Styrene tar utilization method and utilization system

Abstract

The invention relates to the field of petrochemical waste treatment, and discloses a styrene tar utilization method and system, and the method comprises the following steps: when a coke tower is shifted to a coke forming period, styrene tar and a heated coking raw material are mixed, and are introduced into the coke tower from the bottom of the coke tower for delayed coking reaction; wherein the conditions of the coke forming period are as follows: the operation temperature is 480-500 DEG C. According to the method disclosed by the invention, the styrene tar is used as a resource to be recycled in the coking tower, so that the hazardous waste treatment cost is saved, waste recycling is realized, the product value is increased, the production cost of an enterprise is reduced, the method does not cause coking of equipment such as a fractionating tower, and safe and stable operation of the reaction is ensured.

Description

Technical Field

[0001] The invention relates to the technical field of petrochemical waste treatment, and in particular to a styrene tar utilization method and utilization system. Background Art

[0002] Styrene tar is the residue produced during the distillation and purification of styrene. Its main components are styrene polymers and styrene derivatives and oligomers with complex compositions. Since styrene tar is easy to self-polymerize at low temperatures, its properties are unstable, and it is difficult to store, most manufacturers burn it as fuel or treat it as hazardous waste, and fail to recycle styrene tar well.

[0003] In order to realize the recycling of styrene tar, styrene tar is mainly used as fuel oil, but the overall utilization rate is not high and the economic value is low. According to relevant literature reports, when styrene tar is used as boiler or cracking furnace fuel, it is not easy to burn, and it is easy to produce black smoke or coking when burning, causing environmental pollution; using styrene tar liquid instead of cheap asphalt as waterproof material, but this is not only a huge waste, but also pollutes the environment; using styrene tar to recover styrene, inhibitor process, etc., but its process is complicated, the operation is difficult, the equipment investment is high, and it is easy to cause catalyst carbon deposition and accelerate catalyst deactivation; using styrene tar to enter the catalytic cracking unit for recycling, but this method has been verified by some companies, or there are problems such as blocking the reactor riser, or the flow meter is inaccurate due to styrene self-polymerization, causing large fluctuations in the device. Summary of the invention

[0004] The purpose of the present invention is to solve the problem of low utilization rate of styrene tar and easy coking of equipment when using styrene tar, and to provide a styrene tar utilization system and utilization method. The utilization method can realize safe, stable and simple waste utilization of styrene tar, reduce the production cost of the device, and increase the added value of the enterprise.

[0005] The first aspect of the present invention provides a method for utilizing styrene tar, the method comprising:

[0006] When the coke drum enters the coking period, the styrene tar is mixed with the heated coking raw materials and introduced into the coke drum from the bottom of the coke drum for delayed coking reaction;

[0007] Among them, the conditions during the coking period include: an operating temperature of 480-500°C.

[0008] A second aspect of the present invention provides a styrene tar utilization system, the system comprising:

[0009] A coking raw material supply unit, used for supplying coking raw materials into the system;

[0010] A styrene tar supply unit, used for supplying styrene tar into the system;

[0011] A heating unit, the heating unit comprising a heating furnace for heating the coking raw material,

[0012] Coke unit, used for delayed coking reaction of styrene tar and heated coking raw materials;

[0013] Wherein, the coke unit includes one or at least two parallel coke towers; the outlet side of the coking raw material supply unit is connected to the inlet side of the heating unit; the outlet side of the heating unit and the outlet side of the styrene tar supply unit are connected to the bottom of the coke tower.

[0014] Compared with the prior art, the present invention has at least the following beneficial effects:

[0015] (1) Styrene tar is recycled in the coke tower, which reduces the cost of hazardous waste treatment, realizes waste recycling, increases product yield, and improves the added value of the device;

[0016] (2) Styrene tar is mixed with the heated coking raw materials and introduced into the coke tower from the bottom of the coke tower for delayed coking reaction, so as to shorten the recycling process and reduce the impact of the agglomeration reaction during the recycling process on the normal production of the equipment. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] Figure 1 Schematic diagram of a styrene tar utilization system in one embodiment of the present invention.

[0018] Description of Reference Numerals

[0019] 1. Coke tower V001 2. Coke tower V002

[0020] 3. Filter 4. Pump

[0021] 5. Heating furnace A, coking raw materials

[0022] B. Styrene tar C. Oil and gas

[0023] D. Circulating oil DETAILED DESCRIPTION

[0024] The endpoints and any values ​​of the ranges disclosed in this article are not limited to the precise 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, the endpoint values ​​of each range and the individual point values, and the individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed in this article.

