CN111253559A - Unsaturated resin pressurization production process - Google Patents
Unsaturated resin pressurization production process Download PDFInfo
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- CN111253559A CN111253559A CN202010170534.4A CN202010170534A CN111253559A CN 111253559 A CN111253559 A CN 111253559A CN 202010170534 A CN202010170534 A CN 202010170534A CN 111253559 A CN111253559 A CN 111253559A
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- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/66—Polyesters containing oxygen in the form of ether groups
- C08G63/668—Polyesters containing oxygen in the form of ether groups derived from polycarboxylic acids and polyhydroxy compounds
- C08G63/676—Polyesters containing oxygen in the form of ether groups derived from polycarboxylic acids and polyhydroxy compounds in which at least one of the two components contains aliphatic unsaturation
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Abstract
The invention relates to an unsaturated resin pressurized production process; the method is characterized in that: the method comprises the following steps: step 1, performing an air tightness experiment; step 2, feeding and stirring; feeding materials into the stirring device; the stirring device is used for stirring the materials; step 3, supplying gas; and 4, step 4: heating the material for the first time; and 5: the material is discharged for the first time; step 6: controlling the condenser temperature, step 7: heating the material for the second time; and 8: the material is discharged for the second time; and step 9: and (5) deflating and sampling. The problems that the existing scheme does not directly heat and stir materials, the materials are not protected, fire and explosion accidents are easy to happen, the heating temperature range is large, water cannot be completely discharged, the quality of the reaction process is not thoroughly reduced due to the water residue, the material reaction time is long due to the large heating temperature range, the unsaturated resin production efficiency is reduced, and the like are solved.
Description
Technical Field
The invention relates to a resin production process, in particular to an unsaturated resin pressurization production process.
Background
In general, an unsaturated resin is a polymer compound containing an unsaturated double bond, which is produced by a polycondensation reaction of a dibasic acid and a diol. The unsaturated resin has strong heat resistance, the heat distortion temperature of most unsaturated resins is 50-60 ℃, and the heat distortion temperature of some unsaturated resins with strong heat resistance can reach 120 ℃. The unsaturated resin has good mechanical property and high tensile, bending and compression strength. The unsaturated resin has high chemical corrosion resistance and good water resistance, dilute acid, dilute alkali resistance and the like.
The product quality of the existing domestic unsaturated resin is not high, mainly caused by incomplete reaction of materials, and the moisture in the reaction of the materials cannot be completely discharged. How to solve this problem becomes crucial.
The existing scheme is that the material is put into a reaction kettle and heated to 160-210 ℃ for reaction to obtain the product. Such a solution has the following problems: (1) the heating and stirring are directly carried out, the material reaction is not protected, and fire and explosion accidents are easy to happen; (2) the heating temperature range is large, the water cannot be completely discharged, and water residue is generated, so that the reaction process is incomplete, and the quality is reduced; (3) the heating temperature range is large, so that the reaction time of the materials is long, and the production efficiency of the unsaturated resin is reduced.
Disclosure of Invention
Aiming at the defects of the prior art, the invention discloses an unsaturated resin pressurization production process, which aims to solve the problems that in the prior art, direct heating and stirring are not carried out, the material reaction is protected, fire and explosion accidents are easy to happen, the moisture cannot be completely discharged due to a large heating temperature range, the moisture residue is generated, the quality is not completely reduced in the reaction process, the material reaction time is long due to a large heating temperature range, the unsaturated resin production efficiency is reduced, and the like.
