CN111635467A - Polyolefin powder post-treatment device and method - Google Patents
Polyolefin powder post-treatment device and method Download PDFInfo
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- CN111635467A CN111635467A CN202010365971.1A CN202010365971A CN111635467A CN 111635467 A CN111635467 A CN 111635467A CN 202010365971 A CN202010365971 A CN 202010365971A CN 111635467 A CN111635467 A CN 111635467A
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- 239000000843 powder Substances 0.000 title claims abstract description 277
- 229920000098 polyolefin Polymers 0.000 title claims abstract description 151
- 238000000034 method Methods 0.000 title claims abstract description 32
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 63
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 63
- 238000010438 heat treatment Methods 0.000 claims abstract description 30
- 230000000712 assembly Effects 0.000 claims abstract description 8
- 238000000429 assembly Methods 0.000 claims abstract description 8
- 230000014759 maintenance of location Effects 0.000 claims abstract description 5
- 239000007789 gas Substances 0.000 claims description 85
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 84
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 73
- 229910052757 nitrogen Inorganic materials 0.000 claims description 36
- 239000004215 Carbon black (E152) Substances 0.000 claims description 18
- 229920000642 polymer Polymers 0.000 claims description 17
- 238000006073 displacement reaction Methods 0.000 claims description 14
- 230000005484 gravity Effects 0.000 claims description 12
- 238000009833 condensation Methods 0.000 claims description 11
- 230000005494 condensation Effects 0.000 claims description 11
- 239000000498 cooling water Substances 0.000 claims description 10
- 230000008569 process Effects 0.000 claims description 10
- 230000018044 dehydration Effects 0.000 claims description 7
- 238000006297 dehydration reaction Methods 0.000 claims description 7
- 238000001035 drying Methods 0.000 claims description 7
- 238000010025 steaming Methods 0.000 claims description 7
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 6
- 238000004064 recycling Methods 0.000 claims description 6
- 239000002826 coolant Substances 0.000 claims description 4
- 230000007547 defect Effects 0.000 abstract description 2
- -1 ethylene, propylene, propane Chemical class 0.000 description 26
- 239000004743 Polypropylene Substances 0.000 description 24
- 229920001155 polypropylene Polymers 0.000 description 24
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 18
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 18
- 230000000694 effects Effects 0.000 description 16
- 238000003756 stirring Methods 0.000 description 14
- 239000003054 catalyst Substances 0.000 description 13
- 238000006116 polymerization reaction Methods 0.000 description 10
- 150000001875 compounds Chemical class 0.000 description 9
- 239000000463 material Substances 0.000 description 8
- 239000000203 mixture Substances 0.000 description 8
- 238000007599 discharging Methods 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- 239000007787 solid Substances 0.000 description 6
- 238000001816 cooling Methods 0.000 description 5
- 238000007872 degassing Methods 0.000 description 5
- 230000007613 environmental effect Effects 0.000 description 5
- 238000010525 oxidative degradation reaction Methods 0.000 description 5
- 229910001873 dinitrogen Inorganic materials 0.000 description 4
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- 238000007906 compression Methods 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 230000009849 deactivation Effects 0.000 description 2
- 230000002779 inactivation Effects 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- XJDNKRIXUMDJCW-UHFFFAOYSA-J titanium tetrachloride Chemical compound Cl[Ti](Cl)(Cl)Cl XJDNKRIXUMDJCW-UHFFFAOYSA-J 0.000 description 1
- VOITXYVAKOUIBA-UHFFFAOYSA-N triethylaluminium Chemical compound CC[Al](CC)CC VOITXYVAKOUIBA-UHFFFAOYSA-N 0.000 description 1
- 239000011800 void material Substances 0.000 description 1
- 238000010626 work up procedure Methods 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F6/00—Post-polymerisation treatments
- C08F6/001—Removal of residual monomers by physical means
- C08F6/005—Removal of residual monomers by physical means from solid polymers
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F6/00—Post-polymerisation treatments
- C08F6/02—Neutralisation of the polymerisation mass, e.g. killing the catalyst also removal of catalyst residues
Abstract
The invention relates to a post-treatment device and a post-treatment method for polyolefin powder, which aim to overcome the technical defects that the polyolefin powder has long retention time and can not be in full reverse contact with replacement gas, so that the powder leaving a devolatilization device still carries more hydrocarbons. The utility model provides a polyolefin powder aftertreatment device, includes steamer and desicator, the steamer discharge gate is connected with the desicator: the steamer is a barrel with a conical bottom, the barrel is divided into an upper section and a lower section, the upper section is a powder feeding section, the lower section is a heating section, a powder distributing plate is arranged in the powder feeding section, and the aperture ratio of the powder distributing plate is 30-70%; the lower part of the barrel body of the steamer is a heating section, one or more layers of built-in detachable plate type heat exchange assemblies are arranged in the heating section, and each layer of plate type heat exchange assembly consists of a plurality of heat exchange plates; a steamer cone replacement steam annular distributor communicated with the barrel is arranged on the conical bottom of the barrel; the dryer is similar in structure to the steamer.
Description
Technical Field
The invention relates to a powder treatment device, in particular to a polyolefin powder post-treatment device and a method, and belongs to the technical field of petrochemical industry.
Background
In the process for the production of polyolefins, the polyolefin powder after leaving the polymerization reactor is subjected to a preliminary gas/solid separation to deactivate the catalyst remaining in the polyolefin powder and to economically recover the hydrocarbons carried in the polyolefin powder.
It is known that after the synthesis of polyolefin powders, the polyolefin powders leaving the polymerization system carry with them a certain amount of hydrocarbons, depending on the process for producing the polyolefin, including but not limited to ethylene, propylene, propane, hexane, etc., due to the particular void structure and bulk density of the polyolefin. The first purpose of the post-treatment of the polyolefin powder is to remove these entrained hydrocarbons to ensure the safety and environmental protection of the powder during use. In the removal of hydrocarbons, the hydrocarbons in the polyolefin powder are generally replaced by the addition of low-value inert gases such as steam, nitrogen, etc., alone or in combination, which is generally referred to as steaming, degassing or devolatilization. In addition, if steam or a mixed gas containing more than 10% of steam is introduced, the polyolefin powder is subjected to hydrocarbon removal, and then the steam carried in the polyolefin powder needs to be removed by nitrogen, which is generally referred to as drying of the polyolefin powder. Meanwhile, in order to improve the effect of removing hydrocarbons in the polyolefin powder by water vapor and nitrogen, the polyolefin powder can be heated to a certain temperature to promote the volatilization of the hydrocarbons.
