WO2022011868A1 - Reaction system and method for hydrogenation of anthracene oil - Google Patents

Abstract

A reaction system and method for the hydrogenation of an anthracene oil. The reaction system comprises: a micro-interface generator (20) and a hydrogenation reactor (50) which are connected in sequence. Hydrogen and an anthracene oil are introduced into the micro-interface generator (20); and the side wall of the hydrogenation reactor (50) is provided with a hydrogenation product outlet, the product coming out of the hydrogenation product outlet is introduced to a first separation tank (60) for the separation of a hot high molecular weight gas and a hot high molecular weight oil, the hot high molecular weight gas enters a second separation tank (70) and is separated into a cold high molecular weight gas and a cold high molecular weight oil, the hot high molecular weight oil enters a third separation tank (110) and is separated into a hot low-molecular weight gas and a hot low molecular weight oil, the hot low-molecular weight oil enters a cracking reactor (80) for a cracking reaction, and the resulting cracking reaction products then enter a fractionation tower for fractionation. By being combined with the micro-interface generator (20), the reaction system reduces the energy consumption, reduces the reaction temperature, improves the reaction yield, improves the utilization rate of raw materials, particularly improves the utilization rate of hydrogen, and also effectively improves the productivity.

Description

A kind of reaction system and method for hydrogenation of anthracene oil technical field

The invention relates to the field of anthracene oil hydrogenation, in particular to a reaction system and method for anthracene oil hydrogenation.

Background technique

Anthracene oil is a part of coal tar components. The fractions at 280-360 °C are cut from the tar by distillation. It is generally a yellow-green oily liquid. At room temperature, crystals are precipitated. The crystals are yellow and have blue fluorescence. It is soluble in ethanol and ether. Insoluble in water, partially soluble in hot benzene, chlorobenzene and other organic solvents, with strong irritation. It is flammable in case of high temperature and open fire. The main components are anthracene, phenanthrene, fluorene, acenaphthene, carbazole, etc.

The hydrogenation process of anthracene oil can effectively achieve desulfurization, unsaturated hydrocarbon saturation, denitrogenation reaction and aromatic hydrocarbon saturation, thereby improving the stability of anthracene oil, reducing the content of sulfur and nitrogen and reducing the content of aromatic hydrocarbons, and obtaining high-quality naphtha and diesel blend ingredients.

At present, most of the anthracene oil hydrogenation processes are two-stage hydrogenation processes of hydrorefining, hydrocracking or a combination of the two. Although the hydrogenation process is easy to operate and easy to industrialize, it has high energy consumption, and the pressure of the hydrogenation reactor is high. High temperature, high temperature, and low production capacity.

In view of this, the present invention is proposed.

SUMMARY OF THE INVENTION

The first object of the present invention is to provide a reaction system for hydrogenation of anthracene oil, which reduces energy consumption, reduces reaction temperature, and improves reaction yield by combining a hydrogenation reactor and a micro-interface generator. It can improve the utilization rate of raw materials, especially the utilization rate of hydrogen, and at the same time effectively increase the production capacity, thereby improving the quality and yield of products.

The second object of the present invention is to provide a reaction method for hydrogenating anthracene oil by adopting the above reaction system. The hydrogenated anthracene oil obtained by the reaction is environmentally friendly, clean and widely used, which improves the applicability of the anthracene oil itself, and is worthy of widespread application. .

In order to realize the above-mentioned purpose of the present invention, the following technical solutions are specially adopted:

The invention provides a reaction system for hydrogenation of anthracene oil, comprising: a micro-interface generator and a hydrogenation reactor connected in sequence;

Hydrogen and anthracene oil are introduced into the micro-interface generator; a hydrogenation product outlet is provided on the side wall of the hydrogenation reactor, and the product from the hydrogenation product outlet is passed into the first separation tank for separation Hot high fraction gas and hot high fraction oil, the hot high fraction gas goes to the second separation tank to be separated into cold high fraction gas and cold high fraction oil; the hot high fraction oil goes to the third separation tank and goes to the third The separation tank is separated into hot low fraction gas and hot low fraction oil, and after the hot low fraction oil enters the cracking reaction tower for cracking reaction, the obtained cracking reaction product goes to the fractionation tower for fractionation, and the cold high fraction gas, Cold high fraction oil and hot low fraction gas are collected and discharged separately.

