CN110614732B - High-performance processing technology and equipment for supercritical fluid micro-explosion disentangled polymer - Google Patents
High-performance processing technology and equipment for supercritical fluid micro-explosion disentangled polymer Download PDFInfo
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- CN110614732B CN110614732B CN201910989169.7A CN201910989169A CN110614732B CN 110614732 B CN110614732 B CN 110614732B CN 201910989169 A CN201910989169 A CN 201910989169A CN 110614732 B CN110614732 B CN 110614732B
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C49/00—Blow-moulding, i.e. blowing a preform or parison to a desired shape within a mould; Apparatus therefor
- B29C49/071—Preforms or parisons characterised by their configuration, e.g. geometry, dimensions or physical properties
-
- 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
- B29B11/00—Making preforms
- B29B11/06—Making preforms by moulding the material
- B29B11/10—Extrusion moulding
-
- 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
- B29B11/00—Making preforms
- B29B11/14—Making preforms characterised by structure or composition
-
- 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
- B29B9/00—Making granules
- B29B9/02—Making granules by dividing preformed material
- B29B9/06—Making granules by dividing preformed material in the form of filamentary material, e.g. combined with extrusion
-
- 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
- B29B9/00—Making granules
- B29B9/12—Making granules characterised by structure or composition
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/14—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor characterised by the particular extruding conditions, e.g. in a modified atmosphere or by using vibration
- B29C48/144—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor characterised by the particular extruding conditions, e.g. in a modified atmosphere or by using vibration at the plasticising zone
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C2949/00—Indexing scheme relating to blow-moulding
- B29C2949/07—Preforms or parisons characterised by their configuration
- B29C2949/0715—Preforms or parisons characterised by their configuration the preform having one end closed
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29K—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES B29B, B29C OR B29D, RELATING TO MOULDING MATERIALS OR TO MATERIALS FOR MOULDS, REINFORCEMENTS, FILLERS OR PREFORMED PARTS, e.g. INSERTS
- B29K2027/00—Use of polyvinylhalogenides or derivatives thereof as moulding material
- B29K2027/06—PVC, i.e. polyvinylchloride
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Physics & Mathematics (AREA)
- Geometry (AREA)
- Manufacturing & Machinery (AREA)
- Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
- Extrusion Moulding Of Plastics Or The Like (AREA)
Abstract
The invention discloses a high-performance processing technology and equipment for a supercritical fluid micro-explosion disentangled polymer, which are characterized in that a supercritical fluid is immersed into a molecular chain group to perform micro-explosion disentanglement on a chain segment while aligning the chain segment, and the alignment effect after micro-explosion is kept by mixing and exhausting at the same time, and gas is secondarily aligned and exhausted; completely orienting chain groups in the material by matching with a lamination process to obtain a texture structure material; the reinforcing material finally obtained is free of bubbles. The equipment comprises a drying system, an impregnating system, a micro-explosion system, an exhaust extrusion system, a temperature control system and other basic systems. The processing technology and equipment can continuously and efficiently disentangle the polymer chain groups/primary particles in a low-cost way by utilizing a supercritical fluid micro-explosion mode, and can keep the chain segments which are oriented by micro-explosion to smoothly enter the next-stage orientation in a mechanical exhaust way, and the material which does not contain bubbles and has higher orientation degree and orderly molecular chain arrangement is formed by combining a lamination extrusion technology, so that the usability of the polymer is optimized.
Description
Technical Field
The invention relates to the field of processing and forming of high polymer materials and advanced manufacturing, in particular to a high-performance processing technology and equipment for a supercritical fluid micro-explosion disentangled polymer.
Background
The macro molecular chain of the amorphous high molecular polymer is bent due to the rotation effect in the chain link in the polymerization process, so that a macro structure in the forms of random coil, chain ball and the like is formed; in the application process, it is generally desirable to obtain regular structures such as orientation states or weaving states or orderly structures to improve the performance of the product. The existing processing modes of the high polymer such as mixing, unidirectional stretching, bidirectional stretching and the like can obtain a certain effect in the processing of materials, but the processing modes of the high polymer still have segment orientation rather than molecular chain orientation for a part of the materials such as PVC and the like, and a part of the segments still exist in an agglomerated form, so that the physical properties of the high polymer cannot be completely reflected macroscopically. In view of this, it is important to realize further orientation after the polymer molecular chain or long chain segment which is not easy to be opened in the ordinary processing mode is completely opened.
Supercritical fluids, when at different pressures and temperatures, typically exhibit various modes, such as gaseous, liquid, and solid states. In particular to supercritical carbon dioxide, which has very unique physicochemical properties, and has the characteristics of large diffusion coefficient, small viscosity and the like in a supercritical state. The porous solid material has high diffusivity, reduces mass transfer resistance, is particularly beneficial to extraction of compounds in porous loose solid materials and cellular materials, and has good impregnation effect; and because it is particularly sensitive to operating conditions (e.g., pressure, temperature), this provides convenience for flexibility and adjustability of operation; meanwhile, the modified polyurethane has low chemical activity and toxicity, stable chemical property and green safety. Therefore, the supercritical fluid is widely applied to the aspects of high polymer material molding and biological material processing.
