CN212174854U - Nylon salt solution evaporation polymerization device - Google Patents
Nylon salt solution evaporation polymerization device Download PDFInfo
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- CN212174854U CN212174854U CN202020662384.4U CN202020662384U CN212174854U CN 212174854 U CN212174854 U CN 212174854U CN 202020662384 U CN202020662384 U CN 202020662384U CN 212174854 U CN212174854 U CN 212174854U
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Abstract
The utility model relates to an evaporation polymerization device of nylon salt solution, the outlet of dehydration salt solution pipe and additive injection pipe is connected with the material inlet of flash evaporator together, the material outlet of flash evaporator is connected with the feed inlet of gas-liquid separator through the flash evaporation discharging pipe, the bottom outlet of gas-liquid separator is connected with the feed inlet of horizontal disc reactor, the discharge outlet of horizontal disc reactor is connected with the inlet of polymer material delivery pump I, the outlet of polymer material delivery pump I is connected with granulator I and spinning civilian silk equipment; the outlet of the first polymer material conveying pump is also connected with the feed inlet of the vertical polymerization reaction kettle through a post-polymerization feed pipe, the discharge outlet at the lower end of the vertical polymerization reaction kettle is connected with the inlet of a second polymer material conveying pump, and the outlet of the second polymer material conveying pump is connected with a second granulator and industrial yarn spinning equipment. The molecular weight distribution of the polymer material of the device is uniform, the product quality can be greatly improved, and the product requirements of direct spinning civil filaments, engineering plastics and industrial filaments can be met.
Description
Technical Field
The utility model relates to an evaporation polymerization device especially relates to an evaporation polymerization device of nylon salt solution, belongs to nylon production facility technical field.
Background
Most of nylon polymers are prepared by taking diamine and dibasic acid as raw materials and pure water as a carrier, performing neutralization reaction to produce a nylon salt aqueous solution, concentrating the nylon salt aqueous solution, performing polymerization reaction to generate a nylon high-molecular melt, and granulating the nylon high-molecular melt by a granulator, wherein the representative products include nylon 56, nylon 66 and the like.
The concentrated nylon salt solution enters a U-shaped tube reactor for further dehydration, a certain polymerization reaction is completed under the pressure of 1.75-2.1MPa, the molecular weight of the material at the outlet of the U-shaped tube reactor can reach 5000, and the temperature is 240-270 ℃. The conventional products are: nylon prepolymer +10% moisture; the full-dull special products are as follows: nylon prepolymer +13% moisture (about 3% more water than the ordinary product). The nylon prepolymer from the U-shaped tube reactor enters a flash evaporator to continuously evaporate water, enters a front polymerizer to continuously polymerize after flash evaporation, and enters a rear polymerizer to further react after coming out of the front polymerizer, so that the melt viscosity meets the requirements of corresponding products.
In the traditional flash evaporator, a material coil is placed in biphenyl steam, the biphenyl steam heats the material, the temperature of the material is improved by about 30 ℃, and heat is provided for the gasification of moisture. The material coil mainly extends and makes a round trip to turn back along water flat line, and what adopt from entry end to exit end is step by step low arrangement, causes the material all to be in half a tub of state when the last one-level of pipeline very easily, has reduced effective heat transfer area, and heat exchange efficiency is low.
Due to the special properties of the nylon material, the retention time of the material in the flash evaporator can not exceed eight minutes in order to ensure the product quality; meanwhile, the average temperature difference between a heat carrier (diphenyl ether steam) for heating the materials and the materials is not more than 30 ℃, and the pressure of the materials needs to be reduced from 1.75-2.1MPa to normal pressure in the flash evaporation process. Meanwhile, considering the above-mentioned functions of temperature rise, evaporation, pressure reduction and transportation, the structure of the conventional flash evaporator needs to be made very long.
