CN202730054U - Caprolactam monomer recovery system for high-volume production of polyamide slice - Google Patents
Caprolactam monomer recovery system for high-volume production of polyamide slice Download PDFInfo
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- CN202730054U CN202730054U CN 201220370309 CN201220370309U CN202730054U CN 202730054 U CN202730054 U CN 202730054U CN 201220370309 CN201220370309 CN 201220370309 CN 201220370309 U CN201220370309 U CN 201220370309U CN 202730054 U CN202730054 U CN 202730054U
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Abstract
The utility model provides a caprolactam monomer recovery system for high-volume production of the polyamide slice. The caprolactam monomer recovery system for the high-volume production of the polyamide slice includes an extraction water sink, a feedwater device, an evaporation and concentration device, a rectification device and a recovery device. The extraction water sink is connected with the evaporation and concentration device and transfers the extraction water from the extraction water sink to the evaporation and concentration device through the feedwater device. The feedwater device is arranged between the extraction water sink and the evaporation and concentration device, the evaporation and concentration device is connected with the rectification device, the extraction water is transferred to the rectification device after evaporation and concentration, and the rectification device is connected with the recovery device and recycles the caprolactam monomer through the recovery device. The caprolactam monomer recovery system for the high-volume production of the polyamide slice has the advantages that by adopting the structure, the extraction water generated from the production of the polyamide slice is subjected to rectifying recovery after evaporation and concentration, the recovery of the monomer is improved greatly, huge amounts of energy is saved and the energy loss and pollution to the environment are avoided. Further the caprolactam monomer recovery system for the high-volume production of the polyamide slice is low in energy consumption, low in production cost, good in production stability and convenient to control.
Description
Technical field
The production technique of the utility model design polymeric amide section relates in particular to the caprolactam monomer recovery system that a kind of large capacity is produced the polymeric amide section.
Background technology
The Pa-6 Polymerization suitability for industrialized production generally adopts hexanolactam hydrolytic polymerization Technology, but there are the problems such as contaminate environment and the wasting of resources in the caprolactam polymerization suitability for industrialized production, the hexanolactam hydrolytic-polymeric reaction is the chemical reaction of a reversible balance, can not realize the transformation efficiency of caprolactam monomer 100%, after the polyreaction balance, contain the caprolactam monomer of 7%-8% and about 2% oligopolymer in the polymkeric substance, if do not remove these materials, the following process operation such as spinning, moulding of polyamide fibre 6 will be had a strong impact on.Therefore need to extract chinlon 6 section, simultaneously monomer in the extraction water be recycled.
To the recycling of monomer in the extraction water, in the prior art, mainly be following three kinds of methods:
One, extraction water is carried out first dehydration by evaporation, the weight percentage that obtains water is about 30% concentrated solution, is distilling demonomerization, and the distillation demonomerization is generally intermittent type.
Two, extraction water is carried out first dehydration by evaporation, the weight percentage that obtains de-salted water is about 30% concentrated solution, the redistillation dehydration, and the weight percentage that obtains de-salted water is about 5% concentrated solution, not at distillation dehydration and demonomerization, directly enter polymerization in the pre-polymerization device.
Three, extraction water is carried out first dehydration by evaporation, the weight percentage that obtains de-salted water is about 30% concentrated solution, at distillation dehydration, the weight percentage that obtains de-salted water is about 10% concentrated solution, send into cracker with high-pressure pump, cracking under 290 ℃-300 ℃ of temperature, pressure 2Mpa-2.5Mpa, split product enters polymerization in the pre-polymerization device by a certain percentage with fresh monomer after dehydration, release.
There is in the prior art following deficiency:
1, first method have partial monosomy and oligopolymer to drain as raffinate, so the chinlon 6 section unit consumption of product is higher, and the waste residue, the waste liquid that produce after the distillation has pollution to environment in distillation demonomerization process.
2, second method is produced section by reclaiming monomer (not adding fresh monomer) concentrated solution polymerization fully, and quality product is lower, generally can only be as low-grade injection moulding section and the more low-grade short silk of nylon materials.
3, adopt the third method to need cover high temperature, decomposition under high pressure equipment and a relevant auxiliary facility, operational path is long, and device structure is complicated, and investment is large; Scission reaction is carried out under high temperature, high pressure, and energy consumption is large, and process cost is high; Technique controlling difficulty is large.
The utility model content
Technical problem to be solved in the utility model is to overcome the shortcoming that the prior art caprolactam monomer reclaims, the caprolactam monomer recovery system that control is convenient when providing a kind of large capacity of growing to produce the polymeric amide section, plant energy consumption is low, production stability is good.
To achieve these goals, the technical scheme that adopts of the utility model is:
A kind of large capacity is produced the caprolactam monomer recovery system of polymeric amide section, comprise extraction tank, water feed apparatus, evaporation concentration device, rectifier unit and retrieving arrangement, described extraction tank is connected with evaporation concentration device, and by the water feed apparatus between being arranged on extraction water from the extraction tank be delivered to evaporation concentration device, described evaporation concentration device is connected with rectifier unit, extraction water is delivered to rectifier unit through evaporation concentration, described rectifier unit is connected with retrieving arrangement, by retrieving arrangement caprolactam monomer is recycled.
Wherein, described water feed apparatus comprises extraction water fresh feed pump, strainer and extraction water inlet line, the water-in of described extraction water fresh feed pump is connected with the water outlet of extraction tank, described strainer is arranged in the extraction water inlet line, one end of described extraction water inlet pipe connects the water outlet of extraction water fresh feed pump, the other end connects the water-in of evaporation concentration device, and extraction water is entered the extraction water inlet line and enters evaporation concentration device by the strainer filtration from the extraction water concentrated flow by the effect of extraction water fresh feed pump.
Wherein, described evaporation concentration device is the three-effect evaporation and condensation device, namely is in series by three evaporation concentrators.
Wherein, described rectifier unit is the multistage rectification device, namely is in series by two or more rectifying tower.
Wherein, described retrieving arrangement comprises recovery hexanolactam storage tank, take away pump, pneumavalve and equilibration tube, be connected by equilibration tube between described recovery hexanolactam storage tank and the rectifier unit, described pneumavalve is located on the pipeline of equilibration tube, the outlet of described recovery hexanolactam storage tank links to each other with the import of take away pump, and the caprolactam monomer of recovery can be delivered in the polymerizing reactor by take away pump.
The beneficial effects of the utility model are, adopt said structure, extraction water when producing the polymeric amide section is passed through evaporation concentration, carrying out rectifying reclaims again, the rate of recovery of monomer can be provided greatly, save mass energy, avoid the loss of these energy and to the pollution of environment, the utility model system energy consumption is low in addition, production cost is low, production stability is good and control convenient.
Description of drawings
Fig. 1 is the structural representation that the large capacity of the utility model is produced the caprolactam monomer recovery system of polymeric amide section.
Wherein:
1, extraction tank; 2: water feed apparatus; 3: evaporation concentration device; 4: rectifier unit; 5: reclaim the hexanolactam storage tank.
Embodiment
By describing technology contents of the present utility model, structural attitude in detail, realized purpose and effect, below in conjunction with embodiment and cooperate that accompanying drawing is detailed to give explanation.
See also Fig. 1, as shown in the figure, the embodiment that the large capacity of present embodiment is produced the caprolactam monomer recovery system of polymeric amide section comprises extraction tank 1, water feed apparatus 2, evaporation concentration device 3, rectifier unit 4 and retrieving arrangement, described extraction tank 1, water feed apparatus 2 is connected with evaporation concentration device 3, described water feed apparatus 2 comprises the extraction water fresh feed pump, strainer and extraction water inlet line, the water-in of described extraction water fresh feed pump is connected with the water outlet of extraction tank 1, described strainer is arranged in the extraction water inlet line, one end of described extraction water inlet pipe connects the water outlet of extraction water fresh feed pump, the other end connects the water-in of evaporation concentration device 3, described evaporation concentration device 3 is connected with rectifier unit 4, described rectifier unit 4 is connected with retrieving arrangement, described retrieving arrangement comprises recovery hexanolactam storage tank 5, take away pump, pneumavalve and equilibration tube, be connected by equilibration tube between described recovery hexanolactam storage tank and the rectifier unit, described pneumavalve is located on the pipeline of equilibration tube, and the outlet of described recovery hexanolactam storage tank 5 links to each other with the import of take away pump.
The utility model caprolactam monomer recovery system is when carrying out the caprolactam monomer recovery, the extraction water fresh feed pump of described water feed apparatus 2 is delivered to evaporation concentration device 3 with extraction water from extraction tank 1, extraction water is carried out after the evaporation concentration in evaporation concentration device 3, be delivered to rectifier unit 4 and carry out the rectifying extraction, the caprolactam monomer that reclaims afterwards is integrated in the recovery hexanolactam storage tank 5 of retrieving arrangement, then is delivered to by take away pump and carries out the polymerization section in the polymerizing reactor.
Adopt said structure, extraction water when producing the polymeric amide section is passed through evaporation concentration, carrying out rectifying reclaims again, the rate of recovery of monomer can be provided greatly, save mass energy, avoid the loss of these energy and to the pollution of environment, the utility model system energy consumption is low in addition, production cost is low, production stability is good and control convenient.
For evaporation and rectification effect are provided, the utility model is further optimized, and described evaporation concentration device 3 is the three-effect evaporation and condensation device, namely is in series by three evaporation concentrators.Described rectifier unit 4 is the multistage rectification device, namely is in series by two or more rectifying tower.