A second objective of the polyolefin fluff work-up is to react the residual active catalyst in the fluff, including but not limited to titanium tetrachloride, triethylaluminum, etc., into a safe, stable compound, a process generally referred to as catalyst deactivation or deactivation. The method for deactivating or deactivating the catalyst is to introduce a small amount of water vapor into the polyolefin powder, and the water vapor reacts with the catalyst to produce a stable compound.
At present, the patents of the post-treatment method and the post-treatment device for the polyolefin powder at home and abroad are summarized as follows:
1. steaming and drying. This post-treatment method is adopted in the loop polymerization process described in Japanese patent laid-open No. Sho 58-216735. After a preliminary gas/solid separation of the polymer powder leaving the polymerization reactor, the polymer still carries about 2% by weight of hydrocarbons. The polymer powder enters a steamer with vertical stirring from the top, falls down along with gravity, indirectly heats the polyolefin powder entering the steamer from about 80 ℃ to about 110 ℃ with a large amount of water vapor introduced from the bottom of the steamer, reversely contacts the polyolefin powder and completely removes hydrocarbons, and then the polyolefin powder leaves the steamer from the bottom. The water vapor carries the displaced hydrocarbons to leave from the top of the steamer, and the hydrocarbons are recovered after condensation, dehydration and compression. The steamer is provided with a jacket, and water vapor can be introduced to properly heat the polyolefin powder. While the polymer is contacted with steam in the steamer, the residual catalyst reacts with the steam sufficiently to produce a stable compound.
The polyolefin powder leaving the steamer, which does not carry hydrocarbons, but water vapour, requires further drying treatment. The polyolefin powder containing water vapor enters a drier with a vertical stirrer from the top, falls down along with gravity, is in reverse contact with a large amount of nitrogen introduced from the bottom of the drier, completely removes the water vapor, and leaves the drier from the bottom. The nitrogen gas carries the displaced water vapor to leave from the top of the dryer, and the nitrogen gas after condensation, dehydration and compression returns to the dryer again for recycling.
The method of steaming first and drying later has the advantages that a great amount of water vapor is introduced from the bottom of the steamer to heat the powder and reversely contact the powder, so that the hydrocarbons in the polymer can be completely and thoroughly removed. The dryer can completely remove the water vapor in the polyolefin powder by adopting similar operation. The disadvantages are that the steam inlet amount of the steamer is larger, the inlet amount of the dryer for replacing nitrogen is also larger, the whole powder treatment process is long, the number of equipment is large, and the energy consumption is high.
2. And simultaneously performing devolatilization and inactivation. The polymerization process described in Japanese patent No. Sho 59-230010 (Amoco/Chisso) employs this treatment method. After a preliminary gas/solid separation of the polymer powder leaving the polymerization reactor, the polymer still carries about 2% by weight of hydrocarbons. The polymer powder enters a degassing bin from the top, falls down along with gravity, reversely contacts with a large amount of nitrogen and a small amount of water vapor introduced from the bottom of the degassing bin and completely removes hydrocarbons, and the water vapor reacts with the residual catalyst to produce a stable compound. The method has the advantages of short flow, less equipment and simple operation. The disadvantages are that the degassing bin has no stirring or heating, and a large amount of nitrogen is needed to ensure the effect of removing the hydrocarbons in the powder. In addition, the content of nitrogen in the mixed gas leaving from the top of the degassing bin exceeds 70% Vol, and the hydrocarbon recovery cost is high.
3. Devolatilization is carried out first and then inactivation is carried out. After a preliminary gas/solid separation of the polymer powder leaving the polymerization reactor, the polymer still carries about 2% by weight of hydrocarbons. The polymer powder enters a devolatilization device with a horizontal stirring paddle from the top of one end, and the horizontal stirring shaft, the stirring blades and the jacket of the devolatilization device can be filled with water vapor, so that the temperature of the powder entering the devolatilization device is indirectly heated from about 65 ℃ to about 110 ℃. Under the driving of stirring, the polymer powder leaves the devolatilizer from the bottom of the other end of the devolatilizer and enters a steamer with a vertical stirring paddle from the top. The mixed gas of water vapor and nitrogen is introduced into the bottom of the steamer and contacts with the powder falling along with gravity in the reverse direction, so that the hydrocarbons in the polyolefin powder are further removed, and simultaneously, the water vapor reacts with the residual catalyst to produce stable compounds.
The different polymerization processes operate slightly differently within the horizontal paddle devolatilizer, as described below.
In the process of Japanese patent 56-139520 (Tri-well optimized), a large amount of nitrogen gas is introduced into a devolatilizer with horizontal paddles to displace hydrocarbons in a polyolefin powder, which has the disadvantage that the nitrogen content of the mixed gas leaving the devolatilizer from the top exceeds 80% Vol, resulting in high hydrocarbon recovery costs. And the hydrocarbons carried in the polyolefin powder leaving the devolatilizer from the bottom of the other end are higher, so that the steamer needs to be filled with nitrogen to replace the hydrocarbons in the powder, and the hydrocarbon content in the mixed gas leaving the steamer from the top reaches 2 percent, is difficult to recover, and does not meet the environmental protection standard of exhausting air.
Chinese patent 200410053651.3 does not introduce any displacement gas into the devolatilizer with horizontal stirring paddle, although the hydrocarbons leaving the devolatilizer from the top do not contain other inert gases and can be directly recovered, the hydrocarbons carried in the polyolefin powder leaving the devolatilizer from the bottom of the other end are higher, which causes the steamer to need to introduce a large amount of nitrogen to displace the hydrocarbons in the powder, and the hydrocarbon content in the mixed gas leaving the steamer from the top reaches 8% Vol, which is difficult to recover, the economic loss is large, and the environmental protection standard of exhausting atmosphere is not met.
Chinese patent 201010515744.9 discloses that even if water vapor is introduced, the hydrocarbon can be directly recovered after the mixture gas leaving the devolatilizer from the top is condensed and dehydrated, but the content of hydrocarbon carried by the polyolefin powder leaving the devolatilizer is still high, the steamer needs to introduce a large amount of nitrogen gas to replace the hydrocarbon in the powder, and the hydrocarbon content in the mixture gas leaving the steamer from the top reaches 5% Vol, which is difficult to recover, has large economic loss, and does not meet the environmental protection standard of exhausting air.