As the production capacity requirement of the production line is expanded and the demand of some special products is increased, higher requirements are put on the flash evaporator. For example, all the prior full-dull products are produced by using a batch device, the full-dull product needs to be injected with an aqueous solution containing 10 percent of titanium dioxide at the inlet of a flash evaporator, and the addition amount of the titanium dioxide is about 0.3 percent of the material flow, so that about 27 kilograms of water is needed to be added to each ton of the full-dull product. The added water must be completely evaporated by the corresponding heat provided by the flash evaporator, so that the heat consumption of the flash evaporator is greatly increased, and meanwhile, the corresponding heat can be provided only by enough area. If the productivity of the production line is increased to 10 ten thousand tons every year, the required heat exchange area is larger, the diameter of the heat exchange tube is larger, the length of the heat exchange tube is longer, the investment cost is increased, the occupation of a factory building is increased, and the arrangement of the production line is not facilitated.
The traditional front polymerizer and the traditional rear polymerizer both adopt vertical polymerization reaction kettles, the lower parts of the polymerizer and the front polymerizer are provided with stirrers in a screw and ribbon combined mode, ribbons mainly play a wall-hanging role, screws play a role in assisting in conveying materials left and right, and the materials are in a fully-mixed state in the polymerizer due to the stirring of the ribbons. The nylon polymerization belongs to gradual polymerization, along with the reaction, the molecular chain of the material is gradually lengthened, the viscosity is improved, and the product quality is correspondingly improved. The vertical type full mixing kettle cannot ensure the first-in first-out of materials, and cannot ensure the uniform molecular weight distribution of the materials at the outlet of the front polymerization, so that the requirements of civil yarns or products with high-end requirements are difficult to meet.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to overcome the problem that exists among the prior art, provide an evaporation polymerization device of nylon salt solution, material molecular weight distributes evenly, can increase substantially product quality, can satisfy the product requirement of direct spinning civilian long filament, engineering plastics and industrial yarn simultaneously.
In order to solve the technical problem, the utility model discloses an evaporative polymerization device of nylon salt solution, including the flash vessel, the export of dehydration salt solution pipe and additive injection pipe links to each other with the material entry of flash vessel jointly, the material export of flash vessel links to each other with flash distillation discharging pipe, the export of flash distillation discharging pipe links to each other with vapour and liquid separator's feed inlet, vapour and liquid separator's bottom export links to each other with horizontal disc reactor's feed inlet, horizontal disc reactor's discharge gate links to each other with the entry of polymer material delivery pump one, the export of polymer material delivery pump one links to each other with pelleter one and spinning civilian silk equipment; the outlet of the first polymer material conveying pump is also connected with the feed inlet of the vertical polymerization reaction kettle through a post-polymerization feed pipe, the discharge outlet at the lower end of the vertical polymerization reaction kettle is connected with the inlet of a second polymer material conveying pump, and the outlet of the second polymer material conveying pump is connected with a second granulator and industrial yarn spinning equipment.
Compared with the prior art, the utility model discloses following beneficial effect has been obtained: after being discharged from an outlet pipe of the concentration tank, the concentrated nylon salt solution firstly enters a U-shaped pipe reactor for further dehydration, and simultaneously certain polymerization reaction is completed under the pressure of 1.75-2.1MPa, the molecular weight of the material at the outlet of the U-shaped pipe reactor can reach 5000, and the temperature is 240-270 ℃; conveying the dehydrated nylon salt solution into a material inlet of a flash evaporator through a dehydrated salt solution pipe, simultaneously injecting an aqueous solution containing 10% of titanium dioxide into the material inlet of the flash evaporator from an additive injection pipe, wherein the addition amount of the titanium dioxide is about 0.3% wt of the material flow, and the material entering the flash evaporator contains 10% of free water; evaporating all free water by a flash evaporator, only using water generated by polymerization reaction, and reducing the pressure to normal pressure; the material flowing out of the flash evaporation discharging pipe enters a gas-liquid separator for gas-liquid separation, water in the material is discharged in advance, so that the efficiency of subsequent polymerization reaction is improved, the material is continuously heated while being separated, the polymerization reaction can be further