Production process for cutting and purifying DCPD (dicyclopentadiene) from cracked C9 raw material

Abstract

The invention belongs to the technical field of organic mixture separation, and particularly discloses a production process for cutting and purifying DCPD (dicyclopentadiene) by cracking a C9 raw material. A cracking C9 raw material is fed into a light component removal cutting tower (QL), light components such as ethylbenzene, m-xylene, o-xylene and styrene with the boiling point lower than 160 DEG C are separated out from the tower top, a mixture containing a target product and distilled out from a tower kettle is fed into a heavy component removal cutting tower (QH), components with the boiling point higher than 180 DEG C are separated out from the tower kettle, and a DCPD-rich product with high purity and yield is obtained from the tower top. Based on systematic research on boiling point difference of cracked C9 components, the invention provides a technical scheme of combining step-by-step rectification and cutting with directional separation, and aims to realize efficient enrichment of DCPD with low energy consumption and short process and provide a new path for high-valued utilization of cracked C9 raw materials.

Description

Technical Field

[0001] The invention relates to the technical field of separation of organic mixtures, and more particularly to a production process for cleaving and purifying DCPD by cracking C9 raw materials. Background Art

[0002] The ethylene industry occupies an important position in the field of petrochemicals. The production scale of ethylene directly affects the manufacturing scale of various aromatic products such as benzene, toluene, and xylene. In addition, the scale of ethylene also restricts the extension of downstream products in the chemical industry chain, so it is considered to be a key indicator for determining the production level of the chemical industry. my country's ethylene industry has developed rapidly in recent years, and its production capacity has continued to grow. The mainstream ethylene production process is to use hydrocarbon steam cracking process. In this process, the cracked C9 fraction is a by-product in the ethylene industrial production process, which accounts for about 11% to 18% of the total ethylene production. Due to its complex composition and lack of relevant technology, most domestic ethylene plants will directly burn the cracked C9 as low-grade fuel oil, releasing a large amount of CO2, which has adverse effects on the environment. In recent years, the high-quality utilization of the cracked C9 fraction has mainly focused on the production of various types of petroleum resins and solvent oils, but the deep separation and purification technology of its core component dicyclopentadiene (DCPD) still has significant bottlenecks.

[0003] Dicyclopentadiene (DCPD), as a norbornene olefin compound with endonucleic acid (Endo) and exonucleic acid (Exo) isomers, has become a key intermediate in the field of fine chemicals due to its high reactivity conferred by conjugated double bonds and methylene groups. Its purity level (68% to 99%) directly affects downstream application scenarios: low-purity DCPD can be used for polyester modification and petroleum resin synthesis; high-purity products are widely used in high value-added fields such as EPDM rubber, photocurable resins, drug synthesis and special adhesives. However, there are two contradictions in the existing processing of DCPD in cracked C9: on the one hand, DCPD residues will deteriorate the oxidative stability of C9 petroleum resins and increase the energy consumption and catalyst deactivation risk of solvent oil hydrogenation processes; on the other hand, its separation efficiency as a high-value monomer is insufficient, resulting in waste of resources.

[0004] Current DCPD purification technology mainly relies on the following processes:

[0005] (1) High temperature cracking-distillation method: The DCPD copolymer (such as CPD-MCPD) in C9 is cracked at 200-350℃ to release cyclopentadiene (CPD) monomer, which is then separated by multi-stage distillation and purified by dimerization. However, high temperature environment can easily induce side reactions, resulting in coking of equipment and excessive energy consumption.

[0006] (2) Decompression-depolymerization coupling process: After separating the light and heavy components by vacuum cutting (10 kPa), the heavy components are subjected to depolymerization distillation at 160-220 °C. Although the thermal cracking temperature is reduced, the multi-stage operation makes the process complicated, and the CPD recovery rate is limited by the depolymerization kinetics.