The technical scheme adopted by the invention is as follows:
an unsaturated resin pressurized production process comprises the following steps:
step 1, performing an air tightness experiment;
step 2, feeding and stirring; feeding materials into the stirring device; the stirring device is used for stirring the materials;
step 3, supplying gas; pressurizing and supplying air in the stirring device; adding nitrogen into the stirring device; when the pressure in the stirring device reaches 0.16-0.24 Mpa, the nitrogen gasAccording to the ratio of 0.8-2.2 m3H, supplying gas into the stirring device;
and 4, step 4: heating the material for the first time; heating the material in the stirring device; the temperature rise speed of the material is 1.5-3 ℃/Min, and the material is heated to 200-210 ℃;
and 5: the material is discharged for the first time; the materials are subjected to heat preservation reaction to produce water; the heat preservation time is 25-40 Min; judging whether the material is discharged with water or not; if the material is discharged: carrying out step 6; if the material does not produce water: heating the material at a speed of 1-2.5 ℃/Min, and performing step 6 after the material is discharged;
step 6: controlling the temperature of a condenser, wherein the temperature of the condenser is controlled to be 125-140 ℃;
and 7: heating the material for the second time; the heating speed is 0.1-0.5 ℃/Min, and the material is heated to 225-245 ℃; the nitrogen is in a range of 3-5 m3H, supplying gas into the stirring device;
and 8: the material is discharged for the second time; the materials are subjected to heat preservation reaction to produce water; the heat preservation time is 25-40 Min; judging the water yield of the material; when the water yield of the materials is more than 4.5 percent of the total amount of the materials, performing step 9; when the water yield of the materials is less than 4.5 percent of the total amount of the materials, heating the materials; heating at a speed of 0.1-0.5 ℃/Min, heating the material to 235-255 ℃, and performing step 9 when the water yield of the material is more than 4.5% of the total amount of the material;
and step 9: air bleeding and sampling; the stirring device is internally provided with a stirring device according to the length of 3-5 m3Pressure relief and air release are carried out; the nitrogen gas was completely discharged and then sampled.
The further technical scheme is as follows: the weight percentages of the chemical elements in the material are as follows: terephthalic acid: 10-18%, isophthalic acid: 6-14%, cis-butenedioic acid rod: 27-35%, diethylene glycol: 22-30%, propylene glycol: 15-23%.
The further technical scheme is as follows: the step 1 specifically comprises: the stirring device is in a closed state; adding nitrogen into the stirring device; when the pressure in the stirring device reaches 0.15-0.25 Mpa, keeping 40 Min; the pressure in the stirring device does not drop.
The further technical scheme is as follows: the stirring device is communicated with the condenser; and a heating pipe for circulating hot oil is arranged in the stirring device.
The further technical scheme is as follows: the stirring device is a reaction kettle.
The further technical scheme is as follows: in the step 5, if the material does not produce water: the temperature of the material is less than 240 ℃.
The further technical scheme is as follows: in the step 8, when the water yield of the material is less than 4.5 percent of the total amount of the material, heating the material; the heating speed is 0.1-0.5 ℃/Min, the material is heated to 235-255 ℃, and when the water yield of the material is more than 4.5% of the total amount of the material, the process of the step 9 is carried out; the process is completed within 3-4.5 h.
The further technical scheme is as follows: in the step 9, the process of pressure relief and air release is carried out; the process is completed within 1-2 h.
The invention has the following beneficial effects: the invention designs an unsaturated resin pressurized production process which adopts nitrogen gas to produce materials. And the materials are heated twice, so that the materials are ensured not to have residual moisture. The unsaturated resin pressurized production process brings the following effects: (1) nitrogen is filled in the stirring device, and the materials react under the protection of inert gas, so that fire and explosion accidents can not happen; (2) the temperature is accurately controlled and nitrogen is filled, so that the material reaction time is shortened, and the production efficiency of unsaturated resin is improved; (3) through twice heating processes, the moisture of the material can be completely discharged, and the moisture residue is avoided.
Drawings
FIG. 1 is a flow chart of the present invention.
Detailed Description
FIG. 1 is a flow chart of the present invention. As shown in fig. 1, the production process of the present invention comprises the following steps:
step 1, air tightness experiment.
