CN113651670B - Method for preparing hanging tetrahydrodicyclopentadiene through hydroisomerization of dicyclopentadiene - Google Patents
Method for preparing hanging tetrahydrodicyclopentadiene through hydroisomerization of dicyclopentadiene Download PDFInfo
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Abstract
The invention discloses a method for preparing hanging tetrahydrodicyclopentadiene through hydroisomerization of dicyclopentadiene, which belongs to the technical field of synthesis of tetrahydrodicyclopentadiene and comprises the following steps: hydrogenation: dicyclopentadiene is used as raw material, a two-stage fixed bed reactor is adopted, and a one-stage hydrogenation catalyst Ni/Al is adopted 2 O 3 A catalyst; two-stage hydrogenation catalyst Mo/Al 2 O 3 A catalyst; rectifying a hydrogenation product: firstly, materials at the top of a de-heaving tower enter a de-lightering tower, and high-purity bridge-type tetrahydrodicyclopentadiene is extracted from the bottom of the de-lightering tower; isomerization reaction: bridge type tetrahydrodicyclopentadiene is used as a raw material, and anhydrous AlCl is adopted 3 The catalyst is dichloroethane as solvent, and isomerization reaction is carried out in a stirred tank. The invention adopts various raw materials for hydrogenation, adopts sulfur and nitrogen resistant two-stage catalysts to replace the conventional hydrogenation catalyst, optimizes the reaction conditions, improves the final once conversion rate to more than 98.5 percent, improves the selectivity to more than 99.4 percent, realizes industrialized mass production, reduces the production cost and simplifies the process route.
Description
Technical Field
The invention relates to the technical field of synthesis of tetrahydrodicyclopentadiene, in particular to a method for preparing hanging tetrahydrodicyclopentadiene by hydroisomerization of dicyclopentadiene.
Background
As a key component of liquid propellant or fuel, the high-density fuel has great significance for aerospacecrafts such as airplanes, missiles, rockets and the like with limited volumes. The novel high-density hydrocarbon fuel hanging tetrahydrodicyclopentadiene has excellent comprehensive performance, has the advantages of high energy, large density, low freezing point and the like, and becomes an ideal high-density hydrocarbon fuel for rockets, high-speed aircrafts and cruise missiles. Typically, the pendant tetrahydrodicyclopentadiene is achieved through both hydrogenation and isomerization. Firstly, converting dicyclopentadiene into bridge-type tetrahydrodicyclopentadiene through hydrogenation, and then taking bridge-type tetrahydrobicyclo as a raw material to isomerize in the presence of a catalyst to generate hanging-type tetrahydrodicyclopentadiene; removing the catalyst after the reaction, and rectifying to obtain the high-purity hanging-type tetrahydrodicyclopentadiene.
In the prior art, for hydrogenation reaction, most of raw materials adopt single high-purity dicyclopentadiene as raw materials, and the hydrogenation catalyst is deactivated due to higher nitrogen and sulfur contents of crude dicyclopentadiene, so that impurities in the crude dicyclopentadiene influence subsequent isomerization reaction. At present, a large-scale device for continuously producing bridge-type tetrahydrodicyclopentadiene is not available, and the main reason is that the bridge-type tetrahydrodicyclopentadiene is solid at normal temperature, and a reactor, a pipeline and a rectifying tower are easy to be blocked. The industrial production at the present stage adopts a kettle type reactor, and has the characteristics of low reaction efficiency, low safety coefficient, unstable conversion rate, complex subsequent process after the reaction is finished, and the like. The isomerization reaction temperature is above 75 ℃ under the condition of no solvent addition, and is determined by the melting point of the bridged tetrahydrodicyclopentadiene, so that the isomerization selectivity is reduced due to the fact that the temperature is too high. The primary conversion rate of the existing large-scale isomerization reaction bridge tetrahydrodicyclopentadiene is below 98%, and the selectivity is below 98%.
The patent with publication number CN102924216B discloses a synthesis method of hanging tetrahydrodicyclopentadiene. The method comprises the following steps: (1) After the hydrogenation catalyst is subjected to reduction and activation treatment, catalyzing dicyclopentadiene to perform a primary hydrogenation reaction in a hydrogen atmosphere to obtain a primary hydrogenation product; (2) Under the hydrogen atmosphere, the primary hydrogenation product is subjected to secondary hydrogenation reaction under the catalysis of the hydrogenation catalyst subjected to reduction activation treatment to obtain a secondary hydrogenation product; (3) The secondary hydrogenation product is subjected to isomerization reaction under the catalysis of anhydrous AlCl3 to obtain the hanging tetrahydrodicyclopentadiene. The primary hydrogenation temperature of the process needs to be above 120 ℃, and the secondary hydrogenation temperature needs to be above 190 ℃ to obtain higher yield.