carried out, the molecular weight of the material can reach 5000-10000, and the temperature is 270-285 ℃, so that the viscosity of the material is further improved; then the mixture enters a horizontal disc reactor for pre-polymerization reaction, so that a good film forming effect can be achieved, the reaction speed is improved, the disc stirring rotor has a propelling function, the materials can be guaranteed to be polymerized and propelled towards an outlet in a mode close to a plug flow, the first-in first-out of the materials is guaranteed, the molecular weight distribution of the materials at the outlet of the horizontal disc reactor is uniform, and the product quality is improved; the horizontal disc reactor adopts normal pressure reaction, and avoids the excessive small molecular oligomers carried by the front polymerization exhaust pipe. The pre-polymerization reaction material sent out by the first polymer material conveying pump has the molecular weight of 10000-14500 and the temperature of 270-285 ℃, is cut into particles by a granulator, and is used as a raw material for spinning civil filaments, or directly enters equipment for spinning civil filaments for spinning. The pre-polymerization reaction material can also enter a vertical polymerization reaction kettle for further polymerization to reach higher viscosity, and the post-polymerization reaction material at the outlet of the vertical polymerization reaction kettle is sent out by a second polymer material conveying pump, the molecular weight can reach 14500-16500, and the temperature is 270-285 ℃; and cutting the mixture into granules by a second granulator to be used as a raw material of engineering plastics. The molecular weight of post-polymerization reaction materials can reach 18500-20000, the temperature is 270-285 ℃, the temperature is normal pressure, and the materials are used as raw materials of industrial yarn spinning after being granulated by a granulator II or directly enter industrial yarn spinning equipment for spinning. The residence time in the vertical polymerization reaction kettle is only a few minutes, so the process requirements can be met by adopting the vertical full-mixing kettle, and the vertical polymerization kettle is relatively simple in design and manufacture and low in cost.
As an improvement of the utility model, the flash evaporator comprises a horizontal flash evaporator barrel, a material inlet of the flash evaporator is also connected with an outlet of an additive injection pipe, a biphenyl steam inlet and a biphenyl condensate reflux port are arranged at the bottom of the flash evaporator barrel, the biphenyl condensate reflux port is connected with an inlet of the biphenyl evaporator through a biphenyl reflux pipe, and an outlet of the biphenyl evaporator is connected with the biphenyl steam inlet through a biphenyl steam pipe; the inner cavity of the flash evaporator barrel is provided with a spiral coil which is coaxial with the flash evaporator barrel, the spiral coil comprises a small-diameter spiral coil, a medium-diameter spiral coil and a large-diameter spiral coil which are sequentially connected in series through an expanding joint, fins are arranged on the periphery of the spiral coil, the inlet end of the small-diameter spiral coil extends out of the end socket at one end of the flash evaporator barrel to serve as a material inlet of the flash evaporator, and the outlet end of the large-diameter spiral coil extends out of the end socket at the other end of the flash evaporator barrel to serve as a material outlet of the flash evaporator. The material advances along the spiral coil pipe in the flash evaporator, biphenyl steam at the outlet of the biphenyl evaporator enters a biphenyl steam inlet at the bottom of the cylinder body of the flash evaporator through a biphenyl steam pipe to heat the material so as to evaporate water, and condensed biphenyl is discharged from a biphenyl condensate reflux port and returns to the biphenyl evaporator through a biphenyl reflux pipe to be circularly heated. The material flows through the small-diameter spiral coil pipe to be heated, enters the medium-diameter spiral coil pipe through the first expanding joint to be heated and evaporated, and the pressure of the material is reduced along with the increase of the pipe diameter and the evaporation of water; and then the material enters the large-diameter spiral coil through the second expanding joint to be continuously heated and evaporated, and is discharged from the outlet end of the large-diameter spiral coil after the material is reduced to normal pressure along with the re-increase of the pipe diameter and the continuous evaporation of moisture. Because the material advances along the horizontal spiral coil of axis, most pipeline is in being full of the state in the spiral coil, has increased effective heat transfer area, and the fin of spiral coil periphery has further increased heat transfer area, has improved heat transfer efficiency greatly, under the condition that does not increase flash vessel length, can satisfy the big evaporation capacity demand of full extinction product.
As a further improvement, the top of the flash evaporator barrel is provided with a flash evaporator pressure detection port, a flash evaporator temperature detection port, a flash evaporator safety valve port and a flash evaporator exhaust port.