The step 1 specifically comprises the following steps: the stirring device is in a closed state; adding nitrogen into the stirring device; when the pressure in the stirring device reaches 0.15-0.25 Mpa, keeping 40 Min; the pressure in the stirring device does not drop.
Before the unsaturated resin is pressurized and produced, the stirring device is pressurized and aerated. The unsaturated resin pressurized production process is carried out in a pressurized environment, and the tightness of a stirring device is required to be ensured. When the unsaturated resin is pressurized to produce, the chemical reaction of the materials is violent. The stirring device with strong sealing performance can ensure the stable operation of the production process.
And 2, feeding and stirring. The materials are put into the stirring device. The stirring device stirs the materials.
Preferably, the stirring device is a reaction kettle. The weight percentages of the chemical elements in the material are as follows: terephthalic acid: 10-18%, isophthalic acid: 6-14%, cis-butenedioic acid rod: 27-35%, diethylene glycol: 22-30%, propylene glycol: 15-23%.
The materials of all the components are put into the stirring device from the feeding port of the stirring device according to the proportion. The materials are stirred by the reaction kettle, so that the materials can be uniformly stirred and fully reacted. The reaction kettle is a closed container, and can still keep better sealing property when the materials react violently.
And step 3, supplying gas. The stirring device is internally pressurized for air supply. Nitrogen was added to the stirring apparatus. When the pressure in the stirring device reaches 0.16-0.24 Mpa, the nitrogen is 0.8-2.2 m3And h, supplying gas into the stirring device.
The nitrogen is inert gas, and inert protection is formed in the stirring device. When the nitrogen is filled into the stirring device, the oxygen in the stirring device is discharged, so that explosive mixtures are avoided, and fire and explosion accidents are effectively avoided. When the stirring device stirs the material, nitrogen forms the effect of air current stirring to the material. The materials react in the environment of nitrogen protection, so that the moisture removal can be accelerated and the reaction rate can be improved.
And 4, step 4: the material is heated for the first time. And heating the materials in the stirring device. The material heating speed is 1.5-3 ℃/Min, and the material is heated to 200-210 ℃.
The stirring device is communicated with the condenser. A heating pipe for circulating hot oil is arranged in the stirring device.
A heating pipe is arranged in the stirring device. When the materials in the stirring device need to be heated, hot oil flows in the heating pipe. The heating pipe can be used for stably heating the materials. When the temperature rise speed of the material is too high, the material is heated unevenly. When the temperature rise speed of the materials is too slow, the reaction speed of the materials is seriously influenced. The temperature rise speed is 1.5-3 ℃/Min, so that the material can be rapidly heated up and uniformly heated. When the temperature of the material is raised to 200-210 ℃, the material begins to discharge water.
And 5: and discharging water from the material for the second time. The materials are subjected to heat preservation reaction to obtain water. The heat preservation time is 25-40 Min. And judging whether the material is yielding water or not. If the materials are discharged: step 6 is performed. If the materials do not produce water: and (3) heating the materials at the speed of 1-2.5 ℃/Min, and performing step 6 after the materials are discharged.
In step 5, if the material does not produce water: the temperature of material heating is less than 240 ℃.
And step 5, performing heat preservation on the material to discharge water. The material is in the water process that goes out, need keep the temperature of material for the material thermally equivalent, the material begins to go out water continuously. According to different chemical element compositions of the materials, the temperature of the effluent water can have slight difference. And if the material does not produce water, slowly heating the material. In order to prevent the materials from being overheated in the first water outlet, the temperature of the temperature rise of the materials is less than 240 ℃. The first water outlet of the material is ensured through the step 5.
Step 6: controlling the temperature of the condenser at 125-140 ℃.
Water and materials are separated in the condenser, the temperature of the condenser is controlled to be 125-140 ℃, and the evaporation of the materials in the condenser can be prevented.
And 7: and (4) heating the material for the second time. The heating speed is 0.1-0.5 ℃/Min, and the material is heated to 225-245 ℃. Nitrogen according to the length of 3-5 m3And h, supplying gas into the stirring device.
