CN109719861B - Hard impurity material recycling and regenerating process - Google Patents

Abstract

Translated fromChinese

本发明属于再生塑料回收技术领域，提供了一种硬杂料回收再生工艺，工艺步骤至少包含：硬杂料预处理，盐水除杂，破碎，摩擦清洗，分选，热熔造粒，筛分干燥，废水处理，废气处理。The invention belongs to the technical field of recycled plastics recycling, and provides a hard miscellaneous material recovery and regeneration process. The process steps at least include: hard miscellaneous material pretreatment, salt water impurity removal, crushing, friction cleaning, sorting, hot melt granulation, screening Drying, waste water treatment, waste gas treatment.

Description

Hard impurity material recycling and regenerating process

Technical Field

The invention belongs to the technical field of recycled plastic recycling, and particularly relates to a recycling process of hard sundries.

Background

Plastic, which is a material that takes high molecular weight synthetic resin as an important component and can be molded into a certain shape under certain conditions and keep the shape unchanged at normal temperature, has been widely used in various fields of industry, agriculture, national defense and national economy. With the development of the petrochemical industry, the yield and consumption of plastics are gradually increased worldwide, waste plastics are more and more, and some capital-oriented countries with early development and high yield of the plastic industry already have the quantity of waste plastics of more than one million tons accounting for about 10 ten thousand of the total quantity of garbage, which becomes serious environmental pollution, so that the treatment of waste plastics becomes an extremely important research subject in all countries today.

The recycling of waste plastics is an important means for resource recycling and environmental protection, and is a resource recycling processing industry which is developed at present. The common waste plastic recovery process method is melting liquid state mixing, liquid state extrusion cooling granulation. Generally, recycled waste plastics are mixed in varieties, difficult to sort and even impossible to sort cleanly, and poor in compatibility, if the waste plastics are obtained by a common melting plasticizing and mixing granulation method, the obtained granular materials are mixed in color, poor and unstable in physical properties, and low in application value, so that expensive reactants or compatibilizers are required to be added for improvement, the cost is high, the effect is not ideal, and particularly, the mixed varieties are more and more serious.

At present, the common impurity removal mode of waste plastics is to remove impurities and recycle plastics by various modes such as manual sorting, electrostatic sorting, flotation, density sorting, wind power sorting and cleaning, but the sorting impurity removal effect is poor, the manual sorting can damage human health after long-time work, waste water resource waste can be caused in the process of recycling and regenerating waste materials, and the waste water pollution and waste gas pollution are serious.

Disclosure of Invention

In order to solve the above technical problems, the present invention provides a process for recycling hard impurities, which at least comprises the following steps: pretreating hard sundries, removing impurities by using brine, crushing, rubbing and cleaning, sorting, hot melting and granulating, screening and drying, treating wastewater and treating waste gas;

the hard impurity pretreatment is to remove light impurities and metal from the hard impurity;

the brine impurity removal step is to use a dehydrator for cleaning, and then carry out impurity removal treatment through a brine tank;

the crushing is to carry out wet crushing treatment on the dehydrated hard and impure plastics;

the friction cleaning is to convey the crushed plastic into a clean water washing tank through a screw, a stirring paddle is arranged in the clean water washing tank, hard sundries are classified in the first step to obtain upper floating materials and lower sinking materials, and the upper floating materials and the lower sinking materials are respectively conveyed into a dehydrator for dehydration and packaging;

the sorting is to sort the upper floating material and the lower sinking material which are subjected to the dewatering and packaging treatment respectively into electrostatic sorting equipment to obtain final sorted plastics;

the hot melting granulation is that various sorted plastics are conveyed by a screw to enter a hot melting device for heating and melting the plastics, the molten plastics enter cold water for hardening and bracing after passing through a filter screen and a die head with holes, and the hardened plastic strips are pulled into a granulator for granulation;

the screening and drying step is that granulated granular plastics are screened by a vibrating screen, plastic particles are sorted, and the plastic particles are packaged after being dried by blast air;

the wastewater treatment comprises the steps of performing inclined screen filtration, flocculation precipitation, air flotation impurity removal and oil removal on wastewater generated in the processes of salt water impurity removal, crushing and friction cleaning, and performing biochemical degradation on COD;

the waste gas treatment is to carry out waste gas collection, spray washing, electrostatic oil removal and oxidative decomposition treatment on waste gas generated in the hot melting granulation process, and then to discharge the waste gas.

In some preferred embodiments, the light impurity removal is that the plastic fragments fall from the height of 2-8 m, pass through a Z-shaped folded plate, are subjected to air suction at the upper end, and are subjected to air blowing treatment at the lower end; the metal removing treatment is magnetic roller iron removing and eddy current non-ferrous metal removing.

As a preferable technical scheme, the density of the brine in the brine tank is 1.10-1.20 g/cm³。

As a preferred technical scheme, the instrument used for the wet crushing treatment in the invention is a wet crusher; the mesh opening of the wet crusher is 10-20 mm.

As a preferred technical scheme, the rotating speed of the dehydrator is 100-3000rpm, and the aperture of the screen mesh is 1-2 mm.

As a preferred technical scheme, the rotating speed of the dehydrator is 1000-.

In a preferred embodiment of the present invention, the shape of each selected plastic in the hot-melt granulation is a sheet.

As a preferable technical scheme, the particle size of the plastic particles in the screening and drying process is 1-10 mm.

As a preferable technical scheme, the wastewater treated by the wastewater treatment process is reused in the processes of salt water impurity removal and friction cleaning.

As a preferable technical scheme, the hard impurity recycling and regenerating process is operated by a PLC automatic control system.

Has the advantages that: the invention provides a hard impurity recycling and regenerating process, which is characterized in that impurities on the surface of hard impurities are thoroughly removed through a special light impurity removing and metal removing process, a special dehydrator and a salt water tank cleaning process in the early stage, different types of plastics in the hard impurities can be separated through a clear water separation process and an electrostatic separation process in the middle stage, the separation degree is large, the efficiency is high, the final plastic particles are obtained through special hot melting granulation and screening drying treatment in the later stage, and the different types of plastic particles are finally prepared through the cooperation of the early stage process, the middle stage process and the later stage process; the invention carries out the recovery and regeneration treatment of hard sundries through the reasonable configuration and the matching of a plurality of processes, and has the characteristics of high efficiency, high integration degree, less manpower requirement, stable product quality and the like; in addition, in the process of recycling and regenerating hard sundries, the waste water is correspondingly treated and can be reused as water resources required by brine impurity removal and friction cleaning processes, so that the cyclic utilization of resources is realized, the pollution to the environment and the waste of resources are reduced, the waste gas generated in the hot melting granulation stage is correspondingly treated, the production environment is good, and the beneficial effect of zero pollution to the environment is realized.

Drawings

FIG. 1: FIG. 1 is a flow chart of the process of example 1.

FIG. 2: FIG. 2 is a photograph showing impurity spots of plastic particles prepared by the process described in example 1.

FIG. 3: FIG. 3 is a picture of impurity points of plastic particles prepared by the hard impurity recovery process in the prior art.

Detailed Description

Unless otherwise indicated, implied from the context, or customary in the art, all parts and percentages herein are by weight and the testing and characterization methods used are synchronized with the filing date of the present application. To the extent that a definition of a particular term disclosed in the prior art is inconsistent with any definitions provided herein, the definition of the term provided herein controls.