On the whole, adopt the devolatilizer of taking horizontal stirring rake to come desorption polyolefin powder in the hydrocarbons that carry, though this devolatilizer accessible direct or indirect steam improves the devolatilization temperature of powder, because the powder dwell time is short (the reason that the dwell time is short is horizontal stirring is compared vertical stirring, the resistance is big when the powder stirs, equipment power is big, has restricted horizontal stirring devolatilizer's throughput, can only shorten dwell time under the high throughput), and the polyolefin powder is not enough reverse contact with the replacement gas, leads to leaving the powder of devolatilizer and still carrying more hydrocarbons. After the powder carrying hydrocarbons enters the steamer, more nitrogen is needed to be introduced to continuously replace the hydrocarbons in the powder, and the hydrocarbon content of the replacement tail gas of the steamer is 2-8 percent Vol, which is difficultTo recycle and exceed 60mg/m allowed by environmental laws and regulations3The emission standard of the atmospheric pollutants.
Disclosure of Invention
The invention aims to provide a polyolefin powder post-treatment device to solve the technical defects that the polyolefin powder has long retention time and cannot be fully and reversely contacted with replacement gas, so that the powder leaving a devolatilizer still carries more hydrocarbons.
The invention also provides a polyolefin powder post-treatment method.
The technical scheme adopted by the invention for solving the technical problems is as follows:
the utility model provides a polyolefin powder aftertreatment device, includes steamer and desicator, the steamer discharge gate is connected with the desicator:
the steamer is a barrel with a conical bottom, the barrel is divided into an upper section and a lower section, the upper section is a powder feeding section, the lower section is a heating section, a powder distributing plate is arranged in the powder feeding section, and the aperture ratio of the powder distributing plate is 30-70%; the lower part of the barrel body of the steamer is a heating section, one or more layers of built-in detachable plate type heat exchange assemblies are arranged in the heating section, and each layer of plate type heat exchange assembly consists of a plurality of heat exchange plates; a steamer cone replacement steam annular distributor communicated with the barrel is arranged on the conical bottom of the barrel;
the structure of the dryer is similar to that of a steamer, the upper part of a cylinder body of the dryer is a powder feeding section, a powder distribution plate is arranged in the feeding section, the lower part of the cylinder body of the dryer is a heating section, one or more layers of built-in detachable plate type heat exchange assemblies are arranged in the heating section, and each layer of plate type heat exchange assembly consists of a plurality of heat exchange plates; the conical bottom of the cylinder body is provided with a dryer cone replacement gas annular distributor communicated with the cylinder body.
The design of the powder distribution plate of the steamer can lead the powder passing through the distribution plate to be evenly discharged along with gravity (or called as plug flow discharging), and the discharging mode can lead the flow velocity of the powder at any point in the steamer to be consistent.
The steamer can be used singly or in series, so that the removal effect of hydrocarbons carried in the polyolefin powder is improved, and the steamer can be used in parallel, so that the processing capacity of the polyolefin powder is improved.
The drier can be used singly or in series, so that the removing effect of the water vapor carried in the polyolefin powder is improved, and the drier can be used in parallel, so that the processing capacity of the polyolefin powder is improved.
In the production process of polyolefin, polyolefin powder leaving a polymerization system and subjected to primary gas/solid separation enters a steamer with a powder distribution plate and a built-in detachable plate type heat exchange assembly in the device, is indirectly heated to about 110 ℃ by water vapor, is in reverse contact with the water vapor introduced from the bottom of the steamer to remove hydrocarbons in the polyolefin powder, simultaneously deactivates the residual catalyst, then enters a dryer with the powder distribution plate and the built-in detachable plate type heat exchange assembly, and is in reverse contact with the nitrogen introduced from the bottom of the dryer to remove the water vapor. The built-in detachable plate type heat exchange assembly of the dryer can not only be used for introducing water vapor to indirectly heat the polyolefin powder, but also be used for introducing cooling media such as circulating water and the like to reduce the temperature of the polyolefin powder, so that the polyolefin powder is prevented from thermal oxidative degradation after being treated. Both the steamer and the dryer are operated with a slight positive pressure.
Preferably, the top of the steamer is provided with a feed inlet and a steamer displacement tail gas outlet, and a discharge outlet of the steamer is positioned at the conical bottom of the steamer; the top of the dryer is provided with a dryer replacement tail gas outlet, and the conical bottom of the dryer is provided with a discharge hole.
Preferably, the pore size on the powder distribution plate is 5-50 mm; the included angle between the distributor plate and the horizontal plane of the powder distributor in the steamer and the dryer is 1-5 degrees larger than the repose angle (or called as the angle of repose) of the polyolefin powder, so that the powder passing through the distributor plate is evenly discharged. The best choice is that the included angle between the powder distribution plate and the horizontal plane is about 2 degrees larger than the repose angle of the polyolefin powder.
Preferably, the space between the outer sides of the two heat exchange plates on each layer of plate type heat exchange assembly of the steamer is 5-50 mm; the outer side distance of two heat exchange plates on each layer of plate type heat exchange assembly of the dryer is 10-70 mm. Further optimizing, the outer side distance of two heat exchange plates on each layer of plate type heat exchange assembly of the steamer is 10-30 mm; the outer side distance of the two heat exchange plates on each layer of plate type heat exchange assembly of the dryer is 20-50 mm.
Preferably, the steamer and the dryer cylinder are both provided with a steam jacket.
Preferably, the steamer and the dryer have a lower cone total length of 0.8 to 1.7 times the inner diameter of the cylinder, and preferably, the cone total length is 1.1 to 1.4 times the inner diameter of the cylinder.
A method for post-treating polyolefin powder, comprising the steps of:
1) steaming of polyolefin powder
Polymer powder enters from the top of the steamer, water vapor is introduced into a plate type heat exchange assembly in the steamer, and polyolefin powder which is evenly discharged along with gravity is indirectly heated to 90-110 ℃; replacing water vapor by a steamer cone to replace a vapor annular distributor, reversely contacting with the polyolefin powder from bottom to top, leaving the replaced mixed gas from the top of the steamer, and recovering hydrocarbons after condensation and dehydration; the polyolefin powder in the cone of the steamer is in a uniform blanking state (or called plug flow blanking), so that the polyolefin powder stays in the steamer for a consistent time, the temperature is controlled uniformly, and the gas replacement effect is uniform. The total hydrocarbon carry over of the polyolefin powder leaving the steamer was less than 100 ppmwt. The steam introduced into the bottom of the steamer cone will simultaneously react with the catalyst remaining in the polyolefin powder to produce a stable compound.
