CN117507182A - Isothermal devolatilizer - Google Patents
Isothermal devolatilizer Download PDFInfo
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- CN117507182A CN117507182A CN202410015101.XA CN202410015101A CN117507182A CN 117507182 A CN117507182 A CN 117507182A CN 202410015101 A CN202410015101 A CN 202410015101A CN 117507182 A CN117507182 A CN 117507182A
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- devolatilizer
- isothermal
- heat exchange
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- 238000010438 heat treatment Methods 0.000 claims abstract description 36
- 229920000642 polymer Polymers 0.000 abstract description 18
- 239000004793 Polystyrene Substances 0.000 abstract description 4
- 229920002223 polystyrene Polymers 0.000 abstract description 4
- 239000000155 melt Substances 0.000 description 25
- 239000000463 material Substances 0.000 description 17
- 238000000034 method Methods 0.000 description 12
- 239000012071 phase Substances 0.000 description 9
- 230000008569 process Effects 0.000 description 9
- 239000012530 fluid Substances 0.000 description 6
- 239000000178 monomer Substances 0.000 description 5
- 239000003039 volatile agent Substances 0.000 description 5
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 230000006872 improvement Effects 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000004383 yellowing Methods 0.000 description 3
- 238000004220 aggregation Methods 0.000 description 2
- 230000002776 aggregation Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000006116 polymerization reaction Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000012668 chain scission Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004132 cross linking Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- JMNDBSWHIXOJLR-UHFFFAOYSA-N ethylbenzene;styrene Chemical compound CCC1=CC=CC=C1.C=CC1=CC=CC=C1 JMNDBSWHIXOJLR-UHFFFAOYSA-N 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000000289 melt material Substances 0.000 description 1
- 230000005012 migration Effects 0.000 description 1
- 238000013508 migration Methods 0.000 description 1
- 230000006911 nucleation Effects 0.000 description 1
- 238000010899 nucleation Methods 0.000 description 1
- 230000002028 premature Effects 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B13/00—Conditioning or physical treatment of the material to be shaped
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B13/00—Conditioning or physical treatment of the material to be shaped
- B29B13/02—Conditioning or physical treatment of the material to be shaped by heating
- B29B13/022—Melting the material to be shaped
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B13/00—Conditioning or physical treatment of the material to be shaped
- B29B2013/005—Degassing undesirable residual components, e.g. gases, unreacted monomers, from material to be moulded
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
Abstract
The utility model provides an isothermal devolatilizer, includes the devolatilizer body, sets up in the gas phase export that is linked together rather than the inner chamber on the devolatilizer body, the interface of being connected with the devolatilizer heater has been seted up at the top of devolatilizer body, this internal primary distribution dish that is provided with of devolatilizer, the lower part of devolatilizer body is provided with heating device, this internal isothermal heating pipe subassembly that still is provided with of devolatilizer, isothermal heating pipe subassembly is located primary distribution dish's below, isothermal heating pipe subassembly comprises a plurality of equidistant fin type heat exchange tubes of arranging, the circulation has the heat transfer medium in the fin type heat exchange tube, through setting up isothermal heating pipe subassembly, overcomes the various shortcoming of current device devolatilizer, makes the devolatilizer can better serve the polymer except polystyrene.
Description
Technical Field
The application relates to the technical field of devolatilizers, in particular to an isothermal devolatilizer.
Background
In polystyrene processes, most of the polymer exiting the reactor contains low relative molecular weight components such as monomers, solvents, and reactive oligomers, collectively referred to as volatiles. The removal of these volatiles from the polymer can improve polymer properties, recover monomers and solvents, meet health and environmental requirements, remove odor and increase the degree of polymerization. The process of devolatilizing the bulk of the polymer is referred to as devolatilization.
Polymer devolatilization is a typical two-phase process, which occurs when the vapor pressure of the component to be removed is higher than its partial pressure of gas. The difference between the two is the thermodynamic driving force of devolatilization. Clearly, the simplest way to solve this problem is to operate at high temperature (thermal stability of the polymer must be ensured) to raise the positive pressure of the volatile components, while at the same time applying a low pressure (usually a vacuum) to the gas phase to reduce the partial pressure of the volatile components.