The patent with publication number CN101215218B discloses a preparation method of hanging tetrahydrodicyclopentadiene, which aims to solve the problem that the hydrogenation catalyst is difficult to recycle in the prior art. The invention takes dicyclopentadiene and hydrogen as raw materials, and comprises the following steps: A. in the presence of an alcohol solvent and a hydrogenation catalyst, dicyclopentadiene and hydrogen react in a high-pressure reaction kettle to generate bridge tetrahydrodicyclopentadiene; B. adding the hanging tetrahydrodicyclopentadiene into the reaction product of the step A, and filtering and separating the hydrogenation catalyst; C. performing reduced pressure rectification on the filtrate obtained in the step B, wherein an alcohol solvent is used as a tower top component, and a mixture of hanging tetrahydrodicyclopentadiene and bridge tetrahydrodicyclopentadiene is used as a tower bottom component; D. the kettle component obtained in the step C reacts in the presence of an isomerization catalyst to generate the hanging tetrahydrodicyclopentadiene; E. and D, carrying out reduced pressure rectification on the isomerization reaction product obtained in the step, and obtaining a hanging tetrahydrodicyclopentadiene product. The method has complex process and the yield is only about 90%.
Disclosure of Invention
In order to solve the problems, the inventor obtains a method for preparing the hanging type tetrahydrodicyclopentadiene through hydroisomerization of dicyclopentadiene through trial and error by taking dicyclopentadiene as a raw material and carrying out two-stage hydrogenation reaction to convert the dicyclopentadiene into bridge type tetrahydrodicyclopentadiene, and carrying out isomerization by taking bridge type tetrahydrodicyclopentadiene and aluminum trichloride as an isomer.
A method for preparing hanging tetrahydrodicyclopentadiene through hydroisomerization of dicyclopentadiene, which comprises the following steps:
s1: hydrogenation: dicyclopentadiene is used as raw material, hydrogenation is carried out by adopting a two-stage fixed bed reactor, and one-stage hydrogenation catalyst Ni/Al is adopted 2 O 3 A catalyst; two-stage hydrogenation catalyst Mo/Al 2 O 3 A catalyst;
s2: rectifying a hydrogenation product: after two-stage hydrogenation reaction, firstly, passing through a heavy removal tower, and enabling a material at the tower top of the heavy removal tower to enter a light removal tower, wherein high-purity bridge type tetrahydrodicyclopentadiene is extracted from the tower bottom of the light removal tower;
s3: isomerization reaction: bridge tetrahydrodicyclopentadiene obtained by hydrogenation rectification is used as a raw material, and anhydrous AlCl is used as a raw material 3 As catalyst and dichloroethane as solvent, and isomerization reaction is carried out in a stirred tank。
Further, in the step S1, the inlet temperature is 60-90 ℃, the bed temperature rise is 70-90 ℃ and the space velocity is 0.4-0.65 hr -1 The hydrogen-oil ratio is 700-1000.
Further, in the step S1, the two-stage hydrogenation is carried out at an inlet temperature of 150-170 ℃, a bed temperature rise of 160-180 ℃ and a space velocity of 0.7-0.9 hr -1 The hydrogen-oil ratio is 400-600.
Further, in the step S2, the weight loss tower: the pressure is 0.1+/-0.05 Mpa, the tower top temperature is 184+/-2 ℃, the reflux ratio is 1-1.2, the tower bottom extraction amount is 100-200 kg/h, the tower bottom temperature is 222+/-2 ℃, the tower top extraction amount is 1300-1400 kg/h, the tower plate number is 35, and the feeding temperature is 150-155 ℃.
Further, in the step S2, the weight loss tower: the pressure is 0.1+/-0.05 Mpa, the tower top temperature is 143+/-2 ℃, the reflux ratio is 1.5-2.5, the tower bottom extraction amount is 900-1000 kg/h, the tower bottom temperature is 210+/-2 ℃, the tower top extraction amount is 500-600 kg/h, the tower plate number is 30, and the feeding temperature is 110-120 ℃.