The hydrocarbon removing effect of the polyolefin powder in the steamer is determined by the temperature, the residence time and the flow of the replacement steam. Wherein the residence time of the polyolefin powder in the steamer can be controlled by the powder discharging speed, and the residence time is controlled to be 20-50 min; the temperature of the powder can be controlled at 90-110 ℃ by controlling the flow of heating steam of the built-in detachable plate type heat exchange assembly; the displacement water vapor flow rate can be directly controlled.
The steamer adopts micro-positive pressure operation to improve the removal effect of hydrocarbons in the powder, and the gas phase pressure of the steamer is controlled to be 1-10KPag by controlling the flow of the replaced mixed gas which leaves from the top of the steamer.
2) Drying of polyolefin powder
The polyolefin powder after the removal of hydrocarbons leaves the bottom of the steamer and enters the top of the dryer.
Introducing water vapor into a plate type heat exchange assembly of the dryer, controlling the temperature of the polyolefin powder uniformly discharged along with gravity at 90-110 ℃, or introducing circulating cooling water, chilled water or desalted water into the plate type heat exchange assembly, and controlling the temperature of the polyolefin powder leaving the dryer at 10-90 ℃ by adjusting the flow of a cooling medium;
the replacement gas introduced into the conical replacement gas annular distributor of the dryer is nitrogen and is in reverse contact with the polyolefin powder uniformly discharged from the dryer to replace water vapor in the polyolefin powder; the polyolefin powder freed of water vapour leaves the bottom of the dryer. The nitrogen containing water vapor leaves from the top of the dryer, is condensed, dehydrated and pressurized and then returns to the annular replacement gas distributor at the bottom of the dryer again for recycling;
the polyolefin powder exiting from the bottom of the dryer had a water vapor carry-over of less than 200 ppmwt.
The effect of removing water vapor from polyolefin powder in the dryer is determined by the temperature of the powder, the residence time and the flow rate of the displaced nitrogen. Wherein the residence time of the polyolefin powder in the dryer can be controlled by the discharge speed of the powder, and the residence time is controlled to be 15-45 min; the temperature of the powder can be controlled at 90-110 ℃ by controlling the flow of heating steam of the built-in detachable plate type heat exchange assembly; the flow rate of the displaced nitrogen can be directly controlled. The drier is operated by micro-positive pressure to improve the removal effect of water vapor in the powder, and the gas phase pressure of the drier is controlled to be 1-7KPag by controlling the flow of the replaced mixed gas leaving from the top of the drier.
According to the temperature control requirement of the polyolefin powder leaving the dryer, the built-in detachable plate type heat exchange assembly of the dryer can be filled with water vapor, so that the polyolefin powder leaving the dryer is heated to be above 90-110 ℃; or circulating cooling water, chilled water or desalted water can be introduced into the built-in detachable plate type heat exchange assembly of the dryer, and the temperature of the polyolefin powder material leaving the dryer is controlled to be 10-90 ℃ by adjusting the flow of the cooling medium. For the process and the device for directly producing the polyolefin powder, the thermal oxidative degradation of the polyolefin powder can be effectively prevented by reducing the temperature after the powder treatment (as is known, the thermal oxidative degradation speed of the polyolefin powder is doubled every time the temperature is increased by 10 ℃), which is not reflected in the prior art. If the temperature of the polyolefin powder in the dryer is controlled to be low, the steam removal from the powder can be ensured by increasing the flow rate of the replacement nitrogen.
Preferably, the lowest level of the polyolefin powder in the steamer and the dryer is controlled above the corresponding powder distribution plate.
Preferably, the gas phase pressure in the steamer is controlled at 1-10KPag, and the gas phase pressure in the dryer is controlled at 1-7 KPag.
Preferably, the residence time of the polyolefin powder in the steamer is 20 to 50min, preferably, the residence time of the polyolefin powder is 30 to 40 min; the residence time of the polyolefin powder in the dryer is 15 to 45min, preferably 25 to 35 min.
The invention has the beneficial effects that: the tail gas replaced by the steamer consists of hydrocarbons and water vapor, the water vapor can be completely recovered after condensation and dehydration, and meanwhile, the hydrocarbons carried by polyolefin powder of the steamer are few, so that the tail gas of the dryer can be recycled after condensation and dehydration. In addition, the temperature of the polyolefin powder passing through the dryer can be adjusted within the range of 10 to 90 ℃ depending on the use case.
Drawings
FIG. 1 is a schematic front view of a polyolefin powder post-treatment apparatus according to the present invention;
FIG. 2 is a schematic left side view showing the structure of the polyolefin powder post-treatment apparatus according to example 3;
FIG. 3 is a schematic left side view showing the structure of the polyolefin powder post-treatment apparatus according to example 4;
description of reference numerals:
01 feed inlet
02 steamer powder distributing plate
Built-in detachable plate type heat exchange assembly of 03 steamer
04 steamer cone replacement steam annular distributor
05 steamer
Discharge port of 06 steamer
07 steam device displacement tail gas outlet
08 steamer barrel jacket
Heating steam inlet of 09A steamer with built-in detachable plate type heat exchange assembly
Condensate outlet of built-in detachable plate type heat exchange assembly of 09B steamer
10 dryer
11 powder distributing plate of dryer
12 built-in detachable plate type heat exchange assembly of dryer
13 annular distributor of dryer cone replacement gas
14 discharge port of dryer
15 dryer displacement tail gas outlet
Heating steam inlet of detachable plate type heat exchange assembly arranged in 16A dryer
Cooling water outlet of detachable plate type heat exchange assembly arranged in 16B dryer
Condensate outlet of 17A dryer built-in detachable plate type heat exchange assembly
17B dryer is built-in to dismantle board-like heat exchange assembly cooling water inlet
18 dryer drum jacket.
Detailed Description
The technical solution of the present invention will be further specifically described below by way of specific examples. It is to be understood that the practice of the invention is not limited to the following examples, and that any variations and/or modifications may be made thereto without departing from the scope of the invention.
In the present invention, all parts and percentages are by weight, unless otherwise specified, and the equipment and materials used are commercially available or commonly used in the art. The methods in the following examples are conventional in the art unless otherwise specified.