[0025] The first aspect of the present invention provides a method for utilizing styrene tar, the method comprising:

[0026] When the coke drum enters the coking period, the styrene tar is mixed with the heated coking raw materials and introduced into the coke drum from the bottom of the coke drum for delayed coking reaction;

[0027] Among them, the conditions during the coking period include: an operating temperature of 480-500°C.

[0028] In the present invention, the transition of the coke drum into the coking period refers to the transition of the coke drum from the non-operating period or from the coke drum into the coking period under the coking conditions after the end of the decoking period.

[0029] In the present invention, the method of the present invention can achieve safe, stable and simple waste utilization of styrene tar, reduce the production cost of the device, and improve the added value of the enterprise; compared with the existing process, the inventor found that the mixing of styrene tar with the heated coking raw material and entering the coke tower for reaction will not cause coking of equipment such as the distillation tower, the raw material heating furnace and the feed pipeline, and can ensure the safe and stable operation of the equipment. The inventor speculates that the mixing of styrene tar with the heated coking raw material causes the temperature to rise rapidly, the gasification rate to increase rapidly, the pipeline flow rate to increase, and the rapid advancement to the coke tower Reaction, at the same time, styrene tar and the heated coking raw materials enter the coking tower from the bottom of the coking tower, which can realize that styrene tar enters the high-temperature coke tower reaction at the fastest speed and shortest distance to realize a series of reactions, thereby increasing the maximum reaction degree of styrene tar, and there may be only a small amount of unreacted toluene, ethylbenzene and styrene monomer and other low molecular weight compounds entering the distillation tower for separation with the high-temperature oil and gas after the reaction, which will not only not cause coking and other phenomena, but can also be mixed with gasoline and other side products to enter the downstream device for recycling again, thereby realizing waste recycling, increasing product value and reducing enterprise production costs.

[0030] According to the present invention, as mentioned above, styrene tar is the residue produced during the distillation and purification of styrene, and its main components are styrene polymers and styrene derivatives and oligomers with complex compositions. Its specific composition is not limited. In the present invention, as shown in Table 1, the styrene tar in Table 1 is used as an example to illustrate the methods in the embodiments and examples of the present invention, but the present invention is not limited to the styrene tar shown in Table 1.

[0031] Table 1

[0032]

[0033]

[0034] According to the method of the present invention, as long as the purpose of the present invention can be achieved, technicians in this field can select the desired coking raw materials as needed. In some embodiments, the coking raw materials include one or more of mixed residual oil, catalytic oil slurry and deoiled asphalt mixed raw materials.

[0035] According to the method of the present invention, as long as the purpose of the present invention can be achieved, the temperature of the heated coking raw material is not limited. In some embodiments, the temperature of the heated coking raw material is greater than 482° C., preferably 485-495° C., for example, 485° C., 490° C. or 500° C. The aforementioned embodiment is adopted to increase the pipeline flow rate, quickly advance the reaction in the coke drum, and better ensure the coking effect, so as to obtain sponge coke and / or shot coke with higher practical value.

[0036] According to the method of the present invention, as long as the purpose of the present invention can be achieved, the operating pressure during the coking period is not limited and can be selected according to different coking raw materials. In some embodiments, the conditions during the coking period also include: the operating pressure is 0.1-0.18 MPa, preferably 0.1-0.12 MPa. The above embodiment can increase the yield of the liquid product.

[0037] According to the method of the present invention, as long as the purpose of the present invention can be achieved, the amount of the styrene tar introduced is not limited. In some embodiments, the amount of styrene tar is 0.01-2wt% of the coking raw material, such as 0.01wt%, 0.05wt%, 0.1wt%, 0.25wt%, 0.3wt%, 0.4wt%, 0.5wt%, 1wt% or 2wt%, preferably 0.1-0.5wt%. The above embodiment can increase the yield of liquid products and obtain sponge coke and / or shot coke with higher practical value.

[0038] According to the method of the present invention, in some preferred embodiments, the flow rate of the coking raw material is 150-250 t / h, such as 150 t / h, 200 t / h, 230 t / h, 240 t / h or 250 t / h, preferably 200-240 t / h; in some preferred embodiments, the flow rate of the styrene tar is 0.01-3 t / h, such as 0.01 t / h, 0.05 t / h, 0.1 t / h, 0.2 t / h, 0.5 t / h, 0.8 t / h, 1 t / h, 1.5 t / h, 2 t / h or 3 t / h, preferably 0.2-1 t / h. By adopting the above preferred embodiments, the yield of liquid products can be increased and the yield of coke can be reduced, and the coke obtained is sponge coke and / or shot coke with higher practical value.

[0039] When the coke drum is performing delayed coking reaction, it is an intermittent reaction. According to the method of the present invention, in some embodiments, a coking operation cycle is from switching the feed to filling the coke drum and changing the drum. One coking operation cycle is 18-24 hours, preferably 20-24 hours.

