CN109134717B - Production process for preparing chlorinated polyethylene by segmented temperature rise solid phase method - Google Patents
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Abstract
The invention relates to a production process for preparing chlorinated polyethylene by a solid phase method with sectional heating, which comprises the following steps: 1) introducing nitrogen into the reactor, and removing air in the system; 2) adding a polyethylene raw material, an initiator and an anti-sticking agent into the upper end of a reactor, and introducing chlorine or a mixed gas of the chlorine and an inert gas into the lower end of the reactor; 3) the materials in the reactor rotate along with the reactor barrel, the raw materials move downwards in the axial direction and the radial direction, and the gas reversely contacts with the raw materials from bottom to top to carry out chlorination reaction; 4) the polyethylene raw material enters a low-temperature chlorination stage, and low-temperature chlorination reaction is carried out in the low-temperature chlorination stage; 5) then entering a medium-temperature chlorination section, and carrying out medium-temperature chlorination reaction in the medium-temperature chlorination section; 6) and finally, entering a high-temperature chlorination section, and carrying out high-temperature chlorination reaction in the section. The reactor for preparing chlorinated polyethylene by the solid phase method has the advantages of uniform distribution of reaction materials, large contact area with chlorine, good heat transfer effect, continuous production and high production capacity, and can enlarge the production capacity.
Description
Technical Field
The invention belongs to the technical field of chemical equipment, and particularly relates to a production process for preparing chlorinated polyethylene by a solid phase method.
Background
The chlorinated polyethylene serving as a saturated high-molecular elastomer material has the characteristics of plastics and rubber, has excellent thermal-oxidative aging resistance, ozone aging resistance, acid and alkali resistance, flame resistance, oil resistance, chemical medicine resistance and the like, and also has excellent solubility and adhesiveness, and water vapor and oxygen can hardly permeate. The chlorinated polyethylene material is non-toxic, does not contain heavy metal and polycyclic aromatic hydrocarbon, is an environment-friendly and economic material, and has wide application. Can be used in the fields of plastics, building materials, chemical industry, electrical appliances, textile, shipbuilding, anticorrosive coatings, adhesives and the like, and has wide application prospect.
In the preparation method of chlorinated polyethylene, the solvent is difficult to recover by a solution method, the environmental pollution is serious, the reagent is harmful to people, and the method is basically stopped. The suspension method has large amount of acidic waste water, high equipment requirement and huge investment. The solid phase method is simple to operate, the chlorination reaction is carried out under a dry condition, the discharge amount of three wastes is small, equipment is not easy to corrode, the investment is small, the product is pure, economic and environment-friendly, and almost no pollution is caused. However, this process is exothermic, and heat removal in the reactor is difficult and heat transfer is not uniform. Therefore, the problems of removal of reaction heat, product adhesion and chlorination uniformity in chlorination reaction need to be solved.
At present, the solid phase method is still in a laboratory research stage, and the process is immature. Reactors of the solid phase process are generally a stirring fixed bed and a fluidized bed, and the traditional fixed bed and fluidized bed reactors are sensitive to temperature change, so that product adhesion, nonuniform chlorination and high residual crystallinity can be caused by slight careless operation, and the product quality is influenced. On the other hand, the traditional fixed bed and fluidized bed reactors can only carry out intermittent production, cannot realize continuous production and have small production capacity.
The chlorination reaction of the polyethylene is a strong exothermic reaction, and the reaction temperature is near the melting point of the polyethylene, so that the solid-phase method for preparing the chlorinated polyethylene is easy to cause bonding foaming and sintering of solid particles, so that the chlorination is not uniform, the chlorination reaction rate is reduced, the residual crystallinity of the prepared product is high, and the product quality is lower than that of the product prepared by the suspension method. The exothermic reaction, the product adhesion and the high residual crystallinity are key points for restricting the development of the process for preparing the chlorinated polyethylene by the solid phase method, so that the removal of the reaction heat, the solution of the product adhesion phenomenon and the reduction of the residual crystallinity of the product are important in the research of the process.
Disclosure of Invention
The invention provides a production process for preparing chlorinated polyethylene by a solid phase method, which has the advantages of uniform material distribution, large contact area with chlorine, good heat transfer effect, continuous production and high production capacity, and aims to solve the problems that the heat is generated in the polyethylene chlorination reaction, the heat transfer of the traditional chlorination reaction process is not uniform, the products are agglomerated and bonded, and the continuous production cannot be realized by the traditional reactor in the prior art, so that the production process for preparing the chlorinated polyethylene by the solid phase method has the advantages of uniform material distribution, large production capacity and high production capacity.