In the reaction system for hydrogenation of anthracene oil of the present invention, a micro-interface generator is arranged inside the hydrogenation reactor to disperse and break the incoming hydrogen into micro-bubbles, thereby improving the mass transfer effect. The main function of the anthracene oil is to cooperate with the dispersion and crushing of the gas, which is equivalent to the role of the medium.

In addition, the micro-interface generator is arranged outside the hydrogenation reactor, but for the cracking reaction tower, the micro-interface generator can also be correspondingly installed, and it is better to be installed outside the cracking reaction tower and Internal, it is equivalent to combining the external and internal micro-interface generators at the same time, and the cracking reaction tower itself is a fixed-bed reactor, so the micro-interface generators inside the cracking reaction tower are preferably in a straight line along the vertical direction. It is arranged between the adjacent fixed beds. This arrangement can ensure that the cracking and hydrogenation effect of the gap between the two fixed beds is better when the hydrocracking reaction is carried out, and the cracking of macromolecular substances is improved. The effect of molecular substances is equivalent to the simultaneous dispersing and crushing and the reaction, which also makes the dispersing and crushing operation more closely related to the reaction. It can be fully broken into micro-bubbles, so that the pulverization effect after entering the reactor will be more sufficient, and the effect of coordination and cooperation will be achieved. Therefore, the setting position of the micro-interface generator is also obtained through practical design, and needs to be based on different The different characteristics of the reaction are specifically designed.

Preferably, the cracking reaction tower is provided with multi-layer catalyst beds, and each catalyst bed is filled with a catalyst; the top of the cracking reaction tower is supplied with hydrogen, and the hydrogen is pre-compressed by a compressor, so that the The hot low fraction oil enters from the top of the cracking reaction tower.

More preferably, the catalyst bed is preferably 4 sections, and the micro-interface generators located inside the cracking reaction tower are preferably 3, and each micro-interface generator is arranged in two adjacent catalyst beds. between. The number of 3 micro-interface generators can already ensure the effect of dispersion and crushing.

The micro-interface generator set before the above-mentioned hydrogenation reactor is a pneumatic type. By passing hydrogen and anthracene oil into the micro-interface generator and then dispersing and crushing, the subsequent hydrogenation reaction is strengthened, impurities such as sulfur and nitrogen are removed, and the mass transfer effect is improved. .

The micro-interface generators inside and outside the above-mentioned cracking reaction tower are pneumatic, and the mass transfer effect is improved by passing hydrogen into the micro-interface generator and then directly contacting with the hot low-separation oil and then breaking into micro-bubbles.

Those skilled in the art can understand that the micro-interface generator used in the present invention has been embodied in the inventor's prior patents, such as application numbers CN201610641119. Patents of CN205833127U and CN207581700U. In the previous patent CN201610641119.6, the specific product structure and working principle of the micro-bubble generator (that is, the micro-interface generator) were introduced in detail. There is a cavity, the body is provided with an inlet communicating with the cavity, the opposite first and second ends of the cavity are open, wherein the cross-sectional area of the cavity is from the middle of the cavity to the first and second ends of the cavity. The second end is reduced; the secondary crushing piece is arranged at at least one of the first end and the second end of the cavity, a part of the secondary crushing piece is arranged in the cavity, and both ends of the secondary crushing piece and the cavity are open An annular channel is formed between the through holes of the micro-bubble generator. The micro-bubble generator also includes an air inlet pipe and a liquid inlet pipe." From the specific structure disclosed in the application document, we can know that its specific working principle is: the liquid enters the micron tangentially through the liquid inlet pipe. In the bubble generator, ultra-high-speed rotation and cutting of the gas make the gas bubbles break into micro-bubbles at the micron level, thereby increasing the mass transfer area between the liquid phase and the gas phase, and the micro-bubble generator in this patent belongs to the pneumatic micro-interface generation. device.

