CN202849303U - Treatment device for filter liquor generated in process of para-aramid resin washing - Google Patents
Treatment device for filter liquor generated in process of para-aramid resin washing Download PDFInfo
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- CN202849303U CN202849303U CN 201220508704 CN201220508704U CN202849303U CN 202849303 U CN202849303 U CN 202849303U CN 201220508704 CN201220508704 CN 201220508704 CN 201220508704 U CN201220508704 U CN 201220508704U CN 202849303 U CN202849303 U CN 202849303U
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Abstract
The utility model relates to a treatment device for filter liquor generated in the process of para-aramid resin washing, which comprises a neutralization device, an extraction device, a rectification device and a gas stripping device, wherein the neutralization device mainly comprises a neutralization reaction kettle and a filter liquor and neutralizer conveying and metering device; the extraction device mainly comprises an extraction tower and a filter liquor and extraction agent conveying and metering device; the rectification device mainly comprises an extraction tower, a tower top condensing circulation device and a tower bottom heating circulation device; and the gas stripping device mainly comprises a gas stripping tower, a tower top condensing circulation device and a tower bottom outputting device. Through adopting an extraction technology, the device can extract solvents from the filter liquor by using an extraction agent at room temperature so as to realize the separation of the solvents and water, therefore, compared with an evaporation process, the energy is greatly saved, the recovery rate of solvents is more than 98%, the solvent consumption is reduced, and the production cost of para-aramid is saved.
Description
Technical field
Belong to field of chemical engineering, relate to mixing solutions and process recovery technology.Exactly relate to the treatment unit of the filtrate that produces in a kind of p-aramid fiber resin washing process.
Background technology
Para-aramid fiber also claims the Fanglun 1414, p-aramid fiber is the widest, the organic fibre that has the call of purposes in the world today's three large high-performance fibers, p-aramid fiber is called " changeable Buddha's warrior attendant " by material circle, its purposes is very extensive, be the first-selection of making high-strength light plate armour and special type protection material, be widely used in the fields such as space flight, aviation, military project, electromechanics, building, automobile, sports goods.
The p-aramid fiber resin is in washing process, can produce a large amount of filtrates, acid is arranged in the filtrate, salt is arranged, also has organic solvent, direct emission of serious pollution of environment, and contain expensive solvent in the filtrate and also should not directly discharge, so the treatment process of filtrate directly affects the production cost of surrounding enviroment and p-aramid fiber enterprise.
Chinese patent CN101457414A, CN1810851A, CN101289548A, CN1112140A, CN101550233A disclose the treatment process of p-aramid fiber resin wash filtrate, but equal unexposed its treatment unit.
Chinese patent CN201089749Y discloses a kind of PPTA polymerization solvent recovery unit, this device by desalination, slightly heat up in a steamer, rectifying and four cell arrangements of purifying form, this device serialization degree is high, rate of recovery NMP quality high and that reclaim is high, can satisfy the harsh requirement of PPTA polymerization.But the desalination unit device that this patent is announced mainly adopts thin-film evaporator, nmp solvent in the filtrate and water together evaporated enter rectifying tower, because the boiling point of nmp solvent is higher, even employing underpressure distillation, this process energy consumption is not low yet, and the nmp solvent in the II level thin-film evaporator is because the gradually increase of salts contg, and has part residual, can't evaporate away, reduce the rate of recovery of nmp solvent.
Summary of the invention
The purpose of this utility model is to overcome the deficiencies in the prior art, and the treatment unit of the filtrate that produces in a kind of p-aramid fiber resin washing process is provided.
The technical scheme that the utility model is taked is as follows:
The treatment unit of the filtrate that produces comprises neutralising arrangement, extraction plant, rectifier unit and air-lift device in a kind of p-aramid fiber resin washing process; The purpose of neutralising arrangement is the hydrochloric acid in the neutralization filtrate, makes neutralizer be neutral, and mainly by the neutralization reaction still, the conveying of filtrate and neutralizing agent and measuring apparatus form; The purpose of extraction plant is with extraction agent the solvent in the filtrate to be extracted from water, and the realization solvent separates with water, and mainly conveying and the measuring apparatus by extraction tower, filtrate and extraction agent forms; The purpose of rectifier unit is with extraction agent and separated from solvent, mainly by heating cycle installation composition at the bottom of extraction tower, overhead condensation circulation device and the tower; The purpose of air-lift device is that a small amount of extraction agent that will take away in the raffinate is evaporated, and is recycled in the extraction liquid basin, mainly is comprised of take-off equipment at the bottom of stripping tower, overhead condensation circulation device and the tower.
