CN102701941B - Acetone removal device of acetic acid recovery system and removal process of acetone removal device - Google Patents

Acetone removal device of acetic acid recovery system and removal process of acetone removal device Download PDF

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Publication number
CN102701941B
CN102701941B CN201210166338.5A CN201210166338A CN102701941B CN 102701941 B CN102701941 B CN 102701941B CN 201210166338 A CN201210166338 A CN 201210166338A CN 102701941 B CN102701941 B CN 102701941B
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tower
acetone
stripping
stripping tower
acetic acid
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CN102701941A (en
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姚杰
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Nantong Cellulose Fibers Co Ltd
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Nantong Cellulose Fibers Co Ltd
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Abstract

The invention provides an acetone removal device of an acetic acid recovery system and a removal process of the acetone removal device. The original material inlet groove, an acetone stripping tower and the acetone removal device of the acetic acid recovery system are utilized, and a process path for removing acetone through twice rectification is formed. An isopropanol stripping tower and subsidiary equipment of the isopropanol stripping tower are connected between the material inlet groove and the acetone stripping tower, and the isopropanol stripping tower is used as a primary stripping removal device. Distillates at the tower top of the isopropanol stripping tower are firstly condensed by a condenser, are then cooled by a cooler and enter the acetone stripping tower, and the acetone stripping tower is used as a secondary stripping removal device. Outflow materials at the tower bottom of the acetone stripping tower are cooled by a tower bottom cooler and are conveyed back into an acetic acid recovery device. In the acetone removal device, the concentration of acetone in inlet materials of the acetone stripping tower is improved from the original value about 4.6 percent to about 5.8 percent, and the concentration of the acetone in waste materials conveyed to a sewage treatment station is improved from about 80 percent to about 90 percent. The rectification heating steam consumption is reduced, and the extracting agent consumption in the acetic acid recovery process is also reduced.

