CN102219920B - Recycling process of hydroxypropyl methyl cellulose (HPMC) production solvent - Google Patents
Recycling process of hydroxypropyl methyl cellulose (HPMC) production solvent Download PDFInfo
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- CN102219920B CN102219920B CN2011101175495A CN201110117549A CN102219920B CN 102219920 B CN102219920 B CN 102219920B CN 2011101175495 A CN2011101175495 A CN 2011101175495A CN 201110117549 A CN201110117549 A CN 201110117549A CN 102219920 B CN102219920 B CN 102219920B
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Abstract
The invention discloses a recovery process of a hydroxypropyl methyl cellulose (HPMC) production solvent, relating to the field of fine chemistry, wherein the step of distillation or rectification in the traditional process is removed, the production solvent is recovered by using a three-step process, the process is simple, the labor intensity of workers is lowered, the production security is improved; the steam consumption is reduced, compared with the original recovery process, the recovery process has the advantages of reducing the steam consumption by 20-40% in the recovery process of the production solvent per ton of the product, and reducing the solvent consumption; and compared with the original process, the recovery process has the production solvent consumption per ton of the product reduced by 30-70%, and the solvent recovery rate of more than or equal to 99%, which is more than 3%, and avoids the discharge of distillation residue. The recovery process is more energy-saving and environmentally friendly.
Description
Technical field
The present invention relates to field of fine chemical, specifically a kind of Vltra tears (HPMC) is produced the recovery technology of solvent.
Background technology
At present, in the production process of domestic Vltra tears (HPMC), reaction solvent all is to form according to the ratio of 85:15 is composite with two kinds of solvents of toluene-Virahol; These solvents need be retrieved to recycle; Domestic whole employing precipitation still is deviate from solvent, and the mode of rectifying or simple distillation reclaims solvent then, and the impurity in the solvent is removed through residue at the bottom of discharging tower; Investment is big, and energy consumption is high.
Summary of the invention
For solving the technical problem of above-mentioned existence, the present invention provides a kind of Vltra tears (HPMC) to produce the recovery technology of solvent, has removed the step of distillation or rectifying, reduces steam consumption, has also reduced the loss of solvent, energy-conserving and environment-protective.
For achieving the above object, the technical scheme that the present invention adopts is following:
1) gas-liquid separation: the solvent with precipitation still precipitation comes out, carry out gas-liquid separation through gas-liquid separator;
2) condensation: the gas after the separation gets into condensing surface, is condensed into liquid;
3) A cooling: the liquid after the separation gets into water cooler A, and with 20-45 ℃ recirculated water cooling, temperature is cooled to 20-40 ℃ by 70-90 ℃;
4) B cooling: the liquid after the condenser condenses gets into water cooler B, and with 20-45 ℃ recirculated water cooling, temperature 70-90 ℃ by being cooled to 20-40 ℃;
5) one-level layering: through A, two cooled liquid of water cooler of B and stream, get into the middle part of one-level quantizer, liquid come-up in upper strata arrives near vertical upper strata hydrorrhea head piece, and subnatant arrives at the bottom of the awl of one-level quantizer;
6) secondary layering: through the upper strata liquid of overflow after the layering of one-level quantizer, get into the middle part of secondary quantizer, upper strata liquid arrives near vertical upper strata hydrorrhea head piece, and subnatant arrives at the bottom of the awl of secondary quantizer;
7) recycle: the overflowing liquid after the layering of secondary quantizer gets into dosing vessel, recycles through batching; Subnatant confluxes and gets into lower floor's liquid bath at the bottom of the awl of one-level quantizer and secondary quantizer, and preparing burden recycles.
The present invention has removed the step of distillation or rectifying, adopts three-step approach to reclaim and produces solvent, and technology is simple, has reduced staff's labour intensity, has improved production security; Reduce steam consumption, in the removal process of products production solvent per ton, reduced the consumption 20-40% of steam than original recovery technology; Reduced the loss of solvent, the production solvent loss of product per ton reduces 30-70% than former technology, and solvent recovering rate >=99% is higher by 3% than traditional technology, has avoided the discharging of distillation residue simultaneously, more energy-conserving and environment-protective.
Description of drawings
Accompanying drawing is a process flow sheet of the present invention.