[0040] According to the method of the present invention, in some embodiments, the method of the present invention further comprises discharging the oil and gas generated by the delayed coking reaction in the coke tower from the top of the tower into a fractionation tower for fractionation to obtain liquid products and gas products;

[0041] According to the method of the present invention, in some embodiments, the method of the present invention further comprises that the coke generated by the delayed coking reaction in the coke drum remains in the coke drum;

[0042] According to the method of the present invention, in some preferred embodiments, the liquid product includes one or more of gasoline, diesel, wax oil, cycle oil, dry gas, liquefied gas and petroleum coke.

[0043] According to the method of the present invention, in some preferred embodiments, the coke includes sponge coke and / or shot coke.

[0044] According to the method described in the present invention, the inventors found that the obtained coke is solid and has no sticky oil on the surface, which is not only beneficial to the subsequent decoking step, but also further illustrates that most of the styrene tar has reacted with the coking raw materials, thereby fully realizing the utilization of styrene tar.

[0045] According to the method of the present invention, in some embodiments, the circulation ratio during the delayed coking reaction is 0-0.4, preferably 0.1-0.15. The quality of the circulating oil obtained during the fractionation is better than that of the coking raw material. By adopting the above-mentioned embodiment, the utilization rate of styrene tar can be increased to a certain extent, and the degree of coking can be reduced.

[0046] In the present invention, the circulation ratio refers to the ratio of the flow rate of part or all of the circulating oil mixed with the coking feedstock to the flow rate of the coking feedstock. The circulating oil is the liquid product. It can be understood that when the circulation ratio is 0, no circulating oil is mixed with the coking feedstock.

[0047] According to the method of the present invention, in some embodiments, part or all of the circulating oil is filtered before being mixed with the coking feedstock. By adopting the above embodiment, some solid matter in the circulating oil can be filtered to reduce the degree of coking.

[0048] According to the method of the present invention, in some embodiments, the gasoline includes a fraction at 25-250°C.

[0049] According to the method of the present invention, in some embodiments, the diesel comprises a fraction at 169-405°C.

[0050] According to the method of the present invention, in some embodiments, the wax oil includes a fraction at 250-630°C.

[0051] According to the method of the present invention, as mentioned above, when the coke drum is performing the delayed coking reaction, it is an intermittent reaction, and two or more coke drums can be used for alternating reactions as needed. After the coking operation cycle in one coke drum is completed, another coke drum can be used to continue the delayed coking reaction. In some embodiments, the method described in the present invention also includes: after a coking operation cycle in the coke drum is completed, steam is optionally used to purge the pipeline, and then decoking is performed.

[0052] According to the method of the present invention, as long as the purpose of the present invention can be achieved, the decoking method is not limited. In some embodiments, the decoking method is hydraulic decoking; preferably, the pressure of the hydraulic decoking is 32-35 MPa.

[0053] According to the method of the present invention, a person skilled in the art can select a specific operation method of hydraulic decoking as required, and the operation method of hydraulic decoking will not be described in detail in the present invention.

[0054] The second aspect of the present invention provides a styrene tar utilization system, the system comprising:

[0055] A coking raw material supply unit, used for supplying coking raw materials into the system;

[0056] A styrene tar supply unit, used for supplying styrene tar into the system;

[0057] A heating unit, used for heating coking raw materials;

[0058] Coke unit, used for delayed coking reaction of styrene tar and heated coking raw materials;

[0059] Wherein, the coke unit includes one or at least two parallel coke towers; the outlet side of the coking raw material supply unit is connected to the inlet side of the heating unit; the outlet side of the heating unit and the outlet side of the styrene tar supply unit are connected to the bottom of the coke tower.

[0060] According to the present invention, in some preferred embodiments, the outlet side of the heating unit and the outlet side of the styrene tar supply unit are connected to the bottom of the coke drum via a four-way valve. With the above embodiment, at least two parallel coke drums can be better switched for use.

[0061] According to the present invention, in some embodiments, the system of the present invention further comprises a fractionation tower for fractionating the oil and gas generated by the delayed coking reaction into liquid products and gas products.

[0062] According to the present invention, in some preferred embodiments, the top of the coke tower is connected to a fractionation tower.

[0063] According to the present invention, in some preferred embodiments, the fractionation tower is provided with discharge ports for drawing out liquid products and gaseous products.

[0064] According to the present invention, the outlets for leading out liquid products and gas products can be set as needed, which will not be described in detail here.

[0065] According to the present invention, in some preferred embodiments, the fractionation tower is connected to the inlet side of the heating unit for introducing all or part of the liquid product as