In order to achieve the above purpose, the invention adopts the following technical scheme:
a production process for preparing chlorinated polyethylene by a solid phase method with sectional temperature rise comprises the following steps:
1) introducing nitrogen into the reactor, and removing air in the system;
2) adding 100 parts by mass of polyethylene raw material, 2-4 parts by mass of initiator and 50-60 parts by mass of anti-sticking agent into the upper end of a reactor, and introducing 240 parts by mass of chlorine or a mixed gas of chlorine and inert gas into the lower end of the reactor;
3) the materials in the reactor rotate along with the reactor barrel, the raw materials move downwards in the axial direction and the radial direction, and the gas reversely contacts with the raw materials from bottom to top to carry out chlorination reaction;
4) the polyethylene raw material enters a low-temperature chlorination stage, and low-temperature chlorination reaction is carried out in the low-temperature chlorination stage, wherein the reaction temperature is 80-85 ℃, and the reaction time is 30-40 min;
5) then entering a medium-temperature chlorination section, and carrying out medium-temperature chlorination reaction in the section, wherein the reaction temperature is 110-115 ℃, and the reaction time is 30-40 min;
6) finally, entering a high-temperature chlorination section, and carrying out high-temperature chlorination reaction in the section, wherein the reaction temperature is 130-135 ℃, and the reaction time is 50-60 min;
7) and products after the reaction are collected at the outlet section of the reactor, the products are cooled and then collected through a discharge hole, and tail gas is discharged out of the reactor through a gas outlet and is recycled after treatment.
The reactor main part includes entrance, barrel and export section, and the spiral feeder is connected to the entrance, and the entrance top is provided with the gas outlet, and export section side sets up air inlet 1, and the bottom sets up discharge gate 3, is provided with programming firing equipment 5 and bearing 6 on the barrel, and the barrel sets up sealed head 4 with the junction of export section with entrance and seals, and the bearing has motor drive 7 through gear connection.
The barrel is internally provided with a low-temperature reaction section, a medium-temperature reaction section and a high-temperature reaction section, wherein the length of the low-temperature reaction section is 1/4 of the length of the barrel, the length of the medium-temperature reaction section is 1/4 of the length of the barrel, and the length of the high-temperature reaction section is 1/2 of the length of the barrel.
The ratio of the inner diameter of the cylinder body to the length of the cylinder body is 0.03-0.08.
The cylinder body inclines downwards from the inlet section to the outlet section, and the inclination angle is 2-5 degrees.
The interior of the cylinder body is a concave-convex inner member with a flow groove, and the surface of the inner member is coated with an anticorrosive material. The inner member can make the polyethylene raw material move axially and radially uniformly, increase the contact area with chlorine, increase the retention time of the raw material in the barrel, absorb the heat released by chlorination reaction, and reduce the bonding condition of the product.
The motor transmission equipment enables the cylinder to rotate through a gear bearing outside the cylinder, and the rotating speed of the cylinder is 1.2 r/min.
The outer surface of the cylinder body is provided with a temperature programming heating device, the device collects feedback information through a thermocouple, and the output power of the heating device is controlled by means of output voltage so as to prevent the temperature runaway phenomenon in the heating process.
The chlorine flow direction is opposite to the raw material movement direction. Polyethylene raw materials are added to the upper end of the cylinder body through a spiral feeder 11, gas is introduced to the lower end of the cylinder body through a gas inlet 1, the raw materials move axially and radially along with the cylinder body, and the gas reversely contacts with the raw materials from bottom to top to carry out chlorination reaction.
The chlorination reaction gas can be pure chlorine gas or a mixed gas of chlorine gas and inert gas.
The invention has the beneficial effects that:
the reactor for preparing chlorinated polyethylene by the solid phase method has the advantages of uniform distribution of reaction materials, large contact area with chlorine, good heat transfer effect, continuous production and high production capacity, and can enlarge the production capacity.
Drawings
Fig. 1 is a schematic structural view of the present invention.
The device comprises a gas inlet 1, a gas outlet 2, an outlet section 3, a discharge port 4, a sealing head 5, a temperature programming heating device 6, a bearing 7, a motor transmission device 8, a support frame 9, a cylinder 10, a gas outlet 11, a spiral feeder 12 and an inlet section.