And step 7 is a heating step before the material is discharged for the second time. The heating speed of the material is less than the temperature rise speed of the material in the step 4. At this time, the temperature of the material is high, the reaction inside the material is violent, and rapid heating should not be performed. Through slow heating, make the material inside be heated evenly, the inside chemical reaction of material is complete.
By increasing the nitrogen supply, the chemical reaction in the material is violent after the temperature is raised, and the nitrogen provides inert protection. After the materials are discharged for the first time, the liquid level of the materials in the stirring device is reduced. The stirring device can be quickly filled by increasing the gas supply amount of nitrogen, so that oxygen is prevented from entering the stirring device. Effectively avoiding the occurrence of fire and explosion accidents.
And 8: and discharging water from the material for the second time. The materials are subjected to heat preservation reaction to obtain water. The heat preservation time is 25-40 Min. And (5) judging the water yield of the material. And (5) when the water yield of the materials is more than 4.5 percent of the total amount of the materials, performing the step 9. When the water yield of the materials is less than 4.5 percent of the total amount of the materials, the materials are heated. The heating speed is 0.1-0.5 ℃/Min, the material is heated to 235-255 ℃, and when the water yield of the material is more than 4.5% of the total amount of the material, the step 9 is carried out.
In step 8, when the water yield of the material is less than 4.5% of the total amount of the material, heating the material. The heating speed is 0.1-0.5 ℃/Min, the material is heated to 235-255 ℃, and when the water yield of the material is more than 4.5% of the total amount of the material, the process of the step 9 is carried out. The process is completed within 3-4.5 h.
And step 8, performing heat preservation and water outlet on the materials. The material is in the water process that goes out, need keep the temperature of material for the material thermally equivalent, the material begins to go out water continuously. According to different chemical element compositions of the materials, the temperature of the effluent water can have slight difference. And if the material does not produce water, slowly heating the material. The moisture in the material can be completely discharged through the step 8. The second water outlet of the material is ensured through step 8.
Too short effluent reaction time in the step 8 can cause incomplete effluent reaction of materials and residual moisture in the materials. The effluent reaction time of the step 8 is too long, which can cause the reaction efficiency of effluent of materials to be low. By controlling the completion time of the production steps, the production time can be shortened, and the production efficiency is improved.
And step 9: and (5) deflating and sampling. 3-5 m inside the stirring device3And/h, pressure relief and air release are carried out. Complete discharge of nitrogenAnd sampling after the sampling.
And 9, pressure relief and air release. The process is completed within 1-2 h.
And after the material is subjected to secondary water outlet, finishing the water outlet reaction of the material. When sampling, the nitrogen gas in the stirring apparatus must be completely discharged, and then sampling is performed. Through accomplishing the gassing process at 1 ~ 1h, avoid the residue of nitrogen gas for nitrogen gas can discharge completely.
The production process according to the invention is illustrated below by means of three examples:
example 1:
step 1, air tightness experiment. The step 1 specifically comprises the following steps: the stirring device is in a closed state. Nitrogen was added to the stirring apparatus. When the pressure in the stirring device reaches 0.15Mpa, keeping 40 Min; the pressure in the stirring device does not drop.
And 2, feeding and stirring. The materials are put into the stirring device. The stirring device stirs the materials.
And step 3, supplying gas. The stirring device is internally pressurized for air supply. Nitrogen was added to the stirring apparatus. When the pressure in the stirring device reaches 0.16Mpa, the nitrogen is in a range of 0.8m3H, supplying gas into the stirring device;
and 4, step 4: the material is heated for the first time. And heating the materials in the stirring device. The material temperature rise rate is 1.5 ℃/Min, and the material is heated to 200 ℃.
And 5: the first effluent of the material is subjected to heat preservation reaction to produce water. The incubation time was 25 Min. And (5) discharging water from the material, and performing the step 6.