Embodiment:
Describe the present invention below in conjunction with accompanying drawing and specific embodiment:
As shown in the figure, technological process of the present invention is following:
1) gas-liquid separation: the solvent with precipitation still precipitation comes out, carry out gas-liquid separation through gas-liquid separator, avoid gas entrainment liquid to get into condensing surface, influence condensation efficiency, the gas-liquid separator diameter 800mm of employing, high 1200mm, the bottom is taper;
2) condensation: the gas after the separation gets into condensing surface, is condensed into liquid, and condensing surface adopts the thin tubesheet structure, and heat interchanging area is 50-80M
2, quantity of circulating water is 30-80M
3/ h;
3) A cooling: the liquid after the separation gets into water cooler A, and with 20-45 ℃ recirculated water cooling, temperature is cooled to 20-40 ℃ by 70-90 ℃, and water cooler A adopts the thin tubesheet structure, and heat interchanging area is 30-60M
2, quantity of circulating water is 20-60M
3/ h;
4) B cooling: the liquid after the condenser condenses gets into water cooler B, and with 20-45 ℃ recirculated water cooling, temperature 70-90 ℃ by being cooled to 20-40 ℃, water cooler B employing thin tubesheet structure, heat interchanging area 20-50M
2, quantity of circulating water 20-40M
3/ h;
5) one-level layering: through A, two cooled liquid of water cooler of B and stream, get into the middle part of one-level quantizer, liquid come-up in upper strata arrives near vertical upper strata hydrorrhea head piece, and subnatant arrives at the bottom of the awl of one-level quantizer;
6) secondary layering: through the upper strata liquid of overflow after the layering of one-level quantizer, get into the middle part of secondary quantizer, upper strata liquid arrives near vertical upper strata hydrorrhea head piece, and subnatant arrives at the bottom of the awl of secondary quantizer;
7) recycle: the overflowing liquid after the layering of secondary quantizer gets into dosing vessel, recycles after the process batching reaches technical requirements; Subnatant confluxes and gets into lower floor's liquid bath at the bottom of the awl of one-level quantizer and secondary quantizer, recycles after preparing burden.
Embodiment 1
1) gas-liquid separation: the solvent with precipitation still precipitation comes out, carry out gas-liquid separation through gas-liquid separator;
2) condensation: the gas after the separation gets into condensing surface, is condensed into liquid;
3) A cooling: the liquid after the separation gets into water cooler A, and with 20-25 ℃ recirculated water cooling, temperature is cooled to 20-30 ℃ by 80-90 ℃;
4) B cooling: the liquid after the condenser condenses gets into water cooler B, and with 20-25 ℃ recirculated water cooling, temperature 80-90 ℃ by being cooled to 20-30 ℃;
5) one-level layering: through A, two cooled liquid of water cooler of B and stream, get into the middle part of one-level quantizer, liquid come-up in upper strata arrives near vertical upper strata hydrorrhea head piece, and subnatant arrives at the bottom of the awl of one-level quantizer;
6) secondary layering: through the upper strata liquid of overflow after the layering of one-level quantizer, get into the middle part of secondary quantizer, upper strata liquid arrives near vertical upper strata hydrorrhea head piece, and subnatant arrives at the bottom of the awl of secondary quantizer;
7) recycle: the overflowing liquid after the layering of secondary quantizer gets into dosing vessel, recycles through batching; Subnatant confluxes and gets into lower floor's liquid bath at the bottom of the awl of one-level quantizer and secondary quantizer, and preparing burden recycles.
Embodiment 2
1) gas-liquid separation: the solvent with precipitation still precipitation comes out, carry out gas-liquid separation through gas-liquid separator;
2) condensation: the gas after the separation gets into condensing surface, is condensed into liquid;
3) A cooling: the liquid after the separation gets into water cooler A, and with 30-40 ℃ recirculated water cooling, temperature is cooled to 30-40 ℃ by 70-80 ℃;
4) B cooling: the liquid after the condenser condenses gets into water cooler B, and with 30-40 ℃ recirculated water cooling, temperature 70-80 ℃ by being cooled to 30-40 ℃;
5) one-level layering: through A, two cooled liquid of water cooler of B and stream, get into the middle part of one-level quantizer, liquid come-up in upper strata arrives near vertical upper strata hydrorrhea head piece, and subnatant arrives at the bottom of the awl of one-level quantizer;
6) secondary layering: through the upper strata liquid of overflow after the layering of one-level quantizer, get into the middle part of secondary quantizer, upper strata liquid arrives near vertical upper strata hydrorrhea head piece, and subnatant arrives at the bottom of the awl of secondary quantizer;
7) recycle: the overflowing liquid after the layering of secondary quantizer gets into dosing vessel, recycles through batching; Subnatant confluxes and gets into lower floor's liquid bath at the bottom of the awl of one-level quantizer and secondary quantizer, and preparing burden recycles.
