CN213790086U

CN213790086U - Hydrolysate loop line separator

Info

Publication number: CN213790086U
Application number: CN202022217529.2U
Authority: CN
Inventors: 刘成彬; 汪令杰; 蔺成波; 官伟; 马波; 王德明; 范明; 兰永平
Original assignee: Hesheng Silicon Industry Zhangzhou Co ltd
Current assignee: Hesheng Silicon Industry Zhangzhou Co ltd
Priority date: 2020-09-30
Filing date: 2020-09-30
Publication date: 2021-07-27
Anticipated expiration: 2030-09-30

Abstract

The utility model discloses a hydrolysate loop line separator, including the hydrolysate storage tank, the hydrolysate storage tank passes through the charge pump and is connected with phase separator one end, the phase separator lower extreme is connected with the aqueous phase collecting vat, the phase separator upper end is connected with the pre-heater, the pre-heater is connected with falling film evaporator top one side, falling film evaporator lower extreme is connected with the line body buffer tank, falling film evaporator and line body buffer tank all are connected with the ring body condenser, the ring body condenser is connected with the ring body buffer tank, the ring body buffer tank adopts the pump to be connected with the ring body groove through the ring body, line body buffer tank lower extreme is connected with line body condenser through line body extraction pump, line body condenser is connected with the line body groove. The device of the utility model is simple in structure, convenient to use can carry out the dewatering desalination and the loop separation of hydrolysate fast, has effectively solved among the prior art longer, the yield is lower and manufacturing cost is higher scheduling problem, convenient to popularize and use of separating the required time.

Description

Hydrolysate loop line separator

Technical Field

The utility model belongs to the technical field of the hydrolysate separation, concretely relates to hydrolysate loop line separator.

Background

Currently, dimethyldichlorosilance undergoes saturated acid hydrolysis, and undergoes further condensation reaction with itself or with each other to obtain a hydrolysate, wherein the hydrolysate contains about 30% of cyclosiloxane and about 70% of linear polysiloxane. The hydrolysate is directly used for producing 107 silicon rubber, because the ring opening of the ring body is difficult under the condition of water, the reaction yield is low, the ring body is recycled after the ring body is removed, and the recycling cost is high; the 110 methyl vinyl silicone rubber is produced by reacting the linear body in the hydrolysate through a cracking device to generate cyclosiloxane, and the cyclosiloxane is purified through a rectifying device and can be used as a raw material for producing the 110 methyl vinyl silicone rubber, so that the cracking production device is added, and the production cost is lowered. In order to save cost, the line body and the ring body in the hydrolysate need to be separated to be made into different products. The hydrolysate after the dimethyl hydrolysis is subjected to secondary water washing, secondary alkali washing and primary water washing contains water and salt, so that the quality of the hydrolysate is influenced. If the salinity of the water is higher, the problems of low polymerization yield of the hydrolysate, wide molecular weight distribution, unstable viscosity, unqualified light transmittance and the like can be caused, and in order to avoid the influence on the product quality, the hydrolysate needs to be subjected to long-time sedimentation separation to separate the water and the salinity, so that the exertion of the productivity is restricted to a certain extent. There is a need for a device for rapidly removing water and salt from hydrolysate and then separating the loop.

SUMMERY OF THE UTILITY MODEL

In view of the above, the utility model provides a hydrolysate loop separation device, device simple structure, convenient to use can carry out the dewatering desalination and the loop separation of hydrolysate fast, has effectively solved among the prior art longer, the yield is lower and manufacturing cost is higher scheduling problem, convenient to popularize and use.