In the molding of polymeric materials, supercritical fluids are commonly used as blowing agents to mold foamed materials. The foaming process has better advantage on the light weight of the product, but reduces the original strength of the product. Typical foaming includes both direct foaming and intermittent foaming. The direct foaming is to obtain a foaming material by mixing supercritical fluid into a melted high polymer melt, then releasing pressure, expanding, cooling and shaping, and the problems of uneven dispersion of foam cores, low foam core refinement degree caused by easy aggregation of fluid and the like generally exist; the intermittent foaming is a foaming material obtained by foaming again after pre-foaming, and the pre-foaming is carried out by immersing supercritical fluid into the material by an immersion method, so that the dispersion is good, and the bubble refinement degree is high. However, both foaming processes are relatively static foams, which cool directly after the material is spread, so that bubbles remain in the product. And the foaming process only uses gas to prop up the molecular chains without subsequent treatment, when the bubble pressure is consistent with the external pressure and is not cooled in time, the molecular chains return to a loose state, and the orientation effect of the bubbles is invalid. Related processes similar to foaming have not been used as an auxiliary orientation or the like, and a stretching but not retaining an orientation effect is formed.
It is therefore necessary to open the molecular chains and leave them oriented for subsequent stretch orientation to give a stronger material.
Taking polyvinyl chloride (PVC) material as an example: polyvinyl chloride (PVC) materials have stable physical and chemical properties, are not easy to corrode by acid and alkali, and have good flame retardant property, and are often used as raw materials of flame retardant products. PVC can be changed from hard to soft by adding a plasticizer, is easier to process and form by various processing modes, and waste can be recycled and reused, so that the PVC is an environment-friendly material which is used in various places in modern industry and life. The processing of polyvinyl chloride comprises a plurality of modes such as mixing, injection molding, extrusion stretch molding, film blowing stretch molding and the like, but the long chain of the polyvinyl chloride is generally coated by taking an initiator as a center to form primary particles in the polymerization process, and the primary particle chain is difficult to open and intertwine with other molecular chains in the common processing mode, so that the excellent performance of the molded product cannot be fully reflected. Much research has been done in China on the aspect of unwinding polyvinyl chloride. The lamination methods described in the patent ZL200910237622 and the patent ZL2014101359933 can strengthen the multi-time stretching orientation of the molten material in a uniform lamination mode, and the lamination methods have great advantages in the aspects of film blowing and extrusion granulation of PVC, but still cannot completely open the primary particles of the PVC. Aiming at the problems, the invention provides a high-performance processing technology of a supercritical fluid micro-explosion disentangled polymer, which opens a high polymer chain group from the primary particle layer surface in a supercritical fluid micro-explosion mode to form a loose long chain capable of being entangled with other long chains, and simultaneously cooperates with a lamination extrusion technology to further release the potential performance of the high polymer.
Disclosure of Invention
Aiming at the problem that the prior art cannot completely disentangle high polymer primary particles and cannot continuously optimize the material service performance, the invention provides a supercritical fluid micro-explosion disentangled polymer high-performance processing technology and equipment, and the invention is explained by the detailed description of the processing of an example material (PVC). The main innovation points of the invention are as follows: the supercritical fluid is immersed into the molecular chain groups to be micro-exploded and twined, meanwhile, the chain segments are oriented, and the orientation effect after micro-explosion is kept in a mode of mixing and exhausting (mechanical exhausting) and simultaneously, the gas is secondarily oriented and exhausted; completely orienting chain groups in the material by matching with a lamination process to obtain a texture structure material; the reinforcing material finally obtained is free of bubbles. The method is characterized in that a supercritical fluid is utilized to open single molecular chain groups, then mixing and exhausting are carried out in a molten state, and lamination reinforcement orientation is carried out, so that a high-performance material without bubbles is obtained, and corresponding manufacturing equipment is improved according to the process design.
The present invention is theoretically capable of untangling the coated long chains of the PVC primary particles or increasing the orientation of the coated long chains with the surrounding long chains to release the original performance potential of the PVC material and enhance the physical strength of the molded article thereof.
The process route of the high-performance processing technology and equipment of the supercritical fluid micro-explosion disentangled polymer comprises the following steps: drying materials, low-temperature high-pressure dipping, heating micro-explosion, mixing and exhausting, and laminating and extruding. The basic idea of the process route is that primary particles of materials are disentangled in a supercritical fluid micro-explosion mode to form loose molecular chains with chain segment orientation, then the disentangled particles are deformed in a mode of mixing and exhausting (mechanical exhausting) at the same time, the chain segment orientation effect is kept, secondary chain segment orientation is carried out, all gases in the materials are exhausted, and finally the molecular chains are further oriented through a lamination process to obtain the texture structure material.
The drying materials in the process route are all the unbound water in the materials and are evaporated, so that the influence of the unbound water on the impregnation effect in the impregnation process is prevented.