In addition, the previous patent 201610641251.7 records that the primary bubble breaker has a circulating liquid inlet, a circulating gas inlet and a gas-liquid mixture outlet, and the secondary bubble breaker communicates the feed port with the gas-liquid mixture outlet, indicating that the bubble breaker is both It needs to be mixed with gas and liquid. In addition, it can be seen from the following drawings that the primary bubble breaker mainly uses circulating liquid as power, so in fact, the primary bubble breaker belongs to the hydraulic micro-interface generator, and the secondary bubble breaker is a gas-liquid breaker. The mixture is simultaneously fed into the elliptical rotating ball for rotation, so that the bubbles are broken during the rotation, so the secondary bubble breaker is actually a gas-liquid linkage type micro-interface generator. In fact, both hydraulic micro-interface generators and gas-liquid linkage micro-interface generators belong to a specific form of micro-interface generators. However, the micro-interface generators used in the present invention are not limited to the above-mentioned forms. , the specific structure of the bubble breaker described in the prior patent is only one of the forms that the micro-interface generator of the present invention can take. In addition, the previous patent 201710766435.0 recorded that "the principle of the bubble breaker is to achieve high-speed jets to achieve gas collision", and also stated that it can be used in micro-interface enhanced reactors to verify the relationship between the bubble breaker and the micro-interface generator. and the prior patent CN106187660 also has related records for the specific structure of the bubble breaker, see the specific description in paragraphs [0031]-[0041], and the accompanying drawings, which are related to the bubble breaker S-2 The specific working principle of the bubble breaker is explained in detail. The top of the bubble breaker is the liquid phase inlet, and the side is the gas phase inlet. The liquid phase entering from the top provides the entrainment power, so as to achieve the effect of crushing into ultra-fine bubbles, which can also be seen in the accompanying drawings. The bubble breaker has a conical structure, and the diameter of the upper part is larger than that of the lower part, so that the liquid phase can provide better entrainment power. Since the micro-interface generator was just developed in the early stage of the previous patent application, it was named as micro-bubble generator (CN201610641119.6), bubble breaker (201710766435.0), etc., and later changed its name to micro-interface generator with continuous technological improvement. The micro-interface generator in the present invention is equivalent to the previous micro-bubble generator, bubble breaker, etc., but the names are different.

To sum up, the micro-interface generator of the present invention belongs to the prior art, although some bubble breakers belong to the type of pneumatic bubble breakers, some belong to the type of hydraulic bubble breakers, and some belong to the type of gas bubble breakers. The type of liquid-linked bubble breaker, but the difference between the types is mainly selected according to the specific working conditions. In addition, the connection between the micro-interface generator and the reactor and other equipment, including the connection structure and connection position, depends on the micro-interface generator. It depends on the structure of the interface generator, which is not limited.

Preferably, the type of the hydrogenation reactor for the hydrogenation reaction is a fixed bed reactor, the catalyst in the fixed bed reactor is fixed on the bed layer, and the catalyst for the hydrogenation reaction is generally a nickel-based catalyst, preferably the catalyst can be a supported catalyst The nickel-based catalyst of the type, or the nickel-based catalyst modified with an alkaline earth metal oxide or a rare earth metal oxide is more preferable, and the carrier is selected as silicon oxide or aluminum oxide.

Preferably, the active components of the catalyst for cracking and hydrogenation are oxides of nickel, cobalt, and molybdenum, and the carrier is alumina, silicon-alumina oxide or molecular sieve.

The function of the hydrogenation reactor is to remove impurities such as sulfur and nitrogen to improve the quality of anthracene oil products. The function of the cracking reaction tower is to process the heavy oil, so that under the action of the catalyst, the macromolecules are cracked into small molecules, and most of the slag can be cracked. The oil is converted into fuel oil, liquefied gas, etc., so as to provide the utilization rate of oil products, and the olefin content in the products will be relatively high.