Description

Acetone removal device and the removing process thereof of acetic acid recovery system
Technical field
The present invention relates to acetone removal process unit in the waste water of chemical enterprise emission, acetone removal process unit in the streams that espespecially acetic acid recovery system produces.
Background technology
In the production line of the Chemicals such as Cellulose diacetate, contain acetic acid recovery system, in dilute acetic acid solution material stream in acetic acid recovery system, tend to produce certain density acetone, because acetone is miscible in multi-solvents and water, the extraction process to dilute acetic acid and extraction efficiency are had a negative impact.Therefore, when the acetone content in dilute acetic acid solution is too high, just must remove acetone, acetone stripping tower designs for the acetone of removing in solution.But the acetone concentration that traditional acetone stripping tower tower top after treatment flows out in material (overhead product) also only has 35%-80% left and right, removes acetone thorough not, and can take away the useful extraction agent raw materials such as part hexane.
In addition, when the isopropanol content in acetic acid recovery system is too high, also must be removed.If do not removed, can affect the cycle of operation of equipment.Virahol stripping tower is that the Virahol for removing in solution designs.Virahol stripping tower and acetone stripping tower all belong to rectifying tower, but the temperature of Virahol stripping tower when work top of tower and tower bottom is all higher than the temperature of the corresponding site of acetone stripping tower.And the Virahol that Virahol stripping tower removes, is present in bottom product; The acetone that acetone stripping tower removes, is present in overhead product.
Number of patent application is disclosed one " method of recovering acetone from dilute acetone water solution by reduced-pressure steam stripping type rectification " in 201110006970.9 specification sheets, discloses the method for recovering acetone from dilute acetone water solution by reduced-pressure steam stripping type rectification.The method emits the dilute solution that contains acetone high-temperature kettle liquid by tower reactor in interchanger and rectifying tower carries out heat exchange, reaches after 85-95 ℃, between rectifying tower 8#-16# column plate, enters rectifying tower; Tower top operation pressure is 0.07-0.09MPa; Tower reactor operation pressure is 0.120-0.130MPa; The overhead product of rectifying tower is cooled to after 40-55 ℃ through condenser, and part overhead product is as product acetone extraction, and part overhead product is as backflow, and the reflux ratio of controlling reflux mass and quality product is 0.5-6.6: 1.This invention has reduced for the consumption of the water coolant of condensation overhead vapours with for the consumption of the bottom steam that heats, though can reduce distillation operation expense, for purification concentration and the purification efficiency of acetone, there is not large improvement.
Technological transformation > > mono-literary composition of the < < acetone stripping tower system of second phase < < chemical industry progress > > in 2000 publication, retain former acetone stripping tower, from effluent liquid column overhead discharging pipeline, connect pipeline charging as acetone stripping tower to acetone stripping tower, discharging at the bottom of acetone tower tower is connected to the quantizer heavy phase side of main distillation tower.This reforming equipment working stability, the efficiency that removes acetone improves.The present invention, on the basis of this operational path, removes device by the Virahol of itself and acetic acid recovery system and reconfigures, and forms the twice rectification process route that removes acetone, has further improved the efficiency that removes acetone.Both reduce rectifying heating steam and consumed, reduced again the extraction agent consumption of Reclaim Process of Acetic Acid.
Summary of the invention
goal of the invention:reduce the consumption of the heating steam of acetone removal rectifying, reduce the extraction agent consumption of Reclaim Process of Acetic Acid,, a kind of acetone removal device that adopts different stripping tower parts to remove is at twice provided.
technical scheme:a kind of acetic acid recovery system provided by the invention flows out the acetone removal device in dilute acetic acid solution material, outside acetic acid recovery device, comprise feed chute, acetone stripping tower, condenser B, sewage works, the water cooler B at the bottom of tower B, tower that boils again, also comprise Virahol stripping tower, condenser A, return tank, the water cooler A at the bottom of tower A, tower that boils again.Between feed chute and acetone stripping tower, be connected with Virahol stripping tower, Virahol stripping tower (adopts equipment and the stripping process of Virahol stripping tower as stripper plant for the first time, can at the bottom of tower, first remove the non-acetone materials such as Virahol), acetone stripping tower is as stripper plant for the second time (adopting equipment and the stripping process of acetone stripping tower).
The tower top of described Virahol stripping tower is connected with condenser A, then is connected with return tank, and then is connected to the entrance of acetone stripping tower.The tower top of acetone stripping tower is connected with condenser B, after condenser B, has bye-pass to be connected to sewage works, and all the other connect back the tower top of acetone stripping tower separately bye-pass.At the bottom of the tower of acetone stripping tower, be connected with water cooler B at the bottom of boil again tower B, tower, at the bottom of tower after water cooler B or have pipeline to connect acetic acid recovery device.
At the bottom of the tower of described Virahol stripping tower, can be connected with successively the tower A that boils again, can also be connected with water cooler A at the bottom of tower, its bottom stream material has pipeline to connect acetic acid recovery device after water cooler A at the bottom of tower is cooling, and bottom stream material recycles, cost-saving, reduce discharge.