The devolatilizer of the existing industrial device is basically a falling strip type devolatilizer. In order to reduce the residence time of the materials in the high temperature area, a devolatilization preheater is arranged at the top of the devolatilizer, and the materials enter the devolatilizer in a free falling manner. The nominal diameter of the heat exchange tube of the devolatilization heater is basically 25mm, and the falling fluid is a large fluid.
In the initial stage of devolatilization, the melt viscosity is low, the volatile component content is high, a large amount of bubbles nucleate after the material is heated, the material expands through liquid phase mass transfer and aggregation, steam is rapidly separated, the viscosity of the fallen melt material is increased, and the flow pattern is changed into laminar flow. The monomer content in the melt reaches thermodynamic equilibrium, and the temperature of the melt is reduced due to flash evaporation of the material, and the monomer content in the melt reaches thermodynamic separation limit. The melt from which most of the volatiles were removed falls to the bottom of the devolatilizer.
The melt, after removal of most of the volatiles, has reduced superheat, increased viscosity, bubble formation and growth become rate-limiting. Even with multi-stage devolatilization, the decrease in superheat is slowed down, little or no new bubbles are generated, the existing bubble growth rate is very small, and the aggregation and separation of bubbles has ceased. Because the pressure in the bubbles is different from the pressure of the gas phase above the devolatilizer, the entrained bubbles can only slowly rise against the gravity, and the mass transfer effect in the material pool at the bottom of the devolatilizer is poor. The actual pressure of the bubbles in the melt increases further with increasing liquid level. If the devolatilizer is operated at sub-atmospheric pressure, the liquid level above the bubbles is sufficient to re-compress the volatiles back into the melt phase.
Therefore, to enable better devolatilization, increasing the superheat and increasing the pressure difference are two important ways.
The prior industrial device has probably the mode of improving the superheat degree, and firstly, the temperature of the heat conduction oil of the devolatilization heater is improved. However, increasing the temperature of the heat transfer oil has an adverse effect on the polymer, and excessive crosslinking, degradation, polymer chain scission, formation of low relative molecular mass polymers and other unwanted chemical reactions can occur for the styrenic polymer with rubber added, and the product performance does not reach the standard. For polymers such as ABS, SAN, ASA, retention in high temperature areas can lead to yellowing of the material, affecting product quality and appearance. And secondly, the superheat degree is improved, and the conduction oil of the devolatilizer jacket is lifted to maintain the temperature of the melt in the devolatilizer material pool, but the heat transfer coefficient is low unless the movement of the melt is obvious. For polymers, the material can degrade, and for ABS, SAN, ASA, etc., the material at the high temperatures contacting the tank wall can accumulate, degrade and char, thereby contaminating the final product (creating black spots).
The pressure difference is increased by approximately reducing the pressure of the devolatilizer, which has strict requirements on a vacuum pump, and the existing industrial devices basically adopt graded pressure devolatilization, and most of the industrial devices are operated by a Roots vacuum pump and a liquid ring vacuum pump in series. Secondly, low boiling point substances are injected into the system to reduce the partial pressure of the system, desalted water is injected into the existing device, and the partial pressure of the materials is reduced after vaporization. The method can reduce partial pressure, but can also cause problems, namely, water can be injected into the device to be well and evenly mixed with the melt, the flow of tail gas after injection is large, the load of a vacuum pump is improved, the energy consumption is increased, and the waste water amount of the device is increased.
In view of this, there is a need for an improvement of the existing devolatilizers by those skilled in the art to solve the above-mentioned technical problems.
Disclosure of Invention
The main object of the present application is to provide an isothermal devolatilizer, by providing an isothermal heating tube assembly, which overcomes the various drawbacks of prior device devolatilizers, enabling the devolatilizer to better serve polymers other than polystyrene.
