CN109576825B - Cleaning-free waste regeneration process - Google Patents
Cleaning-free waste regeneration process Download PDFInfo
- Publication number
- CN109576825B CN109576825B CN201910052310.0A CN201910052310A CN109576825B CN 109576825 B CN109576825 B CN 109576825B CN 201910052310 A CN201910052310 A CN 201910052310A CN 109576825 B CN109576825 B CN 109576825B
- Authority
- CN
- China
- Prior art keywords
- melt
- crushing
- cutter
- compression
- cavity
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000002699 waste material Substances 0.000 title claims abstract description 101
- 238000000034 method Methods 0.000 title claims abstract description 99
- 230000008569 process Effects 0.000 title claims abstract description 80
- 230000008929 regeneration Effects 0.000 title claims abstract description 17
- 238000011069 regeneration method Methods 0.000 title claims abstract description 17
- 239000000155 melt Substances 0.000 claims abstract description 85
- 238000007906 compression Methods 0.000 claims abstract description 78
- 230000006835 compression Effects 0.000 claims abstract description 72
- 239000000463 material Substances 0.000 claims abstract description 64
- 238000002844 melting Methods 0.000 claims abstract description 54
- 230000008018 melting Effects 0.000 claims abstract description 54
- 238000005056 compaction Methods 0.000 claims abstract description 40
- 230000007246 mechanism Effects 0.000 claims abstract description 24
- 238000000265 homogenisation Methods 0.000 claims abstract description 22
- 239000000835 fiber Substances 0.000 claims abstract description 21
- 230000000670 limiting effect Effects 0.000 claims abstract description 13
- 230000018044 dehydration Effects 0.000 claims abstract description 7
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 7
- 238000001914 filtration Methods 0.000 claims description 58
- 238000010438 heat treatment Methods 0.000 claims description 36
- 239000000428 dust Substances 0.000 claims description 28
- 238000012545 processing Methods 0.000 claims description 27
- 238000001704 evaporation Methods 0.000 claims description 24
- 230000008020 evaporation Effects 0.000 claims description 24
- 238000001125 extrusion Methods 0.000 claims description 23
- 238000004064 recycling Methods 0.000 claims description 15
- 239000003795 chemical substances by application Substances 0.000 claims description 13
- 238000007872 degassing Methods 0.000 claims description 12
- 238000003756 stirring Methods 0.000 claims description 11
- 238000005496 tempering Methods 0.000 claims description 11
- 230000009471 action Effects 0.000 claims description 10
- 238000005086 pumping Methods 0.000 claims description 10
- 238000007599 discharging Methods 0.000 claims description 9
- 238000011010 flushing procedure Methods 0.000 claims description 7
- 238000010036 direct spinning Methods 0.000 claims description 4
- 230000033001 locomotion Effects 0.000 claims description 3
- 230000005540 biological transmission Effects 0.000 claims description 2
- 238000004891 communication Methods 0.000 claims 1
- 229920000728 polyester Polymers 0.000 abstract description 79
- 238000004519 manufacturing process Methods 0.000 abstract description 17
- 239000002994 raw material Substances 0.000 abstract description 9
- 238000011084 recovery Methods 0.000 abstract description 6
- 238000010309 melting process Methods 0.000 abstract description 5
- 238000004140 cleaning Methods 0.000 abstract description 4
- 239000010887 waste solvent Substances 0.000 abstract description 2
- 208000005156 Dehydration Diseases 0.000 abstract 2
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 39
- 239000012535 impurity Substances 0.000 description 36
- 239000000047 product Substances 0.000 description 20
- 238000005520 cutting process Methods 0.000 description 19
- 239000004753 textile Substances 0.000 description 13
- 230000002829 reductive effect Effects 0.000 description 10
- 239000000126 substance Substances 0.000 description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 230000000694 effects Effects 0.000 description 8
- 238000005265 energy consumption Methods 0.000 description 8
- 230000007704 transition Effects 0.000 description 8
- 230000008859 change Effects 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 7
- 239000005020 polyethylene terephthalate Substances 0.000 description 7
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 description 6
- 238000002156 mixing Methods 0.000 description 6
- 229920000139 polyethylene terephthalate Polymers 0.000 description 6
- 238000013461 design Methods 0.000 description 5
- 238000010586 diagram Methods 0.000 description 5
- 230000036961 partial effect Effects 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- 238000000053 physical method Methods 0.000 description 5
- 230000007423 decrease Effects 0.000 description 4
- 230000007547 defect Effects 0.000 description 4
- 238000011161 development Methods 0.000 description 4
- 230000018109 developmental process Effects 0.000 description 4
- 239000004744 fabric Substances 0.000 description 4
- 230000020169 heat generation Effects 0.000 description 4
- 238000003825 pressing Methods 0.000 description 4
- 150000003384 small molecules Chemical class 0.000 description 4
- 238000009987 spinning Methods 0.000 description 4
- 239000002352 surface water Substances 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- -1 assistants Substances 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 230000015556 catabolic process Effects 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000006731 degradation reaction Methods 0.000 description 3
- MTHSVFCYNBDYFN-UHFFFAOYSA-N diethylene glycol Chemical compound OCCOCCO MTHSVFCYNBDYFN-UHFFFAOYSA-N 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000002861 polymer material Substances 0.000 description 3
- 238000006116 polymerization reaction Methods 0.000 description 3
- 239000011347 resin Substances 0.000 description 3
- 229920005989 resin Polymers 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 238000006136 alcoholysis reaction Methods 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000007863 gel particle Substances 0.000 description 2
- 229920002521 macromolecule Polymers 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 238000010008 shearing Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 229920001059 synthetic polymer Polymers 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 238000004804 winding Methods 0.000 description 2
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 229920004933 Terylene® Polymers 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 231100000357 carcinogen Toxicity 0.000 description 1
- 239000003183 carcinogenic agent Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000005238 degreasing Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000001938 differential scanning calorimetry curve Methods 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000032050 esterification Effects 0.000 description 1
- 238000005886 esterification reaction Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000012634 fragment Substances 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000004745 nonwoven fabric Substances 0.000 description 1
- 239000008041 oiling agent Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 238000006068 polycondensation reaction Methods 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 238000003908 quality control method Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 238000005096 rolling process Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 229920002994 synthetic fiber Polymers 0.000 description 1
- 239000012209 synthetic fiber Substances 0.000 description 1
- 239000003440 toxic substance Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000011800 void material Substances 0.000 description 1
- 230000003313 weakening effect Effects 0.000 description 1
- 230000004580 weight loss Effects 0.000 description 1
Classifications
-
- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
- D01F13/00—Recovery of starting material, waste material or solvents during the manufacture of artificial filaments or the like
-
- 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
- B29B17/00—Recovery of plastics or other constituents of waste material containing plastics
- B29B17/04—Disintegrating plastics, e.g. by milling
-
- 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
- B29B17/00—Recovery of plastics or other constituents of waste material containing plastics
- B29B17/04—Disintegrating plastics, e.g. by milling
- B29B2017/0424—Specific disintegrating techniques; devices therefor
- B29B2017/044—Knives
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/50—Manufacturing or production processes characterised by the final manufactured product
- Y02P70/62—Manufacturing or production processes characterised by the final manufactured product related technologies for production or treatment of textile or flexible materials or products thereof, including footwear
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/52—Mechanical processing of waste for the recovery of materials, e.g. crushing, shredding, separation or disassembly
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/62—Plastics recycling; Rubber recycling
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Textile Engineering (AREA)
- Environmental & Geological Engineering (AREA)
- Mechanical Engineering (AREA)
- Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
Abstract
The application provides a cleaning-free waste regeneration process, which belongs to the technical field of recovery of raw materials, waste materials or solvents in the manufacturing process of artificial filaments or the like. Collecting polyester waste, crushing the polyester waste and completing the first dehydration/gas and devolatilization; the crushed materials are transferred into a blanking bin for self-compression blanking, then transferred into a compacting mechanism for compression compaction, and subjected to secondary dehydration/gas and devolatilization in the compression compaction process, then transferred into a melting screw for current limiting segmented melting, and subjected to vacuum suction in the melting process, and the obtained melt is fed into a homogenizing and tackifying reactor after being filtered for one time, and is matched with vacuum suction and EG recovery, so that the melt can be put into use after homogenization and tackifying are finished. The method is applied to the regeneration of polyester waste materials such as waste silk, has the characteristics of no cleaning, zero pollution and zero emission, and can be applied to various fields such as filaments, short fibers and sheets.
Description
Technical Field
The application relates to a cleaning-free waste regeneration process, which belongs to the technical field of recovery of raw materials, waste materials or solvents in the manufacturing process of artificial filaments or the like.
Background
With the rapid development of the world petrochemical industry, the synthetic fiber industry has also developed correspondingly. PET polyester is widely used in industrial, civil and other fields due to its excellent physical and chemical properties, and among many uses of polyester, polyester is used as a dominant raw material for textiles in textile fabrics, clothing and other fields. The huge polyester family has no small number, and the annual production amount of waste materials, waste silk, cloth selvedge materials and the like generated in the production and processing process is over 400 ten thousand tons from the polymerization process to the terminal garment production, and the polyester-series product is developed into the first large synthetic polymer material in the world.
PET polyester is a linear polymer material formed by esterification and polycondensation of purified terephthalic acid PTA and ethylene glycol EG, and is not harmful to the environment directly, but has high chemical inertness due to the existence of a benzene ring which is a rigid group in the molecule, and is difficult to degrade under natural conditions and difficult to decompose by microorganisms. Thus, from the environmental behavior and ecological effects, PET waste has become a global environmental pollution organic matter, forming "white pollution" that poses a serious threat to the ecological environment.
PET polyester as a synthetic polymer material occupies a large amount of landfill space when being directly buried, and damages water quality and soil; a large amount of carbon dioxide and toxic substances are generated in the incineration process, wherein the chlorine-containing waste textiles can generate carcinogens such as dioxin and the like in the incineration process.
