CN110605803B - Post-treatment method for producing butyl rubber - Google Patents
Post-treatment method for producing butyl rubber Download PDFInfo
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- CN110605803B CN110605803B CN201910887580.3A CN201910887580A CN110605803B CN 110605803 B CN110605803 B CN 110605803B CN 201910887580 A CN201910887580 A CN 201910887580A CN 110605803 B CN110605803 B CN 110605803B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B13/00—Conditioning or physical treatment of the material to be shaped
- B29B13/06—Conditioning or physical treatment of the material to be shaped by drying
- B29B13/065—Conditioning or physical treatment of the material to be shaped by drying of powder or pellets
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C43/00—Compression moulding, i.e. applying external pressure to flow the moulding material; Apparatus therefor
- B29C43/02—Compression moulding, i.e. applying external pressure to flow the moulding material; Apparatus therefor of articles of definite length, i.e. discrete articles
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C43/00—Compression moulding, i.e. applying external pressure to flow the moulding material; Apparatus therefor
- B29C43/32—Component parts, details or accessories; Auxiliary operations
- B29C43/58—Measuring, controlling or regulating
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C43/00—Compression moulding, i.e. applying external pressure to flow the moulding material; Apparatus therefor
- B29C43/32—Component parts, details or accessories; Auxiliary operations
- B29C43/58—Measuring, controlling or regulating
- B29C2043/5808—Measuring, controlling or regulating pressure or compressing force
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29K—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES B29B, B29C OR B29D, RELATING TO MOULDING MATERIALS OR TO MATERIALS FOR MOULDS, REINFORCEMENTS, FILLERS OR PREFORMED PARTS, e.g. INSERTS
- B29K2023/00—Use of polyalkenes or derivatives thereof as moulding material
- B29K2023/18—Polymers of hydrocarbons having four or more carbon atoms, e.g. polymers of butylene, e.g. PB, i.e. polybutylene
- B29K2023/22—Copolymers of isobutene, e.g. butyl rubber
Abstract
The invention provides a post-treatment method for producing butyl rubber, which comprises the following steps: a) sequentially carrying out vibration dehydration, extrusion dehydration and pre-expansion drying on the colloidal particle water to obtain a treated rubber material; b) dehydrating and drying the treated rubber material obtained in the step a) by adopting a double-screw expansion dryer at the temperature of 100-130 ℃ and the pressure of 15-110 bar, and performing three-stage drying and cooling in a fluidized bed after flash evaporation to obtain the rubber material with the water content of less than 0.3%; the double-screw expansion dryer adopts high-pressure inert gas as a conveying medium; the temperature of the three-section drying and cooling is respectively 80-90 ℃, 80-90 ℃ and 40-55 ℃; c) briquetting and packaging the sizing material with the water content of less than 0.3% obtained in the step b) to obtain a butyl rubber product. The post-treatment method adopts specific steps, conditions and parameters to realize better interaction, reduces the water content of the sizing material and the temperature of the sizing material, and further reduces the operation temperature of a subsequent fluidized bed, thereby improving the productivity of a drying line.
Description
Technical Field
The invention relates to the technical field of butyl rubber, in particular to a post-treatment method for producing butyl rubber.
Background
The butyl rubber has the characteristics of excellent air tightness, ageing resistance, corrosion resistance, electric insulation, puncture resistance and the like, and is mainly used in the industries of inner tubes, vulcanized capsules, anticorrosive linings, electric insulating materials, waterproof coiled materials, medical products, chewing gum base materials and the like.
