CN106397641A - Device and method for removing volatile matters in polymer powder - Google Patents
Device and method for removing volatile matters in polymer powder Download PDFInfo
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- CN106397641A CN106397641A CN201510450210.5A CN201510450210A CN106397641A CN 106397641 A CN106397641 A CN 106397641A CN 201510450210 A CN201510450210 A CN 201510450210A CN 106397641 A CN106397641 A CN 106397641A
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- Prior art keywords
- polymer powders
- fugitive constituent
- devolatilization
- removing polymer
- distribution grid
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- 229920000642 polymer Polymers 0.000 title claims abstract description 110
- 239000000843 powder Substances 0.000 title claims abstract description 98
- 238000000034 method Methods 0.000 title claims abstract description 53
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 90
- 238000009826 distribution Methods 0.000 claims abstract description 61
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 45
- 239000007789 gas Substances 0.000 claims abstract description 19
- 239000000470 constituent Substances 0.000 claims description 56
- 238000012432 intermediate storage Methods 0.000 claims description 27
- 238000005243 fluidization Methods 0.000 claims description 20
- 238000010438 heat treatment Methods 0.000 claims description 18
- 239000008246 gaseous mixture Substances 0.000 claims description 17
- 238000003756 stirring Methods 0.000 claims description 17
- 238000009413 insulation Methods 0.000 claims description 9
- 239000012530 fluid Substances 0.000 claims description 5
- 229920000098 polyolefin Polymers 0.000 abstract description 8
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 229930195733 hydrocarbon Natural products 0.000 description 24
- 150000002430 hydrocarbons Chemical class 0.000 description 24
- 239000004743 Polypropylene Substances 0.000 description 11
- 229920001155 polypropylene Polymers 0.000 description 11
- 230000000694 effects Effects 0.000 description 10
- 238000006116 polymerization reaction Methods 0.000 description 10
- 230000008569 process Effects 0.000 description 9
- 230000009849 deactivation Effects 0.000 description 8
- 238000007872 degassing Methods 0.000 description 8
- -1 polypropylene Polymers 0.000 description 7
- 230000009286 beneficial effect Effects 0.000 description 6
- 238000001035 drying Methods 0.000 description 6
- 238000012805 post-processing Methods 0.000 description 6
- 239000007787 solid Substances 0.000 description 6
- 239000003054 catalyst Substances 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 230000002159 abnormal effect Effects 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000000796 flavoring agent Substances 0.000 description 2
- 235000019634 flavors Nutrition 0.000 description 2
- 239000000178 monomer Substances 0.000 description 2
- 238000010025 steaming Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 230000009471 action Effects 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 238000000262 chemical ionisation mass spectrometry Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000004087 circulation Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
Abstract
The invention discloses a device and a method for removing volatile matters in polymer powder, which can be applied to a polyolefin production device.A devolatilization tank is a fluidized bed container provided with a distribution plate, the devolatilization device makes the polymer fully contact with the mixed gas of hot nitrogen and steam by utilizing the fluidized bed principle, and the volatile matters are taken away by the discharged air flow, thereby improving the devolatilization efficiency; the apparatus allows the ratio of hot nitrogen to steam to be adjusted while maintaining the dryness of the polymer powder.
Description
Technical field
The present invention relates to a kind of device and method removing fugitive constituent in polymer powders, this device is intermittence
Operation, is applicable to manufacture of polyolefins device.
Background technology
In the polymerization, the difference according to technique and physical property, polymerizate can assume different states, its
Middle compare typically polymer in the form of solid powdery from reactor discharging, such as vapor phase method polyolefin work
Skill.Solid polymer, when reactor is discharged, often remains catalyst non-deactivated on a small quantity in polymer powders
With unreacted monomer, these impurity must degassing drying system in be removed it is therefore an objective to ensure pelletize
Send etc. the safety of the safety that downstream unit runs and polyolefin products storage transport with wind, reduce to greatest extent
The consumption of comonomer, reduces product abnormal flavour.
The process of above-mentioned removing hydro carbons is commonly referred to as degassing or devolatilization, the catalyst of residual is decomposed the mistake of deactivation
Journey is commonly referred to as decatize.Now it is described below：
(1) first decatize, be dried afterwards.Loop po lymerisation technique described in Japanese Patent Laid-Open No. Sho 58-216735 is just
It is using this post-processing approach.The polymer powders leaving polymer reactor are through preliminary gas/solid separation
Afterwards, still carry～polypropylene powder of 2% hydro carbons initially enters the top of a steamer, with
And on vapor adverse current contact.The hydro carbons carrying in polymer is cemented out by vapor, from steamer
Top leave and reclaimed；While polymer contacts vapor in steamer, the catalysis of its residual
Agent is decomposed deactivation.Polymer with part free water leaves from the bottom of steamer, enters a fluidisation
Bed dryer removes moisture content.First decatize, the advantage of rear drying meanss are very easily can will to leave steamer
Gas phase in hydro carbons and vapor separated, such that it is able to thoroughly reclaim hydrocarbons.Its shortcoming is
Post processing needs to consider the removing of free water, needs a large amount of hot nitrogen circulations, and long flow path, equipment are many, take up an area face
Long-pending big.