In order to achieve the above-mentioned purpose, the first aspect provides an isothermal devolatilizer, including the devolatilizer body, set up in the gas phase export that is linked together rather than the inner chamber on the devolatilizer body, the interface of being connected with the devolatilizer heater has been seted up at the top of devolatilizer body, this internal just distributing plate that is provided with of devolatilizer, the lower part of devolatilizer body is provided with heating device, this internal isothermal heating pipe subassembly that still is provided with of devolatilizer, isothermal heating pipe subassembly is located just distributing plate's below, isothermal heating pipe subassembly comprises a plurality of equidistance arrangement's fin type heat exchange tube, the circulation has heat transfer medium in the fin type heat exchange tube.
The isothermal heating pipe assembly comprises an upper heat exchange pipe assembly and a lower heat exchange pipe assembly, wherein the heat exchange pipes in the upper heat exchange pipe assembly are perpendicular to the heat exchange pipes in the lower heat exchange pipe assembly.
Further improved is that the heat exchange medium is heat conducting oil.
Further improved is that a plurality of strip falling holes are uniformly formed on the primary distribution plate.
Further improved is that the diameter A of the strip falling hole is 5-8mm, and the total area S=Npi (A/2) of the strip falling hole on the primary distribution plate 2 And when the pressure in the preheating pipe of the devolatilization heater is more than or equal to the preset pressure, wherein N is the number of the strip falling holes.
Further improved is that a baffle plate is fixedly arranged below the primary distribution plate.
Further improved is that the primary distribution plate is concave circular.
Further improved is that the heating device comprises a coil fixedly arranged on the outer side of the devolatilizer body, and a heating medium flows in the coil.
Further improved is that the coil is a heat conducting oil coil.
The heating device is further improved in that the heating device further comprises a heat conducting oil jacket fixedly arranged on the devolatilizer body, a heat conducting oil inlet and a heat conducting oil outlet are respectively formed in the heat conducting oil jacket, and inner cavities of the heat conducting oil jacket are respectively communicated with two ends of the coil pipe.
Compared with the prior art, the isothermal devolatilizer has the beneficial effects that the isothermal heating pipe assembly is arranged, so that the heat exchange area of fluid is increased, the temperature of heat conduction oil of the devolatilizing preheater can be reduced, the temperature is reduced, the residence time of a high-temperature region of a polymer can be reduced, the decomposition is less, and in addition, the yellowing of the polymer such as ABS, SAN, ASA is reduced; in addition, for removing most volatile matters, heat is continuously supplied to keep the melt at a certain temperature, so that the temperature of the melt after flash evaporation is not reduced greatly, the fin type heat exchange tube has high heat exchange efficiency, the required heat exchange area is relatively smaller, the melt is kept at a certain temperature, the melt is kept at a certain viscosity, and bubbles are easy to nucleate and coalesce; finally, because bubbles in the melt with higher viscosity are difficult to nucleate and overflow, the fin type heat exchange tube provides enough surface area to carry out strong surface renewal, and the diffusion mass transfer process can be completed in a shorter exposure time, thereby solving the defects caused by the improvement of the superheat degree and the increase of the pressure difference in order to be capable of better devolatilization in the prior art.
Drawings
FIG. 1 is a schematic diagram of the present invention;
FIG. 2 is a schematic diagram of a primary distribution plate;
FIG. 3 is a schematic view of an upper heat exchange tube assembly;
FIG. 4 is a schematic view of a lower heat exchange tube assembly;
fig. 5 is a schematic view of a fin type heat exchange tube.
Wherein: 1. an interface; 2. a devolatilizer body; 3. a fin type heat exchange tube; 4. an upper heat exchange tube assembly; 5. a lower heat exchange tube assembly; 6. a baffle; 7. a primary distribution plate; 8. a gas phase outlet; 9. a heat conducting oil jacket; 10. a coiled pipe.
