CN113827994A - Flash evaporation optimization method for polymerization powder - Google Patents
Flash evaporation optimization method for polymerization powder Download PDFInfo
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- CN113827994A CN113827994A CN202111130642.XA CN202111130642A CN113827994A CN 113827994 A CN113827994 A CN 113827994A CN 202111130642 A CN202111130642 A CN 202111130642A CN 113827994 A CN113827994 A CN 113827994A
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- vacuumizing
- vacuum pump
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- 238000001704 evaporation Methods 0.000 title claims abstract description 83
- 230000008020 evaporation Effects 0.000 title claims abstract description 83
- 239000000843 powder Substances 0.000 title claims abstract description 60
- 238000000034 method Methods 0.000 title claims abstract description 25
- 238000005457 optimization Methods 0.000 title claims abstract description 13
- 238000006116 polymerization reaction Methods 0.000 title claims description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 98
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims abstract description 53
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims abstract description 53
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 49
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 26
- 239000000463 material Substances 0.000 claims abstract description 18
- 229920000642 polymer Polymers 0.000 claims description 10
- 239000007789 gas Substances 0.000 claims description 9
- 238000005086 pumping Methods 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- 238000011084 recovery Methods 0.000 claims description 3
- 238000003860 storage Methods 0.000 claims description 3
- 238000002347 injection Methods 0.000 abstract 1
- 239000007924 injection Substances 0.000 abstract 1
- 239000004743 Polypropylene Substances 0.000 description 8
- -1 polypropylene Polymers 0.000 description 8
- 229920001155 polypropylene Polymers 0.000 description 8
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 238000006073 displacement reaction Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000010924 continuous production Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
Abstract
The invention discloses a flash evaporation optimization method of polymerized powder, which comprises the following steps of A, receiving and water feeding, B, propylene vacuumizing, C, steam pressurizing, D, steam vacuumizing, E, steam secondary pressurizing, F, steam vacuumizing, G, nitrogen injection flash evaporation, H, nitrogen vacuumizing, I, nitrogen pressurizing and conveying, J, nitrogen vacuumizing, after powder pressurizing and conveying are completed, nitrogen vacuumizing before receiving is started, a program control valve KV3307A is closed, a program control valve 330KV 3 3303A is opened, after a buffer tank D332 at the inlet of a nitrogen vacuum pump and a flash evaporation kettle R7002A are subjected to flat pressure, a program control valve HV3301B is closed, a nitrogen vacuum pump P306 vacuumizes a flash evaporation kettle R7002A, after vacuumizing is completed, a program control valve KV3303A is closed, a program control valve KV3308A is opened to receive materials, a program control valve KV3301A is opened to flat pressure, the warm water receiving process is repeated, the powder is fully contacted with powder for a long time, the temperature of the powder is ensured to be uniformly reduced in advance, and the upper part of the powder is not to be low, the lower part is at a high temperature, even with water. The material temperature can be flexibly adjusted.
Description
Technical Field
The invention relates to the technical field of polymer powder, in particular to a flash evaporation optimization method of polymer powder.
Background
At present, a polypropylene device (SPG continuous process) powder dryer and a flash evaporation kettle system have the following operation flow before modification.
The polypropylene powder falls by gravity to the dryer M301. The dryer M301 is a paddle feeder, steam is introduced into a hot shaft, a paddle and an equipment jacket to heat the powder, a small amount of direct steam is introduced into the dryer to further remove propylene gas in the powder, and the function of the dryer M301 is to further devolatilize the polypropylene powder, recover hydrocarbons as far as possible and reduce the content of hydrocarbons carried in the powder entering the flash evaporation kettle R7002 AB. M301 establishes a material seal through a dipleg, the material level is detected by an admittance installed on the dipleg, and the rotating speed of the rotary valve is controlled in cascade.