(2) first dry, rear decatize.Japanese Patent Laid-Open No. Sho 58-157807, clear 56-139520 (three well oil
Change) described in polymerization technique be exactly using this post-processing approach.Leave the polymer powders of polymer reactor
After preliminary gas/solid separation, still carry～polypropylene powder of 2% hydro carbons initially enters one and crouches
The blade dryer of formula, can be passed through vapor and enter inside the chuck of exsiccator, shaft, stirring vane
Row heating.Under heating, the multiple action stirring and be passed through nitrogen, the hydro carbons carrying in polymer is by big portion
Divide and cement out.Polymer powders enter back into a steamer, contact with the nitrogen containing vapor, gather
The micro hydro carbons carrying in compound is cemented out further, and the catalyst of residual is decomposed deactivation by vapor,
Leave the nitrogen of steamer, in vapor containing hydro carbons seldom, can directly discharge air.The advantage of this method
It is that process CIMS is brief.Its shortcoming is also to contain substantial amounts of nitrogen in the tail gas leave exsiccator in addition to hydro carbons
The molecular weight polymers steaming when gas and heating are it is difficult to thoroughly be reclaimed with economic method.Domestic existing
There is device all directly to go flare discharge even to discharge on the spot, increased unit consumption and the carbon dioxide of polymerized monomer
Discharge, cause the pollution of environment.
(3) it is dried in degassing cabin simultaneously, deactivate.The clear 59-230010 of Japan Patent (Amoco/Chisso)
Described polymerization technique is exactly to adopt this post-processing approach.The polymer powders leaving paradigmatic system are through just
After the gas/solid separation of step, still carry～polypropylene powder of 2% hydro carbons enters a vertical degassing
Storehouse, degassing cabin operates without stirring, moving bed.It is passed through nitrogen and micro vapor to degassing cabin.Poly-
Hydro carbons in compound is replaced out, and the catalyst of residual is decomposed deactivation by vapor.The advantage of this method is stream
Journey is more brief.Its shortcoming is that operation temperature is relatively low, and the removing degree of fugitive constituent is relatively low, in addition leaves degassing
Substantial amounts of nitrogen is also contained in addition to hydro carbons it is difficult to thoroughly be returned with economic method in the tail gas in storehouse
Receive.
(4) first degassing, again decatize deactivation.Chinese patent (200410053651.3) polypropylene powder post processing side
Method.The feature of the method be the polymer powders leaving paradigmatic system after preliminary gas/solid separation,
Still carry the～polypropylene powder of 2% hydro carbons, first by polymer powders under conditions of not contacting nitrogen
Most of hydro carbons remove out and then carry out decatize, deactivation again.The advantage of its method be by heating,
Stirring (mechanical agitation or fluid bed, air-flow conveying), extend the method for the powder time of staying by polypropylene powder
Most of hydro carbons in material removes out and is reclaimed, but its shortcoming is in the condition not contacting nitrogen
The polypropylene powder of lower removing hydro carbons still carries the hydro carbons more than comparison when entering decatize, deactivation equipment, these
Difficult to reach environmental protection when hydro carbons is difficult to reclaim after being mixed with a large amount of nitrogen in decatize, deactivation process, discharges
Requirement.Chinese patent (200410053651.3) ratio (2) Japanese Patent Laid-Open No. Sho 58-157807, clear
The substantial improvements of " first dry, rear decatize " post-processing approach of 56-139520 (three well oilings) are exactly drying
No longer it is passed through nitrogen in device, but by the heating of exsiccator, stirring, the hydro carbons of 100% form is released out
Reclaimed after coming.But still can not thoroughly solve the problems, such as to reduce unit consumption.Due to obstructed in exsiccator
Enter nitrogen, polypropylene powder enters, by exsiccator, the hydro carbons carrying during steamer and compares Japanese Patent Laid-Open No. Sho
58-157807, clear 56-139520 (three well oilings) enters decatize by exsiccator when being passed through nitrogen in exsiccator
The hydro carbons carrying during device is many, brings the problem in environmental protection during steamer exhaust emissions.