Detailed Description
The utility model provides a reactor of solid phase legal system preparation chlorinated polyethylene, this reactor main part includes inlet section 12, barrel 9 and export section 2, spiral feeder 11 is connected to the inlet section, the inlet section top is provided with gas outlet 10, export section side sets up air inlet 1, the bottom sets up discharge gate 3, be provided with programming firing equipment 5 and bearing 6 on the barrel, the junction of barrel and inlet section and export section sets up sealed head 4 and seals, bearing 6 has motor drive 7 through gear connection, motor drive supports and fixes a position through support frame 8. The motor transmission equipment enables the cylinder to rotate through a gear bearing outside the cylinder, and the rotating speed of the cylinder is 1.2 r/min.
The barrel is internally provided with a low-temperature reaction section, a medium-temperature reaction section and a high-temperature reaction section, wherein the length of the low-temperature reaction section is 1/4 of the length of the barrel, the length of the medium-temperature reaction section is 1/4 of the length of the barrel, and the length of the high-temperature reaction section is 1/2 of the length of the barrel. The ratio of the inner diameter of the cylinder body to the length of the cylinder body is 0.03-0.08. The cylinder body inclines downwards from the inlet section to the outlet section, and the inclination angle is 2-5 degrees. The interior of the cylinder body is a concave-convex inner member with a flow groove, and the surface of the inner member is coated with an anticorrosive material. The inner member can make the polyethylene raw material move axially and radially uniformly, increase the contact area with chlorine, increase the retention time of the raw material in the barrel, absorb the heat released by chlorination reaction, and reduce the bonding condition of the product. The outer surface of the cylinder body is provided with a temperature programming heating device, the device collects feedback information through a thermocouple, and the output power of the heating device is controlled by means of output voltage so as to prevent the temperature runaway phenomenon in the heating process. The chlorine flow direction is opposite to the raw material movement direction. Polyethylene raw materials are added to the upper end of the cylinder body through a spiral feeder 11, gas is introduced to the lower end of the cylinder body through a gas inlet 1, the raw materials move axially and radially along with the cylinder body, and the gas reversely contacts with the raw materials from bottom to top to carry out chlorination reaction. The chlorination reaction gas can be pure chlorine gas or a mixed gas of chlorine gas and inert gas.
The production method for preparing the chlorinated polyethylene by adopting the equipment comprises the following steps:
1) introducing nitrogen into the reactor through an air inlet 1 to remove air in the system;
2) adding 100 parts by mass of polyethylene raw material, 2-4 parts by mass of initiator and 50-60 parts by mass of anti-sticking agent into the upper end of a cylinder 9 through a screw feeder 11, and introducing 240 parts by mass of chlorine or a mixed gas of the chlorine and inert gas into the lower end of the cylinder 9 through an air inlet 1;
3) the cylinder 9 is driven by the motor transmission device 7 to rotate, the raw material moves along the cylinder in the axial and radial directions, and the gas reversely contacts with the raw material from bottom to top to carry out chlorination reaction;
4) firstly, polyethylene raw materials enter a low-temperature chlorination stage, and low-temperature chlorination reaction is carried out in the low-temperature chlorination stage, wherein the reaction temperature is 80-85 ℃, and the reaction time is 30-40 min;
5) then the raw materials enter a medium-temperature chlorination section, and medium-temperature chlorination reaction is carried out in the section, wherein the reaction temperature is 110-115 ℃, and the reaction time is 30-40 min;
6) finally, the raw materials enter a high-temperature chlorination section, and high-temperature chlorination reaction is carried out in the section, wherein the reaction temperature is 130-135 ℃, and the reaction time is 50-60 min;
7) and products after the reaction are collected at the outlet section, are cooled and then are collected through the discharge port 3, and tail gas is discharged out of the reactor through the gas outlet 10 and is recycled after treatment.
The main industrial index requirements of the product prepared by the suspension method are as follows: 30-40% of chlorine content, less than or equal to 2J/g of melting heat, less than or equal to 70 Shore hardness, more than or equal to 8MPa of tensile strength, more than or equal to 500% of breaking elongation, less than or equal to 0.3% of volatile matter content, more than or equal to 8min of thermal stabilization time, and less than or equal to 4.5% of combustion residue.