The product from the hydrogenation reactor is separated by the first separation tank, the second separation tank and the third separation tank. The separation tank will adjust the pressurized pressure according to the separated products. The top of the cracking reaction tower enters the cracking and hydrogenation process together with hydrogen. By connecting the hydrogenation reaction and the hydrocracking cycle in parallel, the hydrogenation effect is improved, and the reaction depth is also increased accordingly.

Preferably, the bottom of the cracking reaction tower is provided with a cracking reaction product outlet for discharging the cracking reaction product, the cracking reaction product outlet is connected to a fourth separation tank for oil and gas separation, and the bottom of the fourth separation tank separates The oil phase goes to the fractionation column.

Preferably, the oil phase separated from the bottom of the fourth separation tank goes to the fifth separation tank for further separation, and then the oil phase separated from the bottom of the fifth separation tank goes to the fractionation tower.

Preferably, the gas phase separated from the top of the fourth separation tank is returned to the cracking reaction tower to perform the cracking reaction again.

Preferably, the cold high fraction gas from the top of the second separation tank goes to the fourth separation tank for further separation.

Preferably, the cold high fraction oil from the bottom of the second separation tank goes to the fifth separation tank for further separation.

The cracking reaction product from the cracking reaction tower will also undergo different degrees of gas-liquid separation through the fourth separation tank and the fifth separation tank. At the same time, the product in the previous separation tank can also enter the subsequent separation tank for re-separation. Improve the separation effect.

Preferably, the fractionation tower is provided with multi-layer trays, the trays are filled with packings that contribute to the effect of fractionation, and the overhead gas from the top of the fractionation tower is discharged through a pipeline, and the The tail oil from the bottom of the column is discharged through the pipeline, and the different fractions from the middle part of the column section of the fractionation column are collected separately. The function of the fractionation column is to collect different fractions for corresponding applications according to different purposes. The fractions in the middle column section are fuel oil, naphtha and liquefied gas.

The present invention also provides a reaction method of an anthracene oil hydrogenation reaction system, comprising:

The anthracene oil and hydrogen mixed micro-interface are dispersed and broken, and then hydrogenation reaction is carried out, and then separation, hydrocracking, gas-liquid separation and fractionation are carried out.

Preferably, the pressure of the hydrogenation reaction is 8-10MPa, and the temperature of the hydrogenation reaction is 220-230°C;

Preferably, the pressure of the hydrocracking is 8-10MPa, and the temperature is 220-230°C.

In the above reaction method, compared with the previous reaction, the hydrogenation reaction and the cracking hydrogenation reaction both reduce the energy consumption, simultaneously improve the reaction effect, and improve the utilization rate of raw materials, especially the utilization rate of hydrogen.

The oil product obtained by the hydrogenation reaction of the anthracene oil of the invention has good quality and high yield, and the desulfurization rate can reach 99.95%.

The anthracene oil hydrogenation reaction method of the invention has low reaction temperature, greatly reduced pressure and high liquid hourly space velocity, which is equivalent to increasing the production capacity, and the final desulfurization rate is close to 100%, which is nearly 1 percentage point higher than the previous one.

Compared with the prior art, the beneficial effects of the present invention are:

(1) the reaction system of anthracene oil hydrogenation of the present invention reduces energy consumption, reduces reaction temperature, improves reaction yield, and improves the utilization rate of raw materials by combining hydrogenation reactor and micro-interface generator;

(2) the reaction system of anthracene oil hydrogenation of the present invention is most favorable for improving mass transfer effect by setting the micro-interface generator at a specific position;

(3) The reaction method for hydrogenating anthracene oil of the present invention has low reaction temperature, greatly reduced pressure and high liquid hourly space velocity, which is equivalent to increasing the production capacity, and the final desulfurization rate is close to 100%, which is nearly 1 percentage point higher than before.