The feature of Chinese patent CN 102453160A polypropylene powder after-treating method be using be dried,
Under the occasion of decatize aftertreatment technology：No longer to have steam indirect heating, with stirring exsiccator lead to
Enter nitrogen, but be passed through open steam, exsiccator is transformed into recovery hydro carbons and removing polypropylene powder
Middle fugitive constituent, makes the catalyst of residual deactivate, does not contain free water in the polypropylene powder leaving exsiccator
Stream dryer device；Polymer after quite a few hydro carbons of above-mentioned removing enters back into what existing process was adopted
Steamer, is passed through nitrogen and removes the vapor carrying in powder, be no longer passed through vapor, by vapour in steamer
Steaming device is transformed into the moisture eliminator of water vapor removing.Its shortcoming is that operating process is complicated, simultaneously it cannot be guaranteed that gathering
Close the drying of powder.
Content of the invention
It is an object of the invention to provide a kind of device and method removing fugitive constituent in polymer powders, this devolatilization
Device makes polymer and the gaseous mixture of hot nitrogen and steam be fully contacted using fluidized bed principle, fugitive constituent quilt
The air-flow of emptying is taken away, thus improving devolatilization efficiency；This device can adjust the ratio of hot nitrogen and steam,
Keep the drying of polymer powders simultaneously.
The present invention provides a kind of device of fugitive constituent in removing polymer powders, including devolatilization tank, intermediate storage tank
And filter is it is characterised in that described devolatilization tank is the fluidized bed container being provided with distribution grid.
The device of fugitive constituent in removing polymer powders of the present invention, wherein, described devolatilization tank is preferably
Pressure vessel.
The device of fugitive constituent in removing polymer powders of the present invention, wherein, described devolatilization tank and filtration
The outer wall of device is preferably provided with heating tape.
The device of fugitive constituent in removing polymer powders of the present invention, wherein, described devolatilization tank and filtration
The outer wall of device is preferably also provided with heat-insulation layer, and described heat-insulation layer is arranged on the outside of heating tape.
The device of fugitive constituent in removing polymer powders of the present invention, wherein, described distribution grid is preferably
Single flow distribution grid or lateral flow type distribution grid.
The device of fugitive constituent in removing polymer powders of the present invention, wherein, described lateral flow type distribution grid
Preferably equipped with conical cowl in distribution plate orifices.
The device of fugitive constituent in removing polymer powders of the present invention, these, it is preferred to, described point
The support shaft two ends of fabric swatch are connected with rotary shaft, are supported by chamber wall, and wherein one end and motor connection have
Teletransmission control unit controls, and described rotary shaft is sealed into mechanical seal with chamber wall.
The device of fugitive constituent in removing polymer powders of the present invention, wherein, described distribution grid and rotation
The axle preferably mode in order to dismantle connects, more preferably bonded or pin connection.
The device of fugitive constituent in removing polymer powders of the present invention, wherein, described distribution grid is rotatable,
The rotational angle of distribution grid is preferably 90 °～360 °.
The device of fugitive constituent in removing polymer powders of the present invention, wherein, described devolatilization tank is further preferably
It is provided with stirring paddle.
The present invention also provide a kind of removing polymer powders in fugitive constituent method, wherein, polymer powders from
The devolatilization tank top of device enters, and the gaseous mixture of hot nitrogen and steam enters from the devolatilization pot bottom of described device
Enter, polymer powders and gaseous mixture are fully contacted, form fluid bed, carry out devolatilization, gas passes through described dress
The filter above devolatilization tank side put is vented.
The method of fugitive constituent in removing polymer powders of the present invention, wherein, the fluidisation of described devolatilization tank
Time is preferably 5min～60min, more preferably 10min～30min, can be adjusted according to devolatilization effect.
The method of fugitive constituent in removing polymer powders of the present invention, wherein, the operation of described devolatilization tank
Pressure is preferably 0.1MPa～0.7MPa, more preferably 0.2MPa～0.7MPa, can be carried out according to fluidized state
Adjustment.
The method of fugitive constituent in removing polymer powders of the present invention, wherein, the temperature of described hot nitrogen
It is preferably 30 DEG C～100 DEG C, more preferably 70 DEG C～100 DEG C, can be adjusted according to devolatilization effect.
The method of fugitive constituent in removing polymer powders of the present invention, wherein, hot nitrogen and steam mixed
In conjunction gas, vapour volume content is excellent accounts for, more preferably steam content 1%～10% adjustable 0%～100%.
The method of fugitive constituent in removing polymer powders of the present invention, wherein, the temperature of described heating tape
Preferably 30 DEG C～100 DEG C, more preferably 60 DEG C～100 DEG C.
The method of fugitive constituent in removing polymer powders of the present invention, wherein, the rotating speed of described stirring paddle
Preferably 5r/h～300r/h, more preferably 50r/h～100r/h.