The low-temperature high-pressure impregnation means that the dried material is added into an impregnation kettle through a metering system, supercritical CO2 is added by a supercritical fluid injection system, and the internal environment of the impregnation kettle is kept at a supercritical point (the temperature 31.26OC and the pressure of 72.9 atm). After the sufficient supercritical fluid is injected, the soaking kettle is immediately sealed, so that the material is soaked for 2-6 hours in the soaking environment of the supercritical fluid, auxiliary stirring measures can be adopted in the soaking process to optimize the soaking efficiency, and the stirring measures can be selected from a mechanical stirring method, an ultrasonic method and the like; the specific time of impregnation is determined by the material to ensure complete impregnation of the supercritical fluid within the material while improving efficiency.
The heating micro-explosion means that the immersed raw material is introduced into a melt extruder, the raw material is heated to a viscous state in the melt extruder, and the space occupied by the raw material with unit mass is kept unchanged all the time in the heating process, and the solution is that the space size is controlled by controlling the groove depth and the lead of a screw; after all materials reach a viscous state, guiding the materials to quickly enter a larger space from a smaller space, and instantly expanding primary particles by utilizing the advantage of vaporization volume expansion of the supercritical fluid to unwrap the primary particles; the materials after micro-explosion continuously flow to the machine head in the screw rod, so that the accumulation of materials is prevented.
The micro-explosion of the materials from small space to large space comprises two solving measures: the first is to introduce the material into a transition pipeline, the flow direction of the material in the transition pipeline should be parallel to the gravity direction downwards, so as to prevent the material from collapsing and the molecular chain from partially rebounding due to the viscous state after the material is micro-exploded, and simultaneously, the material can make room for the subsequent micro-exploded material downwards parallel to the gravity direction and keep continuity. The feeding amount and the discharging amount of the micro-explosion section are controlled by the material conveying amount of the adjacent double-stage screw.
The second solution is to change the groove depth and lead of the screw so as to rapidly increase the space occupied by the material with unit mass. The method for removing the materials in the micro-explosion section in the measure is to improve the material conveying speed at the discharging position of the micro-explosion section by changing the axial roughness of the machine barrel and the like.
The mixing and exhausting process means that the melt after micro-explosion is exhausted in the mixing process, gas in the material is extruded out mainly in a mechanical exhaust mode, molecular chains continue to deform in the mechanical extrusion process due to air gaps, the molecular chains are promoted to be unfolded due to uniform flow of the air gaps, meanwhile, entanglement among different single molecular chains is promoted through the mixing effect of a screw rod, the single molecular chains are prevented from returning to primary particles again, and the strength of the material is improved.
The above-mentioned kneading and venting (mechanical venting) means that the screw kneading is performed while the screw groove depth is reduced, and the gas in the material is discharged. It should be noted that the gas inside the material cannot be pumped out from the outside by means of vacuum pumping while the material is stationary: when the material is static, the direct gas extraction easily causes the unidirectional uneven flow of the gas left in the material after micro-explosion to cause the quality defect of the material; meanwhile, the movement space of the molecular chain is reduced due to the fact that gas in the material is extracted in advance, and the molecular chain is not easy to unfold again. During operation, the material does not stay in the machine barrel for too long to prevent decomposition, and meanwhile, all gases in the material are discharged, so that air holes in the material to be processed later are avoided, and the material performance is affected.
The lamination extrusion means that pressure is built on materials after the exhaust is completed, and molecular chains are stretched and oriented and laminated by utilizing the stretching and orientation function of a lamination device, so that the order of the molecular chains in the PVC materials is enhanced. The extruded melt can be directly used for manufacturing products, or can be used for manufacturing products after extrusion granulation.
Aiming at the high-performance processing technology of the supercritical fluid micro-explosion disentangled polymer, the special processing equipment designed by the invention comprises a basic system such as a drying system, an impregnating system, a micro-explosion system, an exhaust extrusion system, a temperature control system and the like. The impregnating system comprises metering feeding equipment, a supercritical fluid injection system, an impregnating kettle, a pneumatic conveying component, a ventilation component and the like; the micro-explosion system comprises a metering feeding part, a micro-explosion part and the like; the extrusion system comprises a mixing and exhausting integrated extruder, a laminator, a blanking device and the like.
The micro-explosion system and the extrusion system can be integrated on the same extruder, but the structure is complex, the yield is easy to be reduced, the control difficulty is easy to be increased, and the arrangement form of the double-stage extruder is preferably adopted, wherein the arrangement form of the double-stage extruder refers to that a micro-explosion part consists of a melting extruder and a micro-explosion pipeline, and the structure form is described in detail below.