Further, in the step S3, the mass ratio of each component is that the bridge tetrahydrodicyclopentadiene: dichloroethane: alCl 3 =100:10:0.8～1。
In the step S3, the temperature is 15-40 ℃, the reaction time is 20-45 min, and the stirring speed is 400-700 rpm.
Further, dicyclopentadiene is two or more of industrial crude dicyclopentadiene, industrial refined dicyclopentadiene, dicyclopentadiene produced by cracking carbon nine and dicyclopentadiene produced by cracking gasoline.
The synthesis of the hanging tetrahydrodicyclopentadiene takes dicyclopentadiene as a raw material, and the dicyclopentadiene is obtained through hydrogenation, isomerization, separation and purification. In order to search for a catalyst with high hydrogenation rate, high efficiency and long service life, researchers are continuously searching for the catalyst, and the development of the catalyst is greatly improved. The efficiency is improved, the cost is saved, and the research and optimization work of the hydrogenation process is also continuously carried out. For example, huang Caifeng the synthesis and application of hanging tetrahydrodicyclopentadiene has progressed [ J ]. Chemical and medical engineering, 2018 (01): 19-22, the research progress of dicyclopentadiene hydrogenation catalyst and tetrahydrodicyclopentadiene isomerization catalyst has been focused on. Therefore, researchers generally consider that in order to improve the conversion rate and reduce the cost, a catalyst with high catalytic efficiency and long service life is selected and used, and a continuous hydrogenation process can be performed. The patent with publication number CN107417485B discloses a method for directly preparing hanging tetrahydrodicyclopentadiene from dicyclopentadiene, which belongs to the technical field of aviation fuel preparation. The method takes dicyclopentadiene as a main component of a petroleum processing byproduct C5 as a raw material, adopts a bifunctional catalyst combined by layered double metal hydroxide and inorganic solid acid, realizes the coupling of dicyclopentadiene hydrogenation reaction and isomerization reaction, and continuously prepares the hanging-type tetrahydrodicyclopentadiene by a one-step method, but the conversion rate is not very high. Therefore, researchers have been enthusiastic to study catalysts that increase catalytic efficiency and simplify processes in order to reduce costs, but have neglected the impact of raw materials on costs. It is generally thought that the higher the purity of the starting material, the higher the yield obtained, but the higher the purity of the starting material, the more expensive it is. Therefore, there is a need to develop a method of obtaining a high yield of exo-tetrahydrodicyclopentadiene by reducing the cost of raw materials.
The beneficial effects of the invention are as follows:
1. the application adopts a sulfur and nitrogen resistant two-stage catalyst to replace a conventional hydrogenation catalyst, and the activity of the supported catalyst is not easy to be reduced due to sulfur and nitrogen resistance, so that various raw materials can be adopted for hydrogenation reaction, and the diversification of the raw materials is increased.
2. The hydrogenation is carried out by adopting various raw materials, and components except the bridge type tetrahydrodicyclopentadiene exist in the reaction and subsequent rectification processes, so that the bridge type tetrahydropentadiene is dissolved in the reaction and subsequent rectification processes, the blocking condition in the process cannot be caused, the industrialized mass production is realized, the production cost is reduced, the safety risk is reduced, the process route is simplified, and the stability of the conversion rate is improved.
3. The isomerization reaction adopts dichloroethane as a solvent, increases the contact area of the catalyst and bridge-type tetrahydrodicyclopentadiene, reduces the reaction temperature and increases the conversion rate.
4. And (3) optimizing reaction conditions: the ratio of catalyst, hydrogenation product and solvent is controlled and variable method screening is carried out on the conditions of reaction pressure, reaction temperature and reaction time, so that the reaction conversion rate and selectivity are greatly improved, the primary conversion rate is improved to more than 98.5%, and the selectivity is improved to more than 99.4%.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention more clear, the technical solutions of the embodiments of the present invention are clearly and completely described below. It will be apparent that the described embodiments are some, but not all, embodiments of the invention. All other embodiments, which are obtained by a person skilled in the art based on the described embodiments of the invention, fall within the scope of protection of the invention.