The present invention also can be summarized as follows：
In a kind of removing polymer powders, the device and method of fugitive constituent, is applicable to manufacture of polyolefins device,
It is characterized in that, this Devolatilization device includes intermediate storage tank and devolatilization tank, and devolatilization tank is the fluidisation being provided with distribution grid
Bed container, polymer enters from top, and the gaseous mixture of hot nitrogen and steam enters from bottom, polymer and mixed
Close gas to be fully contacted, form fluid bed, carry out devolatilization, gas is vented after the filter above the side,
Distribution grid is rotatable, will be polymerized powder and once discharge devolatilization tank, and devolatilization tank is pressure vessel, and outer wall is provided with companion
Hot heat-insulation layer.
In the device and method of fugitive constituent in above-mentioned removing polymer powders, the implementation process of the present invention is：
This device includes intermediate storage tank and devolatilization tank, is intermittent operation, and the polymer without devolatilization stores up from middle
Tank once enters the devolatilization tank being in fluidized state, after certain time fluidisation devolatilization, the pressure of devolatilization tank
All it is vented, the distribution grid controlling through teletransmission can turn an angle, by the polymer after devolatilization once
Discharge devolatilization tank；Within this section fluidisation time, intermediate storage tank receives the polymerization that the polyolefin reactor coming produces
Thing powder.
The two ends of distribution grid support shaft are connected with rotary shaft, are supported by chamber wall, wherein one end and motor connection,
There is teletransmission control unit to control, can be operated in control room, rotary shaft is sealed into machinery with chamber wall
Sealing.
The volume of described intermediate storage tank can be calculated according to the devolatilization ability of this device.
Described distribution grid may be selected single flow or lateral flow type, lateral flow type distribution grid be in distribution plate orifices equipped with
Conical cowl, air-flow flows out from the side opening of the latasuture boring cap bottom or cone cap surrounding, is most widely used, effect
Preferably a kind of distribution grid, wherein latasuture formula cone cap will not form little dead band at top because of it, and gas is close to
Distribution grid plate face blows out, and can also eliminate the dead band in plate face, thus substantially improving bed under suitable gas speed
Fluidization quality, it is to avoid sintering and distribution grid wear phenomena occur, therefore applies wider.
The invention has the beneficial effects as follows：
In a kind of removing polymer powders that the present invention provides, the device and method of fugitive constituent can improve devolatilization
Efficiency, simultaneously keep polymer powders drying it is ensured that pelletize and wind send wait downstream unit run safety with
The safety of polyolefin products storage transport, reduces product abnormal flavour.
Brief description
Fig. 1：The schematic device of fugitive constituent in a kind of removing polymer powders
Wherein, reference
Intermediate storage tank 1
Filter 2
Devolatilization tank 3
Heating tape 4
Heat-insulation layer 5
Control unit 6
Distribution grid 7；
Fig. 2：The schematic device of fugitive constituent in a kind of removing polymer powders
Wherein, reference
Intermediate storage tank 1
Filter 2
Devolatilization tank 3
Heating tape 4
Heat-insulation layer 5
Control unit 6
Distribution grid 7
Stirring paddle 8；
Fig. 3：The device distribution grid schematic diagram of fugitive constituent in a kind of removing polymer powders.
Specific embodiment
Hereinafter embodiments of the invention are elaborated：The present embodiment is premised on technical solution of the present invention
Under implemented, give detailed embodiment and process, but protection scope of the present invention be not limited to following
Embodiment, the experimental technique of unreceipted actual conditions in the following example, generally according to normal condition.
Referring to the drawings 1, the device of fugitive constituent in the removing polymer powders shown in the present invention, including devolatilization tank
3rd, intermediate storage tank 1 and filter 2, the volume of intermediate storage tank can be carried out according to the devolatilization ability of this device
Calculate, devolatilization tank 3 is the fluidized bed container being provided with distribution grid 7, devolatilization tank is pressure vessel；Devolatilization tank and
The outer wall of filter is provided with heating tape 4.
The outer wall of described devolatilization tank and filter is additionally provided with heat-insulation layer 5, and heat-insulation layer 5 is arranged on heating tape 4
Outside.