The technological process of producing butyl rubber is to copolymerize isobutene and small amount of isoprene in chloromethane solution at low temperature with aluminum chloride as catalyst to obtain butyl rubber product; recovering the pure solvent from the unreacted monomer and solvent through flash evaporation, compression and rectification, and then circulating the pure solvent back to the polymerization section to send the isobutene out of the battery limit area for refining; all impurities are completely removed; and finally, conveying the polymer water slurry from the reaction working section to a post-treatment working section for drying, briquetting, packaging and packaging. Wherein, the polymerization and flash evaporation process specifically comprises the following steps: after the mixed feed and the catalyst solution are prepared, feeding the mixed feed and the catalyst solution into a polymerization reactor, producing the butyl rubber in water slurry, and separating unreacted monomers by flash evaporation; the monomer refining process specifically comprises the following steps: the monomer with the required purity is provided for the front-path polymerization by distilling the raw materials from outside the battery limits; the process of compressing and refining the circulating gas comprises the following steps: drying, pressurizing and refining the circulating gas from flash evaporation to obtain pure chloromethane, isobutene and the like; the refrigeration process specifically comprises the following steps: the refrigeration section is used for cooling the polymerization reactor to a very low temperature and is also used for other sections requiring refrigeration in a butyl rubber device; the drying and packaging process specifically comprises the following steps: the polymer slurry is dewatered, briquetted, and packaged in order to obtain the final rubber bales for sale.
At present, a double-screw expansion dryer is mainly adopted in the domestic post-treatment method for producing the butyl rubber, the equipment adopts a machine head reflux heating technology, so that the raw rubber is internally rubbed and heated, the physical properties of the rubber can be better protected, and simultaneously, the power and the energy consumption of the equipment are lower than those of the similar equipment abroad. However, the equipment is used for post-treatment of butyl rubber, the process temperature is as high as 130-160 ℃, the rubber material is rubbed by a double screw and then blown to a fluidized bed by conveying wind, and the process temperature is high, so that the following defects are caused: (1) resulting in higher sizing temperatures and increased mooney degradation; (2) the plasticized rubber is easily formed in the fluidized bed, and the rejection rate is increased; (3) the high temperature causes the adhesion of the packaging film, which affects the use of downstream users; (4) due to the difficulty in controlling the volatile components, the capacity is limited; (5) the high temperature increases the risk of color change of the block during storage or use by downstream customers, which negatively affects company brands.
Disclosure of Invention
In view of the above, the present invention provides a post-treatment method for producing butyl rubber, which can reduce the water content of the rubber material and the temperature of the rubber material, and further reduce the operation temperature of the subsequent fluidized bed, thereby improving the productivity of the drying line.
The invention provides a post-treatment method for producing butyl rubber, which comprises the following steps:
a) sequentially carrying out vibration dehydration, extrusion dehydration and pre-expansion drying on the colloidal particle water to obtain a treated rubber material;
b) dehydrating and drying the treated rubber material obtained in the step a) by adopting a double-screw expansion dryer at the temperature of 100-130 ℃ and the pressure of 15-110 bar, and performing three-stage drying and cooling in a fluidized bed after flash evaporation to obtain the rubber material with the water content of less than 0.3%; the double-screw expansion dryer adopts high-pressure inert gas as a conveying medium; the temperature of the three-section drying and cooling is respectively 80-90 ℃, 80-90 ℃ and 40-55 ℃;
c) briquetting and packaging the sizing material with the water content of less than 0.3% obtained in the step b) to obtain a butyl rubber product.
Preferably, the water content of the crumb water in step a) is 95% to 97%.
Preferably, the vibration dehydration in the step a) is carried out by adopting a vibration sieve, so that the water content of the colloidal particle water is reduced to 45-55 percent; the rotating speed of a motor of the vibrating screen is 800 r/min-1200 r/min, and the amplitude is 5.5 mm-7.5 mm.
Preferably, the extrusion dehydration in the step a) is carried out by using an extrusion dehydrator, so that the water content of the rubber material is reduced to 8% -12%; the operating temperature of the extrusion dehydrator is 80-130 ℃, and the pressure is 30-35 bar.
Preferably, the pre-expansion drying in the step a) is carried out by adopting a pre-expansion dryer, so that the water content of the sizing material is 5-7%; the operation temperature of the pre-expansion dryer is 80-140 ℃, and the pressure is 16-38 bar.
Preferably, the high-pressure inert gas in the step b) is air, nitrogen or carbon dioxide gas with the pressure of 50-80 bar; wherein the purity of the nitrogen is more than or equal to 99.9 wt%.