The textile industry is closely related to life of people, and the textile industry in the world faces two major problems, on one hand, along with the development of world economy and science and technology, the application field of textiles is gradually expanded, but the service period is shortened, and in addition, the world population is rapidly increased, the consumption of the textiles is rapidly increased, so that the raw materials of the textiles are short, and the price is greatly raised. More textile fibre resources will be required, but polyesters are part of the petrochemical downstream industry. One of the raw materials for synthesizing polyesters, purified Terephthalic Acid (PTA), is derived from petroleum. The global petroleum resources are gradually exhausted, and the textile fiber resources are greatly restricted. On the other hand, a large number of waste textiles are mostly buried as garbage and burned, which not only causes resource waste, but also brings crisis to the environment. Therefore, the recycling of PET polyester waste can save a large amount of resources and reduce the pollution of textile industry to the environment. The recycling of polyester waste should take two basic principles: firstly, secondary pollution to the environment is avoided; second, commercial operation, i.e., cost versus product quality, is possible.
The development process of the regeneration technology according to the waste polyester fiber products can be divided into: primary recycling, physical method regeneration, physical and chemical method regeneration.
(1) Primary recycling: the method is simple, the equipment investment is limited, and the admission threshold is low. However, the quality of the regenerated product is poor due to the mere macroscopic form change of the waste material.
(2) Physical method regeneration technology: the polyester waste is melted and spun into fiber after being cleaned, crushed and dried, the process mainly relates to the change of the aggregation state structure of the polyester macromolecules, and the method has the advantages of simple process, low cost, easy industrialized popularization and the like. However, the existing physical method for recycling has the problems of lower recycling level, serious degradation, large water resource consumption, low efficiency caused by small waste silk stacking density and the like.
(3) Physical and chemical regeneration technology: after the recovered polyester waste is melted, the liquid phase or solid phase is thickened, so that the molecular weight is properly increased, and volatile low molecular substances are extracted. The method mainly uses a physical method and is assisted by a chemical method to improve the molecular weight and reduce the impurity content, and the process mainly relates to the change of macromolecular condensation state. The method can effectively improve the quality of regenerated products and realize differential regeneration under the condition of small increase of production cost. However, there are many disadvantages in the related melt tempering and viscosity-controlling technology and product quality control technology for the regeneration of polyester waste materials with complicated source components and high impurity content (especially impurities which cannot be removed, such as dyes, assistants, catalysts, etc.).
Disclosure of Invention
In view of the above, the present application provides a cleaning-free type waste recycling process, which aims at the current situations that the source of polyester waste is complex, the impurity content is high, the stacking density is small, the current recycling scheme of the physical method of the recycled polyester waste has water consumption, high energy consumption, low efficiency, low end of product application, high chemical recycling cost, no breakthrough of partial technical problems and the like, and the process can recycle and recycle the waste of the whole industrial chain of the polyester without cleaning and drying, can prepare the differential functional recycled polyester, and can be used for spinning the recycled polyester filaments to realize the repeated recycling of the recycled polyester product.
Specifically, the application is realized through the following scheme:
a cleaning-free waste regeneration process comprises the steps of crushing, blanking, compressing, compacting, melting, primary filtering, tempering, tackifying and secondary filtering sequentially after the waste to be treated is collected, so that the cast strip can be cut into slices or transferred into a melt for direct spinning; the crushing procedure is provided with a suction system in a matching way, and the first dehydration and devolatilization are completed during crushing; the crushed materials are transferred into a blanking bin, a dust remover is arranged at the top of the blanking bin, a beater and a roller are arranged at the bottom of the blanking bin, the roller forms extrusion and dragging actions on the materials falling onto the beater, the beater is arranged below the roller, the materials extruded and dragged by the roller are loosened and crushed again, and the beater and the roller are matched to complete self-compression blanking of the materials; the material is transferred to a compression compacting process through a blanking process, the compression compacting process is completed in a compacting mechanism, the compacting mechanism comprises a second suction system and a compacting cavity, the suction system is positioned at the top of the compacting cavity, and the compression compacting process is matched to complete the second degassing and devolatilization; the melting process is completed in a melting screw, the material after compression and compaction is sent into the melting screw through a feeding screw, the melting screw comprises a screw sleeve, a compression melting section and a homogenization flash evaporation section, wherein the compression melting section and the homogenization flash evaporation section are arranged on two sides of the screw sleeve, a flow limiting ring is sleeved between the screw sleeve and the tail end of the compression melting section, the compression ratio is 3-30, the melt pressure at the flow limiting ring is more than 10MPa, the melt enters the homogenization flash evaporation section in a film shape through a slit between the flow limiting ring and the screw sleeve, the homogenization flash evaporation section is connected with a suction system III, the vacuum degree of the homogenization flash evaporation section is ensured to be 50-5000Pa, and the third suction is completed; the melt extruded by melting is filtered once, and is pumped for the fourth time through the tempering and tackifying process provided with a pumping system four, and then is filtered twice to be output as a finished product melt. Wherein, the suction system adopts a fan or a vacuum machine to realize degassing and devolatilization; the second suction system adopts a fan or a vacuum machine to realize degassing and devolatilization; the third suction system adopts a vacuum machine to perform vacuum suction; and the suction system IV adopts a vacuum machine to carry out vacuum suction.
In the regeneration process of the polyester waste, a first suction system is used for realizing the first dehydration, degassing and devolatilization in the crushing process, a second suction system is arranged in the compacting mechanism and is matched with a cutter disc, a compression movable cutter and a compression fixed cutter to realize the second crushing and compression of the waste, and a heating air inlet is matched with the friction heat generation of the materials to remove all surface water, most of low-boiling-point organic impurities and dust generated by crushing, so that the second degassing and devolatilization in the compression compacting process are completed; the third suction of the melting screw is completed under the vacuum action of the homogenizing flash evaporation section, the melt film is instantaneously released under the pressure of the section, the flash evaporation effect occurs, and part of high boiling point organic impurities remained in the melt are gasified and rapidly taken away by a vacuum suction system; the last suction is carried out in a homogenizing and tackifying reactor, so that small molecules generated by the reaction are removed, and the uniformity of the viscosity of the product is improved; the method has the advantages that the filtering is arranged before and after the tempering and tackifying process, the organic impurities are removed by four times of degassing and devolatilization and the mechanical impurities in the product are removed by two times of filtering in the design of the whole technical scheme, the defect that the impurities are removed by water washing in the traditional production mode is overcome, a large amount of water resources are saved, the serious pollution of random sewage discharge to the environment is avoided, and the sewage discharge can be reduced by about 20 ten thousand tons per year according to the yield of 5 ten thousand tons per year. The single machine of the scheme has large productivity, and the unit energy consumption is only 80% of the energy consumption of the traditional bubble material production; in the waste material processing process, mechanical impurities and various organic impurities in raw materials are effectively removed, the spinnability of the regenerated slices is close to that of the original slices, the regenerated slices can replace the original polyester slices, and the regenerated slices can be widely applied to various fields such as filaments, short fibers and non-woven fabrics by a spun-bonding method, and the defect that the traditional bubble material recovery process can only be applied to the field of low-end short fibers due to unstable product viscosity and high impurity content is overcome.
Based on the scheme, the heat-transfer crusher is researched, and the preferable setting is determined as follows: the heat-conducting crusher comprises a processing cavity for crushing, a push plate, a swing arm and a crushing cutter, wherein the push plate, the swing arm and the crushing cutter are arranged in the processing cavity, a suction port is arranged at the top of the processing cavity, a heating medium inlet is arranged at the bottom of the processing cavity, a feeding port is arranged at the upper part of the processing cavity, a material to be processed enters the processing cavity through the feeding port, the swing arm is provided with an independent drive, the drive drives the push plate to reciprocate through the swing arm, the material entering the processing cavity is pushed into the crushing cutter, a discharge port is arranged at the bottom of the crushing cutter, and the crushed material is fed into a discharging bin through the discharge port. More preferably, the heating medium introduced by the heating medium inlet is dry air with the temperature of 100-150 ℃; the connecting rod is arranged on the cavity wall of the treatment cavity, the other end of the connecting rod is connected with the push plate, the middle part of the connecting rod is connected with the swing arm, and when the swing arm is driven to swing or stretch, the push plate is driven to swing through the connecting rod, one end of the connecting rod is fixed with the cavity wall of the treatment cavity, the other end of the connecting rod is connected with the push rod, and the connecting rod and the push rod form a movable structure together, so that the stability of the movement of the push plate is improved; the crushing cutter comprises a cutter body, a crushing fixed cutter, a filter screen and a crushing movable cutter, wherein the crushing movable cutter is arranged on the outer wall of the cutter body, the filter screen is wrapped outside the cutter body, the crushing fixed cutters are arranged in two rows and are respectively arranged at the outer edges of the two ends of the filter screen, so that the crushing fixed cutter is positioned above the cutter body, and the crushing fixed cutter and the crushing movable cutter are matched to realize the crushing of fibers; the baffle plate is arranged in the processing cavity and positioned below the push plate, and extends from the lower part of the crushing cutter to the inner wall of the processing cavity at the opposite side of the crushing cutter, so that the phenomenon of material leakage caused by bringing waste silk into the push plate when the push plate returns is avoided, the cleaning work is reduced, meanwhile, in the whole crushing process, no material is brought back by the push plate, and the working efficiency is improved; the heating crusher solves the problem of small single-machine yield of the traditional crusher, the single-machine yield is improved by 3-4 times, and can reach 3 tons/hour, and particularly, the crushing cutter designed for the characteristics of flexible materials such as fibers has the characteristic of winding prevention, so that the device can pretreat polyester full-industrial chains such as large-scale pulp blocks, waste fibers, waste cloth and the like and all forms of waste materials; the bottom of the heating crusher is provided with a heating medium inlet for supplying dry and hot air, materials are preheated (such as near 120 ℃), moisture and partial low-boiling organic impurities are removed, the top of the heating crusher is provided with a suction port which is communicated with a suction system, the devolatilization efficiency is improved, and dust generated by crushing is collected.