Step 6: the condenser temperature was controlled at 125 ℃.
And 7: and (4) heating the material for the second time. The heating rate was 0.1 ℃/Min and the batch was heated to 225 ℃. Nitrogen according to 3m3And h, supplying gas into the stirring device.
And 8: the material is discharged for the second time, and the material is subjected to heat preservation reaction to discharge water. The incubation time was 25 Min. And when the water yield of the materials is 5 percent of the total amount of the materials, performing the step 9.
In the specific step 8, when the water yield of the material is 5% of the total amount of the material, the step 9 is performed. The process was completed in 3 h.
And step 9: and (5) deflating and sampling. The inner part of the stirring device is 3m3And/h, pressure relief and air release are carried out. The nitrogen gas was completely discharged and then sampled.
Specifically, in step 9, the process of pressure relief and air release. The process was completed in 1 h.
In example 1. The weight percentage of each chemical element in the material is shown in table 1.
| Terephthalic acid (TPA) | Isophthalic acid | Cis-nailing enedioic acid rod | Diethylene glycol | Propylene glycol |
| 10％ | 7％ | 33％ | 27％ | 23％ |
Example 2:
step 1, air tightness experiment. The step 1 specifically comprises the following steps: the stirring device is in a closed state. Nitrogen was added to the stirring apparatus. When the pressure in the stirring device reaches 0.25Mpa, keeping 40 Min; the pressure in the stirring device does not drop.
And 2, feeding and stirring. The materials are put into the stirring device. The stirring device stirs the materials.
And step 3, supplying gas. The stirring device is internally pressurized for air supply. Adding into a stirring deviceNitrogen gas. When the pressure in the stirring device reaches 0.24Mpa, the nitrogen is 2.2m3H, supplying gas into the stirring device;
and 4, step 4: the material is heated for the first time. And heating the materials in the stirring device. The material heating rate is 3 ℃/Min, and the material is heated to 210 ℃.
And 5: the material is discharged water for the first time. The materials are subjected to heat preservation reaction to obtain water. The incubation time was 40 Min. And (4) the material does not go out of water, the temperature of the material is increased according to the speed of 2.5 ℃/Min, and the step 6 is carried out after the material goes out of water.
Specifically, in the step 5, water does not flow out of the material, and the temperature of the material is increased to 236 ℃.
Step 6: the condenser temperature was controlled at 140 ℃.
And 7: and (4) heating the material for the second time. The heating rate was 0.5 ℃/Min and the batch was heated to 245 ℃. Nitrogen according to 5m3And h, supplying gas into the stirring device.
And 8: the material is discharged for the second time, and the material is subjected to heat preservation reaction to discharge water. The incubation time was 40 Min. When the water yield of the material is 4 percent of the total amount of the material, the material is heated. The heating speed is 0.5 ℃/Min, the materials are heated to 255 ℃, and when the water yield of the materials is 5 percent of the total amount of the materials, the step 9 is carried out.
In the specific step 8, when the water yield of the material is 4% of the total amount of the material, the material is heated. The heating speed is 0.5 ℃/Min, the materials are heated to 255 ℃, and when the water yield of the materials is 5 percent of the total amount of the materials, the step 9 is carried out. The process was completed in 4.5 h.
And step 9: 5m inside the air discharge sampling stirring device3And/h, pressure relief and air release are carried out. The nitrogen gas was completely discharged and then sampled.
Specifically, in step 9, the process of pressure relief and air release. The process was completed in 2 h.
In example 2. The weight percentages of the components of the chemical elements in the material are shown in table 2.
| Terephthalic acid (TPA) | Isophthalic acid | Cis-nailing enedioic acid rod | Diethylene glycol | Propylene glycol |
| 18％ | 10％ | 30％ | 22％ | 20％ |
Example 3:
step 1, air tightness experiment. The step 1 specifically comprises the following steps: the stirring device is in a closed state. Nitrogen was added to the stirring apparatus. When the pressure in the stirring device reaches 0.22Mpa, keeping 40 Min; the pressure in the stirring device does not drop.