The specific installation mode of the high-performance processing equipment for the supercritical fluid micro-explosion disentangled polymer is as follows: the material is injected into the material inlet of the dipping kettle from the material outlet of the drying system through the metering feeding equipment, the supercritical fluid injection system is connected with the air inlet of the dipping kettle through an electromagnetic valve, and the electromagnetic valve controls the communication state of the supercritical fluid injection system. The two impregnating kettles are connected through basic elements such as a filter, an electromagnetic valve, an air compressor and the like, the electromagnetic valve is arranged between the filter and the air compressor, and the electromagnetic valve and the filter are arranged between the air compressor and each impregnating kettle. The material enters the melt extruder under the combined action of the gas pushing and the metering feeding component arranged at the feeding port of the melt extruder. The heating and cooling part of the melting extruder strictly controls the temperature of the feeding port and the temperature of the feeding port adjacent to the machine barrel, so that the situation that the excessive pressure and bridging are caused by the fact that gas in the material is released in advance due to overheating of the feeding port is prevented. The head of the melting extruder is connected with the mouth of the mixing exhaust extruder through a micro-explosion pipeline, the main axis of the micro-explosion pipeline is parallel to the gravity direction, and the feed inlet of the mixing exhaust extruder is lower than the discharge outlet of the melting extruder. The head part of the mixing exhaust extruder is provided with a laminator, the other end of the laminator is connected with a granulating device, and cut granules enter the aggregate device after being rapidly cooled by an air cooling cavity.
The supercritical fluid is preferably supercritical CO2, which is nontoxic and harmless because of easier acquisition and control; fluids such as H2, N2, water vapor and the like can also be used for micro-explosion unwrapping.
The impregnating kettle of the impregnating system is mainly designed in a pressure reaction kettle, and is an autoclave, and the design pressure of the impregnating kettle is designed to be capable of bearing at least 15MPa, so that a sufficient safety coefficient is reserved, and overpressure is prevented. The material storage amount of the dipping kettle is designed according to the productivity, and a day storage tank with larger material storage amount is optimized; the number of the impregnating kettles can be set to be one or more, and two impregnating kettles are preferred in the invention, so that the cost is saved, and the efficiency is improved.
The ventilation part mainly comprises an airflow flowing pipeline, a filter, an electromagnetic valve and a bidirectional air compressor, and the design requirement of the ventilation part is the same as the design safety coefficient of the dipping kettle. The filter is mainly used for preventing PVC materials from entering the air compressor when CO2 is extracted/exchanged, and preferably a filter adopting a multi-stage filtration mode is adopted, so that the filtration effect is improved; the air compressor is mainly used for extracting most of redundant CO2 after the impregnation is finished into another impregnation kettle, so that the waste of supercritical CO2 is reduced; it should be noted that the air compressor should not cause negative pressure to form in the impregnation tank, so as to facilitate the normal operation of the later pneumatic conveying.
The pneumatic conveying component utilizes CO2 which is not completely extracted from the impregnating kettle and is not impregnated into the materials as driving gas to drive the materials in the kettle to move along the pneumatic conveying pipeline, and the materials in the kettle are fed into the mixing extruder by matching with the metering feeding component.
The metering and feeding device at the feed inlet of the melt extruder according to the invention should have a venting function. The exhaust function is mainly used for exhausting the power gas conveyed pneumatically, so that the influence of the part of gas on subsequent processing is reduced.
The melting extruder of the micro-explosion system is mainly used for melting materials, meanwhile, the space occupied by the materials with unit mass is kept unchanged in the melting process, and the conditions can be controlled by controlling the groove depth of the screw. The micro-explosion pipeline is preferably a cylindrical pipeline, the axial length of the vertical section of the micro-explosion pipeline is larger than the inner diameter, the inner diameter of the vertical section is larger than the outlet diameter of the melt extruder, and the specific diameter ratio is determined by the required micro-explosion coefficient. It is recommended in the design process to fix the diameter of the micro-explosion pipeline and control the diameter proportion by reducing the outlet diameter of the melt extruder, and the diameter of the micro-explosion pipeline should not exceed the diameter of the feed inlet or the inner diameter of the barrel of the mixing exhaust extruder.
The screw groove depth of the mixing exhaust extruder should be gradually reduced, meanwhile, the screw is guaranteed to have a strong mixing effect according to the material type, so that the opened single long chain and other long chains are entangled, the single long chain is prevented from being coated again, and the combination modes of the single screw, the double screws, the planetary screws and the like can be selected. The operation mode of the mixing and exhausting extruder is that the mixing and exhausting are carried out while the normal pressure exhausting is kept in the exhausting process, and the pressure is built up for extrusion after the gas is completely exhausted. During the design process of the screw, the problem of material decomposition caused by excessive temperature and long residence time should be considered.
In the processing of PVC materials, the screw form of the mixing exhaust extruder is preferably a planetary screw, and a double-cone screw, a single screw and the like can also be selected. The processing of other polymers is carried out by selecting a screw combination form according to the specific mixing effect.
In the micro-explosion unwrapping process, the supercritical fluid is immersed at low temperature and high pressure, so that the defect that the fluid is aggregated into larger bubble cores or the fluid is aggregated in gaps between molecular chains rather than in single molecular chains due to the fact that the fluid caused by adding the supercritical fluid after melting the materials cannot be well dispersed can be avoided. According to the invention, the gas in the material is discharged by utilizing the action mode of mixing and exhausting after disentangling, the opened loose molecular chain group is deformed and is not easy to return to the original state, the orientation effect in the micro-explosion process is reserved, the orientation processing of the molecular chain in the later stage is easy, the stretched oriented molecular chain with higher proportion is obtained, and the problem that part of the material cannot be completely opened in the melt orientation process is solved.