Based on the scheme, we do further research on the blanking bin and do the following preferable settings: the discharging bin comprises a bin body, a conical bottom and a discharging pipe, wherein the top of the bin body is fed, a dust remover is arranged in the bin body below the feeding, and the dust remover is externally connected with a collecting pipe; more preferably, the lower part of the beater is provided with a pre-feeding screw and a conveying screw in sequence, the pre-feeding screw is positioned in the conical bottom and is horizontally crossed with the beater, and the conveying screw is positioned in the blanking pipe.
Based on the above scheme, we have made further studies on the compacting mechanism and make the following preferred settings: the compression device is characterized in that a cutter disc, a compression fixed cutter and a compression movable cutter are arranged in the compression cavity, the cutter disc is in non-fixed connection with the inner wall of the compression cavity, the compression fixed cutter is driven to rotate by independent driving, the compression fixed cutter is spirally arranged on the inner wall of the compression cavity, a blade section for cutting is arranged on one side of the compression fixed cutter, one end of the compression movable cutter is a connecting section, the connecting section is fixed on the cutter disc, the other end of the compression movable cutter is a rotary cutting section which moves relative to the cutter disc, a gap for accommodating and rotary-cutting materials is arranged between the rotary cutting section and the cutter disc, the rotary cutting section and the upper surface of the connecting section are in descending arrangement in height, the cutter disc, the compression fixed cutter and the compression movable cutter form a guide piece, the compression compaction effect of the materials during rotation along with the cutter disc is ensured, and a heating air inlet is formed in the bottom of the compression cavity; more preferably, the compaction moving knife comprises a connecting section and a rotary cutting section, an extrusion section is further arranged between the connecting section and the rotary cutting section, the compaction moving knife is connected with the cutterhead through the connecting section, the rotary cutting section is connected with the connecting section through the extrusion section, and the distance between the extrusion section and the rotary cutting section and the distance between the rotary cutting section and the cutterhead are increased progressively; the compaction stationary knife further comprises a fixing section and a transition section, one side of the fixing section is fixed on the inner wall of the compaction mechanism above the cutter head, and the other side of the fixing section extends towards the compaction stationary knife through the transition section to form a knife point section with decreasing thickness. The compacting mechanism formed by the scheme is matched with a heating air inlet at the bottom of the cutter disc to form a spiral preheating compression compacting mechanism, and polyester waste materials and the like fed from a storage bin are secondarily crushed and compressed through the cutter disc rotating at high speed and a flow guiding element (such as a compacting fixed cutter, a compacting movable cutter and the like), wherein the stacking density is 200kg/m 3 Lifting to 600kg/m 3 The feeding efficiency is greatly improved; the material temperature is preheated to about 180 ℃ by friction heat generated by high-speed rotation of the cutter head, a heating air inlet is arranged at the bottom of the cutter head, a suction system is arranged at the top of the cutter head, the devolatilization force of the system is improved, all surface water and most of low-boiling-point organic impurities are removed, and dust generated by crushing is collected. More preferably, the cutter head rotation frequency is 10.0-50.0Hz; the temperature of the air entering the heating air inlet is 80-120 ℃.
Based on the above scheme, we have made further studies on the homogenizing and tackifying reactor and made the following preferred settings: the homogenizing and tackifying reactor comprises a kettle body and a stirrer, wherein a reactor inlet and a reactor outlet are arranged at the bottom of the kettle body, the reactor inlet and the reactor outlet are respectively arranged at two ends of the kettle body, the reactor inlet is communicated with primary filtration, melt filtered at one time is fed in, the reactor outlet is communicated with secondary filtration, and the melt after tackifying is output; the top of the kettle body is provided with a vacuumizing interface, the vacuumizing interface is connected with a vacuum pumping system to ensure that the vacuum degree in the kettle body is 50-150Pa (preferably 100-130 Pa), so that partial small molecular impurities are continuously removed along with the evaporation of Ethylene Glycol (EG), the viscosity of a regenerated polyester product is improved, the impurity content is reduced, the vacuumizing interface is connected with a branch pipe, the branch pipe is communicated with a depolymerizing agent inlet, the depolymerizing agent inlet is connected to a pipeline between primary filtration and primary filtration, the recovered EG is used as a depolymerizing agent and is combined with a pure/fresh depolymerizing agent through the branch pipe, and the micro alcoholysis of the regenerated polyester melt after the primary filtration can be realized in the pipeline, so that the molecular weight and molecular weight distribution of the polyester melt are improved; the stirrer is positioned in the kettle body, two ends of the stirrer are respectively connected with the stirring motor in a linkage way through a rotating shaft, a plurality of net plates are arranged in the stirrer, the net plates are arranged in a mutually parallel way, grids are distributed on the net plates, and the grids of two adjacent net plates are in an staggered state so as to improve the stirring efficiency; the rotatable agitator is provided with the fixed kettle body cooperation of reactor entry with the bottom, and the fuse-element forms film under the developments of stirring, and its surface is constantly updated, and the vacuum pumping system of cooperation evacuation interface again, small molecule impurity can be along with the evaporation of Ethylene Glycol (EG) constantly desorption, and the fuse-element viscosity in the kettle body promotes, and impurity content reduces, and parallel arrangement has set up multiunit net dish in the agitator, and the net on two piece adjacent net dishes is the staggered state, has improved the surface renewal efficiency when stirring, can realize the back mixing of regeneration polyester fuse-element, improves the homogeneity of material quality.
The primary filtering comprises a cavity, a plunger, a hydraulic cylinder, a closing slide valve and a heating plate, wherein the heating plate is arranged on the outer wall of the cavity, one end of the plunger is arranged in the cavity, the other end of the plunger is connected with a position rod of the hydraulic cylinder, a melt inlet and a melt outlet are arranged on the cavity, the melt inlet is communicated with the melt outlet through a melt channel, the melt channel penetrates through the cavity, a filter screen group is arranged between the melt inlet and the melt channel, the closing slide valve is arranged on the cavity on one side of the inlet, a back flushing port is arranged on the closing slide valve, the back flushing port is communicated with a cavity of the plunger to form a back flushing channel, a pressure sensor is arranged on the filter screen group, and the pressure sensor is respectively connected with the hydraulic cylinder and the closing slide valve so as to realize the transmission of pressure signals. Under normal conditions, the melt enters a melt flow channel from a melt inlet, is filtered by a filter screen group, and flows out through a melt outlet at the other end of the cavity, so that normal melt filtering and supplying work is completed; with the progress of filtration, impurity on the filter screen group gradually accumulates, and melt pressure rises along with it, and when pressure sensor detects that melt pressure reaches the setting value, pressure sensor sends this signal, and the position pole drives the plunger and outwards removes, and parts such as filter screen group that this plunger corresponds and the entry one end of melt runner break off, and back flush runner is linked together with the melt runner that melt export one end corresponds, and a small part melt in melt runner in melt export one end flows backwards, brings out the impurity that accumulates on the filter screen group, and when the pressure on the filter screen group was less than the setting value, this plunger began to remove backward and reset under the effect of pneumatic cylinder, continues normal melt filtration and transport. Therefore, the filter screen is automatically cleaned once, the filter screen is cleaned, the backwash efficiency is high, production pause is avoided, the yield is increased, the energy is saved, and the production cost is saved; greatly reduces the screen changing frequency and avoids frequent screen changing.
The secondary filtration comprises a lower cover plate, a filter element and an upper cover plate, wherein the side wall of the lower cover plate is provided with a melt inlet, and the top of the lower cover plate is provided with a plurality of shunt ports communicated with the melt inlet; the filter element consists of a filter rod, a filter medium and a framework, wherein a plurality of small holes are formed in the outer wall of the filter rod, a melt channel is formed in the middle of the filter rod, the small holes are communicated with the melt channel, the lower end of the melt channel is close to the bottom of the filter rod, the upper end of the melt channel penetrates through the top of the filter element, the filter medium is wrapped on the filter rod, and the framework is erected on the filter medium; the filter element is arranged between the upper cover plate and the lower cover plate, and the outer cylinder is sleeved outside the filter element; the upper cover plate is provided with a melt outlet which is communicated with the melt channel; the melt enters through the melt inlet, flows through the shunt port, then enters the melt channel through the framework, the filter medium and the small holes, and flows out through the melt outlet, thus completing the whole filtration.
Because the polyester waste material has complex sources, contains impurities such as moisture, catalyst, spinning oil, textile auxiliary agent and the like, has the characteristics of small bulk density, easy winding, bridging and the like, and the domestic polyester waste material is recycled by 95 percent by adopting a physical process route, and the polyester waste material is cleaned, dried and granulated to generate bubble materials, and then enters the next working procedure. In the process route, the collected polyester waste is fed in an open blanking mode without cleaning and drying in the early stage, the collected polyester waste is firstly placed in a through-heating crusher, the materials are heated in the crushing process to dehumidify and devolatilize, then the materials are crushed to a proper length through self-pressing blanking of a blanking bin and flow guiding compression compaction of a compacting mechanism, the materials are fed into a melting screw rod, after high-compression-ratio melting and homogenization flash evaporation are finished in the melting screw rod, the materials are fed into a homogenization tackifying reactor for homogenization and tackifying through primary filtration, after tempering is finished, the finished melt is subjected to secondary filtration to form a slice, or the finished melt is directly fed into a melt direct spinning system for spinning, compared with the traditional production mode, the pretreatment process is shortened, and the material has no large water resource consumption and energy consumption. Compared with the international advanced level, the production line has the advantages that the equipment efficiency is doubled, and the energy consumption of unit products is reduced by 20%.
