CN103752027A - Flash tank and treatment process after production of ethylene-propylene copolymerized elastomer - Google Patents
Flash tank and treatment process after production of ethylene-propylene copolymerized elastomer Download PDFInfo
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- CN103752027A CN103752027A CN201410030671.2A CN201410030671A CN103752027A CN 103752027 A CN103752027 A CN 103752027A CN 201410030671 A CN201410030671 A CN 201410030671A CN 103752027 A CN103752027 A CN 103752027A
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- flash tank
- coil pipe
- tank
- tank body
- propylene
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Abstract
The invention discloses a flash tank and a treatment process after production of an ethylene-propylene copolymerized elastomer. The flash tank comprises a tank body, wherein a feed port is arranged on the top of the tank body, a discharge port is arranged on the bottom of the tank body, an inner coil pipe capable of spiraling upwards is arranged on the lower part in the tank body, an outer coil pipe is arranged on the outer part of the tank body and around the outer wall of the tank body, and an inlet and an outlet of the inner coil pipe pass through the lower part of the tank body and extend from the flash tank. The treatment process comprises the following steps of feeding the materials, recovering ethylene and propylene at a medium pressure, settling the materials, furthermore recovering ethylene and propylene, and recovering the materials. The flash tank has the following beneficial effects that the temperature in the flash tank is relatively uniform, fused discharge of the materials is facilitated, and materials are prevented from being scaled on a polymerizer. The liquid-phase materials are separated from the gas-phase materials. The recovery treatment process can meet the combustible gas treatment requirement, and prevent the combustible gas from being at the explosive limit and furthermore prevent hidden troubles caused by the combustible gas.
Description
Technical field
The present invention relates to a kind of flash tank and for ethene-copolymerization of propylene elastomer produce after treatment process.
Background technology
Ethene-copolymerization of propylene elastomer is the copolymer of ethene and propylene, and ethylene contents is between 8～20%.Compare traditional ethylene-propylene copolymer, its ethylene contents is higher, compares traditional EP rubbers ethylene contents (being greater than 50%), and this value is low again.Special propylene-ethylene hypocrystalline structure can strengthen durability, improve aesthetic effect and multifunctionality, has more pliability during low temperature, and high filling capacity and density are lower lighter.
Due to the more feature of the random thing of ethene-copolymerization of propylene elastomer structure, itself is easily clamminess copolymer.First Exxon Mobil chemical company has released this kind of propylene-based elastomeric (propylene-based elastomer, PBE).This product is to adopt the Exxpol of the said firm solwution method metallocene technology, and under high temperature, reaction generates.At high temperature, reaction product exists with molten condition, there will not be the problem of postprocessing working procedures sizing.
Produce this kind of elastomer except solving the problem of catalyst, also will solve the problem that copolymer structure self is easily clamminess.The ethylene-propylene copolymer elastomer post processing of Exxon Mobil Corporation adopts solution polymerization → solvent removal → finished product high temperature to extrude processing; The discharging technology of ENI company suspension method EP rubbers is stripping → MONOMER RECOVERY and refining → finished product processing, and finished product pack processing is containing dehydration extruding and mechanical drying equipment.The operation of both ethylene-propylene copolymer post processings is all more complicated.
The elastomer that applicant produces is used Ziegler-Natta catalyst, using liquid propylene as suspension, under low temperature, reacts, and product particle is insoluble to liquid propylene; Under low temperature, suspended state is difficult for sticky polymeric kettle.Can solve so sticky still problem, but after discharging recovery, can not adopt polyacrylic normal temperature binder feed bin discharge method, adopt special processing method and special equipment just can complete discharging operation.
Summary of the invention
The object of this invention is to provide a kind of flash tank, make the elastomer can be with the discharging of heat fusing state.
For addressing the above problem, the technical solution used in the present invention is: a kind of flash tank, comprise tank body, described tank body top arranges charging aperture, bottom arranges discharging opening, bottom in tank body arranges spiralling inner coil pipe, and the outside of tank body arranges outer coil pipe around tank wall, and the entrance and exit of described inner coil pipe stretches out outside flash tank through tank body lower part.
As a further improvement on the present invention, the pitch of described inner coil pipe bottom is little, and the pitch on inner coil pipe top is large.