The high-performance processing technology and equipment of the supercritical fluid micro-explosion disentangled polymer can continuously and efficiently disentangle high polymer chain groups/primary particles in a low-cost supercritical fluid micro-explosion mode, and keep the chain segments which are oriented by micro-explosion to smoothly enter the next-stage orientation through a mechanical exhaust mode, and the material which is higher in orientation degree and orderly in molecular chain arrangement and does not contain bubbles is formed by combining a lamination extrusion technology, so that the usability of the high polymer is optimized.
Drawings
FIG. 1 is a schematic diagram of the main equipment body of the process and equipment for high-performance polymer processing by micro-explosion of supercritical fluid.
FIG. 2 is a schematic view showing a part of a micro-explosion and mixing exhaust part of a super critical fluid micro-explosion disentangled polymer high performance processing technology and equipment.
FIG. 3 is a schematic diagram of a micro-explosion pipeline of a high-performance processing technology and equipment for a supercritical fluid micro-explosion disentangled polymer.
Fig. 4 is a schematic diagram of the disentanglement principle of the process and equipment for high-performance polymer disentanglement by micro-explosion of supercritical fluid.
FIG. 5 is a schematic diagram of alternative types of mixing and venting extruder screws used in the process and equipment for high performance polymer processing by micro-explosion of supercritical fluid.
In the figure: 1-a first dipping kettle; 2-a second dipping kettle; 3-air inlet; 4-a stirring motor; 5-a feeding port of the dipping kettle; 6-an air compressor; 7-a micro-explosion pipeline; 8-mixing and exhausting an extruder; 9-a laminator; 10-blanking parts; 11-a melt extruder; 12-metering the feed components; 13-an electromagnetic valve; 14-a discharge port of the dipping kettle; 15-a filter; 16-an electromagnetic valve; 7-1-primary particle schematic; 17-2-schematic diagram of loose chain groups after micro-explosion; 17-3-schematic diagram of a mechanical exhaust rear semi-oriented molecular chain; 17-4-oriented molecular chain schematic.
Detailed Description
The process route of the high-performance processing technology and equipment of the supercritical fluid micro-explosion disentangled polymer comprises the following steps: drying materials, dipping at low temperature and high pressure, heating for micro-explosion, mixing, exhausting and laminating for extrusion. As shown in fig. 4, the basic idea of the process route is to disentangle the primary particles 17-1 of the material by a supercritical fluid micro-explosion method to form loose molecular chains 17-2 with chain segment orientation, then deform the disentangled particles by a method of mixing and exhausting (mechanical exhausting) at the same time, retain the chain segment orientation effect and perform secondary chain segment orientation, simultaneously exhaust all the gas in the material to obtain semi-oriented molecular chains 17-3, and finally further orient the molecular chains by a lamination process to obtain oriented molecular chains 17-4.
As shown in figure 1, the high-performance processing equipment for the supercritical fluid micro-explosion disentangled polymer comprises a drying system, an impregnating system, a micro-explosion system, an exhaust extrusion system, a temperature control system and other basic systems. The impregnating system comprises a metering feeding device, a supercritical fluid injection system, an impregnating kettle 1 (or 2), a pneumatic conveying component, a ventilation component and the like; the micro-explosion system comprises a metering feeding part 12, a micro-explosion part and the like; the extrusion system comprises a mixing and exhausting integrated extruder 8, a laminator 9, a blanking device 10 and the like.
As shown in fig. 1, the specific installation mode of the supercritical fluid micro-explosion unwrapping polymer high-performance processing equipment is as follows: the material is injected into the feeding port 5 of the dipping kettle through the metering feeding device at the discharging port of the drying system, the supercritical fluid injection system is connected with the air inlet 3 of the dipping kettle through an electromagnetic valve, and the electromagnetic valve controls the communication state of the supercritical fluid injection system. The two impregnating kettles are connected through basic elements such as a filter 15, an electromagnetic valve 16, an air compressor 6 and the like, the electromagnetic valve 16 is arranged between the filter 15 and the air compressor 6, and the electromagnetic valve 16 and the filter 15 are arranged between the air compressor 6 and each impregnating kettle 1 (or 2). The discharge port 14 of the dipping kettle is connected with an electromagnetic valve 13 and is connected with a metering feeding part 12 through a pneumatic conveying pipeline, and materials enter the melting extruder 11 through the combined action of gas pushing and the metering feeding part 12 arranged at the feed port of the melting extruder 11. The heating and cooling components of the melt extruder 11 strictly control the temperature at the feed inlet and adjacent to the barrel, and prevent the feed inlet from overheating and leading to the premature release of fluid in the material, thereby causing overpressure and bridging. The head of the melting extruder 11 is connected with the feed inlet of the mixing exhaust extruder 8 through a micro-explosion pipeline 7, the main axis of the micro-explosion pipeline 7 is parallel to the gravity direction, and the feed inlet of the mixing exhaust extruder 8 is lower than the discharge outlet of the melting extruder 11. The head part of the mixing exhaust extruder 8 is provided with a lamination device 9, the other end of the lamination device is connected with a granulating device 10, and cut granules enter the aggregate device after being rapidly cooled by an air cooling cavity.