Drawings
FIG. 1 is a schematic overall flow diagram of the present application;
FIG. 2 is a schematic structural view of the through-heating crusher of the present application;
FIG. 3 is a schematic side view of the crushing blade of FIG. 2;
fig. 4 is a schematic structural diagram of a blanking bin in the present application;
FIG. 5 is a cross-sectional view of the blanking magazine of FIG. 4;
FIG. 6 is a schematic view of a compacting mechanism of the present application;
FIG. 7 is a schematic view of the cutterhead portion of FIG. 6;
FIG. 8 is a schematic view of the compression melting section structure of the melting screw of the present application;
FIG. 9 is a schematic diagram of the homogenizing flash section of the melting screw of the present application;
FIG. 10 is a schematic diagram of the structure of the primary filtration in the present application;
FIG. 11 is a top view of the primary filtration of the present application;
FIG. 12 is a schematic view of the structure of the secondary filtration in the present application;
FIG. 13 is a schematic view of the structure of the filter element of the present application;
FIG. 14 is a schematic diagram of a homogenizing and tackifying reactor;
FIG. 15 is a plot of shear viscosity vs. shear rate for a regenerated slice and a normal slice at 280 ℃;
FIG. 16 is a plot of the shear viscosity vs. shear rate for a regenerated slice and a normal slice at 285 ℃;
FIG. 17 is a plot of shear viscosity vs. shear rate for a regenerated slice and a normal slice at 290 ℃;
FIG. 18 is a graph showing the variation of non-Newton index with temperature for recycled polyester chips and normal polyester chips at different shear rates;
FIG. 19 is a plot of shear stress vs. numerical vs. shear rate vs. numerical for a regenerated slice, a normal slice, and a mixed slice (mass ratio 1:1) at 290 ℃;
FIG. 20 is a DSC curve of a recycled polyester slice after crystallization drying;
FIG. 21 is a TGA graph of recycled polyester chips.
Reference numerals in the drawings: 1. a heat-transfer crusher; 11. a feed inlet; 12. a push plate; 121. a connecting rod; 13. swing arms; 14. a crushing knife; 141. a cutter body; 142. crushing and fixing a cutter; 143. a filter screen; 144. crushing a movable cutter; 15. a baffle; 151. a through hole; 16. a heating medium inlet; 17. a suction port; 18. a discharge port; 2. a blanking bin; 21. a bin body; 211. a side opening; 22. a conical bottom; 23. discharging pipes; 24. a top cover; 25. a header; 251. a dust remover; 252. dust removing room; 26. a roller; 27. a beater; 28. pre-feeding a screw; 29. a conveyor screw; 3. a compacting mechanism; 31. compacting the movable knife; 311. a connection section; 312. an extrusion section; 313. a rotary cutting section; 32. compacting and fixing a cutter; 321. a fixed section; 322. a transition section; 323. a blade section; 324. a fixed cutter base; 33. a cutterhead; 34. a bottom; 35. an inclined plane; 36. a guide disc; 4. a screw sleeve; 41. compressing the fusion section; 42. a homogenizing flash section; 43. a flow-limiting ring; 5. primary filtering; 51. a cavity; 511. a first melt inlet; 512. a melt channel; 513. a screen set; 514. a first melt outlet; 52. a plunger; 53. a hydraulic cylinder; 531. a position lever; 54. closing the slide valve; 541. a back flushing port; 55. a heating plate; 6. secondary filtration; 61. a lower cover plate; 611. a second melt inlet; 612. a shunt port; 62. a fin; 63. a filter element; 631. a filter stick; 632. a filter medium; 633. a skeleton; 634. a melt channel; 64. an upper cover plate; 641. a second melt outlet; 7. a homogenizing tackifying reactor; 71. a stirrer; 711. a stirring motor; 712. a rotating shaft; 72. a net tray; 73. a kettle body; 74. a reactor inlet; 75. a vacuumizing interface; 751. a branch pipe; 76. the reactor outlet.
Detailed Description
In this case, a process for regenerating the clean-free waste material is described as follows in connection with fig. 1:
after the treated waste is collected, crushing, blanking, compressing, compacting, melting, primary filtering, tempering, tackifying and secondary filtering are sequentially carried out, so that the cast strip is cut into slices or is transferred into a melt for direct spinning; the crushing procedure is provided with a suction system in a matching way, and the first dehydration and devolatilization are completed while crushing; the crushed materials are transferred into a blanking bin, a dust remover is arranged at the top of the blanking bin, a beater and a roller are arranged at the bottom of the blanking bin, the roller forms extrusion and dragging actions on the materials falling onto the beater, the beater is arranged below the roller, the materials extruded and dragged by the roller are loosened and crushed again, and the beater and the roller are matched to complete self-compression blanking of the materials; the material is transferred to a compression compacting process through a blanking process, the compression compacting process is completed in a compacting mechanism, the compacting mechanism comprises a second suction system and a compacting cavity, the suction system is positioned at the top of the compacting cavity, and the compression compacting process is matched to complete the second degassing and devolatilization; the melting process is completed in a melting screw, the material after compression and compaction is sent into the melting screw through a feeding screw, the melting screw comprises a screw sleeve, a compression melting section and a homogenization flash evaporation section, wherein the compression melting section and the homogenization flash evaporation section are arranged on two sides of the screw sleeve, a flow limiting ring is sleeved between the screw sleeve and the tail end of the compression melting section, the compression ratio is 3-30, the melt pressure at the flow limiting ring is more than 10MPa, the melt enters the homogenization flash evaporation section in a film shape through a slit between the flow limiting ring and the screw sleeve, the homogenization flash evaporation section is connected with a suction system III, the vacuum degree of the homogenization flash evaporation section is ensured to be 50-5000Pa, and the third suction is completed; the melt extruded by melting is filtered once, and is pumped for the fourth time through the tempering and tackifying process provided with a pumping system four, and then is filtered twice to be output as a finished product melt.
In the regeneration process of the polyester waste, the crushing adopts the through-heating type crushing and is matched with a suction system I, the first dehydration and devolatilization are completed in the crushing process, a second suction system I is arranged in the compacting mechanism 3 and is matched with the cutter head 33, the compression movable knife 31 and the compression fixed knife 32 to realize the secondary crushing and compression of the waste, and the heating air inlet and the friction heat generation of the material are matched to remove all surface water, most of low-boiling-point organic impurities and dust generated by crushing, so that the second degassing and devolatilization are completed; the third suction of the melting screw is completed under the vacuum action of the homogenizing flash evaporation section 42, the melt film is instantaneously released under the pressure of the section, the flash evaporation effect occurs, and part of high boiling point organic impurities remained in the melt are gasified and rapidly taken away by a vacuum suction system; the last suction is carried out in the homogenizing and tackifying reactor, small molecules generated by the reaction are removed, the uniformity of the viscosity of the product is improved, the design of the whole technical scheme adopts four times of degassing and devolatilization to remove organic impurities, and two-stage filtration to remove mechanical impurities in the product, so that the defect that the traditional production mode is required to rely on water washing to remove impurities is overcome.
In particular to a heat-passing crushing procedure, in the crushing process, the principle of small power consumption, strong treatment capacity, narrow crushed material length distribution and no melting in the crushing process is adopted for research and development. Therefore, in the heat-passing crushing process, crushing is realized by adopting a heat-passing crusher, and referring to fig. 2 and 3, the structure of the heat-passing crusher comprises a processing cavity for crushing, a push plate 12, a swing arm 13 and a crushing knife 14 which are arranged in the processing cavity, a suction port 17 is arranged at the top of the processing cavity, a heating medium inlet 16 is arranged at the bottom of the processing cavity, a feeding port 11 is arranged at the upper part of the processing cavity, a material to be processed enters the processing cavity through the feeding port 11, an independent drive (not shown in the drawing) is arranged on the swing arm 13, the swing arm 13 drives the push plate 12 to do reciprocating motion, the material entering the processing cavity is pushed into the crushing knife 14, a discharge port 18 is arranged at the bottom of the crushing knife 14, and the crushed material is sent into the blanking bin 2 through the discharge port 18.
On the basis of the scheme, the crushing cutter 14 comprises a cutter body 141, a crushing fixed cutter 142, a filter screen 143 and a crushing movable cutter 144, wherein the crushing movable cutter 144 is arranged on the outer wall of the cutter body 141, the filter screen 143 is wrapped outside the cutter body 141, the crushing fixed cutters 142 are arranged in two rows and are respectively arranged at the outer edges of the two ends of the filter screen 143, the crushing fixed cutters 142 are positioned above the cutter body 141, and the crushing fixed cutters 142 and the crushing movable cutter 144 are matched to realize crushing of fibers. The screen 413 is provided with screen holes (not shown), and the length of the cut crushed aggregates can be controlled by using screen holes with different diameters; meanwhile, the filter screen 143 with the sieve mesh structure also avoids the problem that crushed aggregates are easy to be entangled on the crushing knife.
The embodiment is applied to crushing waste materials such as waste silk and the like, a detector is arranged at a feed port 11, when the condition that the waste silk enters the feed port is detected, a mechanical arm 13 is started, a push plate 12 is driven to swing anticlockwise along a swing arm 13, the waste silk at the feed port 11 is pushed between a cutter body 141 and a filter screen 143 of a crushing cutter 14, the crushing cutter 14 is automatically started, the cutter body 141 starts to rotate, when the waste silk falls on the cutter body 141, the crushing fixed cutter 142 is in a fixed state due to the fact that the cutter body 141 is in a rotating state, fibers run in a cutter groove, the waste materials such as the waste silk are broken and form broken segments under the friction effect of the crushing fixed cutter 142 and a crushing movable cutter 144, when the broken segments are longer than 10cm, the broken segments are suitable to melt, and the broken segments leak out through the filter screen 143 and are sent into the next working procedure through a discharge port 18; when the crushed sections are longer than 10cm, the crushed sections still circulate between the crushing fixed knife 142 and the knife body 141, and the crushed sections are not sent to the next working procedure until the crushed sections are shorter than 10 cm.
In the heat-introducing crushing step, hot air is introduced into the bottom of the heat-introducing crusher 1 by means of the heating medium inlet 16, and the heating medium introduced into the heating medium inlet 16 is dry hot air with the temperature of 100-150 ℃, so that the water vapor and volatile matters in the oil agent in the polyester waste are removed for the first time. Meanwhile, a suction port 17 is arranged at the top of the matched heat-conducting crusher 1, so that volatile matters are easy to separate from the system, and dust is collected and reentered into the recovery system after the suction and exhaust gas is filtered.