In order to achieve the above object, the present invention provides a technical solution for solving the technical problem: the utility model provides a hydrolysate loop line separator, including the hydrolysate storage tank, the hydrolysate storage tank passes through the charge pump and is connected with phase separator one end, the phase separator lower extreme is connected with the aqueous phase collecting vat, the phase separator upper end is connected with the pre-heater, the pre-heater is connected with falling film evaporator top one side, falling film evaporator lower extreme is connected with the line buffer tank, falling film evaporator and line buffer tank all are connected with the ring body condenser, the ring body condenser is connected with the ring body buffer tank, the ring body buffer tank is connected with the ring body groove through ring body extraction pump, line body buffer tank lower extreme is connected with the line body condenser through line body extraction pump, the line body condenser is connected with the line body groove.

The utility model has the advantages that: when the hydrolysate is separated in a loop, the hydrolysate in the hydrolysate storage tank enters a phase separator through a feed pump, oil and water are quickly separated in a phase separator with high precision, the recombined water is discharged into a water phase collecting tank from the lower end of the phase separator, discharging the light component hydrolysate from the upper end of the phase separator to a preheater for preheating, wherein the temperature of a discharge port of the preheater is 150-160 ℃, heating the hydrolysate after preheating hydrolysis in a falling film evaporator, then carrying out loop-line separation in a line buffer tank under the vacuum degree of-94 to-100 KPa and the temperature of 150-170 ℃, condensing the gas phase loop materials in the falling film evaporator and the line buffer tank and circulating water in a loop condenser, then the condensate enters a ring body buffer tank, and is extracted into a ring body groove under the condition that the liquid level of the ring body buffer tank is about 50 percent through liquid level regulation by a ring body extraction pump; and the line buffer tank continuously extracts the liquid by a line extraction pump under the condition that the liquid level is 50-60%, and conveys the liquid into a line groove after being cooled by a line condenser. The device needs shorter time for carrying out hydrolysate loop separation, and the phase separator can remove most of water in the hydrolysate, so that the content of the hydrolysate is controlled within 0.1%; during the loop separation, the saturated vapor pressure difference of the loop body and the wire body is utilized, the preheated hydrolysate passes through a falling film evaporator and flows from top to bottom in a uniform film shape under the action of gravity, vacuum induction and airflow, cyclosiloxane is heated and vaporized by a heating medium in the flowing process, the generated vapor is separated from liquidus siloxane together, the wire body and the loop body in the hydrolysate are effectively separated, the separated alkylene oxide of the wire body can be directly used for producing 107 silicon rubber, the generation of low molecules is reduced, the product yield is improved, the cyclosiloxane can be directly sent to a rectification system for purification, the load of a cracking system is reduced, the production cost is effectively reduced, the yield is higher, the application prospect is better, and the popularization and the use are convenient. After the hydrolysate is separated by the device, the water content in the hydrolysate can be reduced to be below 0.1 percent, the sedimentation and drainage processes of the hydrolysate are reduced, the light transmittance of the hydrolysate can reach more than 90 percent required by 107 collagen materials, and the quality of a final product is not influenced; before treatment, the siloxane content in the hydrolysate is about 70%, and after treatment by the device, the siloxane content in the hydrolysate can be increased to more than 95%, so that the yield of the product is greatly improved.

Further, the other end of the top of the falling film evaporator is connected with a steam pipeline.

The beneficial effect of adopting the further scheme is that: the hydrolysate is heated by introducing steam into the falling film evaporator through the steam pipeline, so that the heating is convenient.

Further, a tail gas absorption system is arranged on one side of the ring body condenser.

The beneficial effect of adopting the further scheme is that: gas phase ring materials in the falling film evaporator and the line buffer tank are condensed with circulating water in the ring condenser, non-condensable gas and a small part of condensable gas are absorbed by a tail gas absorption system and the condensable gas is absorbed by a high ring, and the non-condensable gas is discharged into the atmosphere through a vacuum pump.

Further, the inlet and outlet communicating valve is opened to half when the ring body buffer tank and the wire body buffer tank are started.

The beneficial effect of adopting the further scheme is that: prevent that ring body buffer tank and line body buffer tank liquid level are low, do not produce and lead to the pump to suppress pressure, influence the use of device and going on of subsequent handling.