The technical features of the technical solutions provided by the present invention are further clearly and completely described below with reference to the specific embodiments, and the scope of protection is not limited thereto.

The words "preferred", "preferably", "more preferred", and the like, in the present invention, refer to embodiments of the invention that may provide certain benefits, under certain circumstances. However, other embodiments may be preferred, under the same or other circumstances. Furthermore, the recitation of one or more preferred embodiments does not imply that other embodiments are not useful, nor is it intended to exclude other embodiments from the scope of the invention.

The invention provides a hard impurity recycling and regenerating process, which at least comprises the following process steps: pretreating hard sundries, removing impurities by using brine, crushing, rubbing and cleaning, sorting, hot melting and granulating, screening and drying, treating wastewater and treating waste gas;

the hard impurity pretreatment is to remove light impurities and metal from the hard impurity;

the brine impurity removal step is to use a dehydrator for cleaning, and then carry out impurity removal treatment through a brine tank;

the crushing is to carry out wet crushing treatment on the dehydrated hard and impure plastics;

the friction cleaning is to convey the crushed plastic into a clean water washing tank through a screw, a stirring paddle is arranged in the clean water washing tank, hard sundries are classified in the first step to obtain upper floating materials and lower sinking materials, and the upper floating materials and the lower sinking materials are respectively conveyed into a dehydrator for dehydration and packaging;

the sorting is to sort the upper floating material and the lower sinking material which are subjected to the dewatering and packaging treatment respectively into electrostatic sorting equipment to obtain final sorted plastics;

the hot melting granulation is that various sorted plastics are conveyed into hot melting equipment through a screw to be heated and melted, and hot melted plastic melt enters cold water to be hardened and pulled after passing through a filter screen and a die head with holes. Drawing the hardened plastic strips into a granulator for granulation;

the screening and drying step is that granulated granular plastics are screened by a vibrating screen, plastic particles are sorted, and the plastic particles are packaged after being dried by blast air;

the wastewater treatment comprises the steps of performing inclined screen filtration, flocculation precipitation, air flotation impurity removal and oil removal on wastewater generated in the processes of salt water impurity removal, crushing and friction cleaning, and performing biochemical degradation on COD;

the waste gas treatment is to carry out waste gas collection, spray washing, electrostatic oil removal and oxidative decomposition treatment on waste gas generated in the hot melting granulation process, and then to discharge the waste gas.

The hard sundries in the invention can be common waste plastics; preferably, the hard sundries are a mixture of PP, PS and ABS plastics.

Pretreatment of hard sundries

In some embodiments, the hard impurity pretreatment is a light impurity removal and metal removal treatment for the hard impurity.

In some embodiments, the light impurity removal is that the plastic fragments fall from the height of 2-8 m, pass through a Z-shaped folded plate, are subjected to air suction at the upper end, and are subjected to air blowing treatment at the lower end; the metal removing treatment is magnetic roller iron removing and eddy current non-ferrous metal removing.

In some preferred embodiments, the light impurity removal is that the plastic fragments fall from the height of 4-7 m, pass through a Z-shaped folded plate, are subjected to air suction at the upper end, and are subjected to air blowing treatment at the lower end; more preferably, the light impurities are removed by dropping the plastic chips from the height of 6m, passing through the Z-shaped folded plate, exhausting air at the upper end and blowing air at the lower end.

In the invention, the light impurities can be removed by adopting a Z-shaped separator, hard impurity fragments fall from a certain height, air is drawn at the upper end through a plurality of folded plates, and air is blown at the lower end to remove the light impurities, mainly removing foams, dust, cloth strips, label paper and the like.

Removing impurities from brine

In some embodiments, the brine removal is performed by washing and dewatering with a dewatering machine, and then removing impurities through a brine tank.

In some embodiments, the brine tank has a brine density of 1.10 to 1.20g/cm³(ii) a Preferably, the density of the brine in the brine tank is 1.15-1.18g/cm³(ii) a More preferably, the density of the brine in the brine tank is 1.16g/cm³。

In some embodiments, the cleaning process of the dehydrator in the brine impurity removal process can be performed in combination with an auxiliary agent.

In some embodiments, the adjunct is selected from the group consisting of one or more of alkaline detergents, nonionic surfactants, silicates; preferably, the auxiliary agent is a combination of a nonionic surfactant and silicate.

In some embodiments, the weight ratio of the nonionic surfactant to the silicate in the present invention is 1: (0.1-2); preferably, the weight ratio of the nonionic surfactant to the silicate is 1: (0.5-1.5); more preferably, the weight ratio of the nonionic surfactant to the silicate is 1: 1.

in some embodiments, the nonionic surfactant of the present invention is selected from the group consisting of one or more of alkylphenol ethoxylates, polyoxyethylene fatty acid esters, polyoxyethylene octylphenol ethers, polyoxyethylene sorbitan monolaurate, and polyoxyethylene stearyl alcohol; preferably, the nonionic surfactant is selected from one or more of alkylphenol polyoxyethylene, octyl phenol polyoxyethylene and stearyl alcohol polyoxyethylene; more preferably, the nonionic surfactant is selected from one or more of alkylphenol ethoxylates and octylphenol polyoxyethylene ether; most preferably, the nonionic surfactant is alkylphenol ethoxylates.

In some embodiments, the silicate of the present invention is sodium metasilicate and/or layered sodium silicate; preferably, the silicate in the invention is layered sodium silicate.

In the invention, silicate and nonionic surfactant are selected to be mixed in the dehydrator to thoroughly clean stains, grease, impurities and the like of waste hard impurities, the cleaning power is strong, and particularly, the applicant finds that the cleaning effect of the compound use of the layered sodium silicate and alkylphenol ethoxylates is the most excellent, presumably because the layered sodium silicate has a certain cleaning effect in the dehydrator, but the cleaning effect of the hard impurities is influenced because the surface of the layered sodium silicate contains a large amount of hydroxyl groups and the group phenomenon can not exist stably in the grease environment, but the compound use of the alkylphenol ethoxylates and the layered sodium silicate has a good synergistic effect, and the cleaning effect of the hard impurities is greatly increased. The mutual matching of the dehydrator and the formula auxiliary agent not only can improve the cleaning degree of various stains, grease and impurities, but also can avoid the problems of damage to the structure of the hard sundries and poor normal-temperature cleaning effect caused by the joint use of hot cleaning and the formula auxiliary agent, and improve the quality and value of the regenerated hard sundries.

In the invention, the hard impurity materials are subjected to preliminary pretreatment by adopting special light impurity removal treatment and metal removal treatment, the surface impurity removal and removal rate is high, and the surface of the hard impurity materials is further subjected to relatively thorough removal treatment by combining the cleaning of a dehydrator and the cleaning of a salt water tank; wherein, the brine impurity removal process can further clean the hard impurity plastics and heavy impurities such as sand, metal and the like, and the concentration of the impurities is 1.10-1.20 g/cm³The brine concentration not only compares in current salt water separation technique concentration lower and can not cause the waste of salt matter, can also effectively clear away plastics surface impurity to realize that hard miscellaneous plastics and surface impurity thoroughly separate, do benefit to going on of follow-up technology.

Crushing

In some embodiments, the crushing is a wet crushing treatment of the dehydrated hard and miscellaneous plastic.