Comparative example 1
a, preparing a suspension solution, namely adding 4000L of 10% hydrochloric acid solution into a 5000L acid-resistant reaction kettle, adding 400kg of high-density polyethylene with melt index MI (190 ℃/5kg) of 0.2-l.0g/L for 0min and MFR of 10-30, 1.0kg of dispersing agent fatty alcohol-polyoxyethylene ether and 2.0kg of anti-sticking agent white carbon black under the stirring state, uniformly stirring to prepare the suspension solution, and then sealing the acid-resistant reaction kettle.
b, chlorination reaction, namely introducing chlorine gas into the suspension solution for chlorination reaction in two sections:
a temperature rising section, wherein the initial chlorine introducing temperature is controlled to be 75 ℃, the temperature is gradually raised to 130 ℃, and the chlorine introducing amount of the temperature rising section is 220 kg;
a constant temperature section, wherein the temperature of the constant temperature section is controlled to be 130 ℃, the temperature is kept constant, and the chlorine introducing amount is 220 kg;
the whole reaction process controls the chlorine introducing temperature to be 75-130 ℃, the chlorine introducing amount is 440kg, and the reaction time is 4 hours.
And (3) separating and washing, namely cooling the chlorinated product to a temperature lower than 80 ℃ in the reaction kettle after the reaction is finished, conveying the material to a vacuum filter by using compressed air for vacuum filtration, recycling the filtered hydrochloric acid, washing the filtered chlorinated product repeatedly by using water, dehydrating by using a centrifugal machine, drying by using hot air, grinding and grinding, and homogenizing by using a bin to obtain the chlorinated polyethylene product with the chlorine content of 34.0 percent, DSC2.5J/g and the Shore hardness of 67.
Comparative example 2
a, preparing a suspension solution, namely adding 8700L of 17 percent hydrochloric acid solution into a 12500L of acid-resistant reaction kettle, and stirring
1300kg of high-density polyethylene with melt index MI (190 ℃/5kg) of 0.2-l.0g/l0min and MFR of 10-30, 1.6kg of dispersant polyethylene pyrrolidone and 2kg of anti-sticking agent D17 are added under the state, and the mixture is stirred uniformly to prepare a suspension solution, and then the acid-resistant reaction kettle is sealed.
b, chlorination reaction, namely introducing chlorine gas into the suspension solution for chlorination reaction in two sections:
a temperature rising section, wherein the initial chlorine introducing temperature is controlled to be 60 ℃, the temperature is gradually raised to 130 ℃, and the chlorine introducing amount of the temperature rising section is 780 kg;
a constant temperature section, wherein the temperature of the constant temperature section is controlled to be 130 ℃, the temperature is kept constant, and the chlorine introducing amount is 520 kg;
the whole reaction process controls the chlorine introducing temperature to be 60-130 ℃, the chlorine introducing amount is 1300kg, and the reaction time is 4.5 h.
c. And (3) separating and washing, namely cooling the chlorinated product to a temperature lower than 80 ℃ in the reaction kettle after the reaction is finished, conveying the material to a vacuum filter by using compressed air for vacuum filtration, recycling the filtered hydrochloric acid, washing the filtered chlorinated product repeatedly by using water, dehydrating by using a centrifugal machine, drying by using hot air, grinding and grinding, and homogenizing by using a bin to obtain the chlorinated polyethylene product, wherein the chlorine content of the chlorinated polyethylene product is 33.3%, DSC2.0J/g and the Shore hardness is 69.
Comparative example 3
a, preparing a suspension, namely adding 8000L of 25% hydrochloric acid rocholate solution into a 12500L acid-resistant reaction kettle, adding 1600kg of high-density polyethylene with melt index MI (190 ℃/5kg) of 0.2-1.0g/10min and MFR of 10-30, 3kg of dispersant methyl acrylate-methacrylic acid copolymer and 8kg of anti-sticking agent talcum powder under the stirring state, uniformly stirring to prepare a suspension, and then sealing the acid-resistant reaction kettle.
b, chlorination reaction, namely uniformly introducing chlorine into the suspension solution in two sections for chlorination reaction:
a temperature rising section, wherein the initial chlorine introducing temperature is controlled to be 30 ℃, the temperature is gradually raised to 125 ℃, and the chlorine introducing amount of the temperature rising section is 800 kg;
and (3) a constant temperature section, namely, the temperature of the constant temperature section is controlled to be 125 ℃, the temperature is kept constant, and the chlorine introducing amount is 350kg:
the whole reaction process controls the chlorine introducing temperature to be 30-125 ℃, the chlorine introducing amount is 1150kg, and the reaction time is 5 hours.
c. And (3) separating and washing, namely cooling the chlorinated product to a temperature lower than 80 ℃ in the reaction kettle after the reaction is finished, conveying the material to a vacuum filter by using compressed air for vacuum filtration, recycling the filtered hydrochloric acid, washing the filtered chlorinated product repeatedly by using water, dehydrating by using a centrifugal machine, drying by using hot air, grinding and grinding, and homogenizing by using a bin to obtain the chlorinated polyethylene product, wherein the chlorine content of the chlorinated polyethylene product is 22%, DSC3.0J/g and the Shore hardness is 70.