Positively effect of the present utility model is:
(1) this device adopts extraction tower, utilizes extraction agent that solvent is extracted from filtrate under the normal temperature, and the realization solvent separates with water, compares evaporation technology, has greatly saved energy;
(2) this device can realize that solvent recovering rate more than 98%, saved solvent cost;
(3) this device is applicable to large-scale industrialization and processes continuously the filtrate that produces in the p-aramid fiber resin washing process.
Description of drawings
Fig. 1 is the structural representation of the utility model production equipment
Embodiment
Now by reference to the accompanying drawings production equipment of the present utility model is described further.
The treatment unit of the filtrate that produces comprises neutralising arrangement, extraction plant, rectifier unit and air-lift device in a kind of p-aramid fiber resin washing process; The connecting relation of neutralising arrangement is: connecting filtrate transferpump (2) and flow of filtrate meter (3) between the filtrate input terminus of the output terminal of filtrate tank (1) and neutralization reaction still (6), between the neutralizing agent input terminus of the output terminal of neutralizing agent feed bin (4) and neutralization reaction still (6), connect neutralizing agent weighing balance (5), between the input terminus of the output terminal of neutralization reaction still (6) and neutralization filtrate basin (10), connecting neutralization filtrate transferpump (8) and neutralization filtrate strainer (9); The connecting relation of extraction plant is: connecting filtrate transferpump (11) and flow of filtrate meter (12) between the bottom filtrate input terminus of the output terminal of neutralization filtrate basin (10) and extraction tower (16), between the top extraction agent input terminus of the output terminal of extraction agent basin (13) and extraction tower (16), connecting extraction agent transferpump (14) and extraction agent under meter (15), the top raffinate output terminal of extraction tower (16) and the input terminus of raffinate basin (31) join, and the bottom extraction liquid output terminal of extraction tower (16) and the input terminus of extraction liquid basin (17) join; The connecting relation of rectifier unit is: connecting extraction liquid transferpump (18) between the input terminus of the output terminal of extraction liquid basin (17) and rectifying tower (21), extraction liquid preheater (19) and extraction liquid flow meter (20), the recycle system is connecting reboiler (22) output terminal and input terminus at the bottom of rectifying tower (21) tower, connecting solvent delivery pump (23) and solvent flux meter (24) at the bottom of the tower of rectifying tower (21) between output terminal and the solvent tanker (25), the trim the top of column system of rectifying tower (21) is connecting extraction agent condenser (26) successively, condensation abstraction agent basin (27), condensation abstraction agent transferpump (28) and return flow meter (29), another output terminal of extraction agent condenser (26) is connecting vacuum pump (30), and the output terminal of extraction agent transferpump (28) is connecting the input terminus of return flow meter (29) and an input terminus of extraction agent basin (13); The connecting relation of air-lift device is: connecting raffinate transferpump (32) and raffinate flow meter (33) between the middle part input terminus of the output terminal of raffinate basin (31) and gas stripping column (34), the trim the top of column system of gas stripping column (34) is connecting condenser (35) successively, phlegma basin (36), phlegma transferpump (37) and under meter (38), another output terminal of condenser (35) is connecting vacuum pump (39), and the output terminal of phlegma transferpump (37) is connecting the input terminus of under meter (38) and another input terminus of extraction agent basin (13); The input terminus of output terminal and waste water transferpump (40) joins at the bottom of the tower of gas stripping column (34).
Described neutralizing agent weighing balance (5) is Weightlessness Electronic Scale.
Described neutralization reaction still (6) is the vertical mixing reactor.
Described neutralization filtrate strainer (9) filtering accuracy≤5 microns.
Described extraction tower (16) extraction progression 〉=8 grade.
Described extraction liquid preheater (19) is taked plate-type heat exchanger or tube and shell heat exchanger, preferentially selects plate-type heat exchanger.
Described reboiler (22), extraction agent condenser (26) and condenser (35) adopt tube and shell heat exchanger.
Described rectifying tower (21) adopts single tower or double-column in series, and the pattern of tower adopts sieve-board type or material filling type, and the rectifying mode adopts atmospheric distillation or rectification under vacuum, preferentially selects double-column in series, and the pattern of tower is material filling type, and the rectifying mode is rectification under vacuum.