The polypropylene powder leaving the dryer falls to 2 displacement kettle flash evaporation kettles R7002AB which are connected in parallel and operated alternately in batches by virtue of gravity, the displacement kettle after receiving the materials is finished, propylene gas is firstly pumped out by a propylene vacuum pump P305AB, then steam and process water are introduced, the temperature of the polypropylene powder is reduced to about 70 ℃ by the gasification of the process water, hydrocarbons and moisture in the polypropylene powder are thoroughly removed by a nitrogen vacuum pump P306AB, then the polypropylene powder is conveyed to powder packaging by nitrogen pressure, a pressure conveying pipe is provided with a cooling water jacket, the polypropylene powder is continuously cooled in the pressure conveying process, and the following problems are easily caused in the design of the original scheme:
1) when receiving materials, because KV3308A and KV3301A are simultaneously opened, the negative pressure is pumped by a subsequent system, and great potential safety hazard exists.
2) In the flash evaporation process, the temperature of the powder is not easy to control, the blanking temperature of the originally designed dryer is 100 ℃, and the blanking temperature is controlled by the temperature of blanking-section jacket heat tracing steam, but in the flash evaporation process, because the steam and water are introduced after the vacuum pumping, the temperature is often lower, the powder carries water, and the powder temperature is higher (more than 70 ℃) due to the fact that the water is not introduced, so that potential safety hazards are caused.
3) The temperature of the powder is high, and the powder is cooled by circulating water in the back clamping sleeve, so that the effect is not good, and the energy consumption is high.
Disclosure of Invention
The present invention aims to provide a method for flash evaporation optimization of polymer powder to solve the problems mentioned in the background art.
In order to achieve the purpose, the invention is realized by the following technical scheme: a flash evaporation optimization method for polymerization powder comprises the following steps:
A. receiving and introducing water, feeding the powder into a flash evaporation kettle R7002A through a program control valve KV3308A, finishing time setting through the program control valve KV3301A after the pressure of the flash evaporation kettle is micro-positive, opening the flat pressure, sending propylene gas and water vapor in the powder to a C303 inlet cooler E303 through KV3301A, passing through a C303 inlet buffer tank D304, and pressurizing an external gas delivery branch or a spherical tank by a propylene recovery compressor C303;
B. vacuumizing for the first time, wherein a propylene vacuum pump P305 vacuumizes the flash kettle R7002A;
C. steam is pressurized, after the flash evaporation kettle R7002A is vacuumized, the program control valve KV3301A is closed, meanwhile, the program control valve HV3301A of the propylene vacuum pump inlet buffer tank D331 is opened, the propylene vacuum pump P305 continues to vacuumize, the program control valve KV3304A is opened, and low-pressure steam of 0.3MPa is used for pressurizing the flash evaporation kettle R7002A;
D. vacuumizing for the second time, wherein after the pressure of the flash evaporation kettle R7002A is slightly positive, the program control valve KV3304A is closed, the program control valve KV03301A is opened, and the flash evaporation kettle R7002A is vacuumized by the propylene vacuum pump P305;
E. steam secondary pressurizing, after secondary vacuum pumping of the flash evaporation kettle R7002A, closing the program control valve KV3301A, simultaneously opening the program control valve HV3301A of an inlet buffer tank D331 of the propylene vacuum pump, continuously vacuumizing the propylene vacuum pump P305, opening the program control valve KV3304A, and pressurizing the flash evaporation kettle R7002A by low-pressure steam of 0.3 MPa;
F. vacuumizing for the third time, wherein after the pressure of the flash evaporation kettle R7002A is slightly positive, the program control valve KV3304A is closed, the program control valve KV03301A is opened, and the flash evaporation kettle R7002A is vacuumized by the propylene vacuum pump P305;
G. injecting nitrogen for flash evaporation, after the flash evaporation kettle R7002A is vacuumized for the fourth time, closing the program control valve KV3301A, simultaneously opening the program control valve HV3301A of the propylene vacuum pump inlet buffer tank D331, continuously vacuumizing the propylene vacuum pump P305, opening the program control valve KV3305A, and pressurizing the flash evaporation kettle R7002A by pressurizing nitrogen at 0.5 MPa;
H. vacuumizing for the fourth time, wherein a nitrogen vacuum pump P306 is used for vacuumizing the flash kettle R7002A;
I. after the fifth vacuumizing is finished, closing the program control valve KV3303A, opening the program control valve KV3305A, simultaneously opening the program control valve HV3301B at the inlet of the nitrogen pump D332, continuously vacuumizing the nitrogen vacuum pump P306, pressurizing the flash evaporation kettle R7002A by compressed nitrogen, simultaneously opening the program control valve KV3307A, and conveying the powder to a storage bin;
J. and (4) performing the fifth vacuumizing, wherein after the pressure feeding of the powder is finished, the nitrogen vacuum pump P306 continues to perform the vacuumizing.