Example 1
Uniformly mixing 100 parts of polyethylene raw material with the crystallinity of 68.7 percent, the melting point of 134.3 ℃, the particle size of 150-380 um, the wax content of 1.2 percent, the melt flow rate of 0.804g/10min, the specific surface area of 2.047m2.g-1, the pore volume of 3.344 multiplied by 10-3cm3.g-1 and the branching degree of 5.65, 3 parts of benzoyl peroxide initiator and 60 parts of quartz sand anti-bonding agent, adding the mixture into a fixed bed reactor with programmed temperature rise, and introducing nitrogen to remove air in the system after connection. The temperature in the reactor is raised to 85 ℃ by a temperature programming system, and the temperature raising rate is 2 ℃/min. Closing the nitrogen valve, introducing chlorine, opening a chlorine circulating loop valve, adjusting the chlorine flow to be 2.5%/min after the reactor is filled with chlorine, and carrying out low-temperature chlorination reaction for 40 min. Then the temperature is increased to 115 ℃ at the rate of 2 ℃/min, and the chlorination reaction is carried out for 60 min. Then the temperature is increased to 130 ℃ at the rate of 2 ℃/min, and the chlorination reaction is carried out for 30min at high temperature. And finally, closing a chlorine valve, and carrying out heat treatment at 130 ℃ for 30min to keep the chlorine atmosphere in the reactor. After the heat treatment is finished, opening a nitrogen valve, closing a chlorine circulating valve, discharging chlorine in the system, and absorbing the chlorine by a sodium hydroxide solution. And when the temperature in the reactor is reduced to room temperature, taking out the chlorinated polyethylene product, washing the chlorinated polyethylene product to be neutral by using alkali liquor, and drying the chlorinated polyethylene product in an oven to constant weight.
The main indexes of the chlorinated polyethylene product prepared by the invention are as follows: chlorine content 36%, residual crystallinity < 2%, thermal stability time 498s, combustion residue 0.98%, volatiles content 0.199%, hardness 60, tensile strength 10.1MPa, elongation at break 690%.
Example 2
Uniformly mixing 100 parts of polyethylene raw material with the crystallinity of 68.7 percent, the melting point of 134.3 ℃, the particle size of 150-380 um, the wax content of 1.2 percent, the melt flow rate of 0.804g/10min, the specific surface area of 2.047m2.g-1, the pore volume of 3.344 x 10-3cm3.g-1 and the branching degree of 5.65, 2 parts of azodiisobutyronitrile initiator and 50 parts of quartz sand anti-bonding agent, adding the mixture into a fixed bed reactor with programmed temperature rise, and introducing nitrogen to remove air in the system after connection. The temperature in the reactor is raised to 80 ℃ by a temperature programming system, and the temperature raising rate is 2 ℃/min. Closing the nitrogen valve, introducing chlorine, opening a chlorine circulating loop valve, adjusting the chlorine flow to 2%/min after the reactor is filled with chlorine, and carrying out low-temperature chlorination reaction for 30 min. Then the temperature is increased to 115 ℃ at the rate of 2 ℃/min, and the chlorination reaction is carried out for 30min at high temperature. Then the temperature is increased to 130 ℃ at the rate of 2 ℃/min, and the high-temperature chlorination reaction is carried out for 60 min. And finally, closing a chlorine valve, and carrying out heat treatment at 130 ℃ for 30min to keep the chlorine atmosphere in the reactor. After the heat treatment is finished, opening a nitrogen valve, closing a chlorine circulating valve, discharging chlorine in the system, and absorbing the chlorine by a sodium hydroxide solution. And when the temperature in the reactor is reduced to room temperature, taking out the chlorinated polyethylene product, washing the chlorinated polyethylene product to be neutral by using alkali liquor, and drying the chlorinated polyethylene product in an oven to constant weight.
The main indexes of the chlorinated polyethylene product prepared by the invention are as follows: the chlorine content was 41%, the residual crystallinity was < 2%, the thermal stabilization time was 505s, the combustion residue was 1%, the volatile content was 0.209%, the hardness was 57, the tensile strength was 10.5MPa, and the elongation at break was 750%.