Detailed Description
In order to better understand the embodiments of the present application, the following description will clearly and completely describe the embodiments of the present application, and it is apparent that the described embodiments are only some embodiments of the present application, not all embodiments. All other embodiments, which can be made by one of ordinary skill in the art based on the embodiments herein without making any inventive effort, shall fall within the scope of the present application.
It should be noted that the terms "first," "second," and the like in the description and in the claims are used for distinguishing between similar objects and not necessarily for describing a particular sequential or chronological order. It is to be understood that the data so used may be interchanged where appropriate in order to describe the embodiments of the present application described herein. Furthermore, the terms "comprises," "comprising," and "having," and any variations thereof, are intended to cover a non-exclusive inclusion, such that a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements expressly listed but may include other steps or elements not expressly listed or inherent to such process, method, article, or apparatus.
Also, some of the terms described above may be used to indicate other meanings in addition to orientation or positional relationships, for example, the term "upper" may also be used to indicate some sort of attachment or connection in some cases. The specific meaning of these terms in this application will be understood by those of ordinary skill in the art as appropriate.
In addition, the term "plurality" shall mean two as well as more than two.
It should be noted that, in the case of no conflict, the embodiments and features in the embodiments may be combined with each other. The present application will be described in detail with reference to examples.
As shown in fig. 1-5, an isothermal devolatilizer comprises a devolatilizer body 2 and a gas phase outlet 8 which is arranged on the devolatilizer body 2 and communicated with the inner cavity of the devolatilizer body, wherein an interface 1 which is connected with a devolatilizer heater is arranged at the top of the devolatilizer body 2, a primary distribution plate 7 is arranged in the devolatilizer body 2, a heating device is arranged at the lower part of the devolatilizer body 2, an isothermal heating pipe component is also arranged in the devolatilizer body 2 and is positioned below the primary distribution plate 7, the isothermal heating pipe component is composed of a plurality of fin heat exchange pipes 3 which are arranged at equal intervals, and heat exchange media, preferably, heat transfer oil is circulated in the fin heat exchange pipes 3.
The working process comprises the following steps: firstly, materials enter a devolatilizer body 2 from an interface 1 after being preheated by a devolatilizing heater, and the materials are low in viscosity and high in monomer content in the initial devolatilizing stage, bubbles are easy to nucleate, bubble nucleates and overflows in the strip falling process to form gas phase and enter a gas phase space to be separated from a melt, a primary distribution plate 7 is arranged for facilitating the overflow of the bubbles, as shown in fig. 2, a plurality of strip falling holes are uniformly formed in the primary distribution plate 7, the diameter A of the strip falling holes is 5-8mm, and the total area S=Npi (A/2) of the strip falling holes in the primary distribution plate 7 2 When the device is used, the pressure in the preheating pipe of the devolatilization heater is more than or equal to the preset pressure, wherein N is the number of strip falling holes, namely the aperture and the number are determined according to the productivity of the device, fluid from the polymerization kettle enters the devolatilization heater after being pressurized by a pump, the devolatilization heater is arranged at the top of the devolatilization heater, and the primary distribution plate 7 is positioned at the lower outlet of the devolatilization heater. The total hole area of the initial distribution plate 7 is controlled, so that certain pressure can be kept in the preheating pipe to avoid the premature devolatilization phenomenon in the devolatilizer preheater pipe, and falling strips can be well formed. The fine strip can enable bubbles in the fine strip to overflow rapidly so as to remove most materials.
For polystyrene system, the melt contains about 20% of volatile component (mainly ethylbenzene styrene), the melt is heated to 240 ℃ and enters a devolatilizer of 4kPaA, the initial distribution plate 7 is added, the falling strips are thinned, and the volatile component content in the melt can be reduced from 1-2% to 0.5-0.8%.