Described distribution grid 7 is lateral flow type distribution grid, and equipped with conical cowl in distribution grid 7 hole, air-flow is from cone
The side opening of the latasuture of cap bottom or cone cap surrounding flows out, and is most widely used, preferably a kind of distribution grid of effect,
Wherein latasuture formula cone cap will not form little dead band at top because of it, and gas is close to the blowout of distribution grid plate face, fits
When the lower dead band that can also eliminate in plate face of gas speed, thus substantially improving the fluidization quality of bed, it is to avoid send out
Raw burn knot and distribution grid wear phenomena, therefore apply wider or single flow distribution grid, distribution grid 7
Support shaft two ends be connected with rotary shaft, supported by chamber wall, wherein one end and motor connection, there is teletransmission
Control unit controls 6, and rotary shaft is sealed into mechanical seal with chamber wall；Distribution grid 7 with rotary shaft so that
Mode in dismounting connects, using bonded or pin connection；Distribution grid is rotatable, distribution grid
Rotational angle is 90 °～360 °.
Referring to the drawings 2, devolatilization tank of the present invention is also provided with stirring paddle 8.
The method of fugitive constituent in the removing polymer powders that the present invention provides, wherein, polymer powders are from device
Devolatilization tank top enter, the gaseous mixture of hot nitrogen and steam enters from the devolatilization pot bottom of described device, gathers
Compound powder and gaseous mixture are fully contacted, and form fluid bed, carry out devolatilization, and gas passes through the de- of described device
Wave the filter above tank side to be vented.
The fluidisation time of described devolatilization tank is preferably 5min～60min, more preferably 10min～30min, can
It is adjusted according to devolatilization effect；If the fluidisation time of devolatilization tank is less than 5min, due to the stream of devolatilization tank
The change time is too short, causes polymer powders can not be fully contacted with gaseous mixture, does not reach preferable devolatilization completely
Effect；And the fluidisation time of devolatilization tank is more than 60min, due to the fluidisation overlong time of devolatilization tank, when causing
Between waste, and because long-time powder between friction can increase fine powder content, be unfavorable for that backwind send and makes
The normal operation of grain operation, has no other beneficial effects.
The operating pressure of described devolatilization tank preferably 0.1MPa～0.7MPa, more preferably 0.2MPa～
0.7MPa, can be adjusted according to fluidized state；If the operating pressure of devolatilization tank is less than 0.1MPa, by
Too small in pressure, cause bed be in can not fluidisation completely state, and the operating pressure of devolatilization tank is more than
0.7MPa, because pressure is excessive, causes the increasing of static content in discharging process, increases potential safety hazard, has no
Other beneficial effects.
The temperature of described hot nitrogen is preferably 30 DEG C～100 DEG C, more preferably 70 DEG C～100 DEG C, can be according to de-
Wave effect to be adjusted；If the temperature of hot nitrogen is less than 30 DEG C, because temperature is too low, cause polymer
The a small amount of alkene component carried secretly in powder can not gasify, and then affects devolatilization effect, and the temperature of hot nitrogen surpasses
Cross 100 DEG C, because temperature is too high, easily cause polymer powders adhesion, caking, affect postorder wind
Send the operation with prilling section, have no other beneficial effects.
In the gaseous mixture of hot nitrogen and steam, vapour volume content is excellent accounts for adjustable 0%～100%, more preferably steams
Vapour content 1%～10%.
Preferably 30 DEG C～100 DEG C of the temperature of described heating tape, more preferably 60 DEG C～100 DEG C；If heat tracing
The temperature of band is less than 30 DEG C, because temperature is too low, causes a small amount of alkene component carried secretly in polymer powders
Can not gasify, and then affect devolatilization effect, and the temperature of heating tape is more than 100 DEG C, because temperature is too high,
Easily cause polymer powders adhesion, caking, impact postorder wind send the operation with prilling section, has no
Other beneficial effects.
The rotating speed of described stirring paddle is preferably 5r/h～300r/h, more preferably 50r/h～100r/h；If stirring
The rotating speed of device is less than 5r/h, because the rotating speed of agitator is too low, does not have and allows polymer powders to fill with gaseous mixture
The effect that tap is touched, and the rotating speed of agitator is more than 300r/h, because the rotating speed of agitator is too high, can increase
Friction between polymer powders, causes the increase of fine powder amount, is unfavorable for that backwind send normal with granulating working procedure
Run, have no other beneficial effects.
In the device and method of fugitive constituent in above-mentioned removing polymer powders, the implementation process of the present invention is：
This device includes intermediate storage tank and devolatilization tank, is intermittent operation, and the polymer without devolatilization stores up from middle
Tank once enters the devolatilization tank being in fluidized state, after certain time fluidisation devolatilization, the pressure of devolatilization tank
All it is vented, the distribution grid controlling through teletransmission can turn an angle, by the polymer after devolatilization once
Discharge devolatilization tank；Within this section fluidisation time, intermediate storage tank receives the polymerization that the polyolefin reactor coming produces
Thing powder.