As a further improvement on the present invention, the pitch of described inner coil pipe bottom is 100mm, and the pitch on inner coil pipe top is 150mm, and the lowermost end of inner coil pipe is apart from discharging opening 150mm.
As a further improvement on the present invention, described outer coil pipe has three, is separately positioned on the outer wall of tank body upper, middle and lower.
As a further improvement on the present invention, described flash tank top is cylindrical, and bottom is conical.
Another object of the present invention is to provide the treatment process after a kind of aforesaid flash tank is produced for ethene-copolymerization of propylene elastomer, solves in prior art ethene-copolymerization of propylene elastomer and produces in last handling process the technological deficiency of wall built-up, sticky still because copolymer self is clamminess.
For addressing the above problem, the technical solution used in the present invention is: the treatment process after aforesaid flash tank is produced for ethene-copolymerization of propylene elastomer, comprise the steps,
A. blowing, is connected flash tank, after polymeric kettle polymerization finishes with polymeric kettle bottom, open polymerization kettle bottom valve, and to keep polymerization kettle bottom valve be open mode, flash tank and polymeric kettle are communicated with up and down, the material that after polymerization, ethene, propylene and product mix is put into flash tank;
B. in, push back receipts, maintenance polymerization kettle bottom valve is open mode, by ethene and the propylene of gas phase in material in the middle pressure recovery line recovery flash tank on polymeric kettle, guarantees in flash tank that temperature is within the scope of 5～10 ℃ after this process completes;
C. sedimentation material, in push back and receive after gas-phase propene finishes, standing 5～10 minutes, the material of ethene to be removed and propylene was settled down to flash tank bottom, closes polymerization kettle bottom valve;
D. further reclaim ethene and propylene, by the pipeline that connects flash tank, carry out the recovery of low pressure-negative pressure-vacuum process, further remove fuel gas to its volume content and be less than 2%, the pipeline being specially by connecting flash tank vacuumizes processing to flash tank;
E. material discharging passes into steam material is heated in the inner coil pipe of flash tank and outer coil pipe, makes material in molten condition, from flash tank bottom, flows out and reclaims.
As a further improvement on the present invention, the volume of described polymeric kettle is 14m
3, the volume of flash tank is 13m
3.
As a further improvement on the present invention, in step b, when temperature in flash tank is during lower than 5 ℃, in the inner coil pipe of polymeric kettle and flash tank, pass into recirculated water, to guarantee that flash tank temperature is not less than 5 ℃.
The invention has the beneficial effects as follows: be arranged on the inner coil pipe of flash tank inside spin rising and be arranged on the outer coil pipe outside flash tank, increase the heat in flash tank and changed area, make thoroughly melting of material, the pitch on inner coil pipe top is large, the pitch of bottom is little, meet the variation of the state of material, facilitate the material of molten condition to flow out from flash tank bottom, outer coil pipe arranges three, respectively on the top of flash tank outer wall, middle part and bottom, pass into the steam of uniform temp, can guarantee that middle part, flash tank top is identical with the temperature of bottom, be that in flash tank, temperature is more even, more be conducive to the melting of material, avoid sticky still wall.
This technique adopts inside and outside coil pipe Steam Heating scheme to flash tank, in conjunction with special flash vaporization kettle structure, by polymeric kettle-flash tank large space recovery process, propylene monomer is reclaimed, then replace by flash distillation, and combustible gas is brought down below to 0.2%.After combustible gas is handled, by coil heat exchange, product melting is flowed out, then become finished product through follow-up comminutor extruding pelletization.So just solved discharging problem of viscosity, the problem of solved material wall built-up, gluing still, has also avoided using complicated subsequent treatment workshop section.Improvement cost is low, simple to operation.Recovery processing technique of the present invention will reach combustible gas processing requirements, prevents fuel gas in explosion limit and the potential safety hazard that produces.
Accompanying drawing explanation
Fig. 1 is the structural representation of flash tank in the present invention.
The specific embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described further.