In some embodiments, the crushing is a wet crushing treatment of the hard miscellaneous plastic after impurity removal treatment of the salt water tank, cleaning with clear water of a dehydrator and dehydration.

In some embodiments, the apparatus used in the wet crushing process is a wet crusher; the aperture of the screen mesh of the wet crusher is 10-20 mm; preferably, the mesh opening of the wet crusher is 13-18 mm; more preferably, the mesh opening size of the wet crusher is 15 mm.

In some embodiments, the spin speed of the dehydrator is 100-3000rpm, and the aperture of the sieve is 1-2 mm; preferably, the rotating speed of the dehydrator is 1000-; more preferably, the rotating speed of the dehydrator is 2000rpm, and the aperture of the screen is 1.5 mm.

Friction cleaning

In some embodiments, the friction cleaning is to convey the crushed plastic into a clean water washing tank through a screw, the clean water washing tank is provided with a stirring paddle, the hard sundries are classified in the first step, an upper floating material and a lower sinking material are obtained, and the upper floating material and the lower sinking material respectively enter a dehydrator for dehydration and packaging.

In some embodiments, the direction of the screw into the clean water in the friction washing is opposite to the rotation direction of the stirring paddle.

In the invention, the feeding mode adopted in the friction cleaning process is spiral conveying, and the stirring paddle is arranged in the clear water washing tank, wherein the direction of the spiral conveying entering the clear water is opposite to the rotation direction of the stirring paddle, so that the impact force of friction cleaning and the collision among plastic sheets can be increased in the friction cleaning process, and the cleaning effect on the hard and miscellaneous plastic sheets is good.

Sorting

In some embodiments, the sorting is to sort the dewatered and packed floating materials and sinking materials into electrostatic sorting equipment respectively to obtain the final sorted plastics.

According to the invention, the wet crusher is used for crushing, so that the subsequent cleaning, dehydration and sorting treatment is facilitated, and the working efficiency of sorting different types of plastics is improved. The applicant finds that when the screen aperture of the dehydrator is 1-2mm, the powder residual quantity of the hard impurities in the dehydrator is reduced, and particularly, under the conditions that the rotating speed of the dehydrator is 2000rpm and the screen aperture is 1.5mm, the powder residual quantity of the dehydrator is the minimum, which can be beneficial to improving the overall working efficiency of the invention.

Hot melt granulation

In some embodiments, the hot-melting granulation is that various sorted plastics are conveyed by a screw to enter a hot-melting device for heating and melting of the plastics, and a hot-melted plastic melt enters cold water to harden and draw strips after passing through a filter screen and a die head with holes. And drawing the hardened plastic strips into a granulator for granulation.

In some embodiments, the hot melt apparatus of the present invention is a dual stage machine, manufactured under the brand name dual stage ATE75/40, available from Esrett mechanical, Inc., or available from other sources.

In some embodiments, the hot melting device provided by the invention is provided with a melt extrusion device of a material agglomerating cylinder, an intermediate back flush and a super-large-area screen changer, and the plastic is cooled and hardened after being extruded.

In some embodiments, the shapes of the various sized plastics in the hot melt granulation are in the form of sheets.

In some embodiments, the hot melt granulation process adds an extraction devolatilization aid during the melt phase.

In some embodiments, the extractive devolatilization aid is supported by a porous polypropylene polymer; the polypropylene is a mixture of atactic polypropylene and isotactic polypropylene.

In some embodiments, the weight ratio of atactic polypropylene to isotactic polypropylene in the present invention is 1: (0.1-5); preferably, the weight-loss ratio of the atactic polypropylene to the isotactic polypropylene is 1: (1-4); more preferably, the weight ratio of the atactic polypropylene to the isotactic polypropylene is 1: (2-3); most preferably, the weight ratio of the atactic polypropylene to the isotactic polypropylene is 1: 2.5.

in some embodiments, the random polypropylene of the present invention has a melt flow rate of 3 to 10g/10 min; preferably, the random polypropylene has a melt flow rate of 4 to 9g/10 min; more preferably, the random polypropylene has a melt flow rate of 6g/10 min.

In some embodiments, the isotactic polypropylene of the present invention has a melt flow rate of 15-35g/10 min; preferably, the isotactic polypropylene has a melt flow rate of 20g/10 min.

The melt flow rate described in the present invention was tested at 230 ℃/2.16kg using ASTM D1238.

In some embodiments, the porous polypropylene polymer of the present invention has a pore size of 5 μm to 15 μm and a porosity of 30 to 70%.

In some preferred embodiments, the porous polypropylene polymer of the present invention has a pore size of 7 μm to 13 μm and a porosity of 40 to 60%.

In some more preferred embodiments, the porous polypropylene polymer of the present invention has a pore size of 10 μm and a porosity of 55%.

The extractive devolatilization aids described in the present invention may be purchased from fertilizer-integrated Innovation lightweight materials, Inc., or may be derived from other sources.

In the invention, the extraction devolatilization auxiliary agent is loaded with polyol type nonionic surfactant and/or low boiling point extractant; preferably, the extraction devolatilization aid supports a polyol-type nonionic surfactant and a low-boiling point extractant.

The polyhydric alcohol type nonionic surfactant is selected from one or more of glycerin fatty acid ester, pentaerythritol fatty acid ester, sorbitol fatty acid ester, sorbitan fatty acid ester, sucrose fatty acid ester and alkylolamide; preferably, the polyhydric alcohol type nonionic surfactant is selected from pentaerythritol fatty acid ester, sorbitan fatty acid ester, alkylolamide; more preferably, the polyhydric alcohol-type nonionic surfactant is a sorbitan fatty acid ester.

In some embodiments, the polyol-type nonionic surfactant of the present invention is present at a loading of 0.1 to 1% by weight of the atactic polypropylene and the isotactic polypropylene; preferably, the loading amount of the polyol type nonionic surfactant is 0.5 percent of the weight of the atactic polypropylene and the isotactic polypropylene.

In some embodiments, the low boiling point extractant of the present invention includes, but is not limited to, one or more of water, ethanol, methanol, isopropanol; preferably, the boiling point extracting agent is water and/or ethanol; more preferably, the boiling point extractant is water.

In the invention, in the hot-melting granulation process, a two-stage machine is used for thoroughly removing VOC from the sorted hard impurities in the sorting process under the synergistic action of the extraction and devolatilization auxiliary agent, wherein the extraction and devolatilization auxiliary agent prepared by taking atactic polypropylene and isotactic polypropylene polymers as carriers of porous polymers and loading polyol type nonionic surfactants has a very good effect on VOC removal, and the probable reason is presumed to be that: the two-stage machine is a double-screw-to-single-screw machine, the adopted extraction devolatilization auxiliary agent carrier is prepared by compounding two polymers of atactic polypropylene and isotactic polypropylene polymer, the two polymers have different melt flow states and are mutually cooperated, the isotactic polypropylene polymer and the carrier have small pore diameters under the combined action, so that the extraction devolatilization auxiliary agent can prevent the extraction agent from premature failure in the early stage of melting of the two-stage machine, the atactic polypropylene can be favorable for achieving good dispersion of the shear melting state of the isotactic polypropylene in the exhaust stage of a melt interface in the process of connecting the double screws and the single screw in the later stage, the low-boiling point extraction agent can be released to the maximum degree in the most appropriate period, the VOC content of mutual-melting extraction is improved, and the VOC removal can be most thoroughly combined with a vacuum removal means. In addition, the applicant finds that the small pore diameter and the proper porosity of the porous polymer carrier for extracting the devolatilization auxiliary agent in the invention also help to prevent the extraction agent from being prematurely deactivated in the pre-melting stage, so that the VOC removal rate is optimal, and the polyol nonionic surfactant loaded in the carrier helps to ensure that the carrier can adsorb the low-boiling-point extraction agent in high content, thereby solving the problem that the small pore diameter is not beneficial to adsorption. The content of VOC in the hard impurity materials recovered in the process is low, and the process can be suitable for preparing products in various fields.