A method for preparing hanging tetrahydrodicyclopentadiene through hydroisomerization of dicyclopentadiene, which comprises the following steps:
s1: hydrogenation: dicyclopentadiene is used as raw material, hydrogenation is carried out by adopting a two-stage fixed bed reactor, and one-stage hydrogenation catalyst Ni/Al is adopted 2 O 3 The catalyst has inlet temperature of 60-90 deg.c, bed temperature rise of 70-90 deg.c and airspeed of 0.4-0.65 hr -1 The hydrogen-oil ratio is 700-1000; two-stage hydrogenation catalyst Mo/Al 2 O 3 The catalyst has inlet temperature of 150-170 deg.c, bed temperature rise of 160-180 deg.c and airspeed of 0.7-0.9 hr -1 The hydrogen-oil ratio is 400-600; the hydrogenation raw material adopts two or more of industrial crude dicyclopentadiene, industrial refined dicyclopentadiene, dicyclopentadiene generated by cracking carbon nine and dicyclopentadiene generated by cracking gasoline;
s2: rectifying a hydrogenation product: rectifying and purifying bridge-type tetrahydrodicyclopentadiene from the second-stage reaction product, wherein the second-stage reaction product firstly passes through a heavy removal tower, materials at the top of the heavy removal tower enter a light removal tower, and high-purity bridge-type tetrahydrodicyclopentadiene is extracted from the bottom of the light removal tower; the rectification column operating parameters are shown in table 1 below;
TABLE 1
S3: isomerization reaction: bridge tetrahydrodicyclopentadiene obtained by hydrogenation rectification is used as a raw material, and anhydrous AlCl is used as a raw material 3 As a catalyst, dichloroethane is used as a solvent, and isomerization reaction is carried out in a stirred tank; the mass ratio of each component is bridge tetrahydrodicyclopentadiene: dichloroethane: alCl 3 =100:10:0.8 to 1; the temperature is 15-40 ℃, the reaction time is 20-45 min, and the stirring speed is 400-700 rpm.
Examples 1 to 20
Wherein, in examples 1-4, industrial crude dicyclopentadiene and industrial refined dicyclopentadiene are adopted as hydrogenation raw materials, and the mass ratio of the industrial crude dicyclopentadiene to the industrial refined dicyclopentadiene is as follows: industrial crude dicyclopentadiene: industrial fine dicyclopentadiene = 2:1; in examples 5 to 8, industrial refined dicyclopentadiene and dicyclopentadiene produced by cracking carbon nine are adopted as hydrogenation raw materials, and the mass ratio of the industrial refined dicyclopentadiene to the dicyclopentadiene is as follows: industrial fine dicyclopentadiene: dicyclopentadiene from cleavage of carbon nine = 1:3; in examples 9 to 12, the hydrogenation raw material was industrial crude dicyclopentadiene and dicyclopentadiene produced from pyrolysis gasoline in the following mass ratio: industrial crude dicyclopentadiene: dicyclopentadiene produced by pyrolysis gasoline = 1:2; in examples 13 to 16, industrial refined dicyclopentadiene, industrial crude dicyclopentadiene and dicyclopentadiene produced by pyrolysis gasoline are adopted as hydrogenation raw materials, and the mass ratio of the industrial refined dicyclopentadiene to the dicyclopentadiene is as follows: industrial crude dicyclopentadiene: dicyclopentadiene produced by pyrolysis gasoline = 1:1.5:2. In examples 17 to 20, the hydrogenation raw material used industrial crude dicyclopentadiene, dicyclopentadiene produced by cracking carbon nine, dicyclopentadiene produced by cracking gasoline, and the mass ratio of the three was industrial crude dicyclopentadiene: cracking dicyclopentadiene produced by carbon nine: dicyclopentadiene produced by pyrolysis gasoline = 1:2:3.
The hydrogenation stage, the isomerization reaction stage, the content of each component and the parameters are shown in table 2, the detection result is shown in table 4, wherein the primary conversion rate is the conversion rate of high-purity bridge type tetrahydrodicyclopentadiene, and the selectivity is the yield of the obtained pendent tetrahydrodicyclopentadiene.