[0007] (3) Multi-stage distillation cutting process: Although the purity of DCPD can be improved by segmented cutting combined with depolymerization-distillation cycle purification, the process cycle is long, the equipment investment is large, and the problem of high-boiling point aromatic residues is prominent.

[0008] (4) Hydrogenation pretreatment coupling process: pre-hydrogenation of unsaturated components such as saturated styrene to reduce the risk of polymerization, but the hydrogenation catalyst is susceptible to sulfide poisoning, and the additional cost of introducing hydrogen limits the economic feasibility.

[0009] The above methods generally have problems such as lengthy process, high energy consumption, and difficulty in balancing product purity and yield.

[0010] In view of this, an innovative process for directly purifying DCPD using cracked C9 as raw material is developed. By optimizing the component cutting strategy and purification path, the existing technical bottleneck is broken, which is of great significance for achieving efficient resource conversion, reducing carbon emissions and promoting the development of high-end chemical materials. Based on a systematic study of the boiling point differences of cracked C9 components, the present invention proposes a technical solution of step-by-step distillation cutting combined with directional separation, aiming to achieve efficient enrichment of DCPD with low energy consumption and short process, and provide a new path for the high-value utilization of cracked C9 raw materials. Summary of the invention

[0011] In order to solve the problems in the prior art, the present invention proposes a production process for cleaving and purifying DCPD by cracking C9 raw materials.

[0012] The mixed system of cracking C9 raw materials contains ethylbenzene, meta-xylene, o-xylene, styrene, meta-ethylmethylbenzene, mesitylene, methyl styrene, dicyclopentadiene, n-decane, trimethylol indene, n-butylbenzene and other substances, among which the high value-added substance dicyclopentadiene (DCPD) accounts for about 10-20%, and the content of other components is relatively small, and the boiling points are also relatively close. This method cuts by boiling point, and the entire process consists of a light cutting tower and a heavy cutting tower. The final purity of the DCPD product reaches more than 58%. Its process flow is calculated by TAC and carbon emissions, and its industrial utilization value is high.

[0013] The technical solution adopted by the present invention comprises at least the following steps:

[0014] (1) The cracked C9 raw material enters the light cut tower (QL) from the middle and lower part of the tower at a flow rate of 10000-12000 kg / h;

[0015] (2) Light components with boiling points lower than 160°C, such as ethylbenzene, m-xylene, styrene, and o-xylene in the cracked C9 raw material, are withdrawn from the top of the light cut column (QL).

[0016] (3) Fractions with higher boiling points, such as DCPD in the cracked C9 raw material, are distilled from the bottom of the light cut column (QL) and enter the heavy cut column (QH).

[0017] (4) Heavy components such as indene, methylindene, n-butylbenzene, undecane, dodecane, and naphthalene flow out from the bottom of the heavy cut column (QH).

[0018] (5) The DCPD-rich fraction is withdrawn from the top of the heavy cut column (QH).

[0019] Further, the mass content of DCPD in the cracked C9 raw material in step (1) is about 10-20%.

[0020] Further, the number of theoretical plates of the light cut column (QL) is 20-40, preferably 25-35.

[0021] Further, the number of theoretical plates of the heavy cut column (QH) is 23-43, preferably 28-38.

[0022] Further, the feed position of the light cut column (QL) in step (1) is the 14th plate (counting from the top down, the topmost is the first plate).

[0023] Further, the feed position of the heavy cut column (QH) in step (3) is the 20th plate (counting from the top down, the topmost is the first plate).

[0024] Further, the operating pressure at the top of the light cut column (QL) in step (2) is 1-10 kPa, preferably 5-8 kPa; the bottom flow rate is 55%-62% of the total feed rate.

[0025] Further, the operating pressure at the top of the heavy cut column (QH) in step (3) is 1-10 kPa, preferably 5-8 kPa, and the bottom flow rate is 27%-32% of the total feed rate.

[0026] Further, the top temperature of the light cut column (QL) in step (3) is 80-90°C, and the bottom temperature is 120-130°C.

