Efficient petroleum resin polymerization system
By optimizing the reactor design of the petroleum resin polymerization system and adopting a self-circulating system of external circulation pumps and heat exchangers, the problems of low heat transfer efficiency and unrecovered energy were solved, achieving efficient petroleum resin production, reducing energy consumption and improving product quality.
Patent Information
- Application Number
- CN202520302812.5
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2025-02-25
- Publication Date
- 2026-02-24
- Estimated Expiration
- 2035-02-25
AI Technical Summary
Existing petroleum resin polymerization systems suffer from problems such as low heat transfer coefficient, lack of energy recovery and utilization, large number of reactors, uneven mixing, and high energy consumption.
Two vertical reactors with agitators are used, and self-circulation is achieved through an external circulation pump and inlet/outlet heat exchangers. Combined with a safety cooler and temperature sensor, the reactor design is optimized to improve heat transfer efficiency and mixing uniformity, and to achieve energy recovery.
The number of reactors was reduced, heat transfer efficiency was improved, the area of cooling equipment was reduced, energy recovery and utilization were achieved, product yield was increased, and energy consumption was reduced.
Smart Images
Figure CN223931395U_ABST
Abstract
Description
Technical Field
[0001] This utility model mainly relates to the technical field of new petroleum resin materials, specifically a high-efficiency petroleum resin polymerization system. Background Technology
[0002] DCPD petroleum resin (oligomers with a molecular weight of 1000-3000) is widely used in paints, adhesives and other products to enhance product adhesion.
[0003] The polymerization of DCPD petroleum resin does not require any catalyst and takes place in a liquid solvent. The polymerization is exothermic and thermally initiated. The initial reaction temperature is typically 70℃. Higher temperatures result in a faster reaction rate. Exceeding a certain temperature limit leads to reverse addition polymerization, causing polymer decomposition, generating large amounts of gas, and causing reactor overpressure. To prevent self-polymerization and solidification of the raw materials, the raw material temperature is generally controlled between 25-40℃. The DCPD petroleum resin polymerization process is short, but the polymerization temperature is high and complex to control. The initial stage involves heating, the middle stage involves cooling and isothermal control (250-280℃), and the final stage involves cooling and discharging. Key parameters such as the softening point of DCPD petroleum resin and the content of liquid resin in byproducts are closely related to the reaction process. Temperature control is a crucial consideration in the design of the reaction system.
[0004] In existing technologies, petroleum resin polymerization systems typically use a standard vertical reactor with an agitator. Different companies have made corresponding improvements based on this. These include: jacketed external heating or cooling, semi-circular tube heating or cooling, external coil heating or cooling, internal coil heating or cooling, feed heat exchanger heating, and discharge cooler cooling. Production capacity is increased by increasing the volume and number of reactors. The main drawbacks of existing technologies are: 1) low heat transfer coefficient; the overall heat transfer coefficient of the internal coil heater is lower than that of a shell-and-tube heat exchanger; and 2) energy is not recovered and utilized. Utility Model Content
[0005] To address the shortcomings of current technology, this utility model, combining existing technology and based on practical applications, provides a highly efficient petroleum resin polymerization system that can solve the following problems: 1. Reduce the number of reactors; 2. Maintain the flexibility of reaction production operations; 3. Improve the heat transfer coefficient and reduce the heat exchange area of cooling components; 4. Energy recovery; 5. Solve the problem of uneven mixing between the upper and lower layers of the reactor.
[0006] The technical solution of this utility model is as follows:
[0007] A high-efficiency petroleum resin polymerization system includes polymerization reactor A and polymerization reactor B. The reaction raw material pipeline is divided into two paths: one path is connected to polymerization reactor B through inlet and outlet heat exchanger A, and the other path is connected to polymerization reactor A through inlet and outlet heat exchanger B. Polymerization reactor A achieves self-circulation through external circulation pump A and inlet and outlet heat exchanger A, and a branch pipeline is set downstream of inlet and outlet heat exchanger A to connect to the reaction product pipeline. Polymerization reactor B achieves self-circulation through external circulation pump B and inlet and outlet heat exchanger B, and a branch pipeline is set downstream of inlet and outlet heat exchanger B to connect to the reaction product pipeline.
[0008] Furthermore, a safety cooler A is installed on the self-circulation pipe of the polymerization reactor A downstream of the feed heat exchanger A, and a branch pipe downstream of the feed heat exchanger A is located between the feed heat exchanger A and the safety cooler A. Similarly, a safety cooler B is installed on the self-circulation pipe of the polymerization reactor B downstream of the feed heat exchanger B, and a branch pipe downstream of the feed heat exchanger B is located between the feed heat exchanger B and the safety cooler B.