Between described condenser A and return tank, be preferably connected with subcooler, the tower top of condensation liquefaction flowed out to material further cooling, to do not affect the temperature stability of material in stripping tower during partial reflux, and be convenient to the subsequent disposal utilization of part extraction.
another object of the present invention:a kind of removing process of the acetone removal device that adopts acetic acid recovery system claimed in claim 1 is provided.
realize another goal of the invention technical scheme:in this goal of the invention removing process, contain following processing step:
1) the outflow material that acetic acid recovery system produces flows to the entrance into Virahol stripping tower, adopts Virahol stripping tower to carry out stripping process for the first time;
2) tower top of Virahol stripping tower flows out material, after condenser A condensation, flows to return tank, then sends into the entrance of acetone stripping tower, adopts acetone stripping tower to carry out stripping process for the second time;
3) tower top of acetone stripping tower flows out material after condenser B condensation, and condensed part tower top flows out material extraction to sewage works, and all the other are back in the tower top of acetone stripping tower; At the bottom of the tower of acetone stripping tower, be connected with water cooler B at the bottom of boil again tower B, tower, its bottom stream material is sent acetic acid recovery device back to after water cooler B at the bottom of tower is cooling.
In the present invention, during the work of Virahol stripping tower, its top of tower temperature range is 70 ℃~80 ℃, preferably 73 ℃; Column bottom temperature is that scope is 78 ℃~88 ℃, preferably 85 ℃.During the work of acetone stripping tower, its top of tower temperature range is 52 ℃~57 ℃, preferably 53 ℃; Column bottom temperature scope is 77 ℃~81 ℃, preferably 79 ℃.
The tower top of the Virahol stripping tower described in above-mentioned technique flows out material after condenser A condensation, then it is cooling to pass through the subcooler degree of depth, is cooled to normal temperature or above zero, then flows to return tank.
The bottom stream material of the Virahol stripping tower described in above-mentioned technique, after the recycle of the A that boils again, through water cooler A cooling process at the bottom of tower, then is sent back in acetic acid recovery device, further saves useful resources, reduces the waste of resource, reduces the discharge of waste material.
beneficial effect:in device of the present invention, the entrance of acetone stripping tower flows to the concentration of acetone in material and brings up to 5.34% left and right from original 4.2% left and right, delivers to the concentration of acetone in the outflow material of sewage works and brings up to 90% left and right from original 80% left and right, even reaches 95%.After the concentration of acetone improves in overhead product, both reduced the acetone consumption of the heating steam of stripping process for the second time, reduced again the consumption of the extraction agent such as hexane of Reclaim Process of Acetic Acid, saved production cost.And, utilized the process byproducts (overhead product) of Virahol stripping tower separating isopropanol (in bottom stream material), extended the cycle of operation of acetone stripping tower.
Accompanying drawing explanation
Accompanying drawing is a structure of the present invention and process flow diagram;
In figure: 1, acetic acid recovery device; 2, the tower A that boils again; 3, feed chute; 4, Virahol stripping tower; 5, condenser A; 6, subcooler; 7, return tank; 8, acetone stripping tower; 9, condenser B; 10, sewage works; 12, water cooler B at the bottom of tower; 13, the tower B that boils again; 14, water cooler A at the bottom of tower.
Embodiment
Embodiment
Choose various parts as shown in the drawing, all parts is coupled together with corresponding pipeline, form an acetic acid recovery system and flow out acetone removal device in material.This device comprises acetic acid recovery device 1, between feed chute 3 and acetone stripping tower 8, is connected with Virahol stripping tower 4.The tower top of described Virahol stripping tower 4 is connected with condenser A5, subcooler 6, then is connected with return tank 7, is then connected to the entrance of acetone stripping tower 8; The tower top of acetone stripping tower 8 is connected with condenser B9, is connected to sewage works 10; At the bottom of the tower of acetone stripping tower 8, be connected with the tower B13 that boils again, then be connected with water cooler B12 at the bottom of tower.
Acetone removal device in acetic acid recovery system waste water shown in the drawings, the removing process adopting in actual production has following processing step:
1) acetic acid recovery system outflow material enters the entrance of Virahol stripping tower 4, adopts Virahol stripping tower 4 to carry out stripping process for the first time; During the work of Virahol stripping tower, its top of tower temperature is about 75 ℃, and column bottom temperature is for being about 80 ℃;
2) tower top of Virahol stripping tower 4 flows out material, and after condenser A5 condensation, then it is cooling to pass through subcooler 6 degree of depth, is cooled to normal temperature, flows to return tank 7, then sends into the entrance of acetone stripping tower 8, adopts acetone stripping tower 8 to carry out stripping process for the second time; During the work of acetone stripping tower, its top of tower temperature is about 55 ℃, and column bottom temperature is about 80 ℃;
3) tower top of acetone stripping tower 8 flows out material after condenser B9 condensation, delivers to sewage works 10; The bottom stream material of acetone stripping tower 8 is after the circulating-heating of the tower B13 that boils again refluxes and utilizes, then the cooling process of passing through water cooler B14 at the bottom of tower;
4) the bottom stream material of Virahol stripping tower 4 is after the recycle of the tower A2 that boils again, then after water cooler A cooling process at the bottom of tower, sends back in acetic acid recovery device 1.