[0027] Further, the top temperature of the heavy cut column (QH) is 80-85°C, and the bottom temperature is 110-125°C.

[0028] The beneficial effects of the present invention are as follows:

[0029] Based on the systematic research on the boiling point differences of cracked C9 components, the present invention proposes a technical solution of stepwise rectification cutting combined with directional separation to achieve the efficient enrichment of DCPD with low energy consumption and short process. Under the conditions of the technical solution of the present invention, the highest purity of the obtained DCPD product can reach 58.91%, and the highest yield can reach 99.39%, providing a new path for the high-value utilization of cracked C9 raw materials.

[0030] In the ranges disclosed in the present invention, the endpoints and any values are not limited to the exact ranges or values, and these ranges or values should be understood to include values close to these ranges or values. For numerical ranges, the endpoint values of each range, between the endpoint values of each range and individual point values, and between individual point values can be combined with each other to obtain one or more new numerical ranges, and these numerical ranges should be regarded as specifically disclosed herein. In the following text, in principle, the various technical solutions can be combined with each other to obtain new technical solutions, which should also be regarded as specifically disclosed herein. BRIEF DESCRIPTION OF THE DRAWINGS

[0031] Figure 1 It is a schematic diagram of the production process flow of the embodiment of the present invention;

[0032] Figure 2 It is a schematic diagram of the production process flow of Comparative Examples 1 and 2;

[0033] Figure 3 It is a schematic diagram of the production process flow of Comparative Example 3.

[0034] Symbol description: S1 is the overhead distillate of the light cutting tower; S2 is the bottom distillate of the light cutting tower; S3 is the overhead distillate of the heavy cutting tower; S4 is the bottom distillate of the heavy cutting tower. DETAILED DESCRIPTION OF THE INVENTION

[0035] The present invention will be specifically described below in conjunction with specific drawings and embodiments. It is necessary to point out here that the following embodiments are only for further illustration of the present invention and cannot be construed as limiting the protection scope of the present invention. Some non-essential improvements and adjustments made by those skilled in the art based on the content of the present invention still fall within the protection scope of the present invention.

[0036] In addition, it should be noted that the various specific technical features described in the following detailed embodiments can be combined in any suitable manner without contradiction. To avoid unnecessary repetition, the present invention will not separately describe various possible combination methods.

[0037] In addition, any combination can be made between various different embodiments of the present invention as long as it does not violate the idea of the present invention. The technical solutions thus formed belong to a part of the original disclosure of this specification and also fall within the protection scope of the present invention.

[0038] For the raw materials used in the examples and comparative examples, if not specifically defined, they are all disclosed in the prior art. For example, they can be directly purchased or prepared according to the preparation methods disclosed in the prior art.

[0039] Unless otherwise specified, all percentages, ratios, etc. mentioned in this specification are based on weight, unless it does not conform to the common understanding of those skilled in the art when based on weight.

[0040] Unless otherwise specified, all pressures mentioned in this specification are absolute pressures.

[0041] The present invention will be further described below through specific embodiments.

[0042] This process route method uses boiling points for cutting. Rectification is a process commonly used to separate liquid mixtures. It is based on the boiling point differences of different components and separates each component by heating the mixture and utilizing the principles of evaporation and condensation. Rectification for cutting different components by boiling points specifically refers to separating different components according to the boiling point differences of each component. The target separation substance studied in the present invention is DCPD, which accounts for about 10 - 20% in the cracked C9 raw material. The cracked C9 raw material is composed of substances such as ethylbenzene, m-xylene, o-xylene, styrene, m-ethyltoluene, mesitylene, methylstyrene, dicyclopentadiene, n-decane, indene, n-butylbenzene, etc. Light components with boiling points below 160 °C such as ethylbenzene, m-xylene, styrene, and o-xylene will be separated from the light-cutting tower, and heavy components with boiling points above 180 °C will be separated in the heavy-cutting tower. To solve the separation problem of the target system of the present invention, a process route for cutting by rectification using boiling points is explored to improve the purity of DCPD.