Sieving and drying

In some embodiments, the screening and drying is to screen the granulated plastic particles through a vibrating screen, sort the plastic particles, dry the plastic particles by blowing air, and then pack the plastic particles.

In some embodiments, the particle size of the plastic particles in the sieving drying process is 1-10 mm; preferably, the particle size of the plastic particles in the screening and drying process is 3-8 mm; more preferably, the particle size of the plastic particles in the screening and drying process is 6 mm.

In some embodiments, the shaker screen comprises 2-3 layers of screen; preferably, the vibrating screen comprises 3 layers of screens.

In the invention, the plastic particles are sieved by a vibrating sieve with a plurality of layers of filter screens to obtain the plastic particles with different particle sizes, and the plastic particles have great influence on the mechanical property of the processed plastic product, so that the applicant finds that the plastic particles with the particle size of 3-8mm are sieved, the tensile strength and the bending strength of the obtained product are higher, and particularly, the mechanical property of the plastic particles with the particle size of 6mm is most excellent, the reason is probably that when the particles with the particle size of less than 8mm are melted again, the degree of melt entanglement among the molecules in the molten state is relatively large, and the hollow formed in the finished product formed again is relatively less, so that the mechanical strength of the whole plastic is improved, although small plastic particles provide a good improvement in the mechanical properties of the finished product, the applicant has found that plastic particles below 3mm do not produce a significant change in the mechanical properties of the finished product.

Treatment of waste water

In some embodiments, the wastewater treatment is a process of performing inclined screen filtration, flocculation precipitation, air flotation impurity removal and oil removal, and biochemical degradation of COD on wastewater generated in the processes of salt water impurity removal, crushing and friction cleaning.

In some embodiments, the wastewater treated by the wastewater treatment process is reused in a brine purification and friction cleaning process.

The waste water treatment in the invention is directed to the procedures of corresponding inclined screen filtration, flocculation precipitation, air flotation impurity removal and oil removal and biochemical degradation of COD for the waste water generated in the process, can be directed to various inorganic substances, various grease, various sizing materials, various additives, various chemical reagents, microorganisms and the like generated in the process, has excellent effect, and can also be recycled for water resources required by salt water impurity removal and friction cleaning processes, thereby realizing the recycling of the resources and reducing the pollution to the environment and the waste of the resources.

Exhaust gas treatment

In some embodiments, the waste gas treatment is to perform waste gas collection, spray washing, electrostatic oil removal, oxidative decomposition treatment on waste gas generated in the hot-melt granulation process, and then perform waste gas discharge.

In the invention, the VOC removal of the hard impurities is relatively thorough in the melting granulation stage, so that the content of the removed VOC is relatively large, but various toxic volatile gases or other wastes are subjected to targeted treatment, and the generated waste gas is subjected to waste gas collection, spray washing, electrostatic oil removal and oxidative decomposition in sequence and then is discharged, so that the zero emission of the polluted gas in the process can be realized, the environment is not polluted, and the process has a very significant effect.

PLC automatic control system

In some embodiments, the hard waste recovery regeneration process is operated using a PLC automated control system.

The hard impurity material recovery process is operated by adopting a PLC automatic control system, the recovery and regeneration process of the hard impurity materials is carried out through reasonable configuration and integration of a plurality of processes, the efficiency is high, the integration degree is high, the product quality is stable, the production environment is good, less manpower is needed, the harm to the body caused by direct contact of workers and hard impurity waste materials is avoided, the efficiency is high, the quality of the recovered hard impurity materials is high, and the industrial production can be realized.

The reaction is specifically described below by way of examples. The following examples are intended to illustrate the present invention and should not be construed as limiting the scope of the invention, and those skilled in the art will be able to make insubstantial modifications and adaptations of the invention in light of the above teachings and are intended to be within the scope of the invention.

Example 1

A hard impurity material recycling and regenerating process comprises the following process steps: pretreating hard sundries, removing impurities by using brine, crushing, rubbing and cleaning, sorting, hot melting and granulating, screening and drying, treating wastewater and treating waste gas;

the hard sundries pretreatment comprises the steps of removing light impurities and metals from the hard sundries, wherein the light impurities are plastic chips falling from the height of 6 meters, passing through a Z-shaped folded plate, exhausting air at the upper end and blowing air at the lower end; the metal removing treatment is magnetic roller iron removal and eddy current non-ferrous metal removal;

the brine impurity removal step is to use a dehydrator for cleaning, and then carry out impurity removal treatment through a brine tank; the density of the brine in the brine tank is 1.16g/cm³(ii) a The process of cleaning by the dehydrator in the brine impurity removal process can be matched with alkylphenol polyoxyethylene ether and layered sodium silicate for cleaning, wherein the weight ratio of the alkylphenol polyoxyethylene ether to the layered sodium silicate is 1: 1;

the crushing is to carry out wet crushing treatment on the dehydrated hard and impure plastics; the wet crushing treatment instrument is a wet crusher, the aperture of a screen of the wet crusher is 15mm, the rotating speed of the dehydrator is 2000rpm, and the aperture of the screen is 1.5 mm;

the friction cleaning is to convey the crushed plastic into a clean water washing tank through a screw, a stirring paddle is arranged in the clean water washing tank, hard sundries are classified in the first step to obtain upper floating materials and lower sinking materials, and the upper floating materials and the lower sinking materials are respectively conveyed into a dehydrator for dehydration and packaging;

the sorting is to sort the upper floating material and the lower sinking material which are subjected to the dewatering and packaging treatment respectively into electrostatic sorting equipment to obtain final sorted plastics;

the hot melting granulation is that various sorted plastics are conveyed into hot melting equipment through a screw to be heated and melted, and hot melted plastic melt enters cold water to be hardened and pulled after passing through a filter screen and a die head with holes. Drawing the hardened plastic strips into a granulator for granulation; the hot melting equipment is a double-stage machine, and various sorted plastics in the hot melting granulation are flaky; in the hot melting granulation process, an extraction devolatilization auxiliary agent is added in a melting stage; the extraction devolatilization auxiliary agent takes a porous polypropylene polymer as a carrier, the polypropylene is a mixture of atactic polypropylene and isotactic polypropylene, and the weight ratio of the atactic polypropylene to the isotactic polypropylene is 1: 2.5, the melt flow rate of the atactic polypropylene is 6g/10min, the melt flow rate of the isotactic polypropylene is 20g/10min, the pore diameter of the porous polypropylene polymer is 10 mu m, the porosity is 55%, the extraction devolatilization auxiliary agent is loaded with a polyol type nonionic surfactant and a low-boiling point extraction agent, the polyol type nonionic surfactant is sorbitan fatty acid ester, the loading amount of the polyol type nonionic surfactant is 0.5% of the weight of the atactic polypropylene and the isotactic polypropylene, and the boiling point extraction agent is water;

the screening and drying step is that granulated granular plastics are screened by a vibrating screen, plastic particles are sorted, and the plastic particles are packaged after being dried by blast air; the particle size of the plastic particles in the screening and drying process is 6mm, and the vibrating screen comprises 3 layers of filter screens;

the wastewater treatment comprises the steps of performing inclined screen filtration, flocculation precipitation, air flotation impurity removal and oil removal on wastewater generated in the processes of salt water impurity removal, crushing and friction cleaning, and performing biochemical degradation on COD; the wastewater treated by the wastewater treatment process is reused for the processes of salt water impurity removal and friction cleaning;

the waste gas treatment is to carry out waste gas collection, spray washing, electrostatic oil removal and oxidative decomposition treatment on waste gas generated in the hot melting granulation process, and then to discharge the waste gas;

the hard impurity recycling and regenerating process is operated by adopting a PLC automatic control system.