Embodiment 1
As shown in figure 1, the device of fugitive constituent includes the intermediate storage tank of 300L in described removing polymer powders
With the devolatilization tank of 600L, the pressure of intermediate storage tank is 0.7MPa, is stored with the polymer of 30kg, devolatilization
The pressure of tank is maintained at 0.5MPa, and outer wall tracing thermal-insulating layer temperature is 80 DEG C.Hot nitrogen and steam lead to simultaneously
Enter devolatilization tank, the temperature of hot nitrogen is 100 DEG C, and flow is 60m3/h；The temperature of steam is 160 DEG C, stream
Measure as 5m3/ h, is passed through time 10min.
It is illustrated in figure 3 the distribution grid in devolatilization tank, is single flow, the two ends of support shaft are connected with rotary shaft,
Connected mode is bonded, is supported by chamber wall, wherein one end and motor connection, has teletransmission control unit control
System, is operated in control room, and rotary shaft is sealed into mechanical seal with chamber wall.
In intermediate storage tank, the polymer of 30kg enters from devolatilization tank top, and hot nitrogen is entering devolatilization with steam
Converge into a line before tank, enter devolatilization tank from discharge line branch road, the fluidisation time is 30min, polymerization
Thing is fully contacted with gaseous mixture, and after complete devolatilization, the pressure of devolatilization tank is all vented, and controls through teletransmission
Distribution grid rotates 90 °, and the polymer after devolatilization is once discharged devolatilization tank, and distribution grid recovers former state afterwards,
Repeat above procedure.
Embodiment 2
As shown in Fig. 2 the device of fugitive constituent includes the intermediate storage tank of 120L in described removing polymer powders
With the devolatilization tank of 300L, the pressure of intermediate storage tank is 0.5MPa, is stored with the polymer of 12kg, devolatilization
The pressure of tank is maintained at 0.3MPa, inside has paddle to stir, and rotating speed is 60r/h, outer wall tracing thermal-insulating layer temperature
For 100 DEG C.Hot nitrogen and steam are passed through devolatilization tank simultaneously, and the temperature of hot nitrogen is 80 DEG C, and flow is
35m3/ h, the temperature of steam is 160 DEG C, and flow is 1m3/ h, is passed through time 10min.
It is illustrated in figure 3 the distribution grid in devolatilization tank, is single flow, the two ends of support shaft are connected with rotary shaft,
Connected mode is pin connection, is supported by chamber wall, wherein one end and motor connection, has teletransmission control unit control
System, is operated in control room, and rotary shaft is sealed into mechanical seal with chamber wall.
In intermediate storage tank, the polymer of 12kg enters from devolatilization tank top, and hot nitrogen is entering devolatilization with steam
Converge into a line before tank, enter devolatilization tank from discharge line branch road, the fluidisation time is 15min, polymerization
Thing is fully contacted with gaseous mixture, and after complete devolatilization, the pressure of devolatilization tank is all vented, and controls through teletransmission
Distribution grid rotates 90 °, and the polymer after devolatilization is once discharged devolatilization tank, and distribution grid recovers former state afterwards,
Repeat above procedure.
Embodiment 3
As shown in figure 1, the device of fugitive constituent includes the intermediate storage tank of 300L in described removing polymer powders
With the devolatilization tank of 600L, the pressure of intermediate storage tank is 0.7MPa, is stored with the polymer of 35kg, devolatilization
The pressure of tank is maintained at 0.7MPa, and outer wall tracing thermal-insulating layer temperature is 30 DEG C.Hot nitrogen and steam lead to simultaneously
Enter devolatilization tank, the temperature of hot nitrogen is 90 DEG C, and flow is 100m3/h；The temperature of steam is 160 DEG C, stream
Measure as 20m3/ h, is passed through time 30min.
It is illustrated in figure 3 the distribution grid in devolatilization tank, is single flow, the two ends of support shaft are connected with rotary shaft,
Connected mode is bonded, is supported by chamber wall, wherein one end and motor connection, has teletransmission control unit control
System, is operated in control room, and rotary shaft is sealed into mechanical seal with chamber wall.
In intermediate storage tank, the polymer of 35kg enters from devolatilization tank top, and hot nitrogen is entering devolatilization with steam
Converge into a line before tank, enter devolatilization tank from discharge line branch road, the fluidisation time is 60min, polymerization
Thing is fully contacted with gaseous mixture, and after complete devolatilization, the pressure of devolatilization tank is all vented, and controls through teletransmission
Distribution grid rotates 90 °, and the polymer after devolatilization is once discharged devolatilization tank, and distribution grid recovers former state afterwards,
Repeat above procedure.