And 2, feeding and stirring. The materials are put into the stirring device. The stirring device stirs the materials.
And step 3, supplying gas. The stirring device is internally pressurized for air supply. Nitrogen was added to the stirring apparatus. When the pressure in the stirring device reaches 0.24MPa, the nitrogen pressure is 1.7m3H, supplying gas into the stirring device;
and 4, step 4: the material is heated for the first time. And heating the materials in the stirring device. The material heating rate is 2.5 ℃/Min, and the material is heated to 205 ℃.
And 5: the material is discharged water for the first time. The materials are subjected to heat preservation reaction to obtain water. The incubation time was 35 Min. And (5) discharging water from the material, and performing the step 6.
Step 6: the condenser temperature was controlled at 135 ℃.
And 7: and (4) heating the material for the second time. Heating rate is0.3 ℃/Min, the batch was heated to 240 ℃. Nitrogen according to 4.5m3And h, supplying gas into the stirring device.
And 8: and discharging water from the material for the second time. The materials are subjected to heat preservation reaction to obtain water. The incubation time was 35 Min. When the water yield of the materials is 3.5 percent of the total amount of the materials, the materials are heated. The heating speed is 0.3 ℃/Min, the materials are heated to 250 ℃, and when the water yield of the materials is 4.8 percent of the total amount of the materials, the step 9 is carried out.
In the specific step 8, when the water yield of the material is 3.5% of the total amount of the material, the material is heated. The heating speed is 0.3 ℃/Min, the materials are heated to 250 ℃, and when the water yield of the materials is 4.8 percent of the total amount of the materials, the step 9 is carried out. The process was completed in 4 h.
And step 9: and (5) deflating and sampling. The inner diameter of the stirring device is 4.5m3And/h, pressure relief and air release are carried out. The nitrogen gas was completely discharged and then sampled.
Specifically, in step 9, the process of pressure relief and air release. The process was completed in 1.8 h.
In example 3. The weight percentages of the components of the chemical elements in the material are shown in table 3.
| Terephthalic acid (TPA) | Isophthalic acid | Cis-nailing enedioic acid rod | Diethylene glycol | Propylene glycol |
| 15％ | 8％ | 32％ | 23％ | 22％ |
In the present embodiment, the stirring apparatus described is a reaction vessel, but the stirring apparatus is not limited thereto, and may be another stirring apparatus within a range capable of performing the function thereof.
In the description of the embodiments of the present invention, it should be further noted that unless otherwise explicitly stated or limited, the terms "disposed" and "connected" should be interpreted broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
The foregoing description is illustrative of the present invention and is not to be construed as limiting thereof, the scope of the invention being defined by the appended claims, which may be modified in any manner without departing from the basic structure thereof.