Preferably, the flash evaporation process in the step b) is specifically as follows:
the dehydrated and dried rubber material is cut by a rotary cutter with the rotating speed of 300 r/min-3500 r/min, the pressure is instantly reduced to normal pressure, the rubber material is exploded into discontinuous and adhesive popcorn shape, more micro pore channels are formed on the surface, the water is evaporated, and the water content of the rubber material is reduced to 0.5% -1%.
Preferably, the rotating speed of a motor of the fluidized bed in the step b) is 400 r/min-500 r/min, and the amplitude is 12 mm-20 mm.
Preferably, the briquetting in the step c) is carried out by a briquetting machine; the main cylinder pressure of the briquetting machine is 0-350 bar, and the side cylinder pressure is 0-200 bar.
The invention provides a post-treatment method for producing butyl rubber, which comprises the following steps: a) sequentially carrying out vibration dehydration, extrusion dehydration and pre-expansion drying on the colloidal particle water to obtain a treated rubber material; b) dehydrating and drying the treated rubber material obtained in the step a) by adopting a double-screw expansion dryer at the temperature of 100-130 ℃ and the pressure of 15-110 bar, and performing three-stage drying and cooling in a fluidized bed after flash evaporation to obtain the rubber material with the water content of less than 0.3%; the double-screw expansion dryer adopts high-pressure inert gas as a conveying medium; the temperature of the three-section drying and cooling is respectively 80-90 ℃, 80-90 ℃ and 40-55 ℃; c) briquetting and packaging the sizing material with the water content of less than 0.3% obtained in the step b) to obtain a butyl rubber product. Compared with the prior art, the post-treatment method provided by the invention adopts specific steps, conditions and parameters to realize better interaction, and can reduce the water content of the sizing material and the temperature of the sizing material, so that the operating temperature of a subsequent fluidized bed is reduced, and the capacity of a drying line is improved. Experimental results show that the temperature of the rubber material in the post-treatment method provided by the invention is as low as 50-65 ℃, the yield of the fluidized bed plasticized rubber is only 180 kg/day, and the qualification rate of products is improved; the drying temperature of three sections of the fluidized bed is lower, the required air supply amount is reduced, and the energy consumption is reduced; after the temperature of the off-line rubber block is reduced, the risk of mucosa of the product in the processes of storage and use by downstream users can be reduced; the risk of color change of the product caused by high off-line temperature is reduced; meanwhile, the average volatile component of the product obtained by the method is 0.15%, the premium grade rate of the volatile component is 95%, the load of a production line is increased, and the capacity is improved, so that the raw material cost is lowered in a phase-changing manner, and the product profit is increased.
In addition, the drying temperature of the sizing material in the post-treatment method provided by the invention is obviously reduced, the steam consumption of the double-screw expansion dryer is only 50kg/h, and the energy consumption is greatly saved.
Drawings
FIG. 1 is a process flow diagram of a post-treatment process for producing butyl rubber as provided in example 1 of the present invention.
Detailed Description
The technical solutions of the present invention will be described clearly and completely with reference to the following embodiments of the present invention, and it should be understood that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The invention provides a post-treatment method for producing butyl rubber, which comprises the following steps:
a) sequentially carrying out vibration dehydration, extrusion dehydration and pre-expansion drying on the colloidal particle water to obtain a treated rubber material;
b) dehydrating and drying the treated rubber material obtained in the step a) by adopting a double-screw expansion dryer at the temperature of 100-130 ℃ and the pressure of 15-110 bar, and performing three-stage drying and cooling in a fluidized bed after flash evaporation to obtain the rubber material with the water content of less than 0.3%; the double-screw expansion dryer adopts high-pressure inert gas as a conveying medium; the temperature of the three-section drying and cooling is respectively 80-90 ℃, 80-90 ℃ and 40-55 ℃;
c) briquetting and packaging the sizing material with the water content of less than 0.3% obtained in the step b) to obtain a butyl rubber product.
The invention firstly carries out vibration dehydration, extrusion dehydration and pre-expansion drying on colloidal particle water in sequence to obtain the treated rubber material. In the invention, the rubber particle water, namely the produced butyl rubber, enters the rubber particle water tank from the polymerization stripping tower; the water content of the colloidal particle water is preferably 95% to 97%, and more preferably 95%. In the preferred embodiment of the invention, the flow rate of the colloidal particle water is preferably 175 t/h-210 t/h, more preferably 180 t/h-205 t/h; controlled by a control valve and then enters the post-treatment section of the invention.