Example 2

A hard impurity material recycling and regenerating process comprises the following process steps: pretreating hard sundries, removing impurities by using brine, crushing, rubbing and cleaning, sorting, hot melting and granulating, screening and drying, treating wastewater and treating waste gas;

the hard sundries pretreatment comprises the steps of removing light impurities and metals from the hard sundries, wherein the light impurities are plastic fragments falling from the height of 2m, passing through a Z-shaped folded plate, exhausting air at the upper end and blowing air at the lower end; the metal removing treatment is magnetic roller iron removal and eddy current non-ferrous metal removal;

the brine impurity removal step is to use a dehydrator for cleaning, and then carry out impurity removal treatment through a brine tank; the density of the brine in the brine tank is 1.1g/cm³(ii) a The process of cleaning the dehydrator in the brine impurity removal process can be matched with alkylphenol polyoxyethylene ether and layered sodium silicate for cleaning, and the weight ratio of the nonionic surfactant to the silicate is 1: 0.1;

the crushing is to carry out wet crushing treatment on the dehydrated hard and impure plastics; the wet crushing treatment instrument is a wet crusher, the aperture of a screen of the wet crusher is 10mm, the rotating speed of the dehydrator is 100rpm, and the aperture of the screen is 1.0 mm;

the friction cleaning is to convey the crushed plastic into a clean water washing tank through a screw, a stirring paddle is arranged in the clean water washing tank, hard sundries are classified in the first step to obtain upper floating materials and lower sinking materials, and the upper floating materials and the lower sinking materials are respectively conveyed into a dehydrator for dehydration and packaging;

the sorting is to sort the upper floating material and the lower sinking material which are subjected to the dewatering and packaging treatment respectively into electrostatic sorting equipment to obtain final sorted plastics;

the hot melting granulation is that various sorted plastics are conveyed into hot melting equipment through a screw to be heated and melted, and hot melted plastic melt enters cold water to be hardened and pulled after passing through a filter screen and a die head with holes. Drawing the hardened plastic strips into a granulator for granulation; the hot melting equipment is a double-stage machine, and various sorted plastics in the hot melting granulation are flaky; in the hot melting granulation process, an extraction devolatilization auxiliary agent is added in a melting stage; the extraction devolatilization auxiliary agent takes a porous polypropylene polymer as a carrier, the polypropylene is a mixture of atactic polypropylene and isotactic polypropylene, and the weight ratio of the atactic polypropylene to the isotactic polypropylene is 1: 1, the melt flow rate of the atactic polypropylene is 3.5g/10min, the melt flow rate of the isotactic polypropylene is 16g/10min, the pore diameter of the porous polypropylene polymer is 5 mu m, the porosity is 30%, the extraction devolatilization auxiliary agent is loaded with a polyol type nonionic surfactant and a low-boiling point extraction agent, the polyol type nonionic surfactant is sorbitan fatty acid ester, the loading amount of the polyol type nonionic surfactant is 0.1% of the weight of the atactic polypropylene and the isotactic polypropylene, and the boiling point extraction agent is water;

the screening and drying step is that granulated granular plastics are screened by a vibrating screen, plastic particles are sorted, and the plastic particles are packaged after being dried by blast air; the particle size of the plastic particles in the screening and drying process is 1mm, and the vibrating screen comprises 3 layers of filter screens;

the wastewater treatment comprises the steps of performing inclined screen filtration, flocculation precipitation, air flotation impurity removal and oil removal on wastewater generated in the processes of salt water impurity removal, crushing and friction cleaning, and performing biochemical degradation on COD; the wastewater treated by the wastewater treatment process is reused for the processes of salt water impurity removal and friction cleaning;

the waste gas treatment is to carry out waste gas collection, spray washing, electrostatic oil removal and oxidative decomposition treatment on waste gas generated in the hot melting granulation process, and then to discharge the waste gas;

the hard impurity recycling and regenerating process is operated by adopting a PLC automatic control system.

Example 3

A hard impurity material recycling and regenerating process comprises the following process steps: pretreating hard sundries, removing impurities by using brine, crushing, rubbing and cleaning, sorting, hot melting and granulating, screening and drying, treating wastewater and treating waste gas;

the hard miscellaneous material pretreatment comprises the steps of removing light impurities and metals from the hard miscellaneous material, wherein the light impurities are plastic fragments falling from the height of 4 m, passing through a Z-shaped folded plate, exhausting air at the upper end and blowing air at the lower end; the metal removing treatment is magnetic roller iron removal and eddy current non-ferrous metal removal;

the brine impurity removal step is to use a dehydrator for cleaning, and then carry out impurity removal treatment through a brine tank; the density of the brine in the brine tank is 1.15g/cm³(ii) a The process of cleaning the dehydrator in the brine impurity removal process can be matched with alkylphenol polyoxyethylene ether and layered sodium silicate for cleaning, and the weight ratio of the nonionic surfactant to the silicate is 1: 0.5;

the crushing is to carry out wet crushing treatment on the dehydrated hard and impure plastics; the wet crushing treatment instrument is a wet crusher, the aperture of a screen of the wet crusher is 13mm, the rotating speed of the dehydrator is 1000rpm, and the aperture of the screen is 1.2 mm;

the friction cleaning is to convey the crushed plastic into a clean water washing tank through a screw, a stirring paddle is arranged in the clean water washing tank, hard sundries are classified in the first step to obtain upper floating materials and lower sinking materials, and the upper floating materials and the lower sinking materials are respectively conveyed into a dehydrator for dehydration and packaging;

the sorting is to sort the upper floating material and the lower sinking material which are subjected to the dewatering and packaging treatment respectively into electrostatic sorting equipment to obtain final sorted plastics;

the hot melting granulation is that various sorted plastics are conveyed into hot melting equipment through a screw to be heated and melted, and hot melted plastic melt enters cold water to be hardened and pulled after passing through a filter screen and a die head with holes. Drawing the hardened plastic strips into a granulator for granulation; the hot melting equipment is a double-stage machine, and various sorted plastics in the hot melting granulation are flaky; in the hot melting granulation process, an extraction devolatilization auxiliary agent is added in a melting stage; the extraction devolatilization auxiliary agent takes a porous polypropylene polymer as a carrier, the polypropylene is a mixture of atactic polypropylene and isotactic polypropylene, and the weight ratio of the atactic polypropylene to the isotactic polypropylene is 1: 4, the melt flow rate of the atactic polypropylene is 4g/10min, the melt flow rate of the isotactic polypropylene is 35g/10min, the pore diameter of the porous polypropylene polymer is 7 mu m, the porosity is 40%, the extraction devolatilization auxiliary agent is loaded with a polyol type nonionic surfactant and a low-boiling point extraction agent, the polyol type nonionic surfactant is sorbitan fatty acid ester, the loading amount of the polyol type nonionic surfactant is 1% of the weight of the atactic polypropylene and the isotactic polypropylene, and the boiling point extraction agent is water;