TABLE 2
TABLE 3 Table 3
| Examples | Bridge tetrahydrodicyclopentadiene: dichloroethane: alCl 3 | Temperature (. Degree. C.) | Reaction time (min) | Stirring rate (rpm) |
| 1 | 100:10:0.8 | 15 | 20 | 700 |
| 2 | 100:10:0.9 | 15 | 25 | 650 |
| 3 | 100:10:1 | 18 | 30 | 600 |
| 4 | 100:10:0.8 | 18 | 35 | 550 |
| 5 | 100:10:0.9 | 20 | 40 | 500 |
| 6 | 100:10:1 | 20 | 20 | 650 |
| 7 | 100:10:0.8 | 25 | 25 | 550 |
| 8 | 100:10:0.9 | 25 | 30 | 500 |
| 9 | 100:10:1 | 28 | 35 | 450 |
| 10 | 100:10:0.8 | 28 | 40 | 400 |
| 11 | 100:10:0.9 | 30 | 20 | 700 |
| 12 | 100:10:1 | 30 | 25 | 650 |
| 13 | 100:10:0.9 | 32 | 30 | 600 |
| 14 | 100:10:0.8 | 32 | 35 | 550 |
| 15 | 100:10:0.9 | 35 | 40 | 400 |
| 16 | 100:10:1 | 35 | 20 | 650 |
| 17 | 100:10:1 | 38 | 25 | 650 |
| 18 | 100:10:0.9 | 38 | 30 | 600 |
| 19 | 100:10:0.8 | 40 | 35 | 600 |
| 20 | 100:10:0.9 | 40 | 40 | 550 |
TABLE 4 Table 4
| Examples | Primary conversion (%) | Selectivity (%) |
| 1 | 98.8 | 99.4 |
| 2 | 98.8 | 99.4 |
| 3 | 98.9 | 99.5 |
| 4 | 98.8 | 99.4 |
| 5 | 98.8 | 99.4 |
| 6 | 98.8 | 99.5 |
| 7 | 98.9 | 99.5 |
| 8 | 98.9 | 99.6 |
| 9 | 98.5 | 99.7 |
| 10 | 98.6 | 99.6 |
| 11 | 98.6 | 99.7 |
| 12 | 98.6 | 99.8 |
| 13 | 98.7 | 99.7 |
| 14 | 98.8 | 99.7 |
| 15 | 98.7 | 99.6 |
| 16 | 98.7 | 99.6 |
| 17 | 98.6 | 99.5 |
| 18 | 98.6 | 99.6 |
| 19 | 98.7 | 99.4 |
| 20 | 98.6 | 99.5 |
Example 21
A method for preparing hanging tetrahydrodicyclopentadiene through hydroisomerization of dicyclopentadiene, which comprises the following steps:
s1: hydrogenation: dicyclopentadiene is used as raw material, hydrogenation is carried out by adopting a two-stage fixed bed reactor, and one-stage hydrogenation catalyst Ni/Al is adopted 2 O 3 The catalyst inlet temperature is 70deg.C, bed temperature is 70deg.C, and space velocity is 0.5hr -1 The hydrogen-oil ratio is 800; two-stage hydrogenation catalyst Mo/Al 2 O 3 The catalyst inlet temperature is 160deg.C, the bed temperature is 160deg.C, and the space velocity is 0.8hr -1 The hydrogen-oil ratio is 500; the hydrogenation raw materials adopt industrial crude dicyclopentadiene, industrial refined dicyclopentadiene, dicyclopentadiene generated by cracking carbon nine and dicyclopentadiene generated by cracking gasoline, and the mass ratio of the industrial crude dicyclopentadiene to the dicyclopentadiene is as follows: industrial fine dicyclopentadiene: cracking dicyclopentadiene produced by carbon nine: dicyclopentadiene produced by pyrolysis gasoline = 1:0.3:3:2;
s2: rectifying a hydrogenation product: rectifying and purifying bridge type tetrahydrodicyclopentadiene from the second-stage reaction product, wherein the second-stage reaction product firstly passes through a heavy removal tower, the material at the top of the heavy removal tower enters a light removal tower, the high-purity bridge type tetrahydrodicyclopentadiene is extracted from the bottom of the light removal tower, and the operation parameters of the rectifying tower are shown in table 1; the primary conversion was found to be 98.8%;
s3: isomerization reaction: bridge tetrahydrodicyclopentadiene obtained by hydrogenation rectification is used as a raw material, and anhydrous AlCl is used as a raw material 3 As a catalyst, dichloroethane is used as a solvent, and isomerization reaction is carried out in a stirred tank; the mass ratio of each component is bridge tetrahydrodicyclopentadiene: dichloroethane: alCl 3 =100:10:1; the reaction time was 30min at 30℃under normal pressure with a stirring rate of 500rpm, and the selectivity was found to be 99.6%.