[0009] Furthermore, valves are installed upstream of both the safety cooler A and the safety cooler B, and valves are also installed downstream of both the branch pipes of the inlet / outlet heat exchanger A and the branch pipes downstream of the inlet / outlet heat exchanger B.
[0010] Furthermore, temperature sensors are installed on the self-circulation pipes of both polymerization reactor A and polymerization reactor B.
[0011] Furthermore, the outlet of the self-circulating pipe of the polymerization reactor A is located at the bottom of the polymerization reactor A, and the inlet is located at the top of the polymerization reactor A; the outlet of the self-circulating pipe of the polymerization reactor B is located at the bottom of the polymerization reactor B, and the inlet is located at the top of the polymerization reactor B.
[0012] Furthermore, both polymerization reactor A and polymerization reactor B are vertical reactors equipped with agitators, and both have external tracing pipes and internal coils.
[0013] The beneficial effects of this utility model are:
[0014] 1. This utility model uses two polymerization reactors, one for reaction and one for discharge. Both reactors can operate continuously while one is under maintenance, or a single reactor can operate at half load. This system uses external circulation for heat extraction, resulting in a high heat transfer coefficient. This reduces the heat exchange area of the heat exchange equipment, which in turn reduces resin adhesion to the walls. Some companies install multiple sets of internal coils in the reactor to increase the heating rate of the internal coils. However, this increases the effective volume of the reactor due to the large number of internal coils, which also increases resin adhesion to the walls. Currently, many devices use multi-reactor operation, with more than 6 reactors. This system has fewer reactors, which reduces potential leaks and promotes safer production.
[0015] 2. Most existing production equipment uses feed heaters or internal coils for heating, and most of them are batch reactions without heat recovery. This system uses alternating reactions in A and B reactors, with hot and cold exchange, to reduce energy consumption.
[0016] 3. In traditional reactors, the agitator blades are arranged in 2-4 layers according to the length of the reactor cylinder. The agitator can make the materials in the same layer highly mixed, but the materials between the upper and lower layers are not easy to mix. The density of the reaction product is greater than that of the solvent, and the product tends to accumulate in the lower layer. This system uses an external circulation pump to circulate the bottom material to the top layer, which makes it easier for the reaction materials to mix evenly, narrows the molecular weight distribution of the reaction products, increases the resin product yield, and reduces the proportion of liquid resin by-product. Attached Figure Description
[0017] Appendix Figure 1 This is a flowchart of the system.
[0018] Appendix Figure 2 This is a schematic diagram of the temperature change during the reaction process of this system.
[0019] The labels shown in the attached diagram are as follows: 1. Polymerization reactor A; 2. Polymerization reactor B; 3. Feed and discharge heat exchanger A; 4. Feed and discharge heat exchanger B; 5. External circulation pump A; 6. External circulation pump B; 7. Security cooler A; 8. Security cooler B. Detailed Implementation
[0020] The present invention will be further described in conjunction with the accompanying drawings and specific embodiments. It should be understood that these embodiments are for illustrative purposes only and are not intended to limit the scope of the present invention. Furthermore, it should be understood that after reading the teachings of this invention, those skilled in the art can make various alterations or modifications to the present invention, and these equivalent forms also fall within the scope defined in this application.
[0021] This embodiment provides a highly efficient petroleum resin polymerization system. This system is a novel reaction system that uses C9 (mainly composed of DCPD), a byproduct of the petrochemical industry, as a raw material to produce DCPD petroleum resin.
[0022] This reaction system design uses a capacity of 30,000 tons / year of DCPD petroleum resin as an example. The reaction system is designed with two 100m³ units. 3 The vertical reactor with a stirrer retains the basic functions of external tracing pipes and internal coils (for safety requirements). The system design adds an external circulation pump (which also serves as a feed pump), inlet and outlet heat exchangers, and a safety cooler.
[0023] System principle as follows Figure 1As shown. Specifically, it includes polymerization reactor A1 and polymerization reactor B2. The reaction raw material pipeline is divided into two paths: one path is connected to polymerization reactor B2 through inlet / outlet heat exchanger A3, and the other path is connected to polymerization reactor A1 through inlet / outlet heat exchanger B4. The bottom outlet of polymerization reactor A1 is connected to the top inlet through external circulation pump A5, inlet / outlet heat exchanger A3, and safety cooler A7 to achieve self-circulation. A branch pipeline is set between inlet / outlet heat exchanger A3 and safety cooler A7 to connect to the reaction product pipeline. The bottom outlet of polymerization reactor B2 is connected to the top inlet through external circulation pump B6, inlet / outlet heat exchanger B4, and safety cooler B8 to achieve self-circulation. A branch pipeline is set between inlet / outlet heat exchanger B4 and safety cooler B8 to connect to the reaction product pipeline.