Embodiment 4
As shown in Fig. 2 the device of fugitive constituent includes the intermediate storage tank of 120L in described removing polymer powders
With the devolatilization tank of 300L, the pressure of intermediate storage tank is 0.5MPa, is stored with the polymer of 10kg, devolatilization
The pressure of tank is maintained at 0.1MPa, inside has paddle to stir, and rotating speed is 5r/h, outer wall tracing thermal-insulating layer temperature
For 90 DEG C.Hot nitrogen and steam are passed through devolatilization tank simultaneously, and the temperature of hot nitrogen is 30 DEG C, and flow is 35m3/ h,
The temperature of steam is 160 DEG C, and flow is 0.35m3/ h, is passed through time 5min.
It is illustrated in figure 3 the distribution grid in devolatilization tank, is single flow, the two ends of support shaft are connected with rotary shaft,
Connected mode is pin connection, is supported by chamber wall, wherein one end and motor connection, has teletransmission control unit control
System, is operated in control room, and rotary shaft is sealed into mechanical seal with chamber wall.
In intermediate storage tank, the polymer of 10kg enters from devolatilization tank top, and hot nitrogen is entering devolatilization with steam
Converge into a line before tank, enter devolatilization tank from discharge line branch road, the fluidisation time is 5min, polymerization
Thing is fully contacted with gaseous mixture, and after complete devolatilization, the pressure of devolatilization tank is all vented, and controls through teletransmission
Distribution grid rotates 90 °, and the polymer after devolatilization is once discharged devolatilization tank, and distribution grid recovers former state afterwards,
Repeat above procedure.
Embodiment 5
As shown in Fig. 2 the device of fugitive constituent includes the intermediate storage tank of 120L in described removing polymer powders
With the devolatilization tank of 300L, the pressure of intermediate storage tank is 0.5MPa, is stored with the polymer of 15kg, devolatilization
The pressure of tank is maintained at 0.4MPa, inside has paddle to stir, and rotating speed is 300r/h, outer wall tracing thermal-insulating layer temperature
Spend for 70 DEG C.Hot nitrogen and steam are passed through devolatilization tank simultaneously, and the temperature of hot nitrogen is 80 DEG C, and flow is
40m3/ h, the temperature of steam is 160 DEG C, and flow is 2m3/ h, is passed through time 8min.
It is illustrated in figure 3 the distribution grid in devolatilization tank, is single flow, the two ends of support shaft are connected with rotary shaft,
Connected mode is pin connection, is supported by chamber wall, wherein one end and motor connection, has teletransmission control unit control
System, is operated in control room, and rotary shaft is sealed into mechanical seal with chamber wall.
In intermediate storage tank, the polymer of 15kg enters from devolatilization tank top, and hot nitrogen is entering devolatilization with steam
Converge into a line before tank, enter devolatilization tank from discharge line branch road, the fluidisation time is 40min, polymerization
Thing is fully contacted with gaseous mixture, and after complete devolatilization, the pressure of devolatilization tank is all vented, and controls through teletransmission
Distribution grid rotates 90 °, and the polymer after devolatilization is once discharged devolatilization tank, and distribution grid recovers former state afterwards,
Repeat above procedure.
Claims (18)
1. a kind of device removing fugitive constituent in polymer powders, including devolatilization tank, intermediate storage tank and mistake
Filter is it is characterised in that described devolatilization tank is the fluidized bed container being provided with distribution grid.
2. as claimed in claim 1 removing polymer powders in fugitive constituent device it is characterised in that
Described devolatilization tank is pressure vessel.
3. as claimed in claim 1 removing polymer powders in fugitive constituent device it is characterised in that
The outer wall of described devolatilization tank and filter is provided with heating tape.
4. as claimed in claim 3 removing polymer powders in fugitive constituent device it is characterised in that
The outer wall of described devolatilization tank and filter is additionally provided with heat-insulation layer, and described heat-insulation layer is arranged on the outer of heating tape
Face.
5. as claimed in claim 1 removing polymer powders in fugitive constituent device it is characterised in that
Described distribution grid is single flow distribution grid or lateral flow type distribution grid.
6. as claimed in claim 5 removing polymer powders in fugitive constituent device it is characterised in that
Described lateral flow type distribution grid is equipped with conical cowl in distribution plate orifices.
7. as claimed in claim 1 removing polymer powders in fugitive constituent device it is characterised in that
The support shaft two ends of described distribution grid are connected with rotary shaft, are supported by chamber wall, wherein one end and motor
Connect, there is teletransmission control unit and control, described rotary shaft is sealed into mechanical seal with chamber wall.
8. as claimed in claim 7 removing polymer powders in fugitive constituent device it is characterised in that
Described distribution grid is connected in order to the mode dismantled with rotary shaft.
9. as claimed in claim 8 removing polymer powders in fugitive constituent device it is characterised in that
Described connected mode is bonded or pin connection.