In the invention, the vibration dehydration is preferably carried out by adopting a vibration sieve; the rotating speed of a motor of the vibrating screen is preferably 800 r/min-1200 r/min, and more preferably 1000 r/min; the amplitude of the vibrating screen is preferably 5.5mm to 7.5mm, more preferably 6.5 mm. The invention adopts the vibration dehydration process to remove most of free water, so that the water content of the colloidal particle water is reduced to 45-55 percent. In the invention, the vibrating screen and the feeding valve are interlocked, and the motor can excite the alarm interlock to stop feeding after stopping; when abnormal belt materials are stopped, firstly cleaning the accumulated glue on the surface, then starting the vibrating screen, and when the accumulated glue on the screen plate is cleaned, the vibrating screen cannot be operated brutally so as to avoid damaging the screen plate.
In the present invention, the press-dewatering is preferably performed by using a press-dewatering machine; the operation temperature of the extrusion dehydrator is preferably 80-130 ℃, and more preferably 100-110 ℃; the operating pressure of the extrusion dewaterer is preferably 30bar to 35bar, more preferably 32bar to 33 bar. When the temperature and the pressure of the template are too low, the dehydration rate of the sizing material cannot be reached, namely the volatile component of the product at the outlet of the extrusion dehydrator is too high; when the temperature and the pressure are too high, the plastified rubber appears, and meanwhile, the temperature of a die head of a back-way double-screw expansion dryer is increased, so that negative effects are brought to products. The invention utilizes the extrusion dehydrator to extrude the water in the sizing material in a mechanical extrusion mode and drain the water from the gap on the cylinder body of the machine, so that the water content of the sizing material is reduced to 8-12 percent.
In the present invention, the pre-expansion drying is preferably performed using a pre-expansion dryer; the operation temperature of the pre-expansion dryer is preferably 80-140 ℃, and more preferably 100-120 ℃; the operating pressure of the pre-expansion dryer is preferably 16bar to 38bar, more preferably 26bar to 28 bar. When the temperature and the pressure of the template are too low, the dehydration rate of the sizing material cannot be reached, namely the volatile content of the product at the outlet of the pre-expansion dryer is too high; when the temperature and the pressure are too high, the plastic glue appears. The invention adopts the pre-expansion drying process, the rubber material at high temperature and high pressure is extruded out of the template by adjusting the opening degree of the die hole, the rubber material is expanded into porous rubber particles by instantly utilizing the flash evaporation principle, the moisture is rapidly gasified, and the water content of the rubber material treated by the pre-expansion drying machine is 5-7 percent.
After the treated rubber material is obtained, the treated rubber material is dehydrated and dried by a double-screw expansion dryer at the temperature of 100-130 ℃ and the pressure of 15-110 bar, and is subjected to three-stage drying and cooling in a fluidized bed after flash evaporation to obtain the rubber material with the water content of less than 0.3%.
In the invention, the double-screw expansion dryer adopts high-pressure inert gas as a conveying medium; in order to realize the twin-screw expansion dryer, high-pressure inert gas can be used as a conveying medium, the invention preferably further comprises:
and (3) opening a cylinder of the double-screw expansion dryer to serve as an injection port for conveying a medium, and stopping using a raw air compressor which is used for providing conveying air to blow the rubber material from the double-screw expansion dryer to the fluidized bed. In the present invention, the high pressure inert gas is preferably air, nitrogen or carbon dioxide gas at a pressure of 50bar to 80bar, more preferably nitrogen at a pressure of 70 bar; the purity of the nitrogen gas is preferably 99.9 wt% or more, more preferably 99.99 wt%.