Description of drawings

Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are for the purpose of illustrating preferred embodiments only and are not to be considered limiting of the invention. Also, the same components are denoted by the same reference numerals throughout the drawings. In the attached image:

1 is a schematic structural diagram of a reaction system for hydrogenation of anthracene oil provided in an embodiment of the present invention.

Description of drawings:

10-hydrogen storage tank; 20-micro interface generator;

30-anthracene oil storage tank; 40-hydrogen preheater;

50-hydrogenation reactor; 60-first separation tank;

70-the second separation tank; 80-cracking reaction tower;

90-the fourth separation tank; 100-fractionation tower;

110-the third separation tank; 120-the fifth separation tank;

801-catalyst bed; 802-cracking reaction product outlet;

1001 - Tray.

detailed description

The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings and specific embodiments, but those skilled in the art will understand that the embodiments described below are part of the embodiments of the present invention, rather than all of the embodiments, It is only used to illustrate the present invention and should not be construed as limiting the scope of the present invention. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative efforts shall fall within the protection scope of the present invention. If the specific conditions are not indicated in the examples, it is carried out according to the conventional conditions or the conditions suggested by the manufacturer. The reagents or instruments used without the manufacturer's indication are conventional products that can be purchased from the market.

In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. The indicated orientation or positional relationship is based on the orientation or positional relationship shown in the accompanying drawings, which is only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the indicated device or element must have a specific orientation or a specific orientation. construction and operation, and therefore should not be construed as limiting the invention. Furthermore, the terms "first", "second", and "third" are used for descriptive purposes only and should not be construed to indicate or imply relative importance.

In the description of the present invention, it should be noted that the terms "installed", "connected" and "connected" should be understood in a broad sense, unless otherwise expressly specified and limited, for example, it may be a fixed connection or a detachable connection Connection, or integral connection; can be mechanical connection, can also be electrical connection; can be directly connected, can also be indirectly connected through an intermediate medium, can be internal communication between two elements. For those of ordinary skill in the art, the specific meanings of the above terms in the present invention can be understood in specific situations.

In order to illustrate the technical solutions of the present invention more clearly, the following descriptions are given in the form of specific embodiments.

Example

Referring to FIG. 1, it is a reaction system for hydrogenation of anthracene oil according to an embodiment of the present invention, which mainly includes a micro-interface generator 20, a hydrogenation reactor 50 and a cracking reaction tower 80;

Hydrogen and anthracene oil are simultaneously introduced into the micro-interface generator 20, the anthracene oil is transported from the anthracene oil storage tank 30, and the hydrogen is transported from the hydrogen storage tank 10 to be preheated by the hydrogen preheater 40 and then passed into the micro-interface generator 20. In the micro-interface generator 20, after the hydrogen is dispersed and broken into small molecules, the mixture of anthracene oil and hydrogen after the dispersed and broken treatment is jointly transported to the hydrogenation reactor 50 for hydrogenation reaction;

The oil after hydrodesulfurization and denitrification comes out of the hydrogenation reactor 50 and is first separated into hot high fraction gas and hot high fraction oil through the first separation tank 60 , and then the hot high fraction gas continues to pass through the second separation tank 70 for separation , separated into cold high fraction gas and cold high fraction oil, the cold high fraction gas at the top of the second separation tank 70 goes to the subsequent fourth separation tank 90 for further separation, and the cold high fraction oil at the bottom of the second separation tank 70 is directly Go to the subsequent fifth separation tank 120 for further separation, the hot high-resolution oil from the first separation tank 60 is separated through the third separation tank 110, and the hot low-resolution oil from the bottom of the third separation tank 110 is separated from the cracking reaction. The top of column 80 enters for hydrocatalytic cracking.

The top of the cracking reaction tower 80 is fed with hydrogen, one part is new hydrogen, and the other part is the gas phase returned from the top of the fourth separation tank 90, which is first compressed by the compressor and then fed into the cracking reaction tower 80, so that the hydrogen and heat The low fraction oil enters into the cracking reaction tower 80 from the top, so as to carry out the cracking catalytic reaction.