Optionally, in the step a, the first vacuum pumping is propylene vacuum pumping, after the flash evaporation kettle R7002A finishes receiving materials, the programmable valve KV3302A is opened, the programmable valve KV3308A and the programmable valve KV3301A are closed at the same time, and after the propylene vacuum pump inlet buffer tank D331 and the flash evaporation kettle R7002A are subjected to flat pressure, the programmable valve HV3301A is closed.
Optionally, in step D, the second evacuation is steam evacuation, and evacuation is performed after the pressure of the propylene vacuum pump inlet buffer tank D331 and the flash evaporation kettle R7002A is equalized, and the programmable valve HV3301A is closed.
Optionally, in step F, the third evacuation is steam evacuation, and after the pressure of the propylene vacuum pump inlet buffer tank D331 and the flash evaporation kettle R7002A is equalized, the programmable valve HV3301A is closed, and evacuation is performed.
Optionally, in the step H, the fourth evacuation is nitrogen evacuation, after the pressure of the flash evaporation kettle R7002A is slightly positive, the programmable valve KV3305A is closed, the programmable valve KV3303A is opened, and after the buffer tank D332 at the inlet of the nitrogen vacuum pump and the flash evaporation kettle R7002A are pressed flatly, the programmable valve HV3301B is closed to perform evacuation.
Optionally, in the step J, the fifth evacuation is nitrogen evacuation, nitrogen evacuation before material receiving is started, the programmable valve KV3307A is closed, the programmable valve KV3303A is opened, after the buffer tank D332 at the inlet of the nitrogen vacuum pump and the flash kettle R7002A are subjected to flat pressure, the programmable valve HV3301B is closed, the flash kettle R7002A is evacuated by the nitrogen vacuum pump P306, after the evacuation is completed, the programmable valve KV3303A is closed, the programmable valve KV3308A is opened for material receiving, the programmable valve KV3301A is opened for flat pressure, the material receiving process is repeated, and at the same time, the buffer tank D332 at the inlet of the propylene pump is opened, and the programmable valve HV3301B is opened for vacuum evacuation.
Optionally, an annular flow channel is additionally arranged at the discharging section of the dryer, and the mixture of the temperature-reducing water and the powder enters the flash evaporation kettle after being mixed through the flow channel. And then the temperature of the powder entering the flash evaporation kettle is controlled between 70 ℃ and 80 ℃ through the temperature reduction water quantity and the jacket heat tracing.
The invention has the technical effects and advantages that:
1. an annular flow passage is additionally arranged at the discharging section of the dryer, and the mixture of the temperature-reducing water and the powder enters the flash evaporation kettle after being mixed by the flow passage. And then the temperature of the powder entering the flash evaporation kettle is controlled between 70 ℃ and 80 ℃ through the temperature reduction water quantity and the jacket heat tracing.
2. Through the full contact of desuperheating water with the powder for a long time in advance, can guarantee that the powder temperature evenly descends, the upper portion temperature can not appear low, the lower part temperature is high, the condition of even taking water appears. The material temperature can be flexibly adjusted.
