heating, 120 ℃ of tower top temperatures, 130 ℃ of tower reactor temperature, the N-BUTYL ACETATE of tower reactor extraction 99.5% (wt).Overhead vapours is as the thermal source of the 3rd rectifying tower T-03 reboiler H-03, and the phlegma after heat exchange enters return tank V1, and a part refluxes, and a part enters the 3rd rectifying tower T-03.The 3rd rectifying tower T-03 theoretical plate number is 42, and 0.3 meter of tower diameter, working pressure are 15KPa, 70 ℃ of tower top temperatures, 75 ℃ of tower reactor temperature, the butanols of tower reactor extraction 99.5% (wt); Overhead vapours enters the second rectifying tower T-02 after the condensation cooling, continue enrichment and purify.
Embodiment 2:
To contain butanols 7% (wt), N-BUTYL ACETATE 5% (wt), water 85% (wt), the flow of organic detritus (or other high boiling material) 3% (wt) is that 0.3 ton/hour waste water is preheated to 50 ℃ through interchanger H-01, enter the first rectifying tower T-01 after being heated to 85 ℃ by interchanger H-02 again, the first rectifying tower T-01 theoretical plate number is 30,0.6 meter of tower diameter, working pressure is normal pressure, tower reactor adopts steam heating, the phlegma of the first rectifying tower T-01 overhead vapours after heat exchange, enter phase separation tank S1, heavy phase refluxes, 90 ℃ of the first rectifying tower T-01 tower top temperatures, 103 ℃ of tower reactor temperature, tower reactor obtain pure water and organic detritus (or other high boiling material).Light phase extraction enters the second rectifying tower T-02, the second rectifying tower T-02 theoretical plate number is 45, and 0.3 meter of tower diameter, working pressure are 150KPa, tower reactor adopts steam heating, 129 ℃ of tower top temperatures, 141 ℃ of tower reactor temperature, the N-BUTYL ACETATE of tower reactor extraction 99.7% (wt), overhead vapours is as the thermal source of the 3rd rectifying tower T-03 reboiler H-03, phlegma after heat exchange enters return tank V1, and a part refluxes, and a part enters the 3rd rectifying tower T-03.The 3rd rectifying tower T-03 theoretical plate number is 39, and 0.5 meter of tower diameter, working pressure are 10KPa, 59 ℃ of tower top temperatures, 65 ℃ of tower reactor temperature, the butanols of tower reactor extraction 99.54% (wt); Overhead vapours enters the second rectifying tower T-02 after the condensation cooling, continue enrichment and purify.
Embodiment 3:
To contain butanols 5% (wt), N-BUTYL ACETATE 3% (wt), water 90% (wt), the flow of organic detritus (or other high boiling material) 2% (wt) is that 1.0 tons/hour waste water is preheated to 52 ℃ through interchanger H-01, enter the first rectifying tower T-01 after being heated to 90 ℃ by interchanger H-02 again, the first rectifying tower T-01 theoretical plate number is 32,0.8 meter of tower diameter, working pressure is normal pressure, tower reactor adopts steam heating, the phlegma of the first rectifying tower T-01 overhead vapours after heat exchange, enter phase separation tank S1, heavy phase refluxes, 95 ℃ of the first rectifying tower T-01 tower top temperatures, 105 ℃ of tower reactor temperature, tower reactor obtain pure water and organic detritus (or other high boiling material).Light phase extraction enters the second rectifying tower T-02, the second rectifying tower T-02 theoretical plate number is 42, and 0.6 meter of tower diameter, working pressure are 200KPa, tower reactor adopts steam heating, 140 ℃ of tower top temperatures, 155 ℃ of tower reactor temperature, the N-BUTYL ACETATE of tower reactor extraction 99.83% (wt), overhead vapours is as the thermal source of the 3rd rectifying tower T-03 reboiler H-03, phlegma after heat exchange enters return tank V1, and a part refluxes, and a part enters the 3rd rectifying tower T-03.The 3rd rectifying tower T-03 theoretical plate number is 46, and 0.7 meter of tower diameter, working pressure are 3KPa, 36 ℃ of tower top temperatures, 43 ℃ of tower reactor temperature, the butanols of tower reactor extraction 99.8% (wt); Overhead vapours enters the second rectifying tower T-02 after the condensation cooling, continue enrichment and purify.