Described gas stripping column (34) adopts single tower or double-column in series, and the pattern of tower adopts sieve-board type or material filling type, preferentially selects double-column in series, and the pattern of tower is material filling type.
Case study on implementation.
Embodiment 1:
The filtrate that p-aramid fiber washing in the filtrate tank (1) produces, after filtrate transferpump (2) conveying and flow of filtrate meter (3) metering, add 7905.9 mass parts in neutralization reaction still (6), then calcium hydroxide powder 116.1 mass parts that take by weighing in the neutralizing agent feed bin (4) by neutralizing agent weighing balance (5) join in the neutralization reaction still (6), stirring reaction 30 minutes, behind neutralization filtrate transferpump (8) and neutralization filtrate strainer (9), enter in the neutralization filtrate basin (10); Neutralization filtrate is behind filtrate transferpump (11) and flow of filtrate meter (12), with 3162.4 mass parts/hour flow velocity enter continuously the bottom of extraction tower (16), extraction agent chloroform in the extraction agent basin (13) is behind extraction agent transferpump (14) and extraction agent under meter (15), with 9390.8 mass parts/hour flow velocity enter continuously the top of extraction tower (16), neutralization filtrate fully mixes in extraction tower (16) with extraction agent, after being separated, raffinate from cat head with 1876.9 mass parts/hour flow velocity continuously flow into the raffinate basin (31), extraction liquid at the bottom of the tower with 10707.1 mass parts/hour flow velocity continuously flow into the extraction liquid basin (17); Extraction liquid is behind extraction liquid preheater (19), temperature rises to 50 ℃, with 10707.1 mass parts/hour flow velocity enter continuously in the rectifying tower (21), rectifying tower (21) adopts the material filling type double-column in series, tower top temperature is 70 ℃, tower top pressure is absolute pressure 20kPa, column bottom temperature is 90 ℃, solvent from discharge port at the bottom of the tower with 1274.7 mass parts/hour the flow velocity continuous discharge to solvent tanker (25), the extraction agent chloroform from cat head after condensation with 9433.4 mass parts/hour the flow velocity continuous discharge to extraction agent basin (13); Raffinate in the raffinate basin (31) with 1876.9 mass parts/hour flow velocity enter continuously in the gas stripping column (34), after air lift, chloroform in the raffinate from the stripping tower cat head after condensation with 7.72 mass parts/hour the flow velocity continuous discharge to extraction agent basin (13), at the bottom of the tower of gas stripping column (34) waste liquid through waste water transferpump (40) with 1954.9 mass parts/hour flow velocity be delivered in the sewage lagoon continuously.The final rate of recovery of calculating solvent is 98.4%.
Embodiment 2:
The filtrate that p-aramid fiber washing in the filtrate tank (1) produces, after filtrate transferpump (2) conveying and flow of filtrate meter (3) metering, add 7905.9 mass parts in neutralization reaction still (6), then calcium hydroxide powder 116.1 mass parts that take by weighing in the neutralizing agent feed bin (4) by neutralizing agent weighing balance (5) join in the neutralization reaction still (6), stirring reaction 30 minutes, behind neutralization filtrate transferpump (8) and neutralization filtrate strainer (9), enter in the neutralization filtrate basin (10); Neutralization filtrate is behind filtrate transferpump (11) and flow of filtrate meter (12), with 3794.9 mass parts/hour flow velocity enter continuously the bottom of extraction tower (16), chloroform in the extraction agent basin (13) is behind extraction agent transferpump (14) and extraction agent under meter (15), with 11269.1 mass parts/hour flow velocity enter continuously the top of extraction tower (16), neutralization filtrate fully mixes in extraction tower (16) with extraction agent, after the separation, raffinate from cat head with 2252.4 mass parts/hour flow velocity continuously flow into the raffinate basin (31), extraction liquid at the bottom of the tower with 12848.5 mass parts/hour flow velocity continuously flow into the extraction liquid basin (17); Extraction liquid is behind extraction liquid preheater (19), temperature rises to 50 ℃, with 12848.5 mass parts/hour flow velocity continuously flow in the rectifying tower (21), rectifying tower (21) adopts the material filling type double-column in series, tower top temperature is 70 ℃, tower top pressure is absolute pressure 10kPa, column bottom temperature is 90 ℃, solvent from discharge port at the bottom of the tower with 1529.6 mass parts/hour the flow velocity continuous discharge to solvent tanker (25), the extraction agent chloroform from cat head after condensation with 11320.1 mass parts/hour the flow velocity continuous discharge to extraction agent basin (13); Raffinate in the raffinate basin (31) with 2252.4 mass parts/hour flow velocity enter continuously in the gas stripping column (34), after air lift, chloroform in the raffinate from the stripping tower cat head after condensation with 9.27 mass parts/hour the flow velocity continuous discharge to extraction agent basin (13), at the bottom of the tower of gas stripping column (34) waste liquid through waste water transferpump (40) with 2345.9 mass parts/hour flow velocity be delivered in the sewage lagoon continuously.The final rate of recovery of calculating solvent is 99.1%.