The open semi-enclosed structure feeding channel of the heat-transfer type crusher 1 improves the efficiency of a single crusher by more than one time, the crushing length is less than or equal to 10cm when the rotating speed of a crushing roller is 60rpm, the yield reaches 3-4t/h, the rated power is only 132kw, and the crushing energy consumption is reduced from 56kwh/t to 16.5kwh/t; in the production process, the hot air at 120 ℃ is introduced, so that about 10% of moisture and oil volatile matters in the polyester waste can be removed. Meanwhile, the structure expands the range of raw materials, and can crush soft waste silk, such as DTY waste silk, terylene waste cloth and other raw materials, and the size of the crushed material is controlled within 10 cm.
As the preference of above-mentioned scheme, still be provided with baffle 15 in the processing chamber, baffle 15 is located push pedal 12 below to extend to the processing chamber inner wall department of crushing sword 14 contralateral side by crushing sword 14 below, baffle 15 is convex structure, the upper end is high with feed inlet 11 etc. and the lower extreme is then located on the shell inner wall of push pedal 12 below, under the condition that does not influence push pedal 12 normal feed at this baffle 15, in avoiding push pedal 12 to return with waste materials such as civilian silk waste silk bring push pedal 12 into, both avoided leaking the material phenomenon, reduce the clearance work, simultaneously, in whole crushing process, will not have the material carried back by push pedal 12, improved its work efficiency. Meanwhile, in order not to influence heating, through holes 151 are further formed in the baffle 15, so that the passage of dry and hot air is facilitated.
The polyester waste silk has small density and strong hydrophobicity, is easy to generate static electricity, is fluffy and is easy to wind and bridge, and a common bin adopts a gravity automatic blanking mode, so that a crushed material section is easy to bridge and can not smoothly blanking. In order to improve the production line efficiency, an intermediate bin is required to be designed to store crushed aggregates, namely, in the self-pressing blanking process in the scheme, in the process, the self-pressing blanking of the materials is completed by combining with fig. 5, the blanking process adopts a blanking bin 2 with a structure shown as 4 and fig. 5 to perform self-pressing blanking, a dust remover 251 is arranged at the top of the blanking bin 2, the blanking bin 2 comprises a bin body 21, a conical bottom 22 and a blanking pipe 23, the bin body 21 is of a square columnar structure, the conical bottom 22 is communicated with the lower part of the bin body 21, and the blanking pipe 23 is communicated with the conical bottom 22; the top of the bin body 21 is provided with an upper opening, a top cover 24 is movably arranged at the upper opening, the top cover 24 is opened for feeding, a dust remover 251 is arranged in the bin body 21, and the dust remover 251 is externally connected with a collecting pipe 25.
The upper opening extends downwards from the top of the bin body 21 to form a front wall, a rear wall, a left wall and a right wall, two dust collectors 251 are respectively arranged on the front wall and the rear wall, water vapor and volatile matters in dust, scraps and waste materials are sucked, discharged after processes such as filtration, electrostatic degreasing and the like, pollution to the environment is avoided, PET dust is effectively reduced and enters a screw rod to cause the reduction of product quality, the front wall and the rear wall extend to two sides respectively and form two dust collecting chambers 252 with the bin body 21, the two dust collecting chambers 252 are communicated through a collecting pipe 25, in the embodiment, the dust collectors 251 are columnar dust collecting bags, and the dust collecting chambers 251, the dust collecting chambers 252 and the collecting pipe 25 form a dust collecting mechanism; a plurality of rollers 26 are horizontally arranged at the joint of the bin body 21 and the conical bottom 22, and a plurality of groups of beater 27 are arranged below the rollers 26; the position of the blanking pipe 23 connected with the conical bottom 22 is provided with a pre-conveying screw 28, the pre-conveying screw 28 is horizontally arranged in the conical bottom 22 and horizontally crossed with the beater 27, the conveying screw 29 is positioned in the blanking pipe 23, the pre-conveying screw 28 is divided into two sections, the screw thread directions of the two sections of pre-conveying screws are opposite, the conveying screw 29 is vertically arranged below the pre-conveying screw 28, and the starting end of the conveying screw 29 is positioned right below the two sections of pre-conveying screws; the thread directions of the two sections of pre-feeding screws are opposite, the waste silk after the beater 27 is loosened is extruded towards the middle, a conveying screw 29 is vertically arranged in the middle of the two sections of pre-feeding screws 28, and the conveying screw 29 extrudes the waste silk downwards to complete the self-compression blanking process.
The present embodiment is applied to the storage of broken waste silk, waste materials such as broken waste silk in the thermal breaking process are fed through an upper opening, then a top cover 24 is covered at the upper opening, at this time, broken waste silk broken segments fall on rollers 26 in a bin body 21, after the adjacent rollers 26 squeeze and primarily disperse the broken fiber segments regularly under the rolling action of the rollers 26, the primarily dispersed broken fiber segments fall into a beater 27, under the action of the beater 27, the broken fiber segments fall into a pre-feeding screw 28 after being loosened and broken again, the rotating speed of the pre-feeding screw 28 is about 30r/min, the rotation of the pre-feeding screw 28 drives materials to be transported in a spiral manner, further pre-homogenizes fibers, after the broken fiber segments fall from the pre-feeding screw 28, the broken fiber segments directly fall on a conveying screw 29, and are homogenized again under the rotation of the conveying screw 29, when the fibers are output from a blanking pipe 23, the broken fiber segments in the state can be directly fed into a twin-screw extrusion melting unit to form a melt with good spinning uniformity.
For further degassing and dewatering, a diversion compression compacting process is further arranged after the self-compression blanking process, and diversion compression compacting is completed in a compacting mechanism 3, specifically, the compacting mechanism 3 comprises an outer cover, a cutter disc 33, a compaction movable cutter 31 and a compaction fixed cutter 32, the outer cover is of a hollow columnar structure, the cutter disc 33 is horizontally arranged on the bottom 34 of the outer cover, an inclined plane 35 is arranged between the bottom 34 and the cutter disc 33, and the compaction movable cutter 31 is spirally arranged on the cutter disc 33 through a guide disc 36; an extrusion section 312 is further arranged between the connecting section 311 and the rotary cutting section 313 of the compaction moving blade 31, the compaction moving blade 31 is connected with the cutterhead 33 through the connecting section 311, the rotary cutting section 313 is connected with the connecting section 311 through the extrusion section 312, and the distances between the extrusion section 312, the rotary cutting section 313 and the cutterhead 33 are increased progressively; the compaction stationary knife 32 further comprises a fixing section 321 and a transition section 322, wherein one side of the fixing section 321 is fixed on the inner wall of the compaction mechanism 3 above the cutterhead 33, and the other side extends towards the compaction movable knife 31 through the transition section 322 to form a blade section 323 with decreasing thickness. The compacting mechanism 3 formed by the scheme cooperates with a heating air inlet (not shown in the figure) at the bottom of the cutter head 33 to form a spiral preheating compression compacting mechanism, and polyester waste materials and the like fed from the blanking bin 2 are secondarily crushed and compressed through the cutter head 33 rotating at high speed and a flow guiding element (such as a compacting fixed cutter 32, a compacting movable cutter 31 and the like), wherein the stacking density is 200kg/m 3 Lifting to 600kg/m 3 The feeding efficiency is greatly improved, and the horizontal distance d between the compaction stationary knife 32 and the compaction movable knife 31 is not less than 10mm; in the setting process, the compaction stationary knife 32 and the compaction movable knife 31 in the above scheme can be preferably set as follows: one end (namely, the connecting section 311) of the compaction moving blade 31 is connected with the cutterhead 33, and the other end (namely, the whole rotary cutting section 313 and part of the extrusion section 312) is not contacted with the cutterhead 33; the compaction moving blade 31 passes through the linkThe connection section 311 is connected with the guide disc 36 and the cutter 33, the rotary cutting section 313 is connected with the connection section 311 through the extrusion section 312, the distance between the extrusion section 312 and the rotary cutting section 313 and the cutter 33 increases progressively, and the upper surface of the rotary cutting section 313 is higher than the upper surface of the extrusion section 312.
In the compacting process, the waste to be treated is led into a housing, equipment is started, the waste rotates along with the rotation of a cutter disc 33, in the rotating process, longer waste such as filaments and fragments can be contacted with a compacting stationary knife 32 which is arranged in a spiral manner under the action of centrifugal force, and the blade sections 323 directly scratch the waste and chop the waste, so that the size of the waste is smaller and smaller, the waste is called a chop section which meets the requirement, the chop section rotates on the cutter disc 33 at a high speed, the chop section is further cut off under the action of a rotary cutting section 313 protruding on the cutter disc 33, and simultaneously, the chop section and the cutter disc 33 and the chop section and the extrusion section 312 rub with each other to generate heat, and along with the rise of temperature, the residual moisture and oil on the chop section are evaporated; meanwhile, under the action of internal pressure, broken segments are uniformly distributed on the cutter head 33, waste wires are gradually compacted, and the upper layer feeding does not affect the compaction of the lower layer waste wires, so that the feeding and compacting processes can be simultaneously carried out, and the compacted waste wires are conveyed to an extrusion melting screw for melting through a screw at the bottom and enter the subsequent treatment process.
In the use process, the compaction stationary knife 31 is preferably arranged in a clockwise ascending spiral manner, the horizontal distance d between the compaction stationary knife 31 and the compaction movable knife 32 is not less than 10mm, so that the waste materials can rotate along the direction of the compaction movable knife 32 to be compressed, and meanwhile, the compaction stationary knife can collide with the stationary knife in the rotation process for crushing the hard solid such as polyester waste materials; the blade section 323 is the most stressed and most easily worn stage, the service cycle is shorter, and the fixed section 321 is used as a fixing mechanism, so that the wear is relatively minimum, in the application, the blade section 323 and the transition section 322 are preferably integrated, the transition section 322 and the fixed section 321 can be integrated or split, when the blade section 323 is worn or broken, the blade section 323 and the transition section 322 can be directly removed, a new blade section 323 can be replaced, and the replacement is convenient and the practicability is strong; the compacting movable knife 31 adopts an all-wing structure, one end of the compacting movable knife is fixed on the cutterhead 33 through a guide disc 36, and the other end of the compacting movable knife is gradually separated from the cutterhead 33, so that the stirring speed of the crushing section is accelerated, the kinetic energy of the crushing section is improved, and meanwhile, the plasticizing is facilitated.