The invention adopts a double-screw expansion dryer to carry out dehydration drying at the temperature of 100-130 ℃ and the pressure of 15-110 bar, preferably at the temperature of 110-120 ℃ and the pressure of 60-65 bar; when the temperature of the die head is too low, the volatile content of the product at the outlet of the double-screw expansion dryer is too high, and the load is added to the processing capacity of a subsequent fluidized bed; when the temperature is too high, the final indexes of the product, such as Mooney property, bromine content and the like, are directly influenced. In addition, the double-screw expansion dryer can also set the screw rotating speed; the rotation speed of the screw is preferably 0-300 r/min, and more preferably 150 r/min; the rotating speed is too low, so that material blockage is easily caused, and the shearing force generated when the rotating speed is too high is too large, so that the performance of the sizing material is influenced.
In the invention, the dehydration and drying temperature of the rubber compound is obviously reduced, the consumption of steam of the double-screw expansion dryer (the steam enters from a steam inlet of the double-screw expansion dryer and is used for heating the double-screw expansion dryer during the starting process, the steam heats the cylinder through the jacket and simultaneously generates corresponding condensate which is discharged from a condensate outlet, and neither the steam nor the condensate is contacted with the rubber particles) is only 50kg/h, and the energy consumption is greatly saved.
In the present invention, the flash evaporation process is preferably specifically:
the dehydrated and dried rubber material is cut by a rotary cutter with the rotating speed of 300 r/min-3500 r/min (when the rotating speed of the cutter is too low, the rotary cutter is easy to block materials, the rubber particles are adhered or too large, and the subsequent drying efficiency and effect are influenced, when the rotating speed is too high, the size of the rubber particles is too small, the rubber powder yield is possibly increased, the rubber particles are attached to a fluidized bed or are pumped out of the room by an exhaust fan), the pressure is instantly reduced to normal pressure, the rubber material is exploded into a discontinuous and adhered popcorn shape, more micro pore channels are formed on the surface, the water is evaporated, and the water content of the rubber material is reduced to 0.5% -1%;
more preferably:
the dehydrated and dried rubber material is cut by a rotary cutter with the rotating speed of 3000r/min, the pressure is instantly reduced to the normal pressure, the rubber material is exploded into a discontinuous and adhesive popcorn shape, more micro pore channels are formed on the surface, the water is evaporated, and the water content of the rubber material is reduced to 0.5-1%.
In the present invention, the fluidized bed is characterized in that: consists of three air chambers, each air chamber having an inlet at the bottom thereof; the air chamber covers the orifice plate to ensure sufficient hot compressed air passes through the fluidized bed; and (3) reducing the water content of the rubber material to be below 0.3 wt% through three-stage drying and temperature reduction.
In the invention, the motor speed of the fluidized bed is preferably 400 r/min-500 r/min, more preferably 450 r/min; the amplitude of the fluidized bed is preferably 12mm to 20mm, more preferably 16 mm. When the vibration angle of the fluidized bed is too small or the Mooney viscosity of colloidal particles is too low, the fluidized bed is easy to glue, so that the vibration angle and the Mooney viscosity of the incoming material in the previous path are increased when the phenomenon occurs.
In the invention, the temperatures of the three sections of drying and cooling are respectively 80-90 ℃, 80-90 ℃ and 40-55 ℃, when the temperature is too low, the devolatilization can not be effectively finished, namely the volatile components are unqualified; when the temperature is too high, the temperature of the off-line product is also increased, and the risks of mucosa and color change are increased; preferably 85 ℃, 85 ℃ and 45 ℃; the heat comes from three blowers to heat the air to a set temperature, and the heat starts to dry the sizing material through the holes on the fluidized bed.
In the post-treatment method provided by the invention, the temperature of the rubber material is as low as 50-65 ℃, the yield of the fluidized bed plasticized rubber is only 180 kg/day, and the qualification rate of the product is improved; the drying temperature of three sections of the fluidized bed is lower, the required air supply amount is reduced, and the energy consumption is reduced.
After the rubber material with the water content of below 0.3% is obtained, the obtained rubber material with the water content of below 0.3% is pressed into blocks and packaged to obtain a butyl rubber product. In the present invention, the briquetting is preferably performed using a briquetting machine; the sizing material is preferably sent to the briquetting machine from the fluidized bed by a material distribution conveyor and a briquetting and feeding machine. In the invention, the main cylinder pressure of the briquetting machine is preferably 0-350 bar, and more preferably 175 bar; the pressure of a side cylinder of the briquetting machine is preferably 0-200 bar, and more preferably 100 bar. In the invention, if the rubber block has flash, the pressure maintaining time is too long, and the pressure maintaining time is reduced; if the rubber block is loose and cannot be formed into a block, the pressure maintaining time and the amount of the anti-sticking agent are adjusted.