Claims (8)
1. The pressurized production process of unsaturated resin is characterized by comprising the following steps:
step 1, performing an air tightness experiment;
step 2, feeding and stirring; feeding materials into the stirring device; the stirring device is used for stirring the materials;
step 3, supplying gas; pressurizing and supplying air in the stirring device; adding nitrogen into the stirring device; when the pressure in the stirring device reaches 0.16-0.24 Mpa, the nitrogen is 0.8-2.2 m3H, supplying gas into the stirring device;
and 4, step 4: heating the material for the first time; heating the material in the stirring device; the temperature rise speed of the material is 1.5-3 ℃/Min, and the material is heated to 200-210 ℃;
and 5: the material is discharged for the first time; the materials are subjected to heat preservation reaction to produce water; the heat preservation time is 25-40 Min; judging whether the material is discharged with water or not; if the material is discharged: carrying out step 6; if the material does not produce water: heating the material at a speed of 1-2.5 ℃/Min, and performing step 6 after the material is discharged;
step 6: controlling the temperature of a condenser, wherein the temperature of the condenser is controlled to be 125-140 ℃;
and 7: heating the material for the second time; the heating speed is 0.1-0.5 ℃/Min, and the material is heated to 225-245 ℃; the nitrogen is in a range of 3-5 m3H, supplying gas into the stirring device;
and 8: the material is discharged for the second time; the materials are subjected to heat preservation reaction to produce water; the heat preservation time is 25-40 Min; judging the water yield of the material; when the water yield of the materials is more than 4.5 percent of the total amount of the materials, performing step 9; when the water yield of the materials is less than 4.5 percent of the total amount of the materials, heating the materials; heating at a speed of 0.1-0.5 ℃/Min, heating the material to 235-255 ℃, and performing step 9 when the water yield of the material is more than 4.5% of the total amount of the material;
and step 9: air bleeding and sampling; the stirring device is internally provided with a stirring device according to the length of 3-5 m3Pressure relief and air release are carried out; the nitrogen gas was completely discharged and then sampled.
2. The unsaturated resin press production process according to claim 1, characterized in that: the weight percentages of the chemical elements in the material are as follows: terephthalic acid: 10-18%, isophthalic acid: 6-14%, cis-butenedioic acid rod: 27-35%, diethylene glycol: 22-30%, propylene glycol: 15-23%.
3. The unsaturated resin press production process according to claim 1, characterized in that: the step 1 specifically comprises: the stirring device is in a closed state; adding nitrogen into the stirring device; when the pressure in the stirring device reaches 0.15-0.25 Mpa, keeping 40 Min; the pressure in the stirring device does not drop.
4. The unsaturated resin press production process according to claim 1, characterized in that: the stirring device is communicated with the condenser; and a heating pipe for circulating hot oil is arranged in the stirring device.
5. The unsaturated resin press production process according to claim 1, characterized in that: the stirring device is a reaction kettle.
6. The unsaturated resin press production process according to claim 1, characterized in that: in the step 5, if the material does not produce water: the temperature of the material is less than 240 ℃.
7. The unsaturated resin press production process according to claim 1, characterized in that: in the step 8, when the water yield of the material is less than 4.5 percent of the total amount of the material, heating the material; the heating speed is 0.1-0.5 ℃/Min, the material is heated to 235-255 ℃, and when the water yield of the material is more than 4.5% of the total amount of the material, the process of the step 9 is carried out; the process is completed within 3-4.5 h.
8. The unsaturated resin press production process according to claim 1, characterized in that: in the step 9, the process of pressure relief and air release is carried out; the process is completed within 1-2 h.
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| JP2005255897A (en) * | 2004-03-12 | 2005-09-22 | Hitachi Chem Co Ltd | Treating liquid for unsaturated polyester resin cured product, and treating method |
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| CN209772041U (en) * | 2019-03-29 | 2019-12-13 | 广西华砻树脂有限公司 | Reaction device for p-benzene type unsaturated polyester resin |
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2020
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|---|---|---|---|---|
| EP1125996A1 (en) * | 2000-02-09 | 2001-08-22 | Ucb, S.A. | Radiation curable powder compositions |
| JP2005255897A (en) * | 2004-03-12 | 2005-09-22 | Hitachi Chem Co Ltd | Treating liquid for unsaturated polyester resin cured product, and treating method |
| CN102603992A (en) * | 2012-03-08 | 2012-07-25 | 宜兴市兴合树脂有限公司 | Unsaturated polyester resin for pultrusion and preparation method for same |
| CN103265668A (en) * | 2013-05-21 | 2013-08-28 | 山东宏信化工股份有限公司 | Preparation method of terephthalic type unsaturated polyester resin |
| CN209772041U (en) * | 2019-03-29 | 2019-12-13 | 广西华砻树脂有限公司 | Reaction device for p-benzene type unsaturated polyester resin |
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