The cracking reaction tower 80 is provided with multi-layer catalyst beds 801, preferably four catalyst beds 801, and each catalyst bed 801 is filled with catalysts. In order to improve the mass transfer effect, the top of the cracking reaction tower 80 is fed. A micro-interface generator 20 is provided at the mouth and between the adjacent catalyst beds 801 in the cracking reaction tower 80. The type of the micro-interface generator 20 is the same as the type of the micro-interface generator 20 set before the hydrogenation reactor 50. It is consistent, and the micro-interface generators 20 of the pneumatic type are selected, and the mass transfer effect of the whole reaction is improved by the synergistic effect of the micro-interface generators 20 arranged in different positions.

After the hydrocracking catalytic reaction, a cracking reaction product outlet 802 for discharging the cracking reaction product is provided at the bottom of the cracking reactor, and the material from the cracking reaction product outlet 802 goes to the fourth separation tank 90 for oil and gas separation, The oil phase separated from the bottom of the fourth separation tank 90 goes to the fifth separation tank 120 for further separation. The gas phase separated from the top of the fourth separation tank 90 is returned to the cracking reaction tower 80 and reused as a raw material for the cracking reaction.

The gas phase exiting from the top of the fifth separation tank 120 is directly discharged, and the oil phase exiting from the bottom of the fifth separation tank 120 goes to the fractionation tower 100 for fractionation. The fillers that help the fractionation effect, commonly used fillers can be Raschig rings, Pall rings, etc.

After the fractionation of the fractionation tower 100, the overhead gas from the top of the tower is discharged through the pipeline, the tail oil from the bottom of the fractionation tower 100 is discharged through the pipeline, and the different fractions from the middle of the column section of the fractionation tower 100 are collected separately, and the different fractions Mainly for liquefied gas, naphtha, fuel oil and so on.

In the above embodiment, in order to increase the effect of dispersion and mass transfer, additional micro-interface generators 20 can also be added, and the installation position is not limited. The side walls of the micro-interface generators 20 are arranged opposite to each other, so as to realize the hedge of the micro-bubbles coming out of the outlet of the micro-interface generator 20 .

In the above embodiment, the type of the hydrogenation reactor 50 can be not only a fixed-bed reactor, but also other types such as a ebullated-bed reactor. In addition, the way of feeding and discharging materials is not limited, and can be fed from below. The top discharging method can also be used for the top feeding and the bottom discharging method, but the method of side feeding and top discharging is more preferable.

In the above embodiment, there is no specific requirement for the number of pump bodies, which can be set at corresponding positions as required.

The working process and principle of the anthracene oil hydrogenation reaction system of the present invention are briefly described below:

Nitrogen purges each equipment in the reaction system, and then starts to operate. Hydrogen and anthracene oil are first subjected to hydrogenation reaction in hydrogenation reactor 50. Before the hydrogenation reaction, hydrogen and anthracene oil are first introduced into the micro-interface to generate After the dispersion and crushing in the vessel 20, the gas forms micro-bubbles, which is more conducive to the efficient reaction. After the hydrogenation reaction, the reaction product is separated by the separation tank and then goes to the cracking reaction tower 80 for catalytic cracking reaction. After the cracking reaction product comes out After separation, it goes to the fractionation tower 100 for fractionation to obtain the final product.

Wherein, the pressure of the above hydrogenation reaction is 8-10MPa, and the temperature of the hydrogenation reaction is 220-230°C.

The pressure of cracking and hydrogenation is 8-10MPa, and the temperature is 220-230℃. By setting the micro-interface generator 20, the operating pressure and temperature are correspondingly reduced, the energy consumption is reduced, and the production capacity is improved.

The above process steps are cycled back and forth to make the entire synthesis system run smoothly.

By adopting the hydrogenation reaction process of the present invention, the removal rate of desulfurization can reach 99.95%, which is increased by nearly 1 percentage point compared with the previous hydrogenation reaction process.

In addition, by laying the micro-interface generator, the pressure and temperature of the hydrogenation reactor are reduced, and the energy consumption is fully reduced.