The rotation frequency of the cutter head 33 is preferably 10.0-50.0Hz, and the cutter head 33 drives the crushed aggregates to rotate at a high speed, so that the crushed aggregates interact with the compaction stationary knife 31 and the compaction movable knife 32 to realize the compaction process of the crushed aggregates. Meanwhile, a heating air inlet is arranged at the bottom of the cutter head 33, a suction system (not shown in the figure) is arranged at the top of the cutter head, the devolatilization force of the system is improved, all surface water and most low-boiling-point organic impurities are removed, and dust generated by compaction and crushing is collected; in the process of heating air at 80-120 ℃ and in the process of driving waste materials to rotate at a high speed by the cutter head 33, due to frictional heat generation, heat medium can be led to the bottom of the cutter head 33 to accompany heat, the temperature of the waste materials is controlled between 100 ℃ and 180 ℃, the maximum temperature can reach 200 ℃ (the temperature can not only contribute to the heat medium, but also contribute to frictional heat generation), and moisture and oiling agents carried in the waste wires can be volatilized and further removed.
The rotation speed of the compacting mechanism 3 can reach 400-500 rpm, and the stacking density is 200kg/m 3 Up to 600kg/m 3 The productivity is 30 tons/day, the feeding efficiency is improved by 80 percent, and the moisture and the volatile matters in the waste silk can be removed by about 10 percent.
The method specifically comprises the step of flow-limiting segmented melting, wherein the state of the polyester waste is changed through extrusion melting of a screw, the degassing and devolatilization effects are also realized in the extrusion melting process of the screw, and the degradation is reduced as much as possible. The sectional screw structure is adopted in this case, and the material is fed and is carried through the feed section, compaction simultaneously gradually, so the screw groove width of screw thread constantly changes.
The compression ratio of the screw thread is large enough to ensure that the material is fully compact, reach the state required by melting, and improve the feeding efficiency. Particles or broken sheet materials are easy to deform on the surface after being compressed and are attached to the inner wall of the machine barrel, so that the particles or broken sheet materials are easy to compress; the powder material has a relatively large sliding property, and therefore, the powder material is retarded in compression melting time and position from those of the particle or sheet material. Meanwhile, as the void ratio of the polyester waste is large and the density of the material is smaller, a large amount of air can be remained in the material, and the solid bed is isolated. The feeding section of the screw in the project adopts a high compression ratio design.
Referring to fig. 8, the compression melting section 41 primarily melts and initially mixes the melt/resin mixture fed from the upstream feed section while establishing pressure. The heat required for melting the polyester waste is provided by the heating equipment of the screw itself and by friction heat. The diameter of the screw rod is 165mm, the total length-diameter ratio is 40, the compression ratio is 3.5, and the friction heat accounts for a larger proportion in the whole energy required by melting; meanwhile, because the resin needs to be primarily dispersed and distributed to be mixed, the melt with too low viscosity is unfavorable for the two mixing processes, and especially under the condition of mixing two or more resins with larger melt viscosity difference, the too high melt temperature is unfavorable for heat transfer and heat dissipation in the melt, so that the temperature of the compression melting section 41 is basically kept between 264 and 282 ℃ by adopting lower temperature control in the project, and meanwhile, the state of high compression ratio (the compression ratio is controlled between 3 and 30) is maintained, and the condition that the overheated melt contains unmelted waste yarns is avoided.
The homogenizing and flashing section 42 adopts a low compression ratio design (the compression ratio is controlled to be 1-2), and the pressure established by the compression and melting section 41 is instantly released when entering the homogenizing and flashing section 42, so that partial volatile matters are promoted to be 'flashed', and the volatile matters are removed by being matched with a vacuum pumping system.
Meanwhile, in order to reduce degradation in the screw extrusion melting process, technological parameters are optimally designed, and the process is realized by reducing the melting extrusion temperature, weakening shearing and other modes, and the feeding section is as follows: 24.0Hz; the rotation speed of the compression melting section 41 was 56rpm, the extrusion temperature: 282-275-273-272-264-295-243-245-247-246-230 ℃.
On the basis of the above, in the embodiment, a flow limiting ring 43 is designed between the compression melting section 41 and the homogenizing flash section 42, the distance between the flow limiting ring 43 and the screw sleeve 4 is extremely small (less than or equal to 5 mm), on one hand, the compression melting section 41 can build higher pressure, and part of high-boiling-point substances can flash and leave the system after being instantaneously released in the homogenizing flash section 42. On the other hand, the regenerated polyester melt passes through the flow limiting ring 43 in a film shape, the specific surface area is larger, the pressure between the screw compression melting section 41 and the homogenizing flash section 42 is instantaneously converted, substances such as moisture, oil volatile matters, ethylene glycol and the like in the regenerated polyester melt are separated from the system, then the regenerated polyester melt is vacuumized by a vacuum pump, and small molecular substances entrained in the melt are volatilized from the surface of the melt and extracted from the melt system, so that most organic impurities in the polyester melt can be removed.
In the existing original polyester polymerization technology, a filter is usually arranged before the polymerization reaction of the polymer is finished or the next procedure, and a conventional regenerated polyester filter is usually filtered by adopting a screen, so that impurities and gel particles are removed to a great extent in the filtering mode, but the filtering precision cannot be further improved due to the defects of the structure of the filter, the filtration and the stopping of impurities and gel particles with smaller particle sizes cannot be realized, and meanwhile, the online replacement cannot be realized conveniently and rapidly, so that the continuity of the production process is influenced; in addition, the impurity content in the polyester waste is high, on the one hand, the impurities in the regenerated polyester melt are removed as much as possible, and on the other hand, the melt viscosity drop caused by higher pressure in the filtering process is reduced. In the filtering process of the embodiment, the filtering adopts combined filtering, namely primary filtering 5 and secondary filtering 6, the primary filtering 5 adopts a coarse filtering structure shown in figures 10-11, the coarse filtering adopts a 4-column backflushing type filter, the on-line switching can be carried out, and the filtering precision is 30-60 mu m; the front end and the rear end of the coarse filtration are provided with pressure sensors, and when the pressure reaches a set value, automatic backflushing filtration is realized; the secondary filtration 6 adopts a fine filtration structure as shown in fig. 12 and 13, the fine filtration adopts a candle core type filter, a filter screen adopts a sintered metal net, the filtration precision is 20 mu m, and the on-line switching is carried out every 30 hours or when the pressure reaches 60 kg. The ash content in the regenerated polyester chip is less than or equal to 0.15 percent, the content of agglomerated particles is less than or equal to 6 per mg of polyester, and the level of spinnable filaments is reached.
The primary filtering 5 and the secondary filtering 6 are respectively arranged before and after the back-mixing tempering and tackifying process, polyester waste can be inevitably degraded in the process of extrusion and melting by a screw, in order to improve the viscosity of regenerated polyester, small molecules such as oil agent and the like in waste silk can be further removed, the quality of regenerated polyester melt is homogenized, the purpose of regenerated products is expanded, the back-mixing tempering and tackifying process is carried out in a homogenizing and tackifying reactor 7, homogenization and tackifying are carried out after the waste silk is extruded and melted, and in combination with fig. 14, the homogenizing and tackifying reactor 7 comprises a kettle body 73 and a stirrer 71, a reactor inlet 74 and a reactor outlet 76 are arranged at the bottom of the kettle body 73, the reactor inlet 74 and the reactor outlet 76 are respectively arranged at two ends of the kettle body 73, the reactor inlet 74 is communicated with the primary filtering 5 by a pipeline (not labeled in the figure), a depolymerizing agent inlet (not labeled in the figure) is also connected to the pipeline, the reactor outlet 76 is communicated with the secondary filtering 6, and the melt after homogenization and tackifying is output; the top of the kettle body 73 is provided with a vacuumizing interface 75, the vacuumizing interface 75 is connected with a vacuum pumping system (not shown in the figure and can be realized by a vacuum machine, a fan and the like), so that the vacuum degree in the kettle body 73 is 50-150Pa (preferably 100-130 Pa), thus, partial micromolecular impurities can be continuously removed along with the evaporation of Ethylene Glycol (EG), the viscosity of a regenerated polyester product is improved, the impurity content is reduced, the vacuumizing interface 75 is connected with a branch pipe, the branch pipe is communicated with a depolymerizing agent inlet, the depolymerizing agent inlet is connected to a pipeline between the primary filtering 5 and the reactor inlet 74, the EG in the pumped micromolecular is recovered and is combined with a pure/fresh depolymerizing agent through a branch pipe 751 to form a depolymerizing agent which is input into the pipeline, and the micro alcoholysis of a regenerated polyester melt can be realized in the pipeline, and the molecular weight distribution of the polyester melt are improved; the stirrer 71 is positioned in the kettle body 73, two ends of the stirrer 71 are respectively connected with the stirring motor 711 through a rotating shaft 712, a plurality of net plates 72 are arranged in the stirrer 71, the net plates 72 are arranged in a mutually parallel mode, grids (not shown in the figure and can adopt meshes of a grid structure) are distributed on the net plates 72, and the grids of two adjacent net plates 72 are in an staggered state so as to improve the stirring efficiency; the rotatable stirrer 71 is matched with a fixed kettle body 73 with a reactor inlet 74 arranged at the bottom, the melt forms a film under stirring, the surface of the melt is continuously updated, then a vacuum pumping system of a vacuum pumping interface 75 is matched, small molecular impurities are continuously removed along with the evaporation of Ethylene Glycol (EG), the viscosity of the melt in the kettle body 73 is improved, the impurity content is reduced, a plurality of groups of net trays 72 are arranged in parallel in the stirrer 71, grids on two adjacent net trays 72 are in a staggered state, the surface updating efficiency during stirring is improved, the back mixing of regenerated polyester melt can be realized, and the uniformity of material quality is improved; wherein, through optimizing parameters such as reaction temperature, vacuum, etc., make final melt index reach the design scope, specifically set as follows: the liquid level at the reactor inlet 74 was controlled at 11.1% and the temperature was 280.4 ℃; the liquid level of the section where the stirrer 71 is positioned is 70-80%, and the rotating speed of the stirrer 71 is 4.0RPM; the pressure in the kettle body 73 is 136.0Pa, and the temperature is 280-282 ℃; the liquid level at the reactor outlet 76 is 20-30% and the pressure is 120-130Pa. The fluctuation range of melt intrinsic viscosity after homogenization and tackifying is less than or equal to 0.025dl/g, the B value is less than 10, the moisture is less than or equal to 50ppm, and the diethylene glycol content is less than or equal to 1.2%.