After the material is heated by a devolatilization heater and subjected to strip falling flash evaporation, temperature drop is inevitably formed, at the moment, volatile components in the fluid are reduced, bubble nucleation is little, and bubble migration is difficult due to the increase of solution viscosity. In order to overcome these disadvantages, as shown in fig. 3, 4 and 5, isothermal heating pipes are provided, the isothermal heating pipes are fin type heat exchange pipes 3, heat conduction oil is utilized in the pipes for heating, the fin type heat exchange pipes are arranged according to a certain gap, the upper layer and the lower layer are arranged in a 90-degree crossed and transverse mode, namely, the isothermal heating pipe assembly comprises an upper layer heat exchange pipe assembly 4 and a lower layer heat exchange pipe assembly 5, the heat exchange pipes in the upper layer heat exchange pipe assembly 4 are perpendicular to the heat exchange pipes in the lower layer heat exchange pipe assembly 5, the heat exchange pipes are provided, the heat exchange area of fluid is increased, the heat conduction oil temperature of the devolatilization preheater can be reduced, the temperature is reduced, the retention time of a polymer in a high temperature area can be reduced, the decomposition is less, and in addition, the yellowing of the polymer such as ABS, SAN, ASA is reduced. Secondly, for removing most volatile matters, heat is continuously supplied, so that the melt keeps a certain temperature, the temperature of the melt after flash evaporation is not reduced greatly, the fin type heat exchange tube 3 has high heat exchange efficiency, the required heat exchange area is relatively small, a certain temperature is kept, and the melt has a certain viscosity, so that bubbles are easy to nucleate and coalesce. Thirdly, because bubbles in the melt with higher viscosity are difficult to nucleate and overflow, the fin type heat exchange tube 3 provides enough surface area to carry out strong surface renewal, the diffusion mass transfer process can be completed in a shorter exposure time, and the arrangement of the isothermal heat exchange tube can reduce the volatile matters in the melt from 0.5-0.8% to 0.08-0.1%.
In addition, in order to fall the material after falling the strip on the isothermal heat exchange tube assembly, baffle 6 is fixedly arranged below the primary distribution plate 7, and in order to fall the material better, the primary distribution plate 7 is in a concave circular shape.
As shown in fig. 1, in this embodiment, preferably, the heating device includes a coil 10 fixedly disposed on the outer side of the devolatilizer body 2, a heating medium is circulated in the coil 10, the heating medium preferably adopts heat conduction oil, the coil 10 is a heat conduction oil pan 10, the heating device further includes a heat conduction oil jacket 9 fixedly disposed on the devolatilizer body 2, a heat conduction oil inlet and a heat conduction oil outlet are respectively disposed on the heat conduction oil jacket 9, and an inner cavity of the heat conduction oil jacket 9 is respectively communicated with two ends of the coil 10, and it is noted that the heat conduction oil in the heat exchange tube may be communicated with the heat conduction oil in the heating device, that is, the same set of heat conduction oil supply system is used, or the two sets of independent heat conduction oil supply systems may be separately disposed, that is, separately disposed.
The foregoing description is only of the preferred embodiments of the present application and is not intended to limit the same, but rather, various modifications and variations may be made by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principles of the present application should be included in the protection scope of the present application.
Claims (10)
1. The utility model provides an isothermal devolatilizer, includes the devolatilizer body, sets up in the gas phase export that is linked together rather than the inner chamber on the devolatilizer body, the interface of being connected with the devolatilizer heater has been seted up at the top of devolatilizer body, this internal primary distribution dish that is provided with of devolatilizer, the lower part of devolatilizer body is provided with heating device, its characterized in that, this internal isothermal heating pipe subassembly that still is provided with of devolatilizer, isothermal heating pipe subassembly is located the below of primary distribution dish, isothermal heating pipe subassembly comprises a plurality of equidistance arrangement's fin type heat exchange tube, the circulation has the heat transfer medium in the fin type heat exchange tube.
2. The isothermal devolatilizer as recited in claim 1, wherein: the isothermal heating pipe assembly comprises an upper heat exchange pipe assembly and a lower heat exchange pipe assembly, and the heat exchange pipes in the upper heat exchange pipe assembly are perpendicular to the heat exchange pipes in the lower heat exchange pipe assembly.