As a further improvement of the utility model, the outlet of the flash evaporation discharge pipe is inserted into the liquid phase space of the gas-liquid separator, the gas outlets of the gas-liquid separator and the horizontal disc reactor are connected with the inlet of the first spray tank through the front polymerization exhaust pipe, and the gas outlet of the first spray tank is connected with the tail gas treatment system; the outlet of the post-polymerization feeding pipe is inserted into the liquid phase space of the vertical polymerization reaction kettle, the exhaust port of the vertical polymerization reaction kettle is connected with the inlet of the second spraying tank through the post-polymerization exhaust pipe, the exhaust port of the second spraying tank is connected with a vacuum system, and the exhaust port of the vacuum system is connected with a tail gas treatment system. The feeding material directly enters the liquid phase space, the distance between the feeding material and the exhaust port is increased, the entrainment of internal materials during exhaust can be reduced, the horizontal disc reactor adopts normal pressure reaction, and the excessive small molecular oligomers entrained by the front polymerization exhaust pipe are avoided; because the molecular weight in the vertical polymerization reaction kettle is larger, materials are not easy to be carried, and the post polymerization is reacted in a vacuum state, so that the reaction speed is accelerated.
As the utility model discloses a further improvement, the export of preceding polymerization heat medium circulating pump links to each other through the cover heat medium entry that presss from both sides of preceding polymerization heat medium supply pipe and horizontal disc reactor bottom, and the cover heat medium export that presss from both sides at horizontal disc reactor top passes through heat medium communicating pipe and links to each other with the cover heat medium entry that presss from both sides of vapour and liquid separator bottom, and the cover heat medium export at vapour and liquid separator top pass through preceding polymerization heat medium back flow with the entry of preceding polymerization heat medium circulating pump links to each other. High-temperature heat conducting oil is sent out by a front polymerization heat medium circulating pump, enters the bottom of a jacket of the horizontal disc reactor through a front polymerization heat medium supply pipe, advances from the discharge port end of the horizontal disc reactor to the feed port end along the jacket space, then flows out from the top of the jacket at the feed port end of the horizontal disc reactor, enters the bottom of the jacket of the gas-liquid separator through a heat medium communicating pipe, is discharged from the top of the jacket of the gas-liquid separator, and returns to the front polymerization heat medium circulating pump for circulation through a front polymerization heat medium return pipe.
As a further improvement of the utility model, the export of postpolymerization heat medium circulating pump links to each other through the clamp cover heat medium entry of postpolymerization heat medium supply pipe and vertical polymerization cauldron bottom, the clamp cover heat medium export at vertical polymerization cauldron top through postpolymerization heat medium back flow with the entry of postpolymerization heat medium circulating pump links to each other. The high-temperature heat conducting oil is sent out by the post-polymerization heat medium circulating pump, enters the bottom of a jacket of the vertical polymerization reaction kettle through the post-polymerization heat medium supply pipe, moves forwards from the lower end of the vertical polymerization reaction kettle to the upper end along the jacket space, then flows out from the top of the jacket at the upper end of the vertical polymerization reaction kettle, and the high-temperature heat conducting oil can be supplemented into an inlet of the post-polymerization heat medium circulating pump.
Drawings
The invention will be described in further detail with reference to the drawings and the detailed description, which are provided for reference and illustration purposes only and are not intended to limit the invention.
FIG. 1 is a flow chart of the nylon salt solution evaporation polymerization device of the present invention.
Fig. 2 is an enlarged view of the flash evaporator of fig. 1.
In the figure: 1. a flash evaporator; 1a, a small-diameter spiral coil; 1b, expanding the first joint; 1c, a medium-diameter spiral coil; 1d, expanding a second connector; 1e, a large-diameter spiral coil pipe; 1f, a biphenyl steam inlet; 1g, a biphenyl condensate reflux port; 1h, a flash evaporator pressure detection port; 1j, a flash evaporator temperature detection port; 1k, a flash evaporator safety valve port; 1m. flash evaporator exhaust port; 2. a biphenyl evaporator; 3. a gas-liquid separator; 4. a horizontal disc reactor; 5. a vertical polymerization reactor; 6. a first granulator; 7. spinning civil silk equipment; 8. a first spraying tank; 9. a second granulator; 10. spinning industrial yarn equipment; 11. a second spraying tank; 12. a vacuum system; 13. a tail gas treatment system; G1. a dewatering saline solution pipe; G2. an additive injection tube; G3. a flash evaporation discharge pipe; G4. a post-polymerization feed pipe; g5a. a pre-polymerization heat medium supply pipe; g5b. a heating medium communicating pipe; g5c. a pre-polymerization heat medium reflux pipe; g6a. a postpolymerization heat medium supply pipe; g6b. a post-polymerization heat medium reflux pipe; B1. a first polymer material conveying pump; B2. a second polymer material conveying pump; B3. a pre-polymerization heat medium circulating pump; B4. and a post-polymerization heat medium circulating pump.