The melt regenerated by the above scheme is tested, and the quality index is shown in table 1.
TABLE 1 quality index summary of regenerated melt
The regenerated slices formed from the above regenerated melt cast and forged slices were tested and compared with conventional slices to obtain the shear viscosity/shear rate graphs shown in the figures (280 ℃, 285 ℃,290 ℃), with specific reference to figures 15 (280 ℃), 16 (285 ℃) and 17 (290 ℃). As can be seen from fig. 15 to 17, the apparent viscosity of the polyester in the molten state decreases with an increase in the shear rate, and the polyester exhibits a characteristic of thinning by shear force. According to the classification of non-newtonian fluids, polyester melts with this feature are referred to as pseudoplastic fluids. Shear thinning is caused by the reversible disruption of the pseudo-network entanglement structure by shear forces. As the shear rate increases, the polyester macromolecules undergo conformational changes under the influence of shear forces, disentanglement and orientation along the flow direction. The breaking speed of the entangled structure is greater and greater than the formation speed as the shear rate increases, so the apparent viscosity is not constant but decreases as the shear rate increases.
The curve "drop" at 290 ℃ is greatest from the slope of the curve at different temperatures, and this drop gradually decreases with increasing temperature. This phenomenon shows that as the melt temperature increases, the effect of the change in shear rate on the apparent viscosity of the melt decreases. Meanwhile, as the temperature increases, the apparent viscosity of the recycled polyester tends to be consistent with the change trend of the shearing rate of the common polyester melt.
FIG. 18 is a graph showing the temperature dependence of non-Newtonian index for recycled and normal polyester chips at various shear rates ranging from 200 to 12000s -1 . It can be seen from fig. 18 that the non-newtonian index of the melt at low shear rates is greater than the non-newtonian index at high shear rates, and that the value of this index is also not constant at a certain shear condition, but increases with increasing temperature. Meanwhile, the change trend of the regenerated polyester is consistent with that of the common polyester.
FIG. 19 is a plot of shear stress vs. numerical vs. shear rate vs. numerical for a regenerated slice, a normal slice, and a mixed slice (mass ratio 1:1) at 290 ℃. As can be seen from fig. 19, the relationship between the shear stress and the shear rate of the conventional polyester chip is nearly a straight line, and the non-newtonian index of the regenerated chip increases with a larger change in the shear rate; the melt viscosity of the final product is between 0.65 dl/g and 0.80 dl/g.
As can be seen from fig. 20 and 21, the melting point of the recycled polyester is 258 ℃, the decomposition temperature at 95% of thermal weight loss is 397.4 ℃, and a better quality index is achieved.
The applicant also summarized the cost, energy consumption, physical properties, reuse use, and the like, and the results are shown in table 2.
Table 2 cost comparison table for different recovery methods
The process has the advantages of wide range of usable raw materials, high automation degree, high production efficiency, low energy consumption, zero pollution and zero emission of the whole process, and stable quality of the regenerated polyester.
Claims (6)
1. A cleaning-free waste regeneration process is characterized in that: after the treated waste is collected, crushing, blanking, compressing, compacting, melting, primary filtering, tempering, tackifying and secondary filtering are sequentially carried out, so that the cast strip is cut into slices or is transferred into a melt for direct spinning;
the crushing procedure is provided with a suction system in a matching way, and the first dehydration and devolatilization are completed during crushing; the crushed materials are transferred into a blanking bin, the top of the blanking bin is provided with a dust remover, the bottom of the blanking bin is provided with a beater and a roller, the roller forms extrusion and dragging actions on the materials falling on the beater, the beater is arranged below the roller, the materials extruded and dragged by the roller are opened and crushed again, the beater and the roller are matched to complete self-compression blanking of the materials,
the crushing is completed by adopting a through-heating type crusher, the crushing device comprises a processing cavity, a push plate, a swing arm and a crushing cutter which are positioned in the processing cavity, wherein a suction port is arranged at the top of the processing cavity, the suction port is connected with a suction system, a heating medium inlet is arranged at the bottom of the processing cavity, dry air with the temperature of 100-150 ℃ is introduced into the heating medium inlet, a feeding port is positioned at the upper part of the processing cavity, materials to be processed enter the processing cavity through the feeding port, the swing arm is provided with an independent drive, the drive drives the push plate to do reciprocating motion through the swing arm, the materials entering the processing cavity are pushed into the crushing cutter, a discharging port is arranged at the bottom of the crushing cutter, and the crushed materials are fed into a blanking bin through the discharging port;
The material is transferred to a compression compacting process through a blanking process, the compression compacting process is completed in a compacting mechanism, the compacting mechanism comprises a second suction system and a compacting cavity, the suction system is positioned at the top of the compacting cavity, the compression compacting process is matched to complete the second degassing and devolatilization,
the discharging bin comprises a bin body, a conical bottom and a discharging pipe, wherein the top of the bin body is fed, a dust remover is arranged in the bin body below the feeding, and the dust remover is externally connected with a collecting pipe; the conical bottom is internally provided with a pre-feeding screw rod which is horizontally crossed with the beater; a conveying screw rod is arranged in the discharging pipe,
the compression device comprises a compaction cavity, a cutter disc, a compression fixed cutter and a compression movable cutter, wherein the cutter disc is in non-fixed connection with the inner wall of the compaction cavity and is driven to rotate by independent driving; the bottom of the compaction cavity is provided with a heating air inlet for supplying heating air at 80-120 ℃;
The material after compression compaction is sent into a melting screw rod through a feeding screw rod to finish melting, the melting screw rod comprises a screw rod sleeve, a compression melting section and a homogenization flash evaporation section, wherein the compression melting section and the homogenization flash evaporation section are arranged on two sides of the screw rod sleeve, a flow limiting ring is sleeved between the screw rod sleeve and the tail end of the compression melting section, the compression ratio is 3-30, the melt pressure at the flow limiting ring is more than 10MPa, the melt enters the homogenization flash evaporation section in a film shape through a slit between the flow limiting ring and the screw rod sleeve, the homogenization flash evaporation section is connected with a suction system III, the vacuum degree of the homogenization flash evaporation section is guaranteed to be 50-5000Pa, and the third suction is finished;
the melt extruded by melting is filtered once, and is pumped for the fourth time by a homogenizing and tackifying reactor provided with a pumping system IV in the tempering and tackifying process, and then is filtered again to be output as a finished product melt.
2. The no-clean waste recycling process according to claim 1, wherein: the crushing cutter comprises a cutter body, a crushing stationary cutter, a filter screen and a crushing movable cutter, wherein the crushing movable cutter is arranged on the outer wall of the cutter body, the filter screen is wrapped outside the cutter body, the crushing stationary cutters are arranged in two rows and are respectively arranged at the outer edges of the two ends of the filter screen, the crushing stationary cutter is positioned above the cutter body, and the crushing stationary cutter and the crushing movable cutter are matched to realize crushing of fibers.
3. The no-clean waste recycling process according to claim 1, wherein: the homogenizing tackifying reactor comprises a kettle body and a stirrer, wherein a reactor inlet and a reactor outlet are arranged at the bottom of the kettle body, the reactor inlet and the reactor outlet are respectively arranged at two ends of the kettle body, the reactor inlet is communicated with primary filtration, and the reactor outlet is communicated with secondary filtration; the top of the kettle body is provided with a vacuumizing interface which is connected with a pumping system IV to ensure that the vacuum degree in the kettle body is 50-150Pa, the vacuumizing interface is connected with a branch pipe, the branch pipe is communicated with a depolymerizing agent inlet, and the depolymerizing agent inlet is connected to a communication pipeline between the reactor inlet and primary filtration; the stirrer is positioned in the kettle body and is connected with the stirring motor in a linkage way, a plurality of net plates are arranged in the stirrer, each net plate is arranged in a mutually parallel way, grids are distributed on the net plates, and the grids of two adjacent net plates are in a staggered state.
4. A no-clean waste recycling process according to any of claims 1-3, characterized in that: the primary filtering comprises a cavity, a plunger, a hydraulic cylinder, a closing slide valve and a heating plate, wherein the heating plate is arranged on the outer wall of the cavity, one end of the plunger is arranged in the cavity, the other end of the plunger is connected with a position rod of the hydraulic cylinder, a melt inlet and a melt outlet are arranged on the cavity, the melt inlet is communicated with the melt outlet through a melt channel, the melt channel penetrates through the cavity, a filter screen group is arranged between the melt inlet and the melt channel, the closing slide valve is arranged on the cavity on one side of the inlet, a back flushing port is arranged on the closing slide valve, the back flushing port is communicated with a cavity of the plunger to form a back flushing channel, a pressure sensor is arranged on the filter screen group, and the pressure sensor is respectively connected with the hydraulic cylinder and the closing slide valve so as to realize the transmission of pressure signals.
5. A no-clean waste recycling process according to any of claims 1-3, characterized in that: the secondary filtration comprises a lower cover plate, a filter element and an upper cover plate, wherein the side wall of the lower cover plate is provided with a melt inlet, and the top of the lower cover plate is provided with a plurality of shunt ports communicated with the melt inlet; the filter element consists of a filter rod, a filter medium and a framework, wherein a plurality of small holes are formed in the outer wall of the filter rod, a melt channel is formed in the middle of the filter rod, the small holes are communicated with the melt channel, the lower end of the melt channel is close to the bottom of the filter rod, the upper end of the melt channel penetrates through the top of the filter element, the filter medium is wrapped on the filter rod, and the framework is erected on the filter medium; the filter element is arranged between the upper cover plate and the lower cover plate, and the outer cylinder is sleeved outside the filter element; the upper cover plate is provided with a melt outlet which is communicated with the melt channel; the melt enters through the melt inlet, flows through the shunt port, then enters the melt channel through the framework, the filter medium and the small holes, and flows out through the melt outlet, thus completing the whole filtration.