In a word, compared with the reaction system for hydrogenation of anthracene oil in the prior art, the reaction system for hydrogenation of anthracene oil of the present invention has fewer equipment components, small footprint, low energy consumption, low cost, high safety, and controllable reaction. , the raw material conversion rate is high, which is equivalent to providing a reaction system with stronger operability for the field of anthracene oil hydrogenation, which is worthy of widespread application.

Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, but not to limit them; although the present invention has been described in detail with reference to the foregoing embodiments, those of ordinary skill in the art should understand that: The technical solutions described in the foregoing embodiments can still be modified, or some or all of the technical features thereof can be equivalently replaced; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the technical solutions of the embodiments of the present invention. Scope.

Claims (10)

1. A reaction system for hydrogenation of anthracene oil, comprising: a micro-interface generator and a hydrogenation reactor connected in sequence;

   Hydrogen and anthracene oil are introduced into the micro-interface generator; a hydrogenation product outlet is provided on the side wall of the hydrogenation reactor, and the product from the hydrogenation product outlet is passed into the first separation tank for separation Hot high fraction gas and hot high fraction oil, the hot high fraction gas goes to the second separation tank to be separated into cold high fraction gas and cold high fraction oil; the hot high fraction oil goes to the third separation tank and goes to the third The separation tank is separated into hot low fraction gas and hot low fraction oil, and after the hot low fraction oil enters the cracking reaction tower for cracking reaction, the obtained cracking reaction product goes to the fractionation tower for fractionation, and the cold high fraction gas, Cold high fraction oil and hot low fraction gas are collected and discharged separately.
2. The reaction system according to claim 1, wherein the cracking reaction tower is provided with multi-layer catalyst beds, and each of the catalyst beds is filled with a catalyst; the top of the cracking reaction tower is fed with hydrogen , the hydrogen is pre-compressed by a compressor, and the hot low-divided oil enters from the top of the cracking reaction tower.
3. The reaction system according to claim 2, characterized in that, the bottom of the cracking reaction tower is provided with a cracking reaction product outlet for discharging the cracking reaction product, and the cracking reaction product outlet is connected to a second outlet for oil and gas separation. Four separation tanks, the oil phase separated from the bottom of the fourth separation tank goes to the fractionation tower.
4. The reaction system according to claim 3, wherein the oil phase separated from the bottom of the fourth separation tank goes to the fifth separation tank for further separation, and then the oil phase separated from the bottom of the fifth separation tank goes to the fifth separation tank for further separation. to the fractionation tower.
5. The reaction system according to claim 3, wherein the gas phase separated from the top of the fourth separation tank is returned to the cracking reaction tower to perform the cracking reaction again.
6. The reaction system according to claim 4, characterized in that, the cold high fraction gas from the top of the second separation tank goes to the fourth separation tank for further separation.
7. The reaction system according to claim 4, wherein the cold high-separate oil from the bottom of the second separation tank goes to the fifth separation tank for further separation.
8. The reaction system according to any one of claims 1 to 7, wherein the fractionation tower is provided with multi-layer trays, the trays are filled with packings that contribute to the fractionation effect, and the fractionation tower is The top gas from the top of the column is discharged through the pipeline, the tail oil from the bottom of the fractionation column is discharged through the pipeline, and the different fractions from the middle part of the column section of the fractionation column are collected separately.
9. Adopt the reaction method of the anthracene oil hydrogenation reaction system described in any one of claim 1-8, is characterized in that, comprises:

   The anthracene oil and hydrogen mixed micro-interface are dispersed and broken, and then hydrogenation reaction is carried out, and then separation, hydrocracking, gas-liquid separation and fractionation are carried out.
10. The reaction method according to claim 9, wherein the pressure of the hydrogenation reaction is 8-10MPa, and the temperature of the hydrogenation reaction is 220-230°C;

    Preferably, the pressure of the hydrocracking is 8-10MPa, and the temperature is 220-230°C.

Images