[0043] The process flow of the present invention is as Figure 1 , and the cracked C9 raw material mixture composed of substances such as ethylbenzene, m-xylene, o-xylene, styrene, m-ethyltoluene, mesitylene, methylstyrene, dicyclopentadiene, n-decane, indene, n-butylbenzene, etc. enters the light-cutting tower (QL), and the light components with boiling points below 160 °C are separated from the top of the tower. The mixture containing DCPD coming out from the bottom of the light-cutting tower (QL) enters the heavy-cutting tower (QH), and the heavy components with boiling points above 180 °C are separated from the bottom of the tower in the QH tower, and a DCPD-rich fraction is obtained from the top of the QH tower.

[0044] Example 1

[0045] The component contents of the cracked C9 fraction are shown in Table 1, which mainly consists of substances such as ethylbenzene, m-xylene, o-xylene, styrene, m-ethyltoluene, mesitylene, methylstyrene, DCPD (dicyclopentadiene), n-decane, sym-trimethylbenzene, indene, n-butylbenzene, etc. Among them, ethylbenzene, m-xylene, o-xylene, styrene, etc. are light components with boiling points below 160 °C, and indene, methylindene, n-butylbenzene, undecane, dodecane, naphthalene, etc. are heavy components with boiling points above 180 °C. All are impurities except DCPD (dicyclopentadiene).

[0046] Table 1

[0047]

[0048]

[0049] The implementation steps are as follows:

[0050] a) The cracked C9 raw material enters the light cut column (QL) from the middle and lower part of the column at a flow rate of 11878.70 kg / h. The heating load at the bottom of the QL column is 1738 kw / t, the number of theoretical plates is 30, the feed position is the 14th plate, and the operating pressure is 10 kPa. The top temperature of the column is 89 °C, and the bottom temperature is 120 °C.

[0051] b) The mixture containing DCPD flows out from the bottom of the QL column at a flow rate of 59% of the total feed.

[0052] c) Light components such as ethylbenzene, m-xylene, o-xylene, styrene (boiling points below 160 °C) are separated from the top of the QL column at a flow rate of 40% of the total feed.

[0053] d) The DCPD-containing mixture flowing out from the bottom of the QL column enters the heavy cut column (QH). The heating load at the bottom of the QH column is 1280.95 kw / t, the number of theoretical plates is 35, the feed position is the 20th plate, and the operating pressure is 10 kPa. The top temperature of the QH column is 80 - 85 °C, and the bottom is 110 - 125 °C.

[0054] e) Heavy components such as indene, methylindene, n-butylbenzene, undecane, dodecane, naphthalene (boiling points above 180 °C) are separated from the bottom of the QH column at a flow rate of 31.2% of the total feed.

[0055] f) The DCPD-rich mixture flows out from the top of the QH column at a flow rate of 27.6% of the total feed.

[0056] The detailed conditions and results of this example are listed in Table 2. The composition of the bottom distillate product of the light removal tower (QL) is listed in Table 3, and the composition of the top distillate product of the heavy removal tower (QH) is listed in Table 4. Based on these conditions, dicyclopentadiene with a purity of 58.773% can be obtained, and the yield is 99.37%.

[0057] Example 2

[0058] The feed and its composition are the same as those in Example 1. According to the Figure 1 process, the cracked C9 raw material is subjected to rectification separation. The implementation steps are basically the same as those in Example 1, except that the number of theoretical plates of the light removal cutting tower (QL) is set to 20. The detailed conditions and results of this example are listed in Table 2. The composition of the bottom distillate product of the light removal tower (QL) is listed in Table 3, and the composition of the top distillate product of the heavy removal tower (QH) is listed in Table 4.

[0059] Based on these conditions, dicyclopentadiene (DCPD) with a purity of 48.895% is finally obtained, and the yield is 94.13%.