[0024] During operation, the reactants are first added to one reactor, and the reaction is initiated by heating through an external heating pipe. During the exothermic reaction and subsequent cooling phases, the material in polymerization reactor A1 is extracted, cooled, and then returned to reactor A1 from the top. This increases the mixing degree of the material within the reactor and removes the heat of reaction. At this point, the reactants are preheated through corresponding inlet and outlet heat exchangers before entering polymerization reactor B2, where they begin a slow reaction after preheating. A corresponding safety cooler is installed downstream of the inlet and outlet heat exchangers to remove excess heat or for use during maintenance of polymerization reactor B.
[0025] Existing production facilities mostly use feed heaters or internal coils for heating, and are primarily batch reactions without heat recovery. This proposed solution uses alternating polymerization reactors A1 and B2, with heat exchange to reduce energy consumption. Temperature changes during the reaction process are shown in [see figure]. Figure 2 .
[0026] In traditional reaction systems, the heat transfer coefficient is low, and the overall heat transfer coefficient of the internal coil heater is smaller compared to that of the shell-and-tube heat exchanger. Taking water-to-water as an example, the comparison of the overall heat transfer coefficients of the internal coil and shell-and-tube heat exchangers is shown in Table 1.
[0027] Table 1 Comparison of Overall Heat Transfer Coefficients
[0028] heating cool down Overall heat transfer coefficient <![CDATA[W / (m 2 ·K)]]> <![CDATA[W / (m 2 ·K)]]> Inner coil 372~535 848~1557 Shell and tube heat exchangers 1395~2836 1162~3951 .
[0029] The technical solution provided in this embodiment includes inlet and outlet cooling. The design utilizes the heat released during the stable reaction (280℃) and the cooling to 220℃ for preheating the feed. The design preheats to 150℃, and the reaction releases heat to 250℃, after which external heat extraction is required. One batch lasts 8 hours, with the constant temperature reaction time maintained for approximately 2 hours and the feeding time for approximately 2 hours.
[0030] Table 2 Energy Recovery Table
[0031] .
[0032] Table 2 shows the energy recovery table corresponding to this technical solution. It has been verified that the heat release exceeds the heat absorption. This solution is designed to recover 17600 MJ of heat, saving both heat and cold sources. Adding an external circulation pump will consume approximately 200 MJ of electricity per batch. Each batch saves 17400 MJ of energy, which is estimated to save about 20 kg of standard oil per ton of resin product. Reduced energy consumption can reduce carbon emissions, which is beneficial to environmental protection.
Claims
1. A high-efficiency petroleum resin polymerization system, characterized in that, The reactor includes polymerization reactor A and polymerization reactor B. The raw material pipeline is divided into two paths: one path is connected to polymerization reactor B through inlet and outlet heat exchanger A, and the other path is connected to polymerization reactor A through inlet and outlet heat exchanger B. Polymerization reactor A achieves self-circulation through external circulation pump A and inlet and outlet heat exchanger A, and a branch pipeline is set downstream of inlet and outlet heat exchanger A to connect to the reaction product pipeline. Polymerization reactor B achieves self-circulation through external circulation pump B and inlet and outlet heat exchanger B, and a branch pipeline is set downstream of inlet and outlet heat exchanger B to connect to the reaction product pipeline.
2. The high-efficiency petroleum resin polymerization system according to claim 1, characterized in that, A safety cooler A is installed on the self-circulation pipe of polymerization reactor A downstream of feed heat exchanger A. A branch pipe downstream of feed heat exchanger A is located between feed heat exchanger A and safety cooler A. A safety cooler B is installed on the self-circulation pipe of polymerization reactor B downstream of feed heat exchanger B. A branch pipe downstream of feed heat exchanger B is located between feed heat exchanger B and safety cooler B.
3. The high-efficiency petroleum resin polymerization system according to claim 2, characterized in that, Valves are installed upstream of both the safety cooler A and the safety cooler B, and valves are also installed downstream of both the branch pipes of the inlet / outlet heat exchanger A and the branch pipes downstream of the inlet / outlet heat exchanger B.
4. The high-efficiency petroleum resin polymerization system according to claim 1, characterized in that, Temperature sensors are installed on the self-circulation pipes of both polymerization reactor A and polymerization reactor B.
5. The high-efficiency petroleum resin polymerization system according to claim 1, characterized in that, The outlet of the self-circulating pipe of polymerization reactor A is located at the bottom of polymerization reactor A, and the inlet is located at the top of polymerization reactor A. The outlet of the self-circulating pipe of polymerization reactor B is located at the bottom of polymerization reactor B, and the inlet is located at the top of polymerization reactor B.
6. The high-efficiency petroleum resin polymerization system according to claim 1, characterized in that, Both polymerization reactor A and polymerization reactor B are vertical reactors equipped with agitators, and both have external tracing pipes and internal coils.