In the invention, the packaging is preferably carried out by adopting a film packaging machine to obtain a butyl rubber product, and finally, the butyl rubber product is boxed by a mechanical arm and sold in a rubber bag. After the temperature of the off-line rubber block is reduced by the post-processing method provided by the invention, the risk of mucosa generated in the processes of storage and use by downstream users of the product can be reduced; the risk of color change of the product caused by high off-line temperature is reduced; meanwhile, the average volatile component of the product obtained by the method is 0.15%, the premium grade rate of the volatile component is 95%, the load of a production line is increased, and the capacity is increased by 10-20%, so that the raw material cost is reduced in a phase-changing manner, and the product profit is increased.
The post-treatment method provided by the invention adopts specific steps, conditions and parameters, realizes better interaction, and can reduce the water content of the sizing material and the temperature of the sizing material, thereby reducing the operation temperature of a subsequent fluidized bed and further improving the productivity of a drying line.
The invention provides a post-treatment method for producing butyl rubber, which comprises the following steps: a) sequentially carrying out vibration dehydration, extrusion dehydration and pre-expansion drying on the colloidal particle water to obtain a treated rubber material; b) dehydrating and drying the treated rubber material obtained in the step a) by adopting a double-screw expansion dryer at the temperature of 100-130 ℃ and the pressure of 15-110 bar, and performing three-stage drying and cooling in a fluidized bed after flash evaporation to obtain the rubber material with the water content of less than 0.3%; the double-screw expansion dryer adopts high-pressure inert gas as a conveying medium; the temperature of the three-section drying and cooling is respectively 80-90 ℃, 80-90 ℃ and 40-55 ℃; c) briquetting and packaging the sizing material with the water content of less than 0.3% obtained in the step b) to obtain a butyl rubber product. Compared with the prior art, the post-treatment method provided by the invention adopts specific steps, conditions and parameters to realize better interaction, and can reduce the water content of the sizing material and the temperature of the sizing material, so that the operating temperature of a subsequent fluidized bed is reduced, and the capacity of a drying line is improved. Experimental results show that the temperature of the rubber material in the post-treatment method provided by the invention is as low as 50-65 ℃, the yield of the fluidized bed plasticized rubber is only 180 kg/day, and the qualification rate of products is improved; the drying temperature of three sections of the fluidized bed is lower, the required air supply amount is reduced, and the energy consumption is reduced; after the temperature of the off-line rubber block is reduced, the risk of mucosa of the product in the processes of storage and use by downstream users can be reduced; the risk of color change of the product caused by high off-line temperature is reduced; meanwhile, the average volatile component of the product obtained by the method is 0.15%, the premium grade rate of the volatile component is 95%, the load of a production line is increased, and the capacity is improved, so that the raw material cost is lowered in a phase-changing manner, and the product profit is increased.
In addition, the drying temperature of the sizing material in the post-treatment method provided by the invention is obviously reduced, the steam consumption of the double-screw expansion dryer is only 50kg/h, and the energy consumption is greatly saved.
To further illustrate the present invention, the following examples are provided for illustration. The water content of the colloidal particle water used in the following embodiment of the invention is 95%, the colloidal particle water enters the colloidal particle water tank from the polymerization stripping tower, the flow rate of the colloidal particle water is controlled to be 180 t/h-205 t/h through a control valve, and the colloidal particle water enters the post-treatment working section of the invention; the twin-screw expansion dryer used was modified as follows: the cylinder is provided with a hole as an injection port of a conveying medium, high-purity high-pressure nitrogen is adopted as the conveying medium, the purity of the high-purity high-pressure nitrogen is 99.99 wt%, and the pressure is controlled to be 70bar through a pressure reducing valve.