[0060] Example 3

[0061] The feed and its composition are the same as those in Example 1. According to the Figure 1 process, the cracked C9 raw material is subjected to rectification separation. The implementation steps are basically the same as those in Example 1, except that the number of theoretical plates of the light removal cutting tower (QL) is 25. The detailed conditions and results of this example are listed in Table 2. The composition of the bottom distillate product of the QL tower is listed in Table 3, and the composition of the top distillate product of the heavy removal tower (QH) is listed in Table 4.

[0062] Based on these conditions, dicyclopentadiene (DCPD) with a purity of 52.49% is finally obtained, and the yield is 96.82%.

[0063] Example 4

[0064] The feed and its composition are the same as those in Example 1. According to the Figure 1 process, the cracked C9 raw material is subjected to rectification separation. The implementation steps are basically the same as those in Example 1, except that the number of theoretical plates of the heavy removal cutting tower is 25. The detailed conditions and results of this example are listed in Table 2. The composition of the bottom distillate product of the light removal tower (QL) is listed in Table 3, and the composition of the top distillate product of the heavy removal tower (QH) is listed in Table 4.

[0065] Based on these conditions, dicyclopentadiene (DCPD) with a purity of 58.91% is finally obtained, and the yield is 97.69%.

[0066] Example 5

[0067] The feed and its composition are the same as those in Example 1. According to the Figure 1The process was used to rectify and separate the cracked C9 raw material. The implementation steps were basically the same as those in Example 1, except that the feed tray position of the heavy removal cutting tower was the 15th tray. The detailed conditions and results of this example are listed in Table 2. The composition of the bottom distillate product of the light removal tower (QL) is listed in Table 3, and the composition of the top distillate product of the heavy removal tower (QH) is listed in Table 4.

[0068] Based on this condition, dicyclopentadiene (DCPD) with a purity of 50.138% was finally obtained, and the yield was 95.25%.

[0069] Example 6

[0070] The feed and its composition were the same as those in Example 1. According to the Figure 1 process, the cracked C9 raw material was rectified and separated. The implementation steps were basically the same as those in Example 1, except that the number of theoretical plates of the light removal cutting tower (QL) in this comparative example was 35. The detailed conditions and results of this example are listed in Table 2. The composition of the bottom distillate product of the light removal tower (QL) is listed in Table 3, and the composition of the top distillate product of the heavy removal tower (QH) is listed in Table 4.

[0071] Based on this condition, dicyclopentadiene (DCPD) with a purity of 56.82% was finally obtained, and the yield was 98.14%.

[0072] Example 7

[0073] The feed and its composition were the same as those in Example 1. According to the Figure 1 process, the cracked C9 raw material was rectified and separated. The implementation steps were basically the same as those in Example 1, except that the number of theoretical plates of the heavy removal cutting tower (QH) in this comparative example was 30. The detailed conditions and results of this example are listed in Table 2. The composition of the bottom distillate product of the light removal tower (QL) is listed in Table 3, and the composition of the top distillate product of the heavy removal tower (QH) is listed in Table 4.

[0074] Based on this condition, dicyclopentadiene (DCPD) with a purity of 56.61% was finally obtained, and the yield was 98.06%.

[0075] Example 8

[0076] The feed and its composition were the same as those in Example 1. According to the Figure 1 process, the cracked C9 raw material was rectified and separated. The implementation steps were basically the same as those in Example 1, except that the feed position of the heavy removal cutting tower (QH) was the 22nd tray. The detailed conditions and results of this example are listed in Table 2. The composition of the bottom distillate product of the light removal tower (QL) is listed in Table 3, and the composition of the top distillate product of the heavy removal tower (QH) is listed in Table 4.

[0077] Based on this condition, dicyclopentadiene (DCPD) with a purity of 57.76% was finally obtained, and the yield was 98.61%.