Example 22
The distinguishing technical features of this embodiment from embodiment 21 are that: in the embodiment, the hydrogenation raw materials adopt industrial crude dicyclopentadiene, industrial refined dicyclopentadiene, dicyclopentadiene generated by cracking carbon nine and dicyclopentadiene generated by cracking gasoline, and the mass ratio of the industrial crude dicyclopentadiene is as follows: industrial fine dicyclopentadiene: cracking dicyclopentadiene produced by carbon nine: dicyclopentadiene produced by pyrolysis gasoline=1:0.3:2:2, and the conversion at one time was 98.7% and the selectivity was 99.6%.
Finally, it is noted that the above-mentioned embodiments are merely for illustrating the technical solution of the present invention, and that other modifications and equivalents thereof by those skilled in the art should be included in the scope of the claims of the present invention without departing from the spirit and scope of the technical solution of the present invention.
Claims (7)
1. A method for preparing hanging tetrahydrodicyclopentadiene through hydroisomerization of dicyclopentadiene is characterized in that: comprises the following steps:
s1: hydrogenation: dicyclopentadiene is used as raw material, hydrogenation is carried out by adopting a two-stage fixed bed reactor, and one-stage hydrogenation catalyst Ni/Al is adopted 2 O 3 A catalyst; two-stage hydrogenation catalyst Mo/Al 2 O 3 A catalyst;
s2: rectifying a hydrogenation product: after two-stage hydrogenation reaction, firstly, passing through a heavy removal tower, and enabling a material at the tower top of the heavy removal tower to enter a light removal tower, wherein high-purity bridge type tetrahydrodicyclopentadiene is extracted from the tower bottom of the light removal tower;
s3: isomerization reaction: bridge tetrahydrodicyclopentadiene obtained by hydrogenation rectification is used as a raw material, and anhydrous AlCl is used as a raw material 3 The catalyst is dichloroethane as solvent, and isomerization reaction is carried out in a stirred tank.
2. The method for preparing the hanging tetrahydrodicyclopentadiene through hydroisomerization of dicyclopentadiene according to claim 1, wherein the method is characterized in that: in the step S1, one-stage hydrogenation is carried out, the inlet temperature is 60-90 ℃, the bed temperature rise is 70-90 ℃, and the airspeed is 0.4-0.65 hr -1 The hydrogen-oil ratio is 700-1000.
3. The method for preparing the hanging tetrahydrodicyclopentadiene through hydroisomerization of dicyclopentadiene according to claim 2, wherein the method is characterized in that: in the step S1, two-stage hydrogenation is carried outThe mouth temperature is 150-170 ℃, the bed temperature rise is 160-180 ℃, and the airspeed is 0.7-0.9 hr -1 The hydrogen-oil ratio is 400-600.
4. A process for hydroisomerizing dicyclopentadiene to make pendent tetrahydrodicyclopentadiene according to claim 3, wherein said process comprises: in the step S2, the weight loss tower: the pressure is 0.1+/-0.05 Mpa, the tower top temperature is 184+/-2 ℃, the reflux ratio is 1-1.2, the tower bottom extraction amount is 100-200 kg/h, the tower bottom temperature is 222+/-2 ℃, the tower top extraction amount is 1300-1400 kg/h, the tower plate number is 35, and the feeding temperature is 150-155 ℃.
5. The method for preparing the hanging-type tetrahydrodicyclopentadiene through hydroisomerization of dicyclopentadiene according to claim 4, wherein the method comprises the steps of: in the step S2, the light component removing tower: the pressure is 0.1+/-0.05 Mpa, the tower top temperature is 143+/-2 ℃, the reflux ratio is 1.5-2.5, the tower bottom extraction amount is 900-1000 kg/h, the tower bottom temperature is 210+/-2 ℃, the tower top extraction amount is 500-600 kg/h, the tower plate number is 30, and the feeding temperature is 110-120 ℃.
6. The method for preparing the hanging-type tetrahydrodicyclopentadiene through hydroisomerization of dicyclopentadiene according to claim 5, wherein the method comprises the steps of: in the step S3, the mass ratio of each component is bridge tetrahydrodicyclopentadiene: dichloroethane: alCl 3 =100:10:0.8～1。
7. The method for preparing the hanging-type tetrahydrodicyclopentadiene through hydroisomerization of dicyclopentadiene according to claim 6, wherein the method comprises the steps of: in the step S3, the temperature is 15-40 ℃, the reaction time is 20-45 min, and the stirring speed is 400-700 rpm.
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