Example 1
The process flow diagram of the post-treatment method for producing butyl rubber provided by the embodiment 1 of the invention is shown in figure 1; the specific process is as follows:
(1) the colloidal particle water firstly enters a vibrating screen for primary dehydration, the rotating speed of a motor of the vibrating screen is 1000r/min, the amplitude is 6.5mm, most of free water can be removed, and the water content of the colloidal particle water is reduced to 45% -55%; the vibrating screen and the feeding valve are interlocked, and the motor can excite the alarm interlock to stop feeding after stopping; when abnormal belt materials are stopped, firstly cleaning the accumulated glue on the surface, then starting the vibrating screen, and when the accumulated glue on the screen plate is cleaned, the vibrating screen cannot be operated brutally so as to avoid damaging the screen plate.
(2) The rubber material from the vibrating screen enters an extrusion dehydrator, the temperature is set to be 100-110 ℃, the pressure is set to be 32-33 bar, the water in the rubber material is extruded out by a mechanical extrusion mode and is discharged from a gap on a cylinder body, and the water content of the rubber material is reduced to 8-12%.
(3) The rubber material from the extrusion dehydrator enters a pre-expansion dryer, the temperature is set to be 100-120 ℃, the pressure is 26-28 bar, and the water content of the rubber material treated by the pre-expansion dryer is 5-7%.
(4) Feeding the rubber material from the pre-expansion dryer into a double-screw expansion dryer, setting the rotating speed of screws at 150r/min, the temperature at 110-120 ℃ and the pressure at 60-65 bar, and further dehydrating and drying; then the sizing material is cut by a rotary cutter with the rotating speed of 3000r/min, the pressure of the cut sizing material is instantly reduced to the normal pressure from 60bar, the sizing material is exploded into discontinuous and adhesive popcorn shape, more micro pore channels are formed on the surface of the sizing material, and the water is evaporated, so that the water content of the sizing material is reduced to 0.5-1%.
(5) And continuously drying and cooling the rubber material from the rotary cutter through a fluidized bed, wherein the rotating speed of a motor of the fluidized bed is 450r/min, the amplitude is 16mm, drying is carried out in three sections, the drying temperatures are 85 ℃, 85 ℃ and 45 ℃ respectively, heat is supplied from three air blowers to heat air to reach a set temperature, and the rubber material starts to be dried through holes in the fluidized bed, so that the water content of the rubber material is reduced to be below 0.3%.
(6) The loose rubber material is conveyed to a briquetting machine from a material distribution conveyor and a briquetting and feeding machine through a fluidized bed, the pressure of a main cylinder of the briquetting machine is 175bar, the pressure of a side cylinder is 100bar, and the loose rubber material is pressed into rubber blocks of 680mm multiplied by 340mm multiplied by 140mm through the briquetting machine.
(7) And finally, packaging the rubber blocks by a film packaging machine, boxing by a manipulator and selling the rubber bags.
Comparative example
The twin-screw expansion dryer used was not modified: an air compressor is adopted to provide air delivery, the rubber material from the double-screw expansion dryer is directly blown to the fluidized bed, the outlet temperature of the air compressor is 80-100 ℃, the pressure is 1-2 bar, and the flow of the air delivery is 16m3/min～20m3/min。
The specific process of the sizing material before entering the twin-screw expansion dryer is the same as that of the example 1; then, the rubber material from the pre-expansion dryer enters a double-screw expansion dryer, the rotating speed of a screw is set to be 150r/min, the temperature is set to be 150 ℃, the pressure is set to be 60-65 bar, and further dehydration and drying are carried out; then the rubber material is flashed by a rotary cutter with the rotating speed of 3000r/min, the rubber material is expanded into porous rubber particles, moisture is gasified rapidly, and partial moisture is taken away by utilizing conveying gas, so that the water content in the rubber material is reduced to 1% -2%.
And continuously drying and cooling the rubber material from the rotary cutter through a fluidized bed, wherein the rotating speed of a motor of the fluidized bed is 450r/min, the amplitude is 16mm, drying is carried out in three sections, the drying temperatures are 115 ℃, 115 ℃ and 70-85 ℃ respectively, heat is supplied from three air blowers to heat air to reach a set temperature, and the rubber material is dried through holes in the fluidized bed to reduce the water content of the rubber material to be below 0.3%.