Embodiment 3
1) gas-liquid separation: the solvent with precipitation still precipitation comes out, carry out gas-liquid separation through gas-liquid separator;
2) condensation: the gas after the separation gets into condensing surface, is condensed into liquid;
3) A cooling: the liquid after the separation gets into water cooler A, and with 40-45 ℃ recirculated water cooling, temperature is cooled to 25-30 ℃ by 85-90 ℃;
4) B cooling: the liquid after the condenser condenses gets into water cooler B, and with 40-45 ℃ recirculated water cooling, temperature 85-90 ℃ by being cooled to 25-30 ℃;
5) one-level layering: through A, two cooled liquid of water cooler of B and stream, get into the middle part of one-level quantizer, liquid come-up in upper strata arrives near vertical upper strata hydrorrhea head piece, and subnatant arrives at the bottom of the awl of one-level quantizer;
6) secondary layering: through the upper strata liquid of overflow after the layering of one-level quantizer, get into the middle part of secondary quantizer, upper strata liquid arrives near vertical upper strata hydrorrhea head piece, and subnatant arrives at the bottom of the awl of secondary quantizer;
7) recycle: the overflowing liquid after the layering of secondary quantizer gets into dosing vessel, recycles through batching; Subnatant confluxes and gets into lower floor's liquid bath at the bottom of the awl of one-level quantizer and secondary quantizer, and preparing burden recycles.
Claims (4)
1. a Vltra tears (HPMC) is produced the recovery technology of solvent, it is characterized in that, is realized by following step:
1) gas-liquid separation: the solvent with precipitation still precipitation comes out, carry out gas-liquid separation through gas-liquid separator;
2) condensation: the gas after the separation gets into condensing surface, is condensed into liquid;
3) A cooling: the liquid after the separation gets into water cooler A, and with 20-45 ℃ recirculated water cooling, temperature is cooled to 20-40 ℃ by 70-90 ℃;
4) B cooling: the liquid after the condenser condenses gets into water cooler B, and with 20-45 ℃ recirculated water cooling, temperature is cooled to 20-40 ℃ by 70-90 ℃;
5) one-level layering: through A, two cooled liquid of water cooler of B and stream, get into the middle part of one-level quantizer, liquid come-up in upper strata arrives near vertical upper strata hydrorrhea head piece, and subnatant arrives at the bottom of the awl of one-level quantizer;
6) secondary layering: through the upper strata liquid of overflow after the layering of one-level quantizer, get into the middle part of secondary quantizer, upper strata liquid arrives near vertical upper strata hydrorrhea head piece, and subnatant arrives at the bottom of the awl of secondary quantizer;
7) recycle: the overflowing liquid after the layering of secondary quantizer gets into dosing vessel, recycles through batching; Subnatant confluxes and gets into lower floor's liquid bath at the bottom of the awl of one-level quantizer and secondary quantizer, recycles through batching.
2. Vltra tears according to claim 1 (HPMC) is produced the recovery technology of solvent, it is characterized in that, described condensing surface adopts the thin tubesheet structure, and heat interchanging area is 50-80m
2, quantity of circulating water is 30-80m
3/ h.
3. Vltra tears according to claim 1 (HPMC) is produced the recovery technology of solvent, it is characterized in that, described water cooler A adopts the thin tubesheet structure, and heat interchanging area is 30-60m
2, quantity of circulating water is 20-60m
3/ h.
4. Vltra tears according to claim 1 (HPMC) is produced the recovery technology of solvent, it is characterized in that, described water cooler B adopts thin tubesheet structure, heat interchanging area 20-50m
2, quantity of circulating water 20-40m
3/ h.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011101175495A CN102219920B (en) | 2011-05-09 | 2011-05-09 | Recycling process of hydroxypropyl methyl cellulose (HPMC) production solvent |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011101175495A CN102219920B (en) | 2011-05-09 | 2011-05-09 | Recycling process of hydroxypropyl methyl cellulose (HPMC) production solvent |
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| Publication Number | Publication Date |
|---|---|
| CN102219920A CN102219920A (en) | 2011-10-19 |
| CN102219920B true CN102219920B (en) | 2012-11-21 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011101175495A Expired - Fee Related CN102219920B (en) | 2011-05-09 | 2011-05-09 | Recycling process of hydroxypropyl methyl cellulose (HPMC) production solvent |
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| CN115417798A (en) * | 2022-08-15 | 2022-12-02 | 山东戴瑞克新材料有限公司 | Continuous liquid separation process for dicyclohexyl disulfide |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101955546A (en) * | 2009-07-15 | 2011-01-26 | 山东赫达股份有限公司 | Process for producing cellulose ether by directly separating and recovering diluent |
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Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101955546A (en) * | 2009-07-15 | 2011-01-26 | 山东赫达股份有限公司 | Process for producing cellulose ether by directly separating and recovering diluent |
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