The heating micro-explosion means that the immersed raw material is introduced into a melt extruder 11, the raw material is heated to a viscous state in the melt extruder 11, and the space occupied by the raw material with unit mass is kept unchanged all the time in the heating process, and the solution is that the space size is controlled by controlling the groove depth and the lead of a screw; after all materials reach a viscous state, guiding the materials to quickly enter a larger space from a smaller space, and instantly expanding primary particles by utilizing the advantage of vaporization volume expansion of the supercritical fluid to unwrap the primary particles; particularly, the discharging amount at the micro-explosion section is slightly larger than the feeding amount of the micro-explosion section, so that the micro-explosion section can remove the micro-exploded materials as soon as possible, and the accumulation of materials is prevented.
The measures for changing the micro-explosion space in the invention comprise two types: first, as shown in fig. 2, the material is introduced into a micro-explosion pipe 7, and the flow direction of the material in the micro-explosion pipe 7 is parallel to the gravity direction. The feeding amount and the discharging amount of the micro-explosion pipeline 7 are controlled by the material conveying amount of the adjacent double-stage screw rods. The second solution is to change the groove depth and lead of the screw so as to rapidly increase the space occupied by the material with unit mass. The method for removing the materials in the micro-explosion section in the measure is to improve the material conveying speed at the discharging position of the micro-explosion section by changing the axial roughness of the machine barrel and the like.
As shown in fig. 3, the micro-explosion pipeline 7 is preferably a cylindrical pipeline, the axial length of the vertical section of the cylindrical pipeline is larger than the inner diameter, and the inner diameter of the vertical section is larger than the outlet diameter of the melt extruder, and the specific diameter ratio is determined by the micro-explosion coefficient. It is recommended in the design process to fix the diameter of the micro-explosion line 7 and control the diameter ratio by reducing the outlet diameter of the melt extruder 11, while the micro-explosion line 7 diameter should not exceed the feed port diameter or barrel inner diameter of the mixing exhaust extruder 8.
As shown in FIG. 5, the screw groove depth of the mixing and exhausting extruder 8 should be gradually reduced, meanwhile, the screw should be guaranteed to have a strong mixing effect according to the material type, so that the opened single long chain and other long chains are entangled, the single long chain is prevented from being coated again, and the combination forms of a single screw, a double screw, a planetary screw and the like can be selected. The operation mode of the mixing and exhausting extruder 8 is that the mixing and exhausting are carried out while the normal pressure exhausting is kept in the exhausting process, and the pressure is built up for extrusion after the gas is completely exhausted. During the design process of the screw, the problem of material decomposition caused by excessive temperature and long residence time should be considered.
The specific operation mode of the invention is as follows: the drying system firstly dries the materials so that the pores of the primary particles 17-1 do not contain moisture; meanwhile, high-pressure air tightness detection (the air tightness detection is required before equipment is started each time) is carried out on the dipping kettle 1 (or 2), the ventilation part, the pneumatic conveying part and the like, and next-stage work is carried out after the detection is qualified.
The dried materials are sent into a first dipping kettle 1 through a metering and feeding system, the volume of the materials in the first dipping kettle 1 is not more than 2/3 of the volume of the dipping kettle, after the materials are fully put into the first dipping kettle 1, air in the kettle can be preferably firstly extracted cleanly, and then supercritical CO2 is injected into the first dipping kettle 1 through a supercritical fluid injection system. After the supercritical fluid submerges the materials in the first dipping kettle 1, the first dipping kettle (1) is sealed for 2-6 hours, and meanwhile, the stirring element 4 in the kettle is kept to be continuously stirred, so that dipping is accelerated.
In the material impregnation process in the first impregnation kettle 1, the material to be impregnated is added into the second impregnation kettle 2, the second impregnation kettle 2 is sealed, a certain amount of supercritical fluid (determined by the supercritical fluid lost by the single kettle impregnation material in the experiment) is added into the second impregnation kettle 2, and the second impregnation kettle 2 is sealed. After the materials in the first dipping kettle 1 are dipped for enough time, an air compressor 6 between the first dipping kettle 1 and the second dipping kettle 2 is opened, and the air pumping direction of the air compressor is from the first dipping kettle 1 to the second dipping kettle 2; after the air compressor 6 runs stably, opening an electromagnetic valve 16 between the air compressor 6 and each kettle, and pumping a part of supercritical fluid which is not immersed in the material in the first immersion kettle 1 into the second immersion kettle 2 through a ventilation component, wherein the material in the first immersion kettle 1 can be left in the first immersion kettle 1 due to the blocking of a filter 15; after the gas extraction is finished, the electromagnetic valve 16 is closed, the second dipping kettle 2 is closed, and then the air compressor 6 is closed. The electromagnetic valve 13 at the discharge hole 14 of the first dipping kettle 1 is opened, and the material enters the melt extruder 11 through the combined action of the metering feeding component arranged at the feed hole of the melt extruder 11 and the pushing of CO2 which is remained in the first dipping kettle 1 and does not enter the material hole. After the materials are completely emptied from the first dipping kettle 1, a discharge hole 14 is closed through an electromagnetic valve 13, and then the non-dipped materials and the supercritical fluid are added into the first dipping kettle 1, and the steps are repeated, so that the first dipping kettle 1 and the second dipping kettle 2 alternately operate.