Detailed Description
As shown in figure 1 and figure 2, the nylon salt solution evaporation polymerization device of the present invention comprises a flash evaporator 1, a horizontal disc reactor 4 and a vertical polymerization reactor 5, wherein the outlet of a dehydrated salt solution pipe G1 and an additive injection pipe G2 are connected with the material inlet of the flash evaporator 1. The flash evaporator 1 comprises a horizontal flash evaporator cylinder, a material inlet of the flash evaporator 1 is also connected with an outlet of an additive injection pipe G2, a biphenyl steam inlet 1f and a biphenyl condensate reflux port 1G are arranged at the bottom of the flash evaporator cylinder, the biphenyl condensate reflux port 1G is connected with an inlet of the biphenyl evaporator 2 through a biphenyl reflux pipe, and an outlet of the biphenyl evaporator 2 is connected with the biphenyl steam inlet 1f through a biphenyl steam pipe; the inner cavity of the flash evaporator barrel is provided with a spiral coil which is coaxial with the flash evaporator barrel, the spiral coil comprises a small-diameter spiral coil 1a, a medium-diameter spiral coil 1c and a large-diameter spiral coil 1e which are sequentially connected in series through an expanding joint, fins are arranged on the periphery of each spiral coil, the inlet end of each small-diameter spiral coil 1a extends out of a seal head at one end of the flash evaporator barrel to serve as a material inlet of the flash evaporator 1, and the outlet end of each large-diameter spiral coil 1e extends out of a seal head at the other end of the flash evaporator barrel to serve as a material outlet of the flash evaporator 1.
The top of the flash evaporator barrel is provided with a flash evaporator pressure detection port 1h, a flash evaporator temperature detection port 1j, a flash evaporator safety valve port 1k and a flash evaporator exhaust port 1m.
A material outlet of the flash evaporator 1 is connected with a flash discharge pipe G3, an outlet of a flash discharge pipe G3 is connected with a feed inlet of a gas-liquid separator 3, an outlet at the bottom of the gas-liquid separator 3 is connected with a feed inlet of a horizontal disc reactor 4, a discharge outlet of the horizontal disc reactor 4 is connected with an inlet of a first polymer material conveying pump B1, and an outlet of the first polymer material conveying pump B1 is connected with a first granulator 6 and civil spinning silk equipment 7; the outlet of the first polymer material conveying pump B1 is also connected with the feed inlet of the vertical polymerization reaction kettle 5 through a post-polymerization feed pipe G4, the discharge outlet at the lower end of the vertical polymerization reaction kettle 5 is connected with the inlet of a second polymer material conveying pump B2, and the outlet of the second polymer material conveying pump B2 is connected with a second granulator 9 and industrial yarn spinning equipment 10.
After being discharged from an outlet pipe of the concentration tank, the concentrated nylon salt solution firstly enters a U-shaped pipe reactor for further dehydration, and simultaneously certain polymerization reaction is completed under the pressure of 1.75-2.1MPa, the molecular weight of the material at the outlet of the U-shaped pipe reactor can reach 5000, and the temperature is 240-270 ℃; the dehydrated nylon salt solution is sent into a material inlet of the flash evaporator 1 through a dehydrated salt solution pipe G1, aqueous solution containing 10 percent of titanium dioxide is simultaneously injected into the material inlet of the flash evaporator 1 from an additive injection pipe G2, the addition amount of the titanium dioxide is about 0.3 percent of the material flow, and the material entering the flash evaporator 1 contains 10 percent of free water; all free water is evaporated by the flash evaporator 1, only water generated by polymerization reaction is generated, and the pressure is reduced to normal pressure.