3. During subsequent flash evaporation, the steam is only used for adjusting the partial pressure of the hydrocarbons in the kettle, so that the flash evaporation effect can be greatly improved.
Drawings
FIG. 1 is a flow chart of the method of the present invention;
FIG. 2 is a schematic representation of a dryer dipleg of the present invention after modification;
FIG. 3 is a diagram showing the process steps and the valve open/close states in the normal production of the flash tank of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments.
The invention provides a method for flash evaporation optimization of polymer powder, which is shown in figures 1-3 and comprises the following steps:
A. receiving and introducing water, feeding the powder into a flash evaporation kettle R7002A through a program control valve KV3308A, finishing time setting after the pressure of the flash evaporation kettle is slightly positive through a program control valve KV3301A, opening the flat pressure, feeding propylene gas and water vapor in the powder into a C303 inlet cooler E303 through KV3301A, feeding the propylene gas and the water vapor into a C303 inlet buffer tank D304 through a C303 inlet, pressurizing an external gas delivery branch or a spherical tank through a propylene recovery compressor C303, additionally arranging an annular flow channel at a blanking section of a dryer, mixing the powder with desuperheating water from the flow channel, feeding the mixture into the flash evaporation kettle, and controlling the temperature of the powder in the flash evaporation kettle to be between 70 and 80 ℃ through desuperheating water quantity and jacket heat tracing.
B. And (3) vacuumizing propylene, opening the program control valve KV3302A after the flash evaporation kettle finishes receiving materials, and closing the program control valve KV3308A and the program control valve KV 3301A. After the pressure between the propylene vacuum pump inlet buffer tank D331 and the flash kettle R7002A is equalized, the programmable valve HV3301A is closed, and the propylene vacuum pump P305 vacuumizes the flash kettle R7002A.
C. And (3) pressurizing steam, closing the program control valve KV3301A after the flash evaporation kettle R7002A is vacuumized, simultaneously opening the program control valve HV3301A of an inlet buffer tank D331 of the propylene vacuum pump, continuously vacuumizing the propylene vacuum pump P305, opening the program control valve KV3304A, and pressurizing the flash evaporation kettle R7002A by low-pressure steam of 0.3 MPa.
D. And (3) steam vacuumizing, wherein after the pressure of the flash kettle R7002A is slightly positive, the programmable valve KV3304A is closed, the programmable valve KV03301A is opened, after the pressure of the propylene vacuum pump inlet buffer tank D331 and the flash kettle R7002A is equalized, the programmable valve HV3301A is closed, and the propylene vacuum pump P305 vacuumizes the flash kettle R7002A.
E. And (3) performing secondary steam pressurization, closing the program control valve KV3301A after the flash evaporation kettle R7002A is subjected to secondary vacuum pumping, simultaneously opening the program control valve HV3301A of an inlet buffer tank D331 of the propylene vacuum pump, continuously vacuumizing the propylene vacuum pump P305, opening the program control valve KV3304A, and pressurizing the flash evaporation kettle R7002A by using low-pressure steam of 0.3 MPa.
F. And (3) steam vacuumizing, wherein after the pressure of the flash kettle R7002A is slightly positive, the programmable valve KV3304A is closed, the programmable valve KV03301A is opened, after the pressure of the propylene vacuum pump inlet buffer tank D331 and the flash kettle R7002A is equalized, the programmable valve HV3301A is closed, and the propylene vacuum pump P305 vacuumizes the flash kettle R7002A.
G. And (3) injecting nitrogen for flash evaporation, after the flash evaporation kettle R7002A is vacuumized for the fourth time, closing the program control valve KV3301A, simultaneously opening the program control valve HV3301A of the propylene vacuum pump inlet buffer tank D331, continuously vacuumizing the propylene vacuum pump P305, opening the program control valve KV3305A, and pressurizing the flash evaporation kettle R7002A by pressurizing nitrogen at 0.5 MPa.