Example 1:
the core of the invention is to provide a post-treatment device of polyolefin powder, which consists of a steamer 05 and a dryer 10, wherein a discharge hole 06 of the steamer is connected with the top of the dryer,
the steamer is a barrel with a conical bottom, the barrel is divided into an upper section and a lower section, the upper section is a powder feeding section, the lower section is a heating section, a steamer powder distribution plate 02 is arranged in the powder feeding section, and the aperture ratio of the powder distribution plate is 30-70%; the lower part of the barrel body of the steamer is a heating section, a plurality of layers of detachable plate type heat exchange assemblies 03 are arranged in the heating section, and each layer of plate type heat exchange assembly consists of a plurality of heat exchange plates; a steamer cone replacement steam annular distributor 04 communicated with the barrel is arranged at the conical bottom of the barrel, and a steamer barrel jacket 08 is arranged outside the steamer barrel;
the structure of the dryer is similar to that of a steamer, the upper part of a cylinder body of the dryer is a powder feeding section, a dryer powder distribution plate 11 is arranged in the feeding section, the lower part of the cylinder body of the dryer is a heating section, a plurality of layers of dryers are arranged in the heating section, detachable plate type heat exchange assemblies 12 are arranged in the heating section, and each layer of plate type heat exchange assemblies consists of a plurality of heat exchange plates; a dryer cone replacement gas annular distributor 13 communicated with the cylinder is arranged at the conical bottom of the cylinder, and a dryer cylinder jacket 18 is arranged outside the dryer cylinder;
the top of the steamer is provided with a feed inlet 01 and a steamer replacement tail gas outlet 07, and a discharge outlet of the steamer is positioned at the conical bottom of the steamer; the top of the dryer is provided with a dryer replacement tail gas outlet 15, and the conical bottom of the dryer is provided with a dryer discharge hole 14.
The pore size of the powder distribution plate of the steamer or the dryer is controlled within the range of 5-50mm and is adjusted according to the actual situation; the included angle between the steaming device and the powder distribution plate in the dryer and the horizontal plane is 1-5 degrees larger than the repose angle (or called as the static angle) of the polyolefin powder, so that the powder passing through the distribution plate is evenly discharged. The best choice is that the included angle between the powder distribution plate and the horizontal plane is about 2 degrees larger than the repose angle of the polyolefin powder.
The space between the outer sides of the two heat exchange plates on each layer of plate type heat exchange assembly of the steamer is 5-50 mm; the outer side distance of two heat exchange plates on each layer of plate type heat exchange assembly of the dryer is 10-70 mm. Optimally, the space between the outer sides of two heat exchange plates on each layer of plate type heat exchange assembly of the steamer is 10-30 mm; the outer side distance of the two heat exchange plates on each layer of plate type heat exchange assembly of the dryer is 20-50 mm.
In the above structure, the total length of the lower cone of the steamer and the dryer is 0.8-1.7 times of the inner diameter of the cylinder, and the optimum setting is that the total length of the cone is 1.1-1.4 times of the inner diameter of the cylinder.
The design of the powder distribution plate of the steamer can lead the powder passing through the distribution plate to be evenly discharged along with gravity (or called as plug flow discharging), and the discharging mode can lead the flow velocity of the powder at any point in the steamer to be consistent.
The steamer can be used singly or in series, so that the removal effect of hydrocarbons carried in the polyolefin powder is improved, and the steamer can be used in parallel, so that the processing capacity of the polyolefin powder is improved.
The drier can be used singly or in series, so that the removing effect of the water vapor carried in the polyolefin powder is improved, and the drier can be used in parallel, so that the processing capacity of the polyolefin powder is improved.
Example 2:
the core of the invention is to provide a post-treatment method of polyolefin powder, which comprises the following steps:
(1) steaming of polyolefin powder
After a preliminary gas/solid separation of the polymer powder leaving the polymerization reactor, the polymer still carries about 2% by weight of hydrocarbons.
The polymer powder enters from the top of the steamer in the polyolefin powder post-treatment device, and the steamer is a vertical steamer without stirring.
Introducing water vapor into a plate type heat exchange assembly in the steamer, and indirectly heating polyolefin powder which is uniformly fed along with gravity from about 65 ℃ to 110 ℃; replacing water vapor by a steamer cone to replace a vapor annular distributor, reversely contacting with the polyolefin powder from bottom to top, leaving the replaced mixed gas from the top of the steamer, and recovering hydrocarbons after condensation and dehydration; the polyolefin powder in the cone of the steamer is in a uniform blanking state (or called plug flow blanking), so that the polyolefin powder stays in the steamer for a consistent time, the temperature is controlled uniformly, and the gas replacement effect is uniform. The total hydrocarbon carry over of the polyolefin powder leaving the steamer was less than 100 ppmwt. The steam introduced into the bottom of the steamer cone will simultaneously react with the catalyst remaining in the polyolefin powder to produce a stable compound.
The hydrocarbon removing effect of the polyolefin powder in the steamer is determined by the temperature, the residence time and the flow of the replacement steam. Wherein the residence time of the polyolefin powder in the steamer can be controlled by the powder discharging speed, and the residence time is controlled to be 20-50 min; the temperature of the powder can be controlled at 90-110 ℃ by controlling the flow of heating steam of the built-in detachable plate type heat exchange assembly; the displacement water vapor flow rate can be directly controlled.
The steamer adopts micro-positive pressure operation to improve the removal effect of hydrocarbons in the powder, and the gas phase pressure of the steamer is controlled to be 1-10KPag by controlling the flow of the replaced mixed gas which leaves from the top of the steamer.
(2) Drying of polyolefin powder
The polyolefin powder after the removal of hydrocarbons leaves the bottom of the steamer and enters the top of the dryer.
Introducing water vapor into a plate type heat exchange assembly of the dryer, and controlling the temperature of the polyolefin powder uniformly discharged along with gravity to be 90-110 ℃. The replacement gas introduced into the conical replacement gas annular distributor of the dryer is nitrogen and is in reverse contact with the polyolefin powder uniformly discharged from the dryer to replace water vapor in the polyolefin powder; the polyolefin powder freed of water vapour leaves the bottom of the dryer. The nitrogen containing water vapor leaves from the top of the dryer, is condensed, dehydrated and pressurized and then returns to the annular replacement gas distributor at the bottom of the dryer again for recycling;
the polyolefin powder exiting from the bottom of the dryer had a water vapor carry-over of less than 200 ppmwt.