Drawings

FIG. 1 is a schematic view of the present invention;

wherein, 1, a hydrolysate storage tank; 2. a feed pump; 3. a phase separator; 4. a water phase collecting tank; 5. a preheater; 6. a falling film evaporator; 7. a line body buffer tank; 8. a line extraction pump; 9. a line condenser; 10. a wire body groove; 11. a loop condenser; 12. a ring buffer tank; 13. a ring extraction pump; 14. a ring body groove.

Detailed Description

The following detailed description of the embodiments of the present invention will be made with reference to the accompanying drawings.

The utility model discloses an embodiment, as shown in FIG. 1, a hydrolysate loop line separator is provided, including hydrolysate storage tank 1, hydrolysate storage tank 1 passes through charge pump 2 and is connected with 3 one ends of phase separator, 3 lower extremes of phase separator are connected with aqueous

phase collecting vat

4, 3 upper ends of phase separator are connected with pre-heater 5, pre-heater 5 is connected with 6 top one sides of falling film evaporator, 6 lower extremes of falling film evaporator are connected with line buffer tank 7, falling film evaporator 6 and line buffer tank 7 all are connected with ring body condenser 11, ring body condenser 11 is connected with ring body buffer tank 12, ring body buffer tank 12 is connected with ring body 14 through ring

body extraction pump

13, 7 lower extremes of line body buffer tank are connected with line body condenser 9 through line body extraction pump 8, line body condenser 9 is connected with line body 10. When in use, hydrolysate in the hydrolysate storage tank 1 enters the phase separator 3 through the feed pump 2, oil and water are quickly separated in the phase separator 3 with high precision, heavy component water is discharged into the water phase collecting tank 4 from the lower end of the phase separator 3, light component hydrolysate is discharged into the preheater 5 from the upper end of the phase separator 3 for preheating, the temperature of a discharge port of the preheater 5 is 150-160 ℃, the hydrolysate after preheating hydrolysis enters the falling film evaporator 6 for heating, then loop separation is carried out in the line buffer tank 7 under the vacuum degree of-94 to-100 KPa and the temperature of 150-170 ℃, gas phase loop materials in the falling film evaporator 6 and the line buffer tank 7 are condensed with circulating water in the loop condenser 11, then the condensate enters the loop buffer tank 12, and the liquid level is adjusted by the loop extraction pump 13 under the condition that the liquid level of the loop buffer tank 12 is about 50 percent, withdrawn into the annulus 14; and the line buffer tank 7 continuously extracts the liquid by a line extraction pump 8 under the condition that the liquid level is 50-60%, and conveys the liquid into a line groove 10 after being cooled by a line condenser 9. The device needs shorter time for carrying out hydrolysate loop separation, and the phase separator 3 can remove most of water in the hydrolysate, so that the content of the hydrolysate is controlled within 0.1 percent; during the loop separation, by utilizing the difference of saturated vapor pressures of the loop body and the wire body, the preheated hydrolysate passes through the falling film evaporator 6 and flows from top to bottom in a uniform film shape under the action of gravity, vacuum induction and airflow, cyclosiloxane is heated and vaporized by a heating medium in the flowing process, the generated vapor is separated from liquid phase linear siloxane together, the wire body and the loop body in the hydrolysate are effectively separated, the separated wire body alkylene oxide can be directly used for producing 107 silicon rubber, the generation of low molecules is reduced, the product yield is improved, the cyclosiloxane can be directly sent to a rectification system for purification, the load of a cracking system is reduced, the production cost is effectively reduced, the yield is higher, the application prospect is better, and the popularization and the use are convenient. After the hydrolysate is separated by the device, the water content in the hydrolysate can be reduced to be below 0.1 percent, the sedimentation and drainage processes of the hydrolysate are reduced, the light transmittance of the hydrolysate can reach more than 90 percent required by 107 collagen materials, and the quality of a final product is not influenced; before treatment, the siloxane content in the hydrolysate is about 70%, and after treatment by the device, the siloxane content in the hydrolysate can be increased to more than 95%, so that the yield of the product is greatly improved.