The temperature at the feed inlet of the melt extruder 11 should be maintained at about 31.26OC to prevent bridging and premature expansion of the supercritical fluid. The melt extruder 11 plasticizes and extrudes the material while ensuring that the space occupied by the material per unit mass is unchanged. The materials extruded from the discharge port of the melt extruder 11 immediately enter the micro-explosion pipeline 7 for unwrapping, and the unwrapped materials directly enter the mixing and exhausting extruder 8 for mixing and exhausting. The feeding amount of the mixing exhaust extruder 8 is slightly larger than the discharging amount of the melt extruder 11, and can be controlled by controlling the rotating speed of the corresponding screw. The molecular chains are secondarily oriented through the mixing action of the mixing extruder 8, other additives (such as color master batches and the like) can be added into the materials as required in the mixing process, after the exhaust is completed, the materials are pressurized, the materials are subjected to further stretching orientation and lamination extrusion through the lamination device 9, and the extruded materials are pelletized through the pelletizing equipment 10 and then air-cooled to obtain high-performance polymer pellets for product processing. The above description is of the specific equipment and process of the present invention, and is described with reference to the drawings. The invention is not limited to the specific apparatus and processes described above, any modifications or substitutions to the related apparatus based on the above description, and any local adjustments to the related process based on the above description are within the spirit and scope of the invention.
Claims (7)
1. The high-performance processing technology of the supercritical fluid micro-explosion disentangled polymer is characterized in that:
first, drying materials: completely evaporating unbound water in the material;
Second, low-temperature high-pressure impregnation: adding the dried material into an impregnating kettle through a metering system, adding supercritical CO2 through a supercritical fluid injection system, keeping the internal environment of the impregnating kettle at a supercritical point, immediately sealing the impregnating kettle after a sufficient amount of supercritical fluid is injected, and impregnating the material in the supercritical fluid impregnating environment for 2-6 hours to ensure that the material is completely impregnated with the supercritical fluid;
Thirdly, heating and micro-blasting: introducing the immersed raw materials into a melt extruder, heating the raw materials to a viscous state in the melt extruder, and keeping the space occupied by the materials with unit mass unchanged all the time in the heating process; after all materials reach a viscous state, guiding the materials to quickly enter a larger space from a smaller space, and expanding primary particles instantly by utilizing the vaporization volume expansion of the supercritical fluid to disentangle the primary particles; the materials after micro explosion continuously flow to the machine head in the screw;
Fourth, mixing and exhausting: the melt after micro explosion is exhausted in the mixing process, gas in the material is extruded out mainly through a mechanical exhaust mode, molecular chains continue to deform in the mechanical extrusion process due to air gaps, the molecular chains are promoted to be unfolded due to uniform flow of the air gaps, meanwhile, entanglement among different single molecular chains is promoted through the mixing effect of a screw rod, and the single molecular chains are prevented from returning to primary particles again;
Fifth step, lamination extrusion: after the exhaust is completed, pressure is built on the material, molecular chains are stretched, oriented and laminated by utilizing the stretching orientation function of a laminator, the order of the molecular chains in the PVC material is enhanced, and the extruded melt is directly used for manufacturing products or is used for manufacturing products after extrusion granulation.
2. The process for processing the high-performance polymer by micro-explosion and disentanglement of the supercritical fluid according to claim 1, wherein the process comprises the following steps: in the second step of dipping process, auxiliary stirring measures are adopted to optimize dipping efficiency, and the stirring measures are mechanical stirring method or ultrasonic method.
3. The process for processing the high-performance polymer by micro-explosion and disentanglement of the supercritical fluid according to claim 1, wherein the process comprises the following steps: the material is micro-exploded from small space to large space, the material is led into a transition pipeline, the flow direction of the material in the transition pipeline is parallel to the gravity direction and downward, the material collapse and the rebound of a molecular chain part caused by the still viscous state after the material micro-explosion are prevented, meanwhile, the space can be vacated for the material of the follow-up micro-explosion and the continuity is kept by downward parallel to the gravity direction, and the feeding amount and the discharging amount of the micro-explosion section are controlled by the material conveying amount of the double-stage screw adjacent to the micro-explosion section.
4. The process for processing the high-performance polymer by micro-explosion and disentanglement of the supercritical fluid according to claim 1, wherein the process comprises the following steps: the materials are slightly exploded from small space to large space, the space occupied by the materials with unit mass is rapidly increased by changing the groove depth and the lead of the screw, and the material conveying speed at the discharging position of the micro-explosion section is improved by changing the axial roughness of the machine barrel.