The effect of removing water vapor from polyolefin powder in the dryer is determined by the temperature of the powder, the residence time and the flow rate of the displaced nitrogen. Wherein the residence time of the polyolefin powder in the dryer can be controlled by the discharge speed of the powder, and the residence time is controlled to be 15-45 min; the temperature of the powder can be controlled at 90-110 ℃ by controlling the flow of heating steam of the built-in detachable plate type heat exchange assembly; the flow rate of the displaced nitrogen can be directly controlled. The drier is operated by micro-positive pressure to improve the removal effect of water vapor in the powder, and the gas phase pressure of the drier is controlled to be 1-7KPag by controlling the flow of the replaced mixed gas leaving from the top of the drier.
According to the temperature control requirement of the polyolefin powder leaving the dryer, the built-in detachable plate type heat exchange assembly of the dryer can be filled with water vapor, so that the polyolefin powder leaving the dryer is heated to be above 90-110 ℃; or circulating cooling water, chilled water or desalted water can be introduced into the built-in detachable plate type heat exchange assembly of the dryer, and the temperature of the polyolefin powder material leaving the dryer is controlled to be 10-90 ℃ by adjusting the flow of the cooling medium. For the process and the device for directly producing the polyolefin powder, the thermal oxidative degradation of the polyolefin powder can be effectively prevented by reducing the temperature after the powder treatment (as is known, the thermal oxidative degradation speed of the polyolefin powder is doubled every time the temperature is increased by 10 ℃), which is not reflected in the prior art. If the temperature of the polyolefin powder in the dryer is controlled to be low, the steam removal from the powder can be ensured by increasing the flow rate of the replacement nitrogen.
Example 3:
a post-treatment method of polyolefin powder comprises the following specific processes: 10000Kg/h of polypropylene powder at 65 ℃ carry 200Kg/h of propylene, and the propylene enters the steamer 05 from the feed inlet 01. Through steamer powder distributing plate 02, powder distributing plate percent of openness 40%, aperture 12mm evenly through built-in board heat exchange assembly 03 dismantled of steamer. The built-in detachable plate type heat exchange assembly 03 of the steamer is composed of 20 heat exchange plates, the distance between the outer sides of every two heat exchange plates is 25mm, the single heat exchange plates are filled with 120 ℃ saturated steam for 35Kg/h from a built-in detachable plate type heat exchange assembly heating steam inlet 09A of the steamer, and condensed water is discharged from a built-in detachable plate type heat exchange assembly condensate outlet 09B of the steamer of the heat exchange plates. The steamer barrel jacket 08 is filled with 120 ℃ steam from the upper part, the flow rate is 125Kg/h, and condensate is discharged from the lower part of the jacket. The temperature of the polypropylene powder entering the plate type heat exchange assembly from the upper part is 72 ℃, and the temperature of the polypropylene powder leaving the plate type heat exchange assembly from the lower part is 101 ℃.
Introducing 250Kg/h of replacement steam at 120 ℃ into a conical replacement steam annular distributor 04 of a steamer, reversely contacting with polypropylene powder in the steamer 05 to replace propylene in the powder, and reacting with a catalyst remained in the polypropylene powder to produce a stable compound. The displaced propylene and part of the steam are discharged from the displaced tail gas outlet 07 of the steamer. The temperature of the mixed gas at the outlet 07 of the steamer displacement tail gas is 70 ℃, wherein 199.1Kg/h of propylene and 125Kg/h of water vapor are contained in the mixed gas. The vapor pressure in the top of the steamer 05 was maintained at 7KPag by controlling the flow of the mixture through the displacement tail gas outlet.
The material outlet 06 of the steamer carries 10000Kg/h of polypropylene powder at 105 ℃ and carries 0.9Kg/h of propylene and 122Kg/h of water vapor, and the mixture enters the dryer 10. The residence time of the polypropylene powder in the steamer 05 is maintained at 35 minutes by controlling the discharge flow of the discharge hole 06 of the steamer, and the material level is controlled above the powder distribution plate.
Through the drier powder distribution plate 11, the powder distribution plate has the aperture ratio of 50 percent and the aperture of 15mm, and is uniformly provided with the detachable plate type heat exchange assembly 12 through the drier. The dryer built-in detachable plate type heat exchange assembly 12 is composed of 12 heat exchange plates, the distance between the outer sides of every two heat exchange plates is 35mm, 15Kg/h of 110 ℃ saturated steam is introduced into a single heat exchange plate through a dryer built-in detachable plate type heat exchange assembly heating steam inlet 16A, and condensed water is discharged from a dryer built-in detachable plate type heat exchange assembly condensate outlet 17A. The dryer cylinder jacket 18 was charged with 110 ℃ steam from the top at a flow rate of 45Kg/h, and the condensate was discharged from the bottom of the dryer cylinder jacket. The temperature of the polypropylene powder entering the dryer built-in detachable plate type heat exchange assembly 12 from the upper part is 103 ℃, and the temperature of the polypropylene powder leaving the dryer built-in detachable plate type heat exchange assembly 12 from the lower part is 112 ℃.
275Kg/h of replacement nitrogen at 20 ℃ is introduced into a conical replacement gas annular distributor 13 of the dryer, and the replacement nitrogen reversely contacts with the polypropylene powder in the dryer 10 and replaces water vapor and trace propylene in the powder. The replaced nitrogen, water vapor and trace propylene are discharged from a dryer replacement tail gas outlet 15 at the top of the dryer 10. The temperature of the mixed gas at the tail gas replacement outlet 15 is 100 ℃, wherein the propylene is 0.9Kg/h, the water vapor is 122Kg/h, and the nitrogen is 200 Kg/h. The gas phase pressure at the top of the dryer 10 was controlled at 2KPag by controlling the flow rate of the mixture at the outlet of the displacement tail gas.
The dryer discharge port 14 at the bottom of the dryer 10 is used for carrying 75Kg/h of nitrogen at 110 ℃ and 10000Kg/h of polypropylene powder. The polypropylene powder retention time of the dryer 10 is maintained at 25 minutes by controlling the discharge flow of the discharge port of the dryer, and the material level is controlled above the powder distribution plate.
In this example, the steamer had a displaced tail gas hydrocarbon content of about 61.43% wt, the remainder being steam. The hydrocarbons can be completely recovered by removing the clear water after cooling and condensation.
The gas phase leaving the top of the dryer 10, about 62% wt, is nitrogen and the remainder is primarily water vapor. After cooling and condensation, the clear water is removed, and the nitrogen can enter the conical replacement gas annular distributor 13 of the dryer again for recycling.