[0078] Example 9

[0079] The feed and its composition are the same as in Example 1. The cracked C9 raw material is subjected to rectification separation according to the Figure 1 process. The implementation steps are basically the same as those in Example 1, except that the feed position of (QH) to the de-heavy cutting tower is the 25th plate. The detailed conditions and results of this example are listed in Table 2, the composition of the bottom distillate product of the de-light tower (QL) is listed in Table 3, and the composition of the top distillate product of the de-heavy tower (QH) is listed in Table 4.

[0080] Based on this condition, dicyclopentadiene (DCPD) with a purity of 56.12% is finally obtained, and the yield is 97.92%.

[0081] Example 10

[0082] The feed and its composition are the same as in Example 1. The cracked C9 raw material is subjected to rectification separation according to the Figure 1 process. The implementation steps are basically the same as those in Example 1, except that the bottom distillate rate of the de-light rectification tower (QL) is 55% of the total feed amount. The detailed conditions and results of this example are listed in Table 2, the composition of the bottom distillate product of the de-light tower (QL) is listed in Table 3, and the composition of the top distillate product of the de-heavy tower (QH) is listed in Table 4.

[0083] Based on this condition, dicyclopentadiene (DCPD) with a purity of 50.38% is finally obtained, and the yield is 92.83%.

[0084] Comparative Example 1

[0085] The feed and its composition are the same as in Example 1. The cracked C9 raw material is subjected to rectification separation according to the Figure 2 process. The difference is that the raw material first enters the de-heavy cutting tower (QH), and the material distilled from the top of the de-heavy cutting tower enters the de-light cutting tower. The feed positions, reflux ratios, pressures, and theoretical plate numbers of the de-heavy cutting tower and the de-light cutting tower are exactly the same as those in Example 1. The detailed conditions and results of this comparative example are listed in Table 5., the composition of the bottom distillate product of the de-light tower (QL) is listed in Table 6, and the composition of the top distillate product of the de-heavy tower (QH) is listed in Table 7.

[0086] Based on this condition, dicyclopentadiene (DCPD) with a purity of 55.79% is finally obtained, and the yield is 94.32%. The heat load of the bottom of the de-heavy tower is as high as 4490 kw / t.

[0087] Comparative Example 2

[0088] The feed and composition are the same as in Example 1. According to the Figure 2The process rectifies and separates the cracked C9 raw material. The difference is that the raw material first enters the de-heavy cutting tower (QH), and the material distilled from the top of the de-heavy cutting tower enters the de-light cutting tower. The pressure of the de-heavy cutting tower is adjusted to 35 kPa, and the top temperature is 90°C - 100°C. The feed position, reflux ratio, and number of theoretical plates of the de-heavy cutting tower and the de-light cutting tower are exactly the same as those in Example 1. The detailed conditions and results of this comparative example are listed in Table 5. The composition of the product distilled from the bottom of the de-light tower (QL) is listed in Table 6, and the composition of the product distilled from the top of the de-heavy tower (QH) is listed in Table 7.

[0089] Based on this condition, dicyclopentadiene (DCPD) with a purity of 53.92% is finally obtained, and the yield is 96.27%. The heat load of the bottom of the de-heavy tower is as high as 4356.4 kw / t.

[0090] Comparative Example 3

[0091] The feed and its composition are the same as those in Example 1. According to Figure 3 the process rectifies and separates the cracked C9 raw material. The difference is that there is only a de-light cutting tower, and no de-heavy cutting is carried out. The operating pressure of the de-light cutting tower is 15 kPa, and the reflux ratio is 6. The top temperature is 60°C, and the bottom temperature is 100°C. The feed position and the number of theoretical plates of the de-light cutting tower are exactly the same as those in Example 1. The detailed conditions and results of this comparative example are listed in Table 2, and the composition of the product distilled from the bottom of the de-light cutting tower (QL) is listed in Table 3.