5. The high-performance processing equipment for the supercritical fluid micro-explosion disentangled polymer is characterized in that: the device comprises a drying system, an impregnating system, a micro-explosion system, an exhaust extrusion system and a temperature control system, wherein the impregnating system comprises metering feeding equipment, a supercritical fluid injection system, an impregnating kettle, a pneumatic conveying component and a ventilation component; the micro-explosion system comprises a metering feeding part and a micro-explosion part; the extrusion system comprises a mixing and exhausting integrated extruder, a laminator and a blanking device; the micro-explosion system and the extrusion system adopt the arrangement form of a double-order extruder, a discharge port of the drying system injects materials into a feed port of the dipping kettle through metering feeding equipment, the supercritical fluid injection system is connected with an air inlet of the dipping kettle through an electromagnetic valve, and the electromagnetic valve controls the communication state of the supercritical fluid injection system; the two impregnating kettles are connected with an air compressor through a filter, an electromagnetic valve, the electromagnetic valve is arranged between the filter and the air compressor, and the electromagnetic valve and the filter are arranged between the air compressor and each impregnating kettle; the material enters the melt extruder under the combined action of gas pushing and a metering feeding component arranged at the feeding port of the melt extruder; the heating and cooling part of the melting extruder strictly controls the temperature at the feed inlet and the temperature adjacent to the machine barrel; the head of the melting extruder is connected with the mouth of the mixing exhaust extruder through a micro-explosion pipeline, the main axis of the micro-explosion pipeline is parallel to the gravity direction, and the feed inlet of the mixing exhaust extruder is lower than the discharge outlet of the melting extruder; a laminator is arranged at the head part of the mixing exhaust extruder, the other end of the laminator is connected with a granulating device, and cut granules enter a collecting device after being rapidly air-cooled through an air-cooled cavity; the ventilation part mainly comprises an airflow circulation pipeline, a filter, an electromagnetic valve and a bidirectional air compressor, wherein the filter is mainly used for preventing PVC materials from entering the air compressor when CO2 is extracted/exchanged, and the filter in a multi-stage filtering mode is adopted to improve the filtering effect; the air compressor is mainly used for extracting most of redundant CO2 after the impregnation is finished into another impregnation kettle, so that the waste of supercritical CO2 is reduced.
6. The supercritical fluid micro-explosion disentangled polymer high-performance processing equipment according to claim 5, characterized in that: the supercritical fluid is supercritical CO2, H2, N2 or water vapor.
7. The supercritical fluid micro-explosion disentangled polymer high-performance processing equipment according to claim 5, characterized in that: the pneumatic conveying component utilizes CO2 which is not completely extracted from the impregnating kettle and is not impregnated into the materials as driving gas to drive the materials in the kettle to move along the pneumatic conveying pipeline, and the materials in the kettle are fed into the mixing extruder by matching with the metering feeding component.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103184540A (en) * | 2011-12-27 | 2013-07-03 | 中原工学院 | Method for preparing micro-porous LiMn2O4 fiber by three-screw mixing extruder spinning |
| CN203077566U (en) * | 2012-12-20 | 2013-07-24 | 华南理工大学 | Injection moulding device for on-line mixing preparation of high-performance microcellular foaming plastic |
| WO2015095790A1 (en) * | 2013-12-20 | 2015-06-25 | The Brigham And Women's Hospital, Inc. | Ductile crosslinked polymers and methods of making the same |
| CN104884530A (en) * | 2012-12-13 | 2015-09-02 | 瑞来斯实业公司 | Easily processable ultrahigh molecular weight polyethylene and a process for preparation thereof |
| CN109837038A (en) * | 2017-11-24 | 2019-06-04 | 北京路德永泰环保科技有限公司 | Self-adhered polymer modified bitumen waterproofing membrane modifying agent and preparation method thereof |
| CN211518153U (en) * | 2019-10-17 | 2020-09-18 | 北京化工大学 | Supercritical fluid micro-explosion disentanglement polymer high-performance processing equipment |
-
2019
- 2019-10-17 CN CN201910989169.7A patent/CN110614732B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103184540A (en) * | 2011-12-27 | 2013-07-03 | 中原工学院 | Method for preparing micro-porous LiMn2O4 fiber by three-screw mixing extruder spinning |
| CN104884530A (en) * | 2012-12-13 | 2015-09-02 | 瑞来斯实业公司 | Easily processable ultrahigh molecular weight polyethylene and a process for preparation thereof |
| CN203077566U (en) * | 2012-12-20 | 2013-07-24 | 华南理工大学 | Injection moulding device for on-line mixing preparation of high-performance microcellular foaming plastic |
| WO2015095790A1 (en) * | 2013-12-20 | 2015-06-25 | The Brigham And Women's Hospital, Inc. | Ductile crosslinked polymers and methods of making the same |
| CN109837038A (en) * | 2017-11-24 | 2019-06-04 | 北京路德永泰环保科技有限公司 | Self-adhered polymer modified bitumen waterproofing membrane modifying agent and preparation method thereof |
| CN211518153U (en) * | 2019-10-17 | 2020-09-18 | 北京化工大学 | Supercritical fluid micro-explosion disentanglement polymer high-performance processing equipment |
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