Claims (4)
1. the N-BUTYL ACETATE in the azeotropic distillation Separation and Recovery waste water and the technology of butanols is characterized in that it is made up of following steps:
Step 1. will contain butanols 0.1～7%(wt), N-BUTYL ACETATE 1～5%(wt), water 85～96%(wt) and organic detritus 1～3%(wt) from storage tank waste water is transported to first interchanger (H-01) heat exchange to 30～50 ℃ by pipeline (1), heating medium is the discharging of first rectifying tower (T-01) tower reactor, then waste water is transported to second interchanger (H-02) and the heat exchange of first rectifying tower (T-01) overhead vapours, after further being preheated to 80～90 ℃, enter in the tower from the opening for feed of first rectifying tower (T-01), carry out enrichment and purify;
Step 2. first rectifying tower (T-01) working pressure is normal pressure, and tower reactor adopts steam heating, the phlegma of first rectifying tower (T-01) overhead vapours after heat exchange, enter phase separation tank (S-01), heavy phase is water, gently is butanols and N-BUTYL ACETATE mixture mutually, the alcohol ester ratio is 5/3, and heavy phase refluxes; Light phase extraction enters in the tower from the opening for feed of second rectifying tower (T-02), 85～95 ℃ of first rectifying tower (T-01) tower top temperatures, and 100～105 ℃ of tower reactor temperature, tower reactor obtains pure water and organic detritus;
Step 3. second rectifying tower (T-02) working pressure is 120～200 KPa, tower reactor adopts steam heating, 120～140 ℃ of tower top temperatures, 130～155 ℃ of tower reactor temperature, tower reactor extraction N-BUTYL ACETATE, cat head is 3/1 ~ 9/1 steam for the alcohol ester ratio, second rectifying tower (T-02) overhead vapours is as the thermal source of the 3rd rectifying tower (T-03) reboiler (H-03), phlegma after heat exchange enters return tank (V-01), a part refluxes, and a part enters in the tower from the opening for feed of the 3rd rectifying tower (T-03);
Step 4. the 3rd rectifying tower (T-03) working pressure is 3～15KPa, 35～70 ℃ of tower top temperatures, 40～75 ℃ of tower reactor temperature, tower reactor extraction butanols; Cat head is 1/3 ~ 1/2 steam for the alcohol ester ratio, after the condensation cooling, enters in the tower from the opening for feed of second rectifying tower (T-02), continues enrichment and purifies.
2. the N-BUTYL ACETATE in the azeotropic distillation Separation and Recovery waste water according to claim 1 and the technology of butanols is characterized in that: described first rectifying tower of step 2 (T-01) employing tray column.
3. the N-BUTYL ACETATE in the azeotropic distillation Separation and Recovery waste water according to claim 1 and the technology of butanols, it is characterized in that: described second rectifying tower of step 3 (T-02) feed plate epimere is that rectifying section adopts packing tower, and the feed plate hypomere is that stripping section adopts tray column.
4. the N-BUTYL ACETATE in the azeotropic distillation Separation and Recovery waste water according to claim 1 and the technology of butanols is characterized in that: described the 3rd rectifying tower of step 4 (T-03) employing packing tower.
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| CN101982450B (en) * | 2010-09-30 | 2013-01-16 | 河北工业大学 | Method for recovering butanol-butyl acetate from waste acid water generated during antibiotic production through reduced pressure distillation |
| CN101973875B (en) * | 2010-10-19 | 2012-03-14 | 重庆大学 | Method for recovering butyl acetate |
| CN102060407A (en) * | 2010-12-05 | 2011-05-18 | 天津市华瑞奕博化工科技有限公司 | System and method for treating butyl acetate waste water |
| CN102617341A (en) * | 2011-01-27 | 2012-08-01 | 甘肃雪晶生化有限责任公司 | Method for recycling residual butyl acetate in waste mycelium of mevastatin |
| CN102417450A (en) * | 2011-12-26 | 2012-04-18 | 天津市康科德科技有限公司 | Method for purifying chromatographic grade butyl acetate |
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| CN102942475B (en) * | 2012-11-23 | 2015-03-04 | 福建师范大学福清分校 | Variable-pressure rectification method for separating ethyl acetate and ethanol azeotropes and production device for azeotropes |
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| CN104086363B (en) * | 2014-07-14 | 2015-12-30 | 河北工业大学 | The energy-saving reclaiming process of N-BUTYL ACETATE and butanols in waste acid water |
| CN104130101B (en) * | 2014-07-29 | 2016-01-20 | 河北工业大学 | Azeotropic distillation and conventional distillation combine the technique reclaiming butanols and N-BUTYL ACETATE |
| CN106008149A (en) * | 2016-05-19 | 2016-10-12 | 安徽理工大学 | Separation method of mixed solvent |
| CN107473932B (en) * | 2017-08-31 | 2020-06-09 | 济南大学 | Method for separating butanol and butyl acetate |
| CN107903150B (en) * | 2017-12-04 | 2021-05-18 | 福州大学 | Method for producing sec-butyl alcohol by continuous hydrolysis |
| CN110041196A (en) * | 2019-05-23 | 2019-07-23 | 南通醋酸纤维有限公司 | The recovery method of esters in waste water |
| CN110437064A (en) * | 2019-07-24 | 2019-11-12 | 江门谦信化工发展有限公司 | A kind of differential pressure type energy-saving processing technique of ethyl acetate |
| CN113149838B (en) * | 2021-05-08 | 2022-06-21 | 青岛科技大学 | Method for separating ethyl acetate-methanol-water by double-tower pressure-swing batch rectification and control structure |
| CN113563364A (en) * | 2021-07-28 | 2021-10-29 | 河北工业大学 | Method for removing alcohol ester in 6-APA mother liquor |
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