The material advances along the spiral coil pipe in flash vessel 1, and the biphenyl steam of biphenyl evaporator 2 export passes through the biphenyl steam pipe and gets into biphenyl steam inlet 1f at the flash vessel barrel bottom, heats the material and makes the moisture evaporate, and the biphenyl after the condensation is discharged from biphenyl condensate backward flow mouth 1g, gets back to biphenyl evaporator 2 through the biphenyl back flow and heats in circulation. The material firstly flows through the small-diameter spiral coil 1a to be heated, enters the medium-diameter spiral coil 1c through the first diameter-expanding joint 1b to be heated and evaporated, and the pressure of the material is reduced along with the increase of the pipe diameter and the evaporation of water; and then the material enters the large-diameter spiral coil 1e through the second expanding joint 1d to be continuously heated and evaporated, and the material is discharged from the outlet end of the large-diameter spiral coil 1e after being reduced to normal pressure along with the re-increase of the pipe diameter and the continuous evaporation of water. Because the material advances along the horizontal spiral coil of axis, most pipeline is in being full of the state in the spiral coil, has increased effective heat transfer area, and the fin of spiral coil periphery has further increased heat transfer area, has improved heat transfer efficiency greatly, under the condition that does not increase 1 length of flash vessel, can satisfy the big evaporation capacity demand of full extinction product.
The material flowing out of the flash evaporation discharging pipe G3 firstly enters a gas-liquid separator 3 for gas-liquid separation, water in the material is discharged in advance to improve the efficiency of subsequent polymerization reaction, the material is continuously heated while being separated, the polymerization reaction can be further carried out, the molecular weight of the material can reach 5000-10000, the temperature is 270-285 ℃, and the viscosity of the material is further improved; then the mixture enters a horizontal disc reactor 4 for pre-polymerization reaction, so that a good film forming effect can be achieved, the reaction speed is improved, the disc stirring rotor has a propelling function, the materials can be guaranteed to be polymerized and propelled towards an outlet in a mode close to a plug flow, the first-in first-out of the materials is guaranteed, the molecular weight distribution of the materials at the outlet of the horizontal disc reactor 4 is uniform, and the product quality is improved; the horizontal disc reactor 4 adopts normal pressure reaction to avoid excessive micromolecule oligomer carried by a front polymerization exhaust pipe. The pre-polymerization reaction material sent out by a polymer material conveying pump I B1 has the molecular weight of 10000-14500 and the temperature of 270-285 ℃, is cut into particles by a granulator I6 and then is used as a raw material for spinning civil filaments, or directly enters a civil filament spinning device 7 for spinning.
The pre-polymerization reaction material can also enter a vertical polymerization reaction kettle 5 for further polymerization to achieve higher viscosity, the post-polymerization reaction material at the outlet of the vertical polymerization reaction kettle 5 is sent out by a polymer material conveying pump II B2, the molecular weight can reach 14500-16500, the temperature is 270-285 ℃, the pressure is normal, and the post-polymerization reaction material is cut into granules by a granulator II 9 and then is used as the raw material of engineering plastics. The post-polymerization reaction material with the molecular weight of 18500-20000 and the temperature of 270-285 ℃ and normal pressure can be used as the raw material of the industrial yarn after being granulated by the second granulator 9 or directly enter the industrial yarn spinning equipment 10 for spinning.
An outlet of the flash evaporation discharge pipe is inserted into a liquid phase space of the gas-liquid separator 3, exhaust ports of the gas-liquid separator 3 and the horizontal disc reactor 4 are connected with an inlet of the first spray tank 8 through a front polymerization exhaust pipe, and an exhaust port of the first spray tank 8 is connected with a tail gas treatment system 13; the outlet of the post-polymerization feeding pipe is inserted into the liquid phase space of the vertical polymerization reaction kettle 5, the exhaust port of the vertical polymerization reaction kettle 5 is connected with the inlet of the second spraying tank 11 through the post-polymerization exhaust pipe, the exhaust port of the second spraying tank 11 is connected with the vacuum system 12, and the exhaust port of the vacuum system 12 is connected with the tail gas treatment system 13. The feeding material directly enters the liquid phase space, the distance between the feeding material and the exhaust port is increased, the entrainment of internal materials during exhaust can be reduced, and the horizontal disc reactor 4 adopts normal pressure reaction to avoid excessive micromolecule oligomers entrained by a front polymerization exhaust pipe; because the molecular weight in the vertical polymerization reaction kettle 5 is larger, materials are not easy to be carried, and the post polymerization is reacted in a vacuum state, so that the reaction speed is accelerated.