The specific procedure was then the same as in example 1.
Comparing the example 1 with the comparative example, it can be known that the temperature of the rubber material is reduced from 70-85 ℃ to 50-65 ℃, the output of the fluidized bed plasticized rubber in the example 1 is only 180 kg/day, the comparative example is 540 kg/day, the output of the fluidized bed plasticized rubber is reduced by two thirds, and the qualification rate of the product is improved; after the drying temperature of the three sections of the fluidized bed is correspondingly reduced, the required air supply amount is reduced, and the energy consumption is reduced; after the temperature of the off-line rubber block is reduced, the risk of mucosa of the product in the processes of storage and use by downstream users can be reduced; the risk of color change of the product caused by high off-line temperature is reduced; meanwhile, the average volatile content of the product in example 1 is 0.15%, and the premium rate of volatile components is 95%, while the average volatile content of the product in the comparative example is 0.30%, and the premium rate of volatile components is 83%; in addition, compared with the comparative example, the load of the production line is increased, the capacity can be increased by 10%, the raw material cost is reduced in a phase change manner, and the product profit is increased in the embodiment 1.
Furthermore, the drying temperature of the size was significantly reduced in example 1 compared to the comparative example, the steam consumption of the twin-screw expansion dryer being 50kg/h in example 1 and 200kg/h in the comparative example.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (6)
1. A post-treatment method for producing butyl rubber comprises the following steps:
a) sequentially carrying out vibration dehydration, extrusion dehydration and pre-expansion drying on the colloidal particle water to obtain a treated rubber material; the vibration dehydration is carried out by adopting a vibration sieve, so that the water content of the colloidal particle water is reduced to 45-55 percent; the rotating speed of a motor of the vibrating screen is 800 r/min-1200 r/min, and the amplitude is 5.5 mm-7.5 mm;
the extrusion dehydration is carried out by adopting an extrusion dehydrator, so that the water content of the rubber material is reduced to 8-12%; the operating temperature of the extrusion dehydrator is 80-130 ℃, and the pressure is 30-35 bar;
the pre-expansion drying is carried out by adopting a pre-expansion dryer, so that the water content of the sizing material is 5-7%; the operation temperature of the pre-expansion dryer is 80-140 ℃, and the pressure is 16-38 bar;
b) dehydrating and drying the treated rubber material obtained in the step a) by adopting a double-screw expansion dryer at the temperature of 100-130 ℃ and the pressure of 15-110 bar, and performing three-stage drying and cooling in a fluidized bed after flash evaporation to obtain the rubber material with the water content of less than 0.3%; the double-screw expansion dryer adopts high-pressure inert gas as a conveying medium; the temperature of the three-section drying and cooling is respectively 80-90 ℃, 80-90 ℃ and 40-55 ℃;
c) briquetting and packaging the sizing material with the water content of less than 0.3% obtained in the step b) to obtain a butyl rubber product.
2. The post-treatment method according to claim 1, wherein the water content of the crumb water in step a) is 95% to 97%.
3. The post-treatment process according to claim 1, characterized in that the high-pressure inert gas in step b) is air, nitrogen or carbon dioxide gas at a pressure of 50 to 80 bar; wherein the purity of the nitrogen is more than or equal to 99.9 wt%.
4. The post-treatment method according to claim 1, wherein the flash evaporation in step b) is carried out by:
the dehydrated and dried rubber material is cut by a rotary cutter with the rotating speed of 300 r/min-3500 r/min, the pressure is instantly reduced to normal pressure, the rubber material is exploded into discontinuous and adhesive popcorn shape, more micro pore channels are formed on the surface, the water is evaporated, and the water content of the rubber material is reduced to 0.5% -1%.
5. The post-treatment method according to claim 1, wherein the fluidized bed in step b) has a motor speed of 400r/min to 500r/min and an amplitude of 12mm to 20 mm.
6. The post-treatment method according to claim 1, wherein the briquetting in step c) is performed using a briquetting machine; the main cylinder pressure of the briquetting machine is 0-350 bar, and the side cylinder pressure is 0-200 bar.
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