[0092] Based on this condition, dicyclopentadiene (DCPD) with a purity of 22.64% is finally obtained, and the yield is 96.78%. The heat load of the de-light cutting tower is as high as 4392.04 kw / t. The yields and purities of the dicyclopentadiene obtained in the above examples and comparative examples are tested. The content of dicyclopentadiene in the cracked C9 fraction is tested in advance, and the content of dicyclopentadiene in this batch of cracked C9 fraction is found to be 16.32%. The yield is calculated using the following formula: Yield = mass of dicyclopentadiene / mass of dicyclopentadiene in the cracked C9 fraction * 100%.

[0093] Table 2

[0094]

[0095]

[0096] Table 3

[0097]

[0099]

[0100] Table 4

[0101]

[0102] Table 5

[0103]

[0104]

[0105] Table 6

[0106]

[0107] Table 7

[0108]

[0109]

[0110] Taking the ideal embodiments of the present invention described above as an inspiration, through the above description, relevant staff can completely make various changes and modifications without departing from the technical idea of this invention. The technical scope of this invention is not limited to the content in the specification, and its technical scope must be determined according to the scope of the claims.

Claims

1. A production process for cracking C9 raw materials to cut and purify DCPD, characterized in that, It includes the following steps: a) Flowing the cracked C9 raw material into the light cut column; b) Taking out light components from the top of the light cut column, and the bottom of the column flows out the component containing DCPD; c) Transporting the component containing DCPD to the heavy cut column; d) Taking out heavy components from the bottom of the heavy cut column, and obtaining a DCPD-rich fraction at the top of the column.

2. The production process for cutting and purifying DCPD from cracked C9 raw materials according to claim 1, wherein, The cracked C9 raw material includes ethylbenzene, m-xylene, o-xylene, styrene, m-ethyltoluene, mesitylene, methylstyrene, dicyclopentadiene, n-decane, indene of trimethylbenzene, n-butylbenzene.

3. The production process for cutting and purifying DCPD from cracked C9 raw materials according to claim 1, characterized in that, The number of theoretical plates of the light cut column is 20 - 40, the pressure is 1 - 10 kPa, the top temperature of the column is 80 - 90 °C, and the bottom temperature of the column is 120 - 130 °C.

4. The production process for cutting and purifying DCPD from cracked C9 raw materials according to claim 1, characterized in that, The flow rate of the cracked C9 raw material flowing into the light cut column is 10000 - 12000 kg / h; The feed plate position of the cracked C9 raw material is the 14th plate of the light cut column.

5. The production process for cutting and purifying DCPD from cracked C9 raw materials according to claim 1, characterized in that, The top flow rate of the light cut column is 38% - 45% of the total feed rate. The bottom flow rate of the light cut column is 55% - 62% of the total feed rate.

6. The production process for cutting and purifying DCPD from cracked C9 raw materials according to claim 1, characterized in that, The light components are the components in the cracked C9 raw material with a boiling point lower than 160 °C, including ethylbenzene, m-xylene, o-xylene, styrene.

7. The production process for cutting and purifying DCPD from cracked C9 raw materials according to claim 1, characterized in that, The number of theoretical plates of the heavy cut column is 23 - 43, the pressure is 1 - 10 kPa, the top temperature of the column is 80 - 85 °C, and the bottom of the column is 110 - 125 °C.

8. The production process for cutting and purifying DCPD from cracked C9 raw materials according to claim 1, characterized in that, The feed plate position of the component containing DCPD is the 20th plate.

9. The production process for cutting and purifying DCPD from cracked C9 raw materials according to claim 1, characterized in that, The bottom flow rate of the heavy cut column is 27% - 32% of the total feed rate.

10. The production process for cutting and purifying DCPD from cracked C9 raw materials according to claim 1, characterized in that, The heavy components are the components in the cracked C9 raw material with a boiling point higher than 180 °C, including indene, methyl indene, n-butylbenzene, undecane, dodecane, naphthalene.

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