Claims (7)

1. the acetone removal device of an acetic acid recovery system, comprise feed chute (3), acetone stripping tower (8), condenser B(9), sewage works (10), the tower B(13 that boils again), water cooler B(12 at the bottom of tower), it is characterized in that: also comprise Virahol stripping tower (4), condenser A(5), return tank (7), the tower A(2 that boils again), water cooler A(14 at the bottom of tower); Between feed chute (3) and acetone stripping tower (8), be connected with Virahol stripping tower (4), Virahol stripping tower (4) conduct stripper plant for the first time, acetone stripping tower (8) conduct stripper plant for the second time;
The tower top of described Virahol stripping tower (4) is connected with condenser A(5), then be connected with return tank (7), and then be connected to the entrance of acetone stripping tower (8); The tower top of acetone stripping tower (8) is connected with condenser B(9), condenser B(9) after have bye-pass to be connected to sewage works (10), separately have bye-pass to connect back the tower top of acetone stripping tower (8); At the bottom of the tower of acetone stripping tower (8), be connected with the tower B(13 that boils again), water cooler B(12 at the bottom of tower), after water cooler at the bottom of tower (12) or have pipeline to connect acetic acid recovery device (1).
2. the acetone removal device of acetic acid recovery system as claimed in claim 1, it is characterized in that: at the bottom of the tower of described Virahol stripping tower (4), be connected with the tower A(2 that boils again in turn), water cooler A(14 at the bottom of tower), its bottom stream material is through water cooler A(14 at the bottom of tower) after have pipeline to connect acetic acid recovery device (1).
3. the acetone removal device of acetic acid recovery system as claimed in claim 1, is characterized in that: at described condenser A(5) and return tank (7) between be connected with subcooler (6).
4. a removing process that adopts the acetone removal device of acetic acid recovery system claimed in claim 1, is characterized in that: contain following processing step:
1) streams that acetic acid recovery system produces enters the entrance of Virahol stripping (4), adopts Virahol stripping tower (4) to carry out stripping process for the first time;
2) tower top of Virahol stripping tower (4) flows out material, through condenser A(5) after condensation, flow to return tank (7), then send into the entrance of acetone stripping tower (8), employing acetone stripping tower (8) carries out stripping process for the second time;
3) tower top of acetone stripping tower (8) flows out material through condenser B(9) after condensation, the extraction of condensed part tower top outflow material is to sewage works (10), and all the other are back in the tower top of acetone stripping tower (8); At the bottom of the tower of acetone stripping tower (8), be connected with the tower B(13 that boils again), water cooler B(12 at the bottom of tower), its bottom stream material is through water cooler B(12 at the bottom of tower) send acetic acid recovery device (1) back to after cooling.
5. the removing process of the acetone removal device of acetic acid recovery system as claimed in claim 4, is characterized in that: during Virahol stripping tower (4) work, its top of tower temperature range is 70 ℃~80 ℃, and column bottom temperature scope is 78 ℃~88 ℃; During acetone stripping tower (8) work, its top of tower temperature range is 52 ℃~57 ℃, and column bottom temperature scope is 77 ℃~81 ℃.
6. the removing process of the acetone removal device of acetic acid recovery system as claimed in claim 5, is characterized in that: during Virahol stripping tower (4) work, its top of tower temperature is 73 ℃, and column bottom temperature is 85 ℃; During acetone stripping tower (8) work, its top of tower temperature is 53 ℃, and column bottom temperature is 79 ℃.
7. the removing process of the acetone removal device of the acetic acid recovery system as described in claim 4 or 5, it is characterized in that: the bottom stream material of described Virahol stripping tower (4) is through the tower A(2 that boils again) recycle after, through water cooler A(14 at the bottom of tower) cooling process, then send back in acetic acid recovery device (1).
CN201210166338.5A 2012-05-27 2012-05-27 Acetone removal device of acetic acid recovery system and removal process of acetone removal device Active CN102701941B (en)

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CN101376623B (en) * 2007-08-31 2011-04-20 中国石油天然气股份有限公司 Method for separating methyl isobutyl ketone synthetic fluid
CN102115436B (en) * 2011-01-13 2013-07-24 华南理工大学 Method for recovering acetone from dilute acetone water solution by reduced-pressure steam stripping type rectification
CN202610130U (en) * 2012-05-27 2012-12-19 南通醋酸纤维有限公司 Acetone removing device of acetic acid recovery system

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