6. A no-clean waste recycling process according to any of claims 1-3, characterized in that: the suction system adopts a fan or a vacuum machine; a fan or a vacuum machine is adopted as the second suction system; the third suction system adopts a vacuum machine to perform vacuum suction; and the suction system IV adopts a vacuum machine to carry out vacuum suction.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910052310.0A CN109576825B (en) | 2019-01-21 | 2019-01-21 | Cleaning-free waste regeneration process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910052310.0A CN109576825B (en) | 2019-01-21 | 2019-01-21 | Cleaning-free waste regeneration process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109576825A CN109576825A (en) | 2019-04-05 |
| CN109576825B true CN109576825B (en) | 2024-01-16 |
Family
ID=65917251
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910052310.0A Active CN109576825B (en) | 2019-01-21 | 2019-01-21 | Cleaning-free waste regeneration process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109576825B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110355908A (en) * | 2019-08-21 | 2019-10-22 | 安徽恒鑫环保新材料有限公司 | A kind of PLA waste recovery system of processing |
| CN111304785B (en) * | 2020-03-19 | 2022-05-27 | 福建永荣锦江股份有限公司 | Waste silk collecting system of spinning workshop |
| CN111334887A (en) * | 2020-03-30 | 2020-06-26 | 江苏志成新材料科技有限公司 | Polyester waste cloth regenerated fiber spinning process with efficient flow and improved quality |
| CN112899796A (en) * | 2021-01-11 | 2021-06-04 | 平顶山神马帘子布发展有限公司 | Preparation method of high-strength regenerated nylon 66 fiber |
| WO2023166433A1 (en) * | 2022-03-01 | 2023-09-07 | Fadebe S.P.A. | Method of recovery and regeneration of polyolefin plastics and relative recycling plants |
Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101967206A (en) * | 2010-09-15 | 2011-02-09 | 罗天韵 | Isoprenerubber post-treatment one-step processing technique and dehydrating and drying machine |
| CN102899729A (en) * | 2012-10-19 | 2013-01-30 | 宁波大发化纤有限公司 | Method for processing regenerated polyester staple fiber by using waste polyester textile |
| CN102990902A (en) * | 2012-12-31 | 2013-03-27 | 浙江栋斌橡机螺杆有限公司 | Extruding machine |
| CN103509205A (en) * | 2013-09-27 | 2014-01-15 | 浙江绿宇再生高分子材料有限公司 | Recovery process and device for synthetic fiber waste |
| CN105082399A (en) * | 2015-07-21 | 2015-11-25 | 浙江绿宇环保有限公司 | Fiber recovery unit for reusing waste silk |
| CN204932996U (en) * | 2015-07-21 | 2016-01-06 | 浙江绿宇环保有限公司 | A kind of filtration system |
| CN105525375A (en) * | 2016-02-22 | 2016-04-27 | 苏州金泉新材料股份有限公司 | Method for preparing polyester staple fibers from waste polyester fibers |
| CN105690600A (en) * | 2016-03-31 | 2016-06-22 | 浙江绿宇环保有限公司 | Waste fiber and product pre-treatment system |
| CN105803585A (en) * | 2016-03-31 | 2016-07-27 | 浙江绿宇环保有限公司 | Polyester-containing waste textile recycling technology |
| CN205588602U (en) * | 2016-03-31 | 2016-09-21 | 浙江绿宇环保有限公司 | Compress closely knit machine |
| CN107214929A (en) * | 2017-07-03 | 2017-09-29 | 刘小洁 | Cross-linked polymer nano-starch particle and preparation method thereof |
| CN208235040U (en) * | 2018-05-30 | 2018-12-14 | 陈大伟 | A kind of polyester disused cloth waste silk reutilization system |
-
2019
- 2019-01-21 CN CN201910052310.0A patent/CN109576825B/en active Active
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101967206A (en) * | 2010-09-15 | 2011-02-09 | 罗天韵 | Isoprenerubber post-treatment one-step processing technique and dehydrating and drying machine |
| CN102899729A (en) * | 2012-10-19 | 2013-01-30 | 宁波大发化纤有限公司 | Method for processing regenerated polyester staple fiber by using waste polyester textile |
| CN102990902A (en) * | 2012-12-31 | 2013-03-27 | 浙江栋斌橡机螺杆有限公司 | Extruding machine |
| CN103509205A (en) * | 2013-09-27 | 2014-01-15 | 浙江绿宇再生高分子材料有限公司 | Recovery process and device for synthetic fiber waste |
| CN105082399A (en) * | 2015-07-21 | 2015-11-25 | 浙江绿宇环保有限公司 | Fiber recovery unit for reusing waste silk |
| CN204932996U (en) * | 2015-07-21 | 2016-01-06 | 浙江绿宇环保有限公司 | A kind of filtration system |
| CN105525375A (en) * | 2016-02-22 | 2016-04-27 | 苏州金泉新材料股份有限公司 | Method for preparing polyester staple fibers from waste polyester fibers |
| CN105690600A (en) * | 2016-03-31 | 2016-06-22 | 浙江绿宇环保有限公司 | Waste fiber and product pre-treatment system |
| CN105803585A (en) * | 2016-03-31 | 2016-07-27 | 浙江绿宇环保有限公司 | Polyester-containing waste textile recycling technology |
| CN205588602U (en) * | 2016-03-31 | 2016-09-21 | 浙江绿宇环保有限公司 | Compress closely knit machine |
| CN107214929A (en) * | 2017-07-03 | 2017-09-29 | 刘小洁 | Cross-linked polymer nano-starch particle and preparation method thereof |
| CN208235040U (en) * | 2018-05-30 | 2018-12-14 | 陈大伟 | A kind of polyester disused cloth waste silk reutilization system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109576825A (en) | 2019-04-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109576825B (en) | Cleaning-free waste regeneration process | |
| CN109652872B (en) | Polyester waste regeneration system | |
| CN105821490B (en) | A kind of polyester disused cloth spinning pumping vacuum and mixing extruder | |
| CN101032826B (en) | Method of processing vegetable fibre formed pipe and the preparing system | |
| CN105082399B (en) | The fibrous recovery unit recycled for waste silk | |
| CN103640104A (en) | Method for recycling, cleaning and granulating waste mulching films | |
| CN107721118A (en) | A kind of multistage sludge high effective dehydration device | |
| CN103509205A (en) | Recovery process and device for synthetic fiber waste | |
| CN111360037A (en) | Kitchen waste wet-heat hydrolysis pretreatment system and wet-heat hydrolysis pretreatment process | |
| CN101905494A (en) | Process for producing regenerated polyester chip by using regenerated bottle chip and device thereof | |
| KR100982072B1 (en) | The rdf manufacture apparatus from mixture of waste plastics and sludge | |
| CN109576826B (en) | Polyester waste recycling process | |
| CN102785301A (en) | Waste plastics treating and utilizing system | |
| CN109435107A (en) | A kind of recycling waste plastic process system | |
| CN102642312A (en) | Processing method for recovering and processing PET (polyethylene glycol terephthalate) waste film in compounding way by using twin-screw extrusion melting | |
| CN104139470A (en) | Thin film type waste plastic recycling, reusing, washing and purifying system | |
| KR20070019318A (en) | method and apparatus for manufacture building materials using waste synthetic resinsand | |
| CN109778326A (en) | Polyester waste material regenerates directly spinning filament spun-bonded needle punched non-woven fabrics production technology | |
| CN206956218U (en) | The spinning system of the waste and old non-woven cloth reworked material fiber of high additive | |
| CN104139471B (en) | Thin film type waste plastic recycling, reusing, washing and purifying method | |
| CN111793836B (en) | Method for preparing fibers by directly spinning waste polyester textiles as raw materials | |
| CN109811416A (en) | A kind of regeneration is producing technology of non-woven fabrics | |
| CN209602678U (en) | A kind of polyester waste material regenerative system | |
| CN203994326U (en) | A kind of film class technics of reclaim of plastic waste recycling washing, purifying system | |
| KR101488150B1 (en) | Manufacturing method and device of recycling resin chip by using waste scrap |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information | ||
| CB02 | Change of applicant information |
Address after: 312000 No.6, Wanghai Road, Yuecheng District, Shaoxing City, Zhejiang Province Applicant after: ZHEJIANG LYUYU ENVIRONMENTAL PROTECTION Co.,Ltd. Address before: 312000 No. 6 hope road, Shaoxing, Shaoxing, Zhejiang Applicant before: ZHEJIANG GRERIAL ENVIRONMENTAL PROTECTION CO.,LTD. |
|
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20210519 Address after: Room 401, R & D building 2, 1567 Yuexiu North Road, Yuecheng District, Shaoxing City, Zhejiang Province, 312000 Applicant after: Zhejiang Lvyu Regeneration Technology Co.,Ltd. Address before: 312000 No.6 Wanghai Road, Yuecheng District, Shaoxing City, Zhejiang Province Applicant before: ZHEJIANG LYUYU ENVIRONMENTAL PROTECTION Co.,Ltd. |
|
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20210617 Address after: 438000 tangjiadu village committee, Yuwang sub district office, Huangzhou District, Huanggang City, Hubei Province Applicant after: HUBEI LYUYU ENVIRONMENTAL PROTECTION Co.,Ltd. Address before: Room 401, R & D building 2, 1567 Yuexiu North Road, Yuecheng District, Shaoxing City, Zhejiang Province, 312000 Applicant before: Zhejiang Lvyu Regeneration Technology Co.,Ltd. |
|
| GR01 | Patent grant | ||
| GR01 | Patent grant |