Example 4:
a post-treatment method of polyolefin powder comprises the following specific processes: 10000Kg/h of polypropylene powder at 65 ℃ carry 200Kg/h of propylene, and the propylene enters the steamer 05 from the feed inlet 01. Through steamer powder distributing plate 02, powder distributing plate percent of openness 40%, aperture 12mm evenly through built-in board heat exchange assembly 03 dismantled of steamer. The built-in detachable plate type heat exchange assembly 03 of the steamer consists of 20 heat exchange plates, the distance between the outer sides of every two heat exchange plates is 25mm, the single heat exchange plate is heated by the built-in detachable plate type heat exchange assembly heating steam inlet 09A of the steamer to be led in 120 ℃ of saturated steam for 35Kg/h, and condensed water is discharged from the built-in detachable plate type heat exchange assembly condensate outlet 09B of the steamer of the heat exchange plates. The steamer barrel jacket 08 is filled with 120 ℃ steam from the upper part, the flow rate is 125Kg/h, and condensate is discharged from the lower part of the jacket. The temperature of the polypropylene powder entering the plate type heat exchange assembly from the upper part is 72 ℃, and the temperature of the polypropylene powder leaving the plate type heat exchange assembly from the lower part is 101 ℃.
Introducing 250Kg/h of replacement steam at 120 ℃ into a conical replacement steam annular distributor 04 of a steamer, reversely contacting with polypropylene powder in the steamer 05, replacing propylene in the powder, and reacting with a catalyst remained in the polypropylene powder to produce a stable compound. The replaced propylene and part of the water vapor are discharged from a replaced tail gas outlet 07 of the top steamer of the steamer 05. The temperature of the mixed gas at the outlet 07 of the steamer displacement tail gas is 75 ℃, wherein, the propylene is 199.1Kg/h, and the water vapor is 125 Kg/h. The vapor pressure in the top of the steamer 05 was maintained at 7KPag by controlling the flow of the mixture through the displacement tail gas outlet.
The material outlet 06 of the steamer carries 10000Kg/h of polypropylene powder at 105 ℃ and carries 0.9Kg/h of propylene and 122Kg/h of water vapor, and the mixture enters the dryer 10. The residence time of the polypropylene powder in the steamer 05 is maintained at 35 minutes by controlling the discharge flow of the discharge hole 06 of the steamer, and the material level is controlled above the powder distribution plate.
Through the drier powder distribution plate 11, the powder distribution plate has the aperture ratio of 50 percent and the aperture of 15mm, and is uniformly provided with the detachable plate type heat exchange assembly 12 through the drier. The dryer built-in detachable plate type heat exchange assembly 12 is composed of 12 heat exchange plates, the distance between the outer sides of every two heat exchange plates is 25mm, 1000Kg/h of cooling water at 10 ℃ is introduced into a single heat exchange plate through a cooling water inlet 17B of the dryer built-in detachable plate type heat exchange assembly, and the cooling water is discharged from a cooling water outlet 16B of the dryer built-in detachable plate type heat exchange assembly. The dryer jacket heats the steam differently. The temperature of the polypropylene powder entering the dryer built-in detachable plate type heat exchange assembly 12 from the upper part is 90 ℃, and the temperature of the polypropylene powder leaving the dryer built-in detachable plate type heat exchange assembly 12 from the lower part is 35 ℃.
Introducing 350Kg/h of replacement nitrogen at 20 ℃ into a conical replacement gas annular distributor 13 of the dryer, reversely contacting the polypropylene powder in the dryer 10 and replacing water vapor and trace propylene in the powder. The replaced nitrogen, water vapor and trace propylene are discharged from a dryer replacement tail gas outlet 15 at the top of the dryer 10. The temperature of the mixed gas at the dryer displacement tail gas outlet 15 is 70 ℃, wherein the propylene is 0.9Kg/h, the water vapor is 122Kg/h, and the nitrogen is 275 Kg/h. The gas phase pressure at the top of the dryer 10 was controlled at 2KPag by controlling the flow rate of the mixture at the outlet of the displacement tail gas.
The discharge port 14 of the dryer at the bottom of the dryer 10 is used for carrying 10000Kg of polypropylene powder at the temperature of 30 ℃ and 75Kg of nitrogen at the same time. The polypropylene powder residence time of the dryer 10 was maintained at 35 minutes by controlling the discharge rate from the dryer discharge port 14 and the level was controlled above the powder distribution plate.
In this example, the steamer had a displaced tail gas hydrocarbon content of 61.54% wt, the remainder being steam. The hydrocarbons can be completely recovered by removing the clear water after cooling and condensation.
The gas phase leaving the top of the dryer 10, about 69% wt, is nitrogen and the remainder is primarily water vapor. After cooling and condensation, the clear water is removed, and the nitrogen can enter the conical replacement gas annular distributor 13 of the dryer again for recycling.
The embodiments are described in a progressive manner, each embodiment focuses on differences from other embodiments, and the same or similar parts among the embodiments are referred to each other. The device disclosed by the embodiment corresponds to the method disclosed by the embodiment, so that the description is simple, and the relevant points can be referred to the method part for description.
The apparatus and method for post-treating polyolefin powder according to the present invention are described in detail above. The principles and embodiments of the present invention are explained herein using specific examples, which are presented only to assist in understanding the method and its core concepts. It should be noted that, for those skilled in the art, it is possible to make various improvements and modifications to the present invention without departing from the principle of the present invention, and those improvements and modifications also fall within the scope of the claims of the present invention.
Claims (10)
1. The utility model provides a polyolefin powder aftertreatment device, includes steamer and desicator, and the steamer discharge gate is connected its characterized in that with the desicator:
the steamer is a barrel with a conical bottom, the barrel is divided into an upper section and a lower section, the upper section is a powder feeding section, the lower section is a heating section, a powder distributing plate is arranged in the powder feeding section, and the aperture ratio of the powder distributing plate is 30-70%; the lower part of the barrel body of the steamer is a heating section, one or more layers of built-in detachable plate type heat exchange assemblies are arranged in the heating section, and each layer of plate type heat exchange assembly consists of a plurality of heat exchange plates; a steamer cone replacement steam annular distributor communicated with the barrel is arranged on the conical bottom of the barrel;
the structure of the dryer is similar to that of a steamer, the upper part of a cylinder body of the dryer is a powder feeding section, a powder distribution plate is arranged in the feeding section, the lower part of the cylinder body of the dryer is a heating section, one or more layers of built-in detachable plate type heat exchange assemblies are arranged in the heating section, and each layer of plate type heat exchange assembly consists of a plurality of heat exchange plates; the conical bottom of the cylinder body is provided with a dryer cone replacement gas annular distributor communicated with the cylinder body.