An outlet of the pre-polymerization heat medium circulating pump B3 is connected to a jacket heat medium inlet at the bottom of the horizontal disc reactor 4 through a pre-polymerization heat medium supply pipe G5a, a jacket heat medium outlet at the top of the horizontal disc reactor 4 is connected to a jacket heat medium inlet at the bottom of the gas-liquid separator 3 through a heat medium communicating pipe G5B, and a jacket heat medium outlet at the top of the gas-liquid separator 3 is connected to an inlet of the pre-polymerization heat medium circulating pump B3 through a pre-polymerization heat medium return pipe G5c. High-temperature heat conducting oil is sent out by a front polymerization heat medium circulating pump B3, enters the bottom of a jacket of the horizontal disc reactor 4 through a front polymerization heat medium supply pipe G5a, advances from the discharge port end of the horizontal disc reactor 4 to the feed port end along the jacket space, then flows out from the top of the jacket of the feed port end of the horizontal disc reactor 4, enters the bottom of the jacket of the gas-liquid separator 3 through a heat medium communicating pipe G5B, is discharged from the top of the jacket of the gas-liquid separator 3, and returns to the front polymerization heat medium circulating pump B3 through a front polymerization heat medium return pipe G5c for circulation, so that the high-temperature heat conducting oil discharged by the horizontal disc reactor 4 is used as a heat source of the gas-liquid separator 3 to realize series circulation, the heat efficiency can be improved, and the high-temperature heat conducting oil can be supplemented.
An outlet of the post-polymerization heat medium circulating pump B4 is connected to a jacket heat medium inlet at the bottom of the vertical polymerization reactor 5 through a post-polymerization heat medium supply pipe G6a, and a jacket heat medium outlet at the top of the vertical polymerization reactor 5 is connected to an inlet of the post-polymerization heat medium circulating pump B4 through a post-polymerization heat medium return pipe G6B. The high-temperature heat conducting oil is sent out by a post-polymerization heat medium circulating pump B4, enters the bottom of a jacket of the vertical polymerization reaction kettle 5 through a post-polymerization heat medium supply pipe G6a, advances from the lower end of the vertical polymerization reaction kettle 5 to the upper end along the jacket space, then flows out from the top of the jacket at the upper end of the vertical polymerization reaction kettle 5, and the high-temperature heat conducting oil can be supplemented into an inlet of a post-polymerization heat medium circulating pump B4.
The above description is only a preferred embodiment of the present invention, and not intended to limit the scope of the present invention. In addition to the above embodiments, the present invention can also have other embodiments, and all technical solutions formed by equivalent replacement or equivalent transformation fall within the protection scope of the present invention. The undescribed technical features of the present invention can be realized by or using the prior art, and are not described herein again.
Claims (6)
1. The utility model provides an evaporation polymerization facility of nylon salt solution, includes the flash vessel, and the export of dehydration salt solution pipe and additive injection pipe is continuous with the material entry of flash vessel jointly, its characterized in that: the material outlet of the flash evaporator is connected with a flash evaporation discharging pipe, the outlet of the flash evaporation discharging pipe is connected with the feed inlet of a gas-liquid separator, the bottom outlet of the gas-liquid separator is connected with the feed inlet of a horizontal disc reactor, the discharge outlet of the horizontal disc reactor is connected with the inlet of a first polymer material conveying pump, and the outlet of the first polymer material conveying pump is connected with a first granulator and civil spinning silk equipment; the outlet of the first polymer material conveying pump is also connected with the feed inlet of the vertical polymerization reaction kettle through a post-polymerization feed pipe, the discharge outlet at the lower end of the vertical polymerization reaction kettle is connected with the inlet of a second polymer material conveying pump, and the outlet of the second polymer material conveying pump is connected with a second granulator and industrial yarn spinning equipment.