Flash tank as shown in Figure 1, comprise tank body 1, described tank body 1 top arranges charging aperture 2, the top of tank body 1 is cylindrical, the bottom of tank body 1 is conical, and tank body 1 bottom arranges discharging opening 3, and the bottom in tank body 1 arranges spiralling inner coil pipe 4, the outside of tank body 1 arranges outer coil pipe around tank wall, and the entrance and exit of described inner coil pipe 4 stretches out outside flash tank 1 through tank body lower part.
Described inner coil pipe 4 upper and lower 13 encloses spiral setting from bottom to top, the spacing (pitch) that the most beneath upwards to the of circle ten of inner coil pipe enclosed two adjacent rings is 100mm, from the tenth circle, to the spacing (pitch) of the top one circle two adjacent rings, be 150mm, the inner coil pipe from bottom to top entrance of every circle is connected with the outlet of a circle above, topmost one ensphere mouthful and bottom the outlet of a circle from tank body 1 distance from bottom discharging opening 250mm-450mm, pass tank body 1 and extend into flash tank outside, the every circle of inner coil pipe 4 is fixed on tank body 1 inside by being welded on the angle steel of flash tank inwall, the inner coil pipe 4 of a bottom circle is 150mm with the distance of discharging opening 3.
Described outer coil pipe has three, is respectively the upper coil pipe 5 that is wrapped in tank body 1 top, is wrapped in the middle coil pipe 6 and the lower coil pipe 7 that is wrapped in tank body 1 bottom at tank body 1 middle part, on tank body 1 outer wall between described upper coil pipe 5 and middle coil pipe 6, hanger 8 is set.
While using flash tank of the present invention, the charging aperture of flash drum overhead 2 and the polymeric kettle outlet of polymeric kettle (prior art, not shown) bottom are connected, the discharging opening 3 of flash tank bottom connects comminutor or material memory device.
Treatment process after foregoing flash tank is produced for ethene-copolymerization of propylene elastomer, comprises following step:
A. blowing, is connected flash tank, after polymeric kettle polymerization finishes with polymeric kettle bottom, open polymerization kettle bottom valve, and to keep polymerization kettle bottom valve be open mode, flash tank and polymeric kettle are communicated with up and down, the material that after polymerization, ethene, propylene and product mix is put into flash tank.
B. in, push back receipts, maintenance polymerization kettle bottom valve is open mode, by ethene and the propylene of gas phase in material in the middle pressure recovery line recovery flash tank on polymeric kettle, guarantees in flash tank that temperature is within the scope of 5～10 ℃ after this process completes.
C. sedimentation material, in push back and receive after gas-phase propene finishes, standing 5～10 minutes, the material of ethene to be removed and propylene was settled down to flash tank bottom, closes polymerization kettle bottom valve.
D. further reclaim ethene and propylene, by the pipeline that connects flash tank, carry out the recovery of low pressure-negative pressure-vacuum process, further remove fuel gas to its volume content and be less than 2%, the pipeline being specially by connecting flash tank vacuumizes processing to flash tank.
E. material discharging passes into steam material is heated in the inner coil pipe of flash tank and outer coil pipe, makes material in molten condition, from flash tank bottom, flows out and reclaims.
In foregoing step, the volume of polymeric kettle is 14m
3, the volume of flash tank is 13m
3.In step b, when temperature in flash tank is during lower than 5 ℃, in polymeric kettle and flash tank inner coil pipe, pass into recirculated water, to guarantee that flash tank temperature is not less than 5 ℃.
Foregoing polymeric kettle is prior art, in this description, does not elaborate, also not shown in figures.What in other all descriptions of the present invention, be not specifically noted is prior art; or can realize by prior art; should be understood that; for those of ordinary skills; can be improved according to the above description or convert, and all these improvement and conversion all should belong to the protection domain of claims of the present invention.
Claims (8)
1. a flash tank, it is characterized in that: comprise tank body, described tank body top arranges charging aperture, bottom arranges discharging opening, bottom in tank body arranges spiralling inner coil pipe, the outside of tank body arranges outer coil pipe around tank wall, and the entrance and exit of described inner coil pipe stretches out outside flash tank through tank body lower part.
2. flash tank according to claim 1, is characterized in that: the pitch of described inner coil pipe bottom is little, and the pitch on inner coil pipe top is large.