The other end of the top of the falling film evaporator 6 is connected with a steam pipeline; and steam is introduced into the falling film evaporator 6 through a steam pipeline to heat the hydrolysate, so that the heating is convenient. A tail gas absorption system is arranged on one side of the ring body condenser 11; gas-phase ring materials in the falling film evaporator 6 and the line buffer tank 7 are condensed with circulating water in the ring condenser 11, non-condensable gas and a small part of condensable gas are absorbed by a tail gas absorption system and the condensable gas is absorbed by a high ring, and the non-condensable gas is discharged into the atmosphere through a vacuum pump. When the ring buffer tank 12 and the line buffer tank 7 are started, the inlet and outlet communicating valve is opened to a half; prevent that ring body buffer tank 12 and line body buffer tank 7 liquid level are low, do not produce and lead to the pump to suppress pressure, influence the use of device and going on of subsequent handling.

When the device is used, hydrolysate in a hydrolysate storage tank 1 enters a phase separator 3 through a feed pump 2, oil and water are quickly separated in the phase separator 3 at high precision, heavy component water is discharged into a water phase collecting tank 4 from the lower end of the phase separator 3, light component hydrolysate is discharged into a preheater 5 from the upper end of the phase separator 3 for preheating, the hydrolysate after preheating hydrolysis enters a falling film evaporator 6 for heating, then loop separation is carried out in a loop buffer tank 7, gas phase loop materials in the falling film evaporator 6 and the loop buffer tank 7 are condensed with circulating water in a loop condenser 11, then condensate enters a loop buffer tank 12, and is extracted into a loop tank 14 under the condition that the liquid level of the loop buffer tank 12 is about 50% through a loop extraction pump 13; and the line buffer tank 7 continuously extracts the liquid by a line extraction pump 8 under the condition that the liquid level is 50-60%, and conveys the liquid into a line groove 10 after being cooled by a line condenser 9. The device of the utility model is simple in structure, convenient to use can carry out the dewatering desalination and the loop separation of hydrolysate fast, has effectively solved among the prior art longer, the yield is lower and manufacturing cost is higher scheduling problem, convenient to popularize and use of separating the required time.

While the present invention has been described in detail and with reference to the accompanying drawings, it is not to be considered as limited to the scope of the invention. Various modifications and changes may be made by those skilled in the art without inventive step within the scope of the appended claims.

Claims

1. A hydrolysate loop separation device is characterized by comprising a hydrolysate storage tank (1), wherein the hydrolysate storage tank (1) is connected with one end of a phase separator (3) through a feeding pump (2), the lower end of the phase separator (3) is connected with a water phase collecting tank (4), the upper end of the phase separator (3) is connected with a preheater (5), the preheater (5) is connected with one side of the top of a falling film evaporator (6), the lower end of the falling film evaporator (6) is connected with a line buffer tank (7), the falling film evaporator (6) and the line buffer tank (7) are both connected with a loop condenser (11), the loop condenser (11) is connected with a loop buffer tank (12), the loop buffer tank (12) is connected with a loop tank (14) through a loop extraction pump (13), the lower end of the line buffer tank (7) is connected with a loop condenser (9) through a line extraction pump (8), the wire condenser (9) is connected with the wire groove (10).

2. The hydrolysate loop separation device according to claim 1, wherein the other end of the top of the falling film evaporator (6) is connected with a steam pipeline.

3. The hydrolysate loop separation device according to claim 1, wherein a tail gas absorption system is arranged at one side of the loop condenser (11).

4. The hydrolysate loop separation device according to claim 1, wherein the inlet and outlet communicating valve is opened to half when the loop body buffer tank (12) and the line body buffer tank (7) are started.