10. as claimed in claim 1 removing polymer powders in fugitive constituent device it is characterised in that
Described distribution grid is rotatable, and the rotational angle of distribution grid is 90 °～360 °.
11. as claimed in claim 1 removing polymer powders in fugitive constituent devices it is characterised in that
Described devolatilization tank is additionally provided with stirring paddle.
12. a kind of removing polymer powders in fugitive constituent methods it is characterised in that polymer powders from
The devolatilization tank top of device enters, and the gaseous mixture of hot nitrogen and steam is from the devolatilization pot bottom of described device
Enter, polymer powders and gaseous mixture are fully contacted, form fluid bed, carry out devolatilization, gas passes through
Filter above the devolatilization tank side of described device is vented, and described device is claim 1～10 times
The device of fugitive constituent in removing polymer powders described in one.
The method of fugitive constituent in 13. removing polymer powders as claimed in claim 12, its feature exists
In the fluidisation time of described devolatilization tank is 5min～60min.
The method of fugitive constituent in 14. removing polymer powders as claimed in claim 12, its feature exists
In the operating pressure of described devolatilization tank is 0.1MPa～0.7MPa.
The method of fugitive constituent in 15. removing polymer powders as claimed in claim 12, its feature exists
In the temperature of described hot nitrogen is 30 DEG C～100 DEG C.
The method of fugitive constituent in 16. removing polymer powders as claimed in claim 12, its feature exists
In in the gaseous mixture of hot nitrogen and steam, vapour volume accounts for 1%～10%.
17. as claimed in claim 12 removing polymer powders in fugitive constituent methods it is characterised in that
The temperature of described heating tape is 30 DEG C～100 DEG C.
18. as claimed in claim 12 removing polymer powders in fugitive constituent methods it is characterised in that
The rotating speed of described stirring paddle is 5r/h～300r/h.
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| CN201510450210.5A CN106397641B (en) | 2015-07-28 | 2015-07-28 | Device and method for removing volatile matters in polymer powder |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111333834A (en) * | 2020-03-05 | 2020-06-26 | 浙江恒澜科技有限公司 | Devolatilization method of nylon 6 melt |
| CN112569640A (en) * | 2020-10-27 | 2021-03-30 | 国家能源集团宁夏煤业有限责任公司 | Volatile component removing device |
| 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 |
| CN114478849A (en) * | 2021-11-05 | 2022-05-13 | 广州创特技术有限公司 | Polymer material devolatilization device |
| CN117225333A (en) * | 2023-11-10 | 2023-12-15 | 海阳科技股份有限公司 | Production device and process for extraction-free drying-free nylon slices |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2258975Y (en) * | 1995-06-14 | 1997-08-06 | 蒋大洲 | Fluidized bed granulating drying apparatus |
| CN1167772A (en) * | 1997-05-22 | 1997-12-17 | 北京燕山石油化工公司研究院 | Method and apparatus for removing residual volatile component from polymer system |
-
2015
- 2015-07-28 CN CN201510450210.5A patent/CN106397641B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2258975Y (en) * | 1995-06-14 | 1997-08-06 | 蒋大洲 | Fluidized bed granulating drying apparatus |
| CN1167772A (en) * | 1997-05-22 | 1997-12-17 | 北京燕山石油化工公司研究院 | Method and apparatus for removing residual volatile component from polymer system |
Non-Patent Citations (1)
| Title |
|---|
| 陈志敏，张万绕，李璇: "<聚丙烯D502流化床干燥器设计与应用>", <石油化工设备技术> * |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111333834A (en) * | 2020-03-05 | 2020-06-26 | 浙江恒澜科技有限公司 | Devolatilization method of nylon 6 melt |
| CN111333834B (en) * | 2020-03-05 | 2022-12-06 | 浙江恒逸石化研究院有限公司 | Devolatilization method of nylon 6 melt |
| 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 |
| CN112569640A (en) * | 2020-10-27 | 2021-03-30 | 国家能源集团宁夏煤业有限责任公司 | Volatile component removing device |
| CN112569640B (en) * | 2020-10-27 | 2022-07-26 | 国家能源集团宁夏煤业有限责任公司 | Volatile component removing device |
| CN114478849A (en) * | 2021-11-05 | 2022-05-13 | 广州创特技术有限公司 | Polymer material devolatilization device |
| CN117225333A (en) * | 2023-11-10 | 2023-12-15 | 海阳科技股份有限公司 | Production device and process for extraction-free drying-free nylon slices |
| CN117225333B (en) * | 2023-11-10 | 2024-03-15 | 海阳科技股份有限公司 | Production device and process for extraction-free drying-free nylon slices |
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