3. The isothermal devolatilizer as recited in claim 1, wherein: the heat exchange medium is heat conduction oil.
4. The isothermal devolatilizer as recited in claim 1, wherein: a plurality of strip falling holes are uniformly formed in the primary distribution plate.
5. The isothermal devolatilizer as recited in claim 4 wherein: the diameter A of the strip falling hole is 5-8mm, and the total area S=Npi (A/2) of the strip falling hole on the primary distribution plate 2 And when the pressure in the preheating pipe of the devolatilization heater is more than or equal to the preset pressure, wherein N is the number of the strip falling holes.
6. The isothermal devolatilizer as recited in claim 1, wherein: a baffle is fixedly arranged below the primary distribution plate.
7. The isothermal devolatilizer as recited in claim 6 wherein: the primary distribution plate is concave round.
8. The isothermal devolatilizer as recited in claim 1, wherein: the heating device comprises a coil fixedly arranged on the outer side of the devolatilizer body, and a heating medium flows in the coil.
9. The isothermal devolatilizer as recited in claim 8 wherein: the coil pipe is a heat conduction oil disc pipe.
10. The isothermal devolatilizer as recited in claim 9, wherein: the heating device further comprises a heat conducting oil jacket fixedly arranged on the devolatilizer body, a heat conducting oil inlet and a heat conducting oil outlet are respectively formed in the heat conducting oil jacket, and inner cavities of the heat conducting oil jacket are respectively communicated with two ends of the coil pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202410015101.XA CN117507182A (en) | 2024-01-05 | 2024-01-05 | Isothermal devolatilizer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202410015101.XA CN117507182A (en) | 2024-01-05 | 2024-01-05 | Isothermal devolatilizer |
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| CN117507182A true CN117507182A (en) | 2024-02-06 |
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| CN202410015101.XA Pending CN117507182A (en) | 2024-01-05 | 2024-01-05 | Isothermal devolatilizer |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108466383A (en) * | 2018-03-26 | 2018-08-31 | 天华化工机械及自动化研究设计院有限公司 | A kind of PP GRANULES material takes off the system and its application process of VOC |
| CN112321754A (en) * | 2020-09-07 | 2021-02-05 | 万华化学集团股份有限公司 | Polymer solution devolatilization device and method |
| CN215087183U (en) * | 2021-03-30 | 2021-12-10 | 上海东庚化工技术有限公司 | Continuous polymer tackifying reactor |
| CN217828977U (en) * | 2022-08-05 | 2022-11-18 | 启东市巨龙石油化工装备有限公司 | PS devolatilization device |
| CN115624791A (en) * | 2022-09-19 | 2023-01-20 | 浙江理工大学 | Falling film devolatilizer with multilayer crossed horizontal tubes |
| CN219963973U (en) * | 2023-03-22 | 2023-11-07 | 浙江智英石化技术有限公司 | Devolatilizer |
-
2024
- 2024-01-05 CN CN202410015101.XA patent/CN117507182A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108466383A (en) * | 2018-03-26 | 2018-08-31 | 天华化工机械及自动化研究设计院有限公司 | A kind of PP GRANULES material takes off the system and its application process of VOC |
| CN112321754A (en) * | 2020-09-07 | 2021-02-05 | 万华化学集团股份有限公司 | Polymer solution devolatilization device and method |
| CN215087183U (en) * | 2021-03-30 | 2021-12-10 | 上海东庚化工技术有限公司 | Continuous polymer tackifying reactor |
| CN217828977U (en) * | 2022-08-05 | 2022-11-18 | 启东市巨龙石油化工装备有限公司 | PS devolatilization device |
| CN115624791A (en) * | 2022-09-19 | 2023-01-20 | 浙江理工大学 | Falling film devolatilizer with multilayer crossed horizontal tubes |
| CN219963973U (en) * | 2023-03-22 | 2023-11-07 | 浙江智英石化技术有限公司 | Devolatilizer |
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