H. And (3) vacuumizing nitrogen, closing the programmable valve KV3305A and opening the programmable valve KV3303A after the pressure of the flash kettle R7002A is slightly positive, closing the programmable valve HV3301B after the buffer tank D332 at the inlet of the nitrogen vacuum pump is in flat pressure with the flash kettle R7002A, and vacuumizing the flash kettle R7002A by the nitrogen vacuum pump P306.
I. And (3) nitrogen pressure feeding, wherein after the fifth vacuumizing is completed, the program control valve KV3303A is closed, the program control valve KV3305A is opened, the program control valve HV3301B is opened at the same time of the buffer tank D332 at the inlet of the nitrogen pump, the nitrogen vacuum pump P306 continues to vacuumize, compressed nitrogen is used for pressurizing the flash evaporation kettle R7002A, the program control valve KV3307A is opened at the same time, and the powder is fed to the storage bin.
J. And (3) vacuumizing nitrogen, after the pressure feeding of the powder is finished, vacuumizing the nitrogen before receiving the powder, closing the programmable valve KV3307A, opening the programmable valve KV3303A, after the pressure between the buffer tank D332 at the inlet of the nitrogen vacuum pump and the flash kettle R7002A is equalized, closing the programmable valve HV3301B, and vacuumizing the flash kettle R7002A by the nitrogen vacuum pump P306. And after the vacuum pumping is finished, closing the programmable valve KV3303A, opening the programmable valve KV3308A for material receiving, opening the programmable valve KV3301A for flat pressure, repeating the material receiving process, simultaneously opening the programmable valve HV3301B of the propylene pump inlet buffer tank D332, and continuously vacuumizing the nitrogen vacuum pump P306.
Although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments or portions thereof without departing from the spirit and scope of the invention.
Claims (7)
1. A method for optimizing flash evaporation of polymerization powder is characterized by comprising the following steps:
A. receiving and introducing water, feeding the powder into a flash evaporation kettle R7002A through a program control valve KV3308A, finishing time setting through the program control valve KV3301A after the pressure of the flash evaporation kettle is micro-positive, opening the flat pressure, sending propylene gas and water vapor in the powder to a C303 inlet cooler E303 through KV3301A, passing through a C303 inlet buffer tank D304, and pressurizing an external gas delivery branch or a spherical tank by a propylene recovery compressor C303;
B. vacuumizing for the first time, wherein a propylene vacuum pump P305 vacuumizes the flash kettle R7002A;
C. steam is pressurized, after the flash evaporation kettle R7002A is vacuumized, the program control valve KV3301A is closed, meanwhile, the program control valve HV3301A of the propylene vacuum pump inlet buffer tank D331 is opened, the propylene vacuum pump P305 continues to vacuumize, the program control valve KV3304A is opened, and low-pressure steam of 0.3MPa is used for pressurizing the flash evaporation kettle R7002A;
D. vacuumizing for the second time, wherein after the pressure of the flash evaporation kettle R7002A is slightly positive, the program control valve KV3304A is closed, the program control valve KV03301A is opened, and the flash evaporation kettle R7002A is vacuumized by the propylene vacuum pump P305;
E. steam secondary pressurizing, after secondary vacuum pumping of the flash evaporation kettle R7002A, closing the program control valve KV3301A, simultaneously opening the program control valve HV3301A of an inlet buffer tank D331 of the propylene vacuum pump, continuously vacuumizing the propylene vacuum pump P305, opening the program control valve KV3304A, and pressurizing the flash evaporation kettle R7002A by low-pressure steam of 0.3 MPa;
F. vacuumizing for the third time, wherein after the pressure of the flash evaporation kettle R7002A is slightly positive, the program control valve KV3304A is closed, the program control valve KV03301A is opened, and the flash evaporation kettle R7002A is vacuumized by the propylene vacuum pump P305;
G. injecting nitrogen for flash evaporation, after the flash evaporation kettle R7002A is vacuumized for the fourth time, closing the program control valve KV3301A, simultaneously opening the program control valve HV3301A of the propylene vacuum pump inlet buffer tank D331, continuously vacuumizing the propylene vacuum pump P305, opening the program control valve KV3305A, and pressurizing the flash evaporation kettle R7002A by pressurizing nitrogen at 0.5 MPa;
H. vacuumizing for the fourth time, wherein a nitrogen vacuum pump P306 is used for vacuumizing the flash kettle R7002A;
I. after the fifth vacuumizing is finished, closing the program control valve KV3303A, opening the program control valve KV3305A, simultaneously opening the program control valve HV3301B at the inlet of the nitrogen pump D332, continuously vacuumizing the nitrogen vacuum pump P306, pressurizing the flash evaporation kettle R7002A by compressed nitrogen, simultaneously opening the program control valve KV3307A, and conveying the powder to a storage bin;
J. and (4) performing the fifth vacuumizing, wherein after the pressure feeding of the powder is finished, the nitrogen vacuum pump P306 continues to perform the vacuumizing.