2. The polyolefin powder post-treatment device according to claim 1, characterized in that: the top of the steamer is provided with a feed inlet and a steamer displacement tail gas outlet, and a discharge outlet of the steamer is positioned at the conical bottom of the steamer; the top of the dryer is provided with a dryer replacement tail gas outlet, and the conical bottom of the dryer is provided with a discharge hole.
3. The polyolefin powder post-treatment device according to claim 1, characterized in that: the aperture size on the powder distribution plate is 5-50 mm;
the included angle between the powder distribution plate in the steamer and the dryer and the horizontal plane is 1-5 degrees larger than the repose angle of the polyolefin powder.
4. The polyolefin powder post-treatment device according to claim 1, characterized in that: the space between the outer sides of the two heat exchange plates on each layer of plate type heat exchange assembly of the steamer is 5-50 mm;
the outer side distance of two heat exchange plates on each layer of plate type heat exchange assembly of the dryer is 10-70 mm.
5. The polyolefin powder post-treatment device according to claim 1, characterized in that: the outer side distance of two heat exchange plates on each layer of plate type heat exchange assembly of the steamer is 10-30 mm;
the outer side distance of the two heat exchange plates on each layer of plate type heat exchange assembly of the dryer is 20-50 mm.
6. The polyolefin powder post-treatment device according to claim 1, characterized in that: the steamer and the dryer cylinder are both provided with steam jackets.
7. The polyolefin powder post-treatment device according to claim 1, characterized in that: the total length of the lower cone of the steamer and the dryer is 0.8-1.7 times the inner diameter of the cylinder.
8. A process for the post-treatment of polyolefin powders using the apparatus of claim 1, characterized in that it comprises the following steps:
1) steaming of polyolefin powder
Polymer powder enters from the top of the steamer, water vapor is introduced into a plate type heat exchange assembly in the steamer, and polyolefin powder which is evenly discharged along with gravity is indirectly heated to 90-110 ℃; replacing water vapor by a steamer cone to replace a vapor annular distributor, reversely contacting with the polyolefin powder from bottom to top, leaving the replaced mixed gas from the top of the steamer, and recovering hydrocarbons after condensation and dehydration; polyolefin powder in the cone of the steamer is in a uniform blanking state;
the total hydrocarbon carry-over of the polyolefin powder leaving the steamer is less than 100 ppmwt;
2) drying of polyolefin powder
The polyolefin powder after hydrocarbon removal leaves from the bottom of the steamer and enters from the top of the dryer;
introducing water vapor into a plate type heat exchange assembly of the dryer, controlling the temperature of the polyolefin powder uniformly discharged along with gravity at 90-110 ℃, or introducing circulating cooling water, chilled water or desalted water into the plate type heat exchange assembly, and controlling the temperature of the polyolefin powder leaving the dryer at 10-90 ℃ by adjusting the flow of a cooling medium;
the replacement gas introduced into the conical replacement gas annular distributor of the dryer is nitrogen and is in reverse contact with the polyolefin powder uniformly discharged from the dryer to replace water vapor in the polyolefin powder; the polyolefin powder after the water vapor is removed leaves from the bottom of the dryer; the nitrogen containing water vapor leaves from the top of the dryer, is condensed, dehydrated and pressurized and then returns to the annular replacement gas distributor at the bottom of the dryer again for recycling;
the polyolefin powder exiting from the bottom of the dryer had a water vapor carry-over of less than 200 ppmwt.
9. The method of claim 1, wherein: the gas phase pressure in the steamer is controlled at 1-10KPag, and the gas phase pressure in the dryer is controlled at 1-7 KPag.
10. The method of claim 1, wherein: the retention time of polyolefin powder in the steamer is 20-50 min; the retention time of the polyolefin powder in the dryer is 15-45 min.
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| PCT/CN2020/136287 WO2021218182A1 (en) | 2020-04-30 | 2020-12-15 | Device and method for postprocessing polyolefin powder |
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| WO2021218182A1 (en) * | 2020-04-30 | 2021-11-04 | 浙江卫星能源有限公司 | Device and method for postprocessing polyolefin powder |
| CN114199049A (en) * | 2021-11-22 | 2022-03-18 | 浙江卫星能源有限公司 | Method and device for cooling polypropylene powder |
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| CN101573390A (en) * | 2006-12-29 | 2009-11-04 | 巴塞尔聚烯烃意大利有限责任公司 | Process for the polyolefin finishing |
| CN204400887U (en) * | 2014-12-18 | 2015-06-17 | 神华集团有限责任公司 | Polypropylene powder after-treatment device |
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| IT1150650B (en) * | 1982-03-10 | 1986-12-17 | Montedison Spa | FLUID BED REACTOR |
| CN1733810A (en) * | 2004-08-11 | 2006-02-15 | 高煦 | Polypropylene powder after-treating method |
| KR101508966B1 (en) * | 2006-12-29 | 2015-04-06 | 바셀 폴리올레핀 이탈리아 에스.알.엘 | Process and apparatus for drying a polymer |
| CN102453161A (en) * | 2010-10-22 | 2012-05-16 | 高煦 | Polypropylene powder postprocessing method |
| CN106397641B (en) * | 2015-07-28 | 2019-05-03 | 中国石油天然气股份有限公司 | Remove the device and method of fugitive constituent in polymer powders |
| CN111635467A (en) * | 2020-04-30 | 2020-09-08 | 浙江卫星能源有限公司 | Polyolefin powder post-treatment device and method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101573390A (en) * | 2006-12-29 | 2009-11-04 | 巴塞尔聚烯烃意大利有限责任公司 | Process for the polyolefin finishing |
| CN204400887U (en) * | 2014-12-18 | 2015-06-17 | 神华集团有限责任公司 | Polypropylene powder after-treatment device |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| WO2021218182A1 (en) * | 2020-04-30 | 2021-11-04 | 浙江卫星能源有限公司 | Device and method for postprocessing polyolefin powder |
| CN114199049A (en) * | 2021-11-22 | 2022-03-18 | 浙江卫星能源有限公司 | Method and device for cooling polypropylene powder |
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