the screening and drying step is that granulated granular plastics are screened by a vibrating screen, plastic particles are sorted, and the plastic particles are packaged after being dried by blast air; the particle size of the plastic particles in the screening and drying process is 3mm, and the vibrating screen comprises 3 layers of filter screens;

the wastewater treatment comprises the steps of performing inclined screen filtration, flocculation precipitation, air flotation impurity removal and oil removal on wastewater generated in the processes of salt water impurity removal, crushing and friction cleaning, and performing biochemical degradation on COD; the wastewater treated by the wastewater treatment process is reused for the processes of salt water impurity removal and friction cleaning;

the waste gas treatment is to carry out waste gas collection, spray washing, electrostatic oil removal and oxidative decomposition treatment on waste gas generated in the hot melting granulation process, and then to discharge the waste gas;

the hard impurity recycling and regenerating process is operated by adopting a PLC automatic control system.

Example 4

A hard impurity material recycling and regenerating process comprises the following process steps: pretreating hard sundries, removing impurities by using brine, crushing, rubbing and cleaning, sorting, hot melting and granulating, screening and drying, treating wastewater and treating waste gas;

the hard sundries pretreatment comprises the steps of removing light impurities and metals from the hard sundries, wherein the light impurities are plastic fragments falling from a height of 7 m, passing through a Z-shaped folded plate, exhausting air at the upper end and blowing air at the lower end; the metal removing treatment is magnetic roller iron removal and eddy current non-ferrous metal removal;

the brine impurity removal step is to use a dehydrator for cleaning, and then carry out impurity removal treatment through a brine tank; the density of the brine in the brine tank is 1.18g/cm³(ii) a The cleaning process of the dehydrator in the brine impurity removal process can be matched with alkylphenol polyoxyethylene ether and layered sodium silicate for cleaning, and the nonionic surfaceThe weight ratio of the active agent to the silicate is 1: 1.5;

the crushing is to carry out wet crushing treatment on the dehydrated hard and impure plastics; the wet crushing treatment instrument is a wet crusher, the aperture of a screen mesh of the wet crusher is 18mm, the rotating speed of the dehydrator is 2500rpm, and the aperture of the screen mesh is 1.8 mm;

the friction cleaning is to convey the crushed plastic into a clean water washing tank through a screw, a stirring paddle is arranged in the clean water washing tank, hard sundries are classified in the first step to obtain upper floating materials and lower sinking materials, and the upper floating materials and the lower sinking materials are respectively conveyed into a dehydrator for dehydration and packaging;

the sorting is to sort the upper floating material and the lower sinking material which are subjected to the dewatering and packaging treatment respectively into electrostatic sorting equipment to obtain final sorted plastics;

the hot melting granulation is that various sorted plastics are conveyed into hot melting equipment through a screw to be heated and melted, and hot melted plastic melt enters cold water to be hardened and pulled after passing through a filter screen and a die head with holes. Drawing the hardened plastic strips into a granulator for granulation; the hot melting equipment is a double-stage machine, and various sorted plastics in the hot melting granulation are flaky; in the hot melting granulation process, an extraction devolatilization auxiliary agent is added in a melting stage; the extraction devolatilization auxiliary agent takes a porous polypropylene polymer as a carrier, the polypropylene is a mixture of atactic polypropylene and isotactic polypropylene, and the weight ratio of the atactic polypropylene to the isotactic polypropylene is 1: 0.1, the melt flow rate of the atactic polypropylene is 9g/10min, the melt flow rate of the isotactic polypropylene is 20g/10min, the pore diameter of the porous polypropylene polymer is 13 mu m, the porosity is 60%, the extraction devolatilization auxiliary agent is loaded with a polyol type nonionic surfactant and a low-boiling point extraction agent, the polyol type nonionic surfactant is sorbitan fatty acid ester, the loading amount of the polyol type nonionic surfactant is 0.5% of the weight of the atactic polypropylene and the isotactic polypropylene, and the boiling point extraction agent is water;

the screening and drying step is that granulated granular plastics are screened by a vibrating screen, plastic particles are sorted, and the plastic particles are packaged after being dried by blast air; the particle size of the plastic particles in the screening and drying process is 8mm, and the vibrating screen comprises 3 layers of filter screens;

the wastewater treatment comprises the steps of performing inclined screen filtration, flocculation precipitation, air flotation impurity removal and oil removal on wastewater generated in the processes of salt water impurity removal, crushing and friction cleaning, and performing biochemical degradation on COD; the wastewater treated by the wastewater treatment process is reused for the processes of salt water impurity removal and friction cleaning;

the waste gas treatment is to carry out waste gas collection, spray washing, electrostatic oil removal and oxidative decomposition treatment on waste gas generated in the hot melting granulation process, and then to discharge the waste gas;

the hard impurity recycling and regenerating process is operated by adopting a PLC automatic control system.

Example 5

A hard impurity material recycling and regenerating process comprises the following process steps: pretreating hard sundries, removing impurities by using brine, crushing, rubbing and cleaning, sorting, hot melting and granulating, screening and drying, treating wastewater and treating waste gas;

the hard sundries pretreatment comprises the steps of removing light impurities and metals from the hard sundries, wherein the light impurities are plastic fragments falling from the height of 8m, passing through a Z-shaped folded plate, exhausting air at the upper end and blowing air at the lower end; the metal removing treatment is magnetic roller iron removal and eddy current non-ferrous metal removal;

the brine impurity removal step is to use a dehydrator for cleaning, and then carry out impurity removal treatment through a brine tank; the density of the brine in the brine tank is 1.2g/cm³(ii) a The process of cleaning the dehydrator in the brine impurity removal process can be matched with alkylphenol polyoxyethylene ether and layered sodium silicate for cleaning, and the weight ratio of the nonionic surfactant to the silicate is 1: 2;

the crushing is to carry out wet crushing treatment on the dehydrated hard and impure plastics; the wet crushing treatment instrument is a wet crusher, the aperture of a screen mesh of the wet crusher is 20mm, the rotating speed of the dehydrator is 3000rpm, and the aperture of the screen mesh is 2 mm;

the friction cleaning is to convey the crushed plastic into a clean water washing tank through a screw, a stirring paddle is arranged in the clean water washing tank, hard sundries are classified in the first step to obtain upper floating materials and lower sinking materials, and the upper floating materials and the lower sinking materials are respectively conveyed into a dehydrator for dehydration and packaging;

the sorting is to sort the upper floating material and the lower sinking material which are subjected to the dewatering and packaging treatment respectively into electrostatic sorting equipment to obtain final sorted plastics;