2. The method for flash evaporation optimization of polymer powder according to claim 1, wherein: and C, vacuumizing propylene for the first time in the step A, opening a program control valve KV3302A after the flash evaporation kettle R7002A finishes receiving materials, closing the program control valve KV3308A and the program control valve KV3301A, and closing the program control valve HV3301A after the propylene vacuum pump inlet buffer tank D331 and the flash evaporation kettle R7002A are subjected to flat pressure.
3. The method for flash evaporation optimization of polymer powder according to claim 1, wherein: and D, performing steam vacuum pumping for the second time in the step D, and performing vacuum pumping after the pressure of the buffer tank D331 at the inlet of the propylene vacuum pump and the flash evaporation kettle R7002A is equalized, and closing the program control valve HV 3301A.
4. The method for flash evaporation optimization of polymer powder according to claim 1, wherein: and F, vacuumizing for the third time by steam, closing the program control valve HV3301A after the pressure of the buffer tank D331 at the inlet of the propylene vacuum pump and the flash evaporation kettle R7002A is equalized, and vacuumizing.
5. The method for flash evaporation optimization of polymer powder according to claim 1, wherein: and D, vacuumizing for the fourth time in the step H by using nitrogen, closing the program control valve KV3305A and opening the program control valve KV3303A after the pressure of the flash evaporation kettle R7002A is slightly positive, and closing the program control valve HV3301B to vacuumize after the pressure of the buffer tank D332 at the inlet of the nitrogen vacuum pump and the flash evaporation kettle R7002A is flat.
6. The method for flash evaporation optimization of polymer powder according to claim 1, wherein: in the step J, the fifth vacuumizing is nitrogen vacuumizing, the nitrogen vacuumizing before material receiving is started, the program control valve KV3307A is closed, the program control valve KV3303A is opened, after the buffer tank D332 at the inlet of the nitrogen vacuum pump is subjected to flat pressure with the flash kettle R7002A, the program control valve HV3301B is closed, the flash kettle R7002A is vacuumized by the nitrogen vacuum pump P306, after the vacuumizing is completed, the program control valve KV3303A is closed, the program control valve KV3308A is opened for material receiving, the program control valve KV3301A is opened for flat pressure, the material receiving process is repeated, and meanwhile, the program control valve HV3301B at the inlet of the propylene pump D332 is opened, and the vacuumizing is performed.
7. The method for flash evaporation optimization of polymer powder according to claim 1, wherein: an annular flow passage is additionally arranged at the discharging section of the dryer, the mixture of the temperature-reducing water and the powder enters the flash evaporation kettle R7002A from the flow passage, and the temperature of the powder entering the flash evaporation kettle R7002A is controlled to be 70-80 ℃ through the temperature-reducing water quantity and the jacket heat tracing.
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Application publication date: 20211224 |