3. flash tank according to claim 2, is characterized in that: the pitch of described inner coil pipe bottom is 100mm, and the pitch on inner coil pipe top is 150mm, and the lowermost end of inner coil pipe is apart from discharging opening 150mm.
4. flash tank according to claim 1, is characterized in that: described outer coil pipe has three, is separately positioned on the outer wall of tank body upper, middle and lower.
5. flash tank according to claim 1, is characterized in that: described flash tank top is cylindrical, and bottom is conical.
6. the flash tank as described in any one in claim 1 to 4 is used for the treatment process after ethene-copolymerization of propylene elastomer is produced, and it is characterized in that: comprise the steps,
A. blowing, is connected flash tank, after polymeric kettle polymerization finishes with polymeric kettle bottom, open polymerization kettle bottom valve, and to keep polymerization kettle bottom valve be open mode, flash tank and polymeric kettle are communicated with up and down, the material that after polymerization, ethene, propylene and product mix is put into flash tank;
B. in, push back receipts, maintenance polymerization kettle bottom valve is open mode, by ethene and the propylene of gas phase in material in the middle pressure recovery line recovery flash tank on polymeric kettle, guarantees in flash tank that temperature is within the scope of 5～10 ℃ after this process completes;
C. sedimentation material, in push back and receive after gas-phase propene finishes, standing 5～10 minutes, the material of ethene to be removed and propylene was settled down to flash tank bottom, closes polymerization kettle bottom valve;
D. further reclaim ethene and propylene, by the pipeline that connects flash tank, carry out the recovery of low pressure-negative pressure-vacuum process, further remove fuel gas to its volume content and be less than 2%, the pipeline being specially by connecting flash tank vacuumizes processing to flash tank;
E. material discharging passes into steam material is heated in the inner coil pipe of flash tank and outer coil pipe, makes material in molten condition, from flash tank bottom, flows out and reclaims.
7. technique according to claim 6, is characterized in that: the volume of described polymeric kettle is 14m
3, the volume of flash tank is 13m
3.
8. technique according to claim 6, is characterized in that: in step b, when temperature in flash tank is during lower than 5 ℃, pass into recirculated water, to guarantee that flash tank temperature is not less than 5 ℃ in the outer coil pipe of flash tank.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410030671.2A CN103752027B (en) | 2014-01-22 | 2014-01-22 | A kind of flash tank and the treatment process after producing for ethene-propylene copolymer elastomers thereof |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410030671.2A CN103752027B (en) | 2014-01-22 | 2014-01-22 | A kind of flash tank and the treatment process after producing for ethene-propylene copolymer elastomers thereof |
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| CN103752027A true CN103752027A (en) | 2014-04-30 |
| CN103752027B CN103752027B (en) | 2015-09-09 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108067009A (en) * | 2018-01-31 | 2018-05-25 | 丹阳同泰化工机械有限公司 | A kind of high efficient gas and liquid separator |
| CN108211994A (en) * | 2018-02-07 | 2018-06-29 | 北京环清环境科技有限公司 | A kind of organic fertilizer hydrolysis device |
| CN111389330A (en) * | 2020-03-25 | 2020-07-10 | 河南神马尼龙化工有限责任公司 | Reaction temperature stability maintaining system of adipic acid production system by nitric acid oxidation method |
| CN113827994A (en) * | 2021-09-26 | 2021-12-24 | 金澳科技（湖北）化工有限公司 | Flash evaporation optimization method for polymerization powder |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108067009A (en) * | 2018-01-31 | 2018-05-25 | 丹阳同泰化工机械有限公司 | A kind of high efficient gas and liquid separator |
| CN108211994A (en) * | 2018-02-07 | 2018-06-29 | 北京环清环境科技有限公司 | A kind of organic fertilizer hydrolysis device |
| CN111389330A (en) * | 2020-03-25 | 2020-07-10 | 河南神马尼龙化工有限责任公司 | Reaction temperature stability maintaining system of adipic acid production system by nitric acid oxidation method |
| CN113827994A (en) * | 2021-09-26 | 2021-12-24 | 金澳科技（湖北）化工有限公司 | Flash evaporation optimization method for polymerization powder |
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| CN103752027B (en) | 2015-09-09 |
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