the hot melting granulation is that various sorted plastics are conveyed into hot melting equipment through a screw to be heated and melted, and hot melted plastic melt enters cold water to be hardened and pulled after passing through a filter screen and a die head with holes. Drawing the hardened plastic strips into a granulator for granulation; the hot melting equipment is a double-stage machine, and various sorted plastics in the hot melting granulation are flaky; in the hot melting granulation process, an extraction devolatilization auxiliary agent is added in a melting stage; the extraction devolatilization auxiliary agent takes a porous polypropylene polymer as a carrier, the polypropylene is a mixture of atactic polypropylene and isotactic polypropylene, and the weight ratio of the atactic polypropylene to the isotactic polypropylene is 1: 5, the melt flow rate of the atactic polypropylene is 9.5g/10min, the melt flow rate of the isotactic polypropylene is 20g/10min, the pore diameter of the porous polypropylene polymer is 15 mu m, the porosity is 70%, the extraction devolatilization auxiliary agent is loaded with a polyol type nonionic surfactant and a low-boiling point extraction agent, the polyol type nonionic surfactant is sorbitan fatty acid ester, the loading amount of the polyol type nonionic surfactant is 0.5% of the weight of the atactic polypropylene and the isotactic polypropylene, and the boiling point extraction agent is water;

the screening and drying step is that granulated granular plastics are screened by a vibrating screen, plastic particles are sorted, and the plastic particles are packaged after being dried by blast air; the particle size of the plastic particles in the screening and drying process is 10mm, and the vibrating screen comprises 3 layers of filter screens;

the wastewater treatment comprises the steps of performing inclined screen filtration, flocculation precipitation, air flotation impurity removal and oil removal on wastewater generated in the processes of salt water impurity removal, crushing and friction cleaning, and performing biochemical degradation on COD; the wastewater treated by the wastewater treatment process is reused for the processes of salt water impurity removal and friction cleaning;

the waste gas treatment is to carry out waste gas collection, spray washing, electrostatic oil removal and oxidative decomposition treatment on waste gas generated in the hot melting granulation process, and then to discharge the waste gas;

the hard impurity recycling and regenerating process is operated by adopting a PLC automatic control system.

Example 6

This example is different from example 1 in that the porous polypropylene polymer has a pore size of 20 μm and a porosity of 80%.

Example 7

This example differs from example 1 in that the extractive devolatilization aid is supported on a porous polypropylene polymer, which is a random polypropylene having a melt flow rate of 15g/10 min.

Example 8

This example differs from example 1 in that the extractive devolatilization aid is supported on a porous polypropylene polymer, the polypropylene being isotactic polypropylene having a melt flow rate of 0.6g/10 min.

Example 9

This example differs from example 1 in that the weight ratio of atactic polypropylene to isotactic polypropylene is 5: 1.

example 10

This example differs from example 1 in that the boiling extractant is ethanol.

Example 11

This example differs from example 1 in that the silicate is sodium metasilicate.

Example 12

This example differs from example 1 in that the silicate is octylphenol polyoxyethylene ether.

Example 13

The difference between the embodiment and the embodiment 1 is that the light impurity removal is to stir and clean the plastic with clear water and then dewater by a dehydrator; the metal removing treatment is removing iron and metal by a magnetic roller.

Example 14

This example differs from example 1 in that the removal of light impurities is the dropping of plastic chips from a height of 1 meter.

Example 15

This example is different from example 1 in that the density of brine in the brine tank is 1.05g/cm³。

Example 16

This example differs from example 1 in that the mesh size of the wet crusher is 5 mm.

Example 17

This example differs from example 1 in that the screen aperture of the wet crusher is 30 mm.

Example 18

This example differs from example 1 in that the dewatering machine has a mesh size of 2.5 mm.

Example 19

This example differs from example 1 in that the dewatering machine has a mesh size of 0.5 mm.

Example 20

The difference between this example and example 1 is that the brine impurity removal process was performed without first cleaning with a dehydrator, and the brine tank impurity removal process was performed.

Example 21

The difference between this example and example 1 is that the screening and drying is to screen the granulated plastic particles through a vibrating screen, sort the plastic particles, and directly pack the plastic particles.

Example 22

The difference between the embodiment and the embodiment 1 is that the wastewater treated by the wastewater treatment process is not reused in the brine impurity removal and friction cleaning process.

Performance testing

1. VOC testing:

the hard trash recyclates obtained in examples 1 to 12 were used as test subjects, and VOC emission test data (μ g/m) thereof were measured in accordance with TSM0508G-2005³) Test size (mm) 100X 3, bag volume 10L.Table 1 shows the detection results of the VOC of the recycled hard and miscellaneous materials obtained by the recycling process of the present invention.

Table 1 VOC test results

2. Testing the water content:

the hard trash recycled materials obtained in examples 1 to 5 and examples 13 to 22 were used as test objects, and the water content of the test objects was measured by a CSY-L5 halogen moisture meter, and the test results are shown in table 2.

3. And (3) testing the impurity content:

(1) quantitative analysis of impurity content:

the hard miscellaneous regrind materials obtained in examples 1 to 5 and examples 13 to 22 were used as test objects, and the amounts of bromine, lead and cadmium contained in plastic particles were measured by energy dispersive X-ray fluorescence spectrometry, and the test results are shown in table 2.

TABLE 2 Water content and impurity test results

(2) The method for analyzing the appearance of the impurities comprises the following steps:

1) placing the lower pressing plate on the plane of a lower heating plate of a flat vulcanizing machine, and paving a layer of high-temperature oilpaper; 2) weighing 5-7 g of plastic particles, placing the plastic particles at the center of a pressing plate, and flattening the plastic particles to circular distribution as much as possible; 3) covering high-temperature oilpaper, pressing an upper pressing plate, and placing the pressing plate at the center of the plane of a lower heating plate of a flat vulcanizing machine; 4) preheating: pressing a motor start button to make the tabletting mold slightly contact with the upper heating plate (the indication of a pressure gauge is less than 1MPa), and preheating for 1 min; 5) starting a motor to pressurize after preheating is finished, controlling the pressure within the range of 1-3MPa during pressurizing, and pressing for 2 min; 6) opening the pressure relief valve through the pressure relief rod to restore the heating plate to the initial position, and taking out the tabletting mold (double-layer gloves or heat-insulating gloves are needed to be taken when the mold is taken out to prevent scalding); 7) taking out the pressed slices and the high-temperature oil paper together, cooling, taking out the pressed slices from the high-temperature oil paper after cooling, and performing impurity point contrast counting by adopting an appearance standard contrast card.

Impurity points of the plastic particles prepared by the preparation process of the embodiment 1 and the plastic particles prepared by the hard impurity recovery process of the prior art are used as test objects to be compared and analyzed, and the result of the embodiment 1 is shown in the attached figure 2; impurity points of plastic particle tabletting prepared by the hard miscellaneous material recovery process in the prior art are shown in figure 3.

The above description is only for the preferred embodiment of the present invention, and is not intended to limit the scope of the present invention, and all equivalent variations and modifications made according to the present invention are included in the scope of the present invention.