Embodiment 3:
The filtrate that p-aramid fiber washing in the filtrate tank (1) produces, after filtrate transferpump (2) conveying and flow of filtrate meter (3) metering, add 7905.9 mass parts in neutralization reaction still (6), then calcium hydroxide powder 116.1 mass parts that take by weighing in the neutralizing agent feed bin (4) by neutralizing agent weighing balance (5) join in the neutralization reaction still (6), stirring reaction 30 minutes, behind neutralization filtrate transferpump (8) and neutralization filtrate strainer (9), enter in the neutralization filtrate basin (10); Neutralization filtrate is behind filtrate transferpump (11) and flow of filtrate meter (12), with 3162.4 mass parts/hour flow velocity enter continuously the bottom of extraction tower (16), chloroform in the extraction agent basin (13) is behind extraction agent transferpump (14) and extraction agent under meter (15), with 12521.1 mass parts/hour flow velocity enter continuously the top of extraction tower (16), neutralization filtrate fully mixes in extraction tower (16) with extraction agent, after the separation, raffinate from cat head with 1874.9 mass parts/hour flow velocity continuously flow into the raffinate basin (31), extraction liquid at the bottom of the tower with 13855.1 mass parts/hour flow velocity continuously flow into the extraction liquid basin (17); Extraction liquid is behind extraction liquid preheater (19), temperature rises to 50 ℃, with 13855.1 mass parts/hour flow velocity continuously flow in the rectifying tower (21), rectifying tower (21) adopts the material filling type double-column in series, tower top temperature is 70 ℃, tower top pressure is absolute pressure 10kPa, column bottom temperature is 90 ℃, solvent from discharge port at the bottom of the tower with 1274.7 mass parts/hour the flow velocity continuous discharge to solvent tanker (25), the extraction agent chloroform from cat head after condensation with 12581.4 mass parts/hour the flow velocity continuous discharge to extraction agent basin (13); Raffinate in the raffinate basin (31) with 1874.9 mass parts/hour flow velocity enter continuously in the gas stripping column (34), after air lift, chloroform in the raffinate from the stripping tower cat head after condensation with 5.67 mass parts/hour the flow velocity continuous discharge to extraction agent basin (13), at the bottom of the tower of gas stripping column (34) waste liquid through waste water transferpump (40) with 1954.7 mass parts/hour flow velocity be delivered in the sewage lagoon continuously.The final rate of recovery of calculating solvent is 98.9%.
Claims (9)
1. the treatment unit of the filtrate that produces in the p-aramid fiber resin washing process is characterized in that: comprise neutralising arrangement, extraction plant, rectifier unit and air-lift device; The connecting relation of neutralising arrangement is: connecting filtrate transferpump (2) and flow of filtrate meter (3) between the filtrate input terminus of the output terminal of filtrate tank (1) and neutralization reaction still (6), between the neutralizing agent input terminus of the output terminal of neutralizing agent feed bin (4) and neutralization reaction still (6), connect neutralizing agent weighing balance (5), between the input terminus of the output terminal of neutralization reaction still (6) and neutralization filtrate basin (10), connecting neutralization filtrate transferpump (8) and neutralization filtrate strainer (9); The connecting relation of extraction plant is: connecting filtrate transferpump (11) and flow of filtrate meter (12) between the bottom filtrate input terminus of the output terminal of neutralization filtrate basin (10) and extraction tower (16), between the top extraction agent input terminus of the output terminal of extraction agent basin (13) and extraction tower (16), connecting extraction agent transferpump (14) and extraction agent under meter (15), the top raffinate output terminal of extraction tower (16) and the input terminus of raffinate basin (31) join, and the bottom extraction liquid output terminal of extraction tower (16) and the input terminus of extraction liquid basin (17) join; The connecting relation of rectifier unit is: connecting extraction liquid transferpump (18) between the input terminus of the output terminal of extraction liquid basin (17) and rectifying tower (21), extraction liquid preheater (19) and extraction liquid flow meter (20), the recycle system is connecting reboiler (22) output terminal and input terminus at the bottom of rectifying tower (21) tower, connecting solvent delivery pump (23) and solvent flux meter (24) at the bottom of the tower of rectifying tower (21) between output terminal and the solvent tanker (25), the trim the top of column system of rectifying tower (21) is connecting extraction agent condenser (26) successively, condensation abstraction agent basin (27), condensation abstraction agent transferpump (28) and return flow meter (29), another output terminal of extraction agent condenser (26) is connecting vacuum pump (30), and the output terminal of extraction agent transferpump (28) is connecting the input terminus of return flow meter (29) and an input terminus of extraction agent basin (13); The connecting relation of air-lift device is: connecting raffinate transferpump (32) and raffinate flow meter (33) between the middle part input terminus of the output terminal of raffinate basin (31) and gas stripping column (34), the trim the top of column system of gas stripping column (34) is connecting condenser (35) successively, phlegma basin (36), phlegma transferpump (37) and under meter (38), another output terminal of condenser (35) is connecting vacuum pump (39), and the output terminal of phlegma transferpump (37) is connecting the input terminus of under meter (38) and another input terminus of extraction agent basin (13); The input terminus of output terminal and waste water transferpump (40) joins at the bottom of the tower of gas stripping column (34).
2. the treatment unit of the filtrate that produces in a kind of p-aramid fiber resin washing process according to claim 1, it is characterized in that: described neutralizing agent weighing balance (5) is Weightlessness Electronic Scale.
3. the treatment unit of the filtrate that produces in a kind of p-aramid fiber resin washing process according to claim 1, it is characterized in that: described neutralization reaction still (6) is the vertical mixing reactor.
4. the treatment unit of the filtrate that produces in a kind of p-aramid fiber resin washing process according to claim 1 is characterized in that: described neutralization filtrate strainer (9) filtering accuracy≤5 microns.
5. the treatment unit of the filtrate that produces in a kind of p-aramid fiber resin washing process according to claim 1 is characterized in that: described extraction tower (16) extraction progression 〉=8 grade.
6. the treatment unit of the filtrate that produces in a kind of p-aramid fiber resin washing process according to claim 1, it is characterized in that: described extraction liquid preheater (19) is taked plate-type heat exchanger or tube and shell heat exchanger.
7. the treatment unit of the filtrate that produces in a kind of p-aramid fiber resin washing process according to claim 1 is characterized in that: described reboiler (22), extraction agent condenser (26) and condenser (35) employing tube and shell heat exchanger.
8. the treatment unit of the filtrate that produces in a kind of p-aramid fiber resin washing process according to claim 1, it is characterized in that: described rectifying tower (21) adopts single tower or double-column in series, the pattern of tower adopts sieve-board type or material filling type, and the rectifying mode adopts atmospheric distillation or rectification under vacuum.
9. the treatment unit of the filtrate that produces in a kind of p-aramid fiber resin washing process according to claim 1 is characterized in that: described gas stripping column (34) the single tower of employing or double-column in series, pattern employing sieve-board type or the material filling type of tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220508704 CN202849303U (en) | 2012-10-05 | 2012-10-05 | Treatment device for filter liquor generated in process of para-aramid resin washing |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220508704 CN202849303U (en) | 2012-10-05 | 2012-10-05 | Treatment device for filter liquor generated in process of para-aramid resin washing |
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| Publication Number | Publication Date |
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| CN202849303U true CN202849303U (en) | 2013-04-03 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN 201220508704 Withdrawn - After Issue CN202849303U (en) | 2012-10-05 | 2012-10-05 | Treatment device for filter liquor generated in process of para-aramid resin washing |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102838249A (en) * | 2012-10-05 | 2012-12-26 | 上海会博新材料科技有限公司 | Device for treating filtrate generated in washing process of para-aramid resin |
-
2012
- 2012-10-05 CN CN 201220508704 patent/CN202849303U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102838249A (en) * | 2012-10-05 | 2012-12-26 | 上海会博新材料科技有限公司 | Device for treating filtrate generated in washing process of para-aramid resin |
| CN102838249B (en) * | 2012-10-05 | 2014-02-19 | 上海会博新材料科技有限公司 | Device for treating filtrate generated in washing process of para-aramid resin |
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Granted publication date: 20130403 Effective date of abandoning: 20140219 |
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