For the industrial product index requirements, the product index pairs of the comparative examples and the examples, as shown in the table below, it can be seen that the chlorinated polyethylene product synthesized by the solid phase method of the present invention can meet the requirements of the current industrialized products, and the product performance is more excellent than that prepared by the suspension method in the prior art.
| Specific index | Product requirements | Comparative example 1 | Comparative example 2 | Comparative example 3 | Example 1 | Example 2 |
| Chlorine content | 30％-40％ | 34.0％ | 33.3％ | 22％ | 36％ | 41％ |
| Heat of fusion | ≤2J/g | 2.5J/g | 2.0J/g | 3.0J/g | 2.0J/g | 2.0J/g |
| Shore hardness | ≤70 | 67 | 69 | 70 | 60 | 57 |
| Elongation at break | ≥500％ | 690％ | 750％ | |||
| Tensile strength | ≥8Mpa | 10.1MPa | 10.5MPa | |||
| Volatile content | ≤0.3％ | 0.199％ | 0.209％ | |||
| Thermal stability time | ≥8min | 498s | 505s | |||
| Combustion residue | ≤4.5％ | 0.98％ | 1％ |
Claims (7)
1. A production process for preparing chlorinated polyethylene by a solid phase method with sectional temperature rise is characterized in that: the method comprises the following steps:
1) introducing nitrogen into the reactor, and removing air in the system;
2) adding a polyethylene raw material, an initiator and an anti-sticking agent into the upper end of a reactor, and introducing chlorine or a mixed gas of the chlorine and an inert gas into the lower end of the reactor;
3) the materials in the reactor rotate along with the reactor barrel, the raw materials move downwards in the axial direction and the radial direction, and the gas reversely contacts with the raw materials from bottom to top to carry out chlorination reaction;
4) the polyethylene raw material enters a low-temperature chlorination section, and low-temperature chlorination reaction is carried out in the low-temperature chlorination section, wherein the reaction temperature is 80-85 ℃, and the reaction time is 30-40 min;
5) then entering a medium-temperature chlorination section, and carrying out medium-temperature chlorination reaction in the section, wherein the reaction temperature is 110-115 ℃, and the reaction time is 30-40 min;
6) finally, entering a high-temperature chlorination section, and carrying out high-temperature chlorination reaction in the section, wherein the reaction temperature is 130-135 ℃, and the reaction time is 50-60 min;
the reactor main body comprises an inlet section, a cylinder body and an outlet section, wherein the inlet section is connected with the spiral feeder, the top of the inlet section is provided with an air outlet, the side surface of the outlet section is provided with an air inlet, the bottom of the inlet section is provided with a discharge hole, the cylinder body is provided with a temperature programming heating device and a bearing, the joint of the cylinder body and the inlet section and the outlet section is provided with a sealing head for sealing, and the bearing is connected with a motor transmission device through a gear; the barrel is internally provided with a low-temperature reaction section, a medium-temperature reaction section and a high-temperature reaction section, wherein the length of the low-temperature reaction section is 1/4 of the length of the barrel, the length of the medium-temperature reaction section is 1/4 of the length of the barrel, and the length of the high-temperature reaction section is 1/2 of the length of the barrel.
2. The production process according to claim 1, wherein: the ratio of the inner diameter of the cylinder body to the length of the cylinder body is 0.03-0.08.
3. The production process according to claim 1, wherein: the cylinder body inclines downwards from the inlet section to the outlet section, and the inclination angle is 2-5 degrees.
4. The production process according to claim 1, wherein: the interior of the cylinder body is a concave-convex inner member with a flow groove, and the surface of the inner member is coated with an anticorrosive material.
5. The production process according to claim 1, wherein: the motor transmission equipment enables the cylinder to rotate through a gear bearing outside the cylinder, and the rotating speed of the cylinder is 1.2 r/min.
6. The production process according to claim 1, wherein: the outer surface of the cylinder body is provided with a temperature programming heating device, the device collects feedback information through a thermocouple and controls the output power of the heating device by means of output voltage.
7. The production process according to claim 1, wherein: the polyethylene raw material is added to the upper end of the cylinder body through the spiral feeder, the gas is introduced to the lower end of the cylinder body through the gas inlet, the raw material moves axially and radially along with the cylinder body, and the gas reversely contacts with the raw material from bottom to top to carry out chlorination reaction.
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