Claims (8)

Translated fromChinese

1.一种硬杂料回收再生工艺，其特征在于，工艺步骤至少包含：硬杂料预处理，盐水除杂，破碎，摩擦清洗，分选，热熔造粒，筛分干燥，废水处理，废气处理；1. a hard miscellaneous material recovery and regeneration process, it is characterized in that, the process step comprises at least: hard miscellaneous material pretreatment, salt water impurity removal, crushing, friction cleaning, sorting, hot melt granulation, screening drying, waste water treatment, waste gas treatment;所述硬杂料预处理为对硬杂料进行除轻质杂质、除金属处理；The pretreatment of the hard miscellaneous materials is to remove light impurities and remove metals from the hard miscellaneous materials;所述盐水除杂为使用脱水机进行清洗，之后再通过盐水槽进行除杂处理；The brine removal is to use a dehydrator to clean, and then to remove impurities through a brine tank;所述破碎是对脱水后的硬杂塑料进行湿式破碎处理；The crushing is wet crushing of the dehydrated hard miscellaneous plastics;所述摩擦清洗为对破碎后的塑料经过螺旋输送进入清水洗涤槽中，清水洗涤槽中设有搅拌桨，进行硬杂料的第一步分类，得到上浮料和下沉料，上浮料和下沉料分别进入脱水机中进行脱水打包处理；The friction cleaning is to convey the crushed plastic into the clean water washing tank through screw conveying, and a stirring paddle is arranged in the clean water washing tank to carry out the first classification of hard miscellaneous materials, and obtain the floating material and the sinking material, the floating material and the bottom material. The sediments enter the dehydrator respectively for dehydration and packaging;所述分选为将脱水打包处理后的上浮料和下沉料分别进入静电分选设备进行分类，得到最终分选塑料；The sorting is to enter the floating material and the sinking material after the dehydration and packaging treatment into the electrostatic sorting equipment for sorting to obtain the final sorting plastic;所述热熔造粒为各种分选塑料通过螺旋输送进入热熔设备进行塑料的加温熔化，热熔后的塑料熔体经过滤网与带有孔洞的模头后，进入冷水中硬化拉条，将硬化的塑料条牵引入切粒机进行切粒造粒；The hot-melt granulation is for various sorting plastics to enter the hot-melt equipment through screw conveying for heating and melting of the plastics. The hardened plastic strip is pulled into the pelletizer for pelletizing;所述筛分干燥为将切粒后的粒状塑料通过振动筛进行筛分，分选塑料粒子，经过鼓风干燥后进行打包；The sieving and drying is to sieve the diced granular plastics through a vibrating sieve, sort the plastic particles, and pack them after drying by blasting;所述废水处理是对盐水除杂、破碎、摩擦清洗工艺过程中产生的废水进行斜筛过滤，絮凝沉淀和气浮除杂除油，生化降解COD工序；The wastewater treatment is to filter the wastewater generated in the process of brine removal, crushing, and friction cleaning through inclined sieves, flocculation sedimentation and air flotation to remove impurities and oil, and biochemically degrade COD;所述废气处理是对热熔造粒工艺过程中产生的废气进行废气收集、喷淋洗涤、静电除油、氧化分解处理，再进行废气排放；The waste gas treatment is to perform waste gas collection, spray washing, electrostatic degreasing, oxidative decomposition treatment on the waste gas generated during the hot melt granulation process, and then discharge the waste gas;所述盐水除杂工艺中脱水机进行清洗的过程可配合助剂进行清洗；所述助剂为非离子表面活性剂、硅酸盐的组合；The cleaning process of the dehydrator in the brine removal process can be cleaned with auxiliary agents; the auxiliary agents are the combination of nonionic surfactant and silicate;所述盐水槽中的盐水密度为1.10～1.20g/cm³；The brine density in the brine tank is 1.10-1.20g/cm³ ;所述除轻质杂质是将塑料碎片从高度为2-8米的高度落下，经过Z形折板，上端抽风，下端吹风处理；所述除金属处理是磁辊除铁和涡电流除有色金属；The removal of light impurities is to drop the plastic fragments from a height of 2-8 meters, pass through a Z-shaped folded plate, exhaust air at the upper end, and blow air at the lower end; the metal removal treatment is magnetic roller iron removal and eddy current removal of non-ferrous metals. ;所述热熔造粒工艺中在熔融阶段加入萃取脱挥助剂；所述萃取脱挥助剂以多孔聚丙烯聚合物为载体；所述聚丙烯为无规聚丙烯和等规聚丙烯的混合物；所述无规聚丙烯和等规聚丙烯的重量比值为1：(0.1-5)；In the hot-melt granulation process, an extraction and devolatilization aid is added in the melting stage; the extraction and devolatilization aid uses a porous polypropylene polymer as a carrier; the polypropylene is a mixture of atactic polypropylene and isotactic polypropylene ; The weight ratio of the atactic polypropylene and the isotactic polypropylene is 1: (0.1-5);所述萃取脱挥助剂负载多元醇型非离子表面活性剂和低沸点萃取剂；所述多元醇型非离子表面活性剂为失水山梨醇脂肪酸酯；所述沸点萃取剂为水。The extraction and devolatilization aid supports a polyol type nonionic surfactant and a low boiling point extractant; the polyol type nonionic surfactant is sorbitan fatty acid ester; the boiling point extractant is water.2.如权利要求1所述的一种硬杂料回收再生工艺，其特征在于，所述湿式破碎处理所用仪器为湿式破碎机；所述湿式破碎机的筛网孔径为10-20mm。2 . The process for recycling and regenerating hard miscellaneous materials according to claim 1 , wherein the instrument used for the wet crushing treatment is a wet crusher; the screen mesh aperture of the wet crusher is 10-20 mm. 3 .3.如权利要求1所述的一种硬杂料回收再生工艺，其特征在于，所述脱水机的转速为100-3000rpm，筛网孔径为1-2mm。3. A kind of hard miscellaneous material recovery and regeneration process as claimed in claim 1 is characterized in that, the rotating speed of described dehydrator is 100-3000rpm, and the screen mesh aperture is 1-2mm.4.如权利要求3所述的一种硬杂料回收再生工艺，其特征在于，所述脱水机的转速为1000-2500rpm，筛网孔径为1.2-1.8mm。4. A kind of hard miscellaneous material recovery and regeneration process as claimed in claim 3, is characterized in that, the rotating speed of described dehydrator is 1000-2500rpm, and the screen mesh aperture is 1.2-1.8mm.5.如权利要求1所述的一种硬杂料回收再生工艺，其特征在于，所述热熔造粒中各种分选塑料的形状为片状。5 . The hard miscellaneous material recovery and regeneration process according to claim 1 , wherein the shapes of various sorted plastics in the hot-melt granulation are sheet-like. 6 .6.如权利要求1所述的一种硬杂料回收再生工艺，其特征在于，所述筛分干燥工艺中的塑料粒子的粒径为1-10mm。6 . The hard miscellaneous material recovery and regeneration process according to claim 1 , wherein the particle size of the plastic particles in the screening and drying process is 1-10 mm. 7 .7.如权利要求1所述的一种硬杂料回收再生工艺，其特征在于，所述废水处理工艺处理后的废水进行回用于盐水除杂、摩擦清洗工艺过程。7. A kind of hard miscellaneous material recovery and regeneration process as claimed in claim 1, is characterized in that, the waste water after described waste water treatment process is reused for brine removal, friction cleaning process.8.如权利要求1-7任一项所述的一种硬杂料回收再生工艺，其特征在于，权利要求1-7任一项所述硬杂料回收再生工艺采用PLC自动化控制系统进行操作。8. a kind of hard miscellaneous material recovery and regeneration process as described in any one of claim 1-7 is characterized in that, the hard miscellaneous material recovery and regeneration process described in any one of claim 1-7 adopts PLC automatic control system to operate .

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