The above only is embodiment of the present utility model; be not so limit claim of the present utility model; every equivalent structure or equivalent flow process conversion that utilizes the utility model specification sheets and accompanying drawing content to do; or directly or indirectly be used in other relevant technical fields, all in like manner be included in the scope of patent protection of the present utility model.
Claims (5)
1. a large capacity is produced the caprolactam monomer recovery system that polymeric amide is cut into slices, it is characterized in that: comprise the extraction tank, water feed apparatus, evaporation concentration device, rectifier unit and retrieving arrangement, described extraction tank is connected with evaporation concentration device, and by the water feed apparatus between being arranged on extraction water from the extraction tank be delivered to evaporation concentration device, described evaporation concentration device is connected with rectifier unit, extraction water is delivered to rectifier unit through evaporation concentration, described rectifier unit is connected with retrieving arrangement, by retrieving arrangement caprolactam monomer is recycled.
2. large capacity according to claim 1 is produced the caprolactam monomer recovery system of polymeric amide section, it is characterized in that: described water feed apparatus comprises the extraction water fresh feed pump, strainer and extraction water inlet line, the water-in of described extraction water fresh feed pump is connected with the water outlet of extraction tank, described strainer is arranged in the extraction water inlet line, one end of described extraction water inlet pipe connects the water outlet of extraction water fresh feed pump, the other end connects the water-in of evaporation concentration device, and extraction water is entered the extraction water inlet line and enters evaporation concentration device by the strainer filtration from the extraction water concentrated flow by the effect of extraction water fresh feed pump.
3. large capacity according to claim 1 is produced the caprolactam monomer recovery system of polymeric amide section, and it is characterized in that: described evaporation concentration device is the three-effect evaporation and condensation device, namely is in series by three evaporation concentrators.
4. large capacity according to claim 1 is produced the caprolactam monomer recovery system of polymeric amide section, and it is characterized in that: described rectifier unit is the multistage rectification device, namely is in series by two or more rectifying tower.
5. large capacity according to claim 1 is produced the caprolactam monomer recovery system of polymeric amide section, it is characterized in that: described retrieving arrangement comprises recovery hexanolactam storage tank, take away pump, pneumavalve and equilibration tube, be connected by equilibration tube between described recovery hexanolactam storage tank and the rectifier unit, described pneumavalve is located on the pipeline of equilibration tube, the outlet of described recovery hexanolactam storage tank links to each other with the import of take away pump, and the caprolactam monomer of recovery can be delivered in the polymerizing reactor by take away pump.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220370309 CN202730054U (en) | 2012-07-27 | 2012-07-27 | Caprolactam monomer recovery system for high-volume production of polyamide slice |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220370309 CN202730054U (en) | 2012-07-27 | 2012-07-27 | Caprolactam monomer recovery system for high-volume production of polyamide slice |
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| CN202730054U true CN202730054U (en) | 2013-02-13 |
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| CN 201220370309 Expired - Fee Related CN202730054U (en) | 2012-07-27 | 2012-07-27 | Caprolactam monomer recovery system for high-volume production of polyamide slice |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103466869A (en) * | 2013-07-23 | 2013-12-25 | 江苏海阳化纤有限公司 | Total reuse and recovery system for polyamide 6 monomer |
| CN103483580A (en) * | 2013-08-07 | 2014-01-01 | 江苏海阳化纤有限公司 | Polyamide-6 granula device and process capable of recovering all monomers |
| CN112843760A (en) * | 2020-12-31 | 2021-05-28 | 南通瀚蓝机械科技有限公司 | Balanced pipeline structure of concentration tower |
-
2012
- 2012-07-27 CN CN 201220370309 patent/CN202730054U/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103466869A (en) * | 2013-07-23 | 2013-12-25 | 江苏海阳化纤有限公司 | Total reuse and recovery system for polyamide 6 monomer |
| CN103483580A (en) * | 2013-08-07 | 2014-01-01 | 江苏海阳化纤有限公司 | Polyamide-6 granula device and process capable of recovering all monomers |
| CN103483580B (en) * | 2013-08-07 | 2016-04-27 | 江苏海阳化纤有限公司 | The chinlon 6 section device of the full reuse of a kind of monomer and flow process |
| CN112843760A (en) * | 2020-12-31 | 2021-05-28 | 南通瀚蓝机械科技有限公司 | Balanced pipeline structure of concentration tower |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address | ||
| CP03 | Change of name, title or address |
Address after: 350209 Airport Industrial Zone, Changle District, Fuzhou City, Fujian Province (Mashan District, Hunan town) Patentee after: Fujian Yongrong Jinjiang Co.,Ltd. Address before: 350212 Fujian city of Fuzhou province Pengcheng Changle Airport Industrial Zone, Road No. 258 Patentee before: FUJIAN JINJIANG TECHNOLOGY Co.,Ltd. |
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| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130213 Termination date: 20210727 |