2. The apparatus for the evaporative polymerization of nylon salt solution as set forth in claim 1, wherein: the flash evaporator comprises a horizontal flash evaporator cylinder, a material inlet of the flash evaporator is also connected with an outlet of the additive injection pipe, a biphenyl steam inlet and a biphenyl condensate reflux port are arranged at the bottom of the flash evaporator cylinder, the biphenyl condensate reflux port is connected with an inlet of the biphenyl evaporator through a biphenyl reflux pipe, and an outlet of the biphenyl evaporator is connected with the biphenyl steam inlet through a biphenyl steam pipe; the inner cavity of the flash evaporator barrel is provided with a spiral coil which is coaxial with the flash evaporator barrel, the spiral coil comprises a small-diameter spiral coil, a medium-diameter spiral coil and a large-diameter spiral coil which are sequentially connected in series through an expanding joint, fins are arranged on the periphery of the spiral coil, the inlet end of the small-diameter spiral coil extends out of the end socket at one end of the flash evaporator barrel to serve as a material inlet of the flash evaporator, and the outlet end of the large-diameter spiral coil extends out of the end socket at the other end of the flash evaporator barrel to serve as a material outlet of the flash evaporator.
3. The apparatus for the evaporative polymerization of nylon salt solution as set forth in claim 2, wherein: the top of the flash evaporator barrel is provided with a flash evaporator pressure detection port, a flash evaporator temperature detection port, a flash evaporator safety valve port and a flash evaporator exhaust port.
4. The apparatus for the evaporative polymerization of nylon salt solution as set forth in claim 1, wherein: an outlet of the flash evaporation discharge pipe is inserted into a liquid phase space of a gas-liquid separator, exhaust ports of the gas-liquid separator and the horizontal disc reactor are connected with an inlet of a first spraying tank through a front polymerization exhaust pipe, and the exhaust port of the first spraying tank is connected with a tail gas treatment system; the outlet of the post-polymerization feeding pipe is inserted into the liquid phase space of the vertical polymerization reaction kettle, the exhaust port of the vertical polymerization reaction kettle is connected with the inlet of the second spraying tank through the post-polymerization exhaust pipe, the exhaust port of the second spraying tank is connected with a vacuum system, and the exhaust port of the vacuum system is connected with a tail gas treatment system.
5. The apparatus for the evaporative polymerization of nylon salt solution as set forth in claim 1, wherein: an outlet of the pre-polymerization heat medium circulating pump is connected with a jacket heat medium inlet at the bottom of the horizontal disc reactor through a pre-polymerization heat medium supply pipe, a jacket heat medium outlet at the top of the horizontal disc reactor is connected with a jacket heat medium inlet at the bottom of the gas-liquid separator through a heat medium communicating pipe, and a jacket heat medium outlet at the top of the gas-liquid separator is connected with an inlet of the pre-polymerization heat medium circulating pump through a pre-polymerization heat medium return pipe.
6. The apparatus for the evaporative polymerization of nylon salt solution as set forth in claim 1, wherein: the outlet of the post-polymerization heat medium circulating pump is connected with the jacket heat medium inlet at the bottom of the vertical polymerization reaction kettle through a post-polymerization heat medium supply pipe, and the jacket heat medium outlet at the top of the vertical polymerization reaction kettle is connected with the inlet of the post-polymerization heat medium circulating pump through a post-polymerization heat medium return pipe.
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| CN202020662384.4U CN212174854U (en) | 2020-04-27 | 2020-04-27 | Nylon salt solution evaporation polymerization device |
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| CN202020662384.4U CN212174854U (en) | 2020-04-27 | 2020-04-27 | Nylon salt solution evaporation polymerization device |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114917856A (en) * | 2022-05-31 | 2022-08-19 | 中国五环工程有限公司 | Process system and method for preparing nylon 11 by polymerizing 11-aminoundecanoic acid |
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2020
- 2020-04-27 CN CN202020662384.4U patent/CN212174854U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114917856A (en) * | 2022-05-31 | 2022-08-19 | 中国五环工程有限公司 | Process system and method for preparing nylon 11 by polymerizing 11-aminoundecanoic acid |
| CN114917856B (en) * | 2022-05-31 | 2023-12-19 | 中国五环工程有限公司 | Process system and method for preparing nylon 11 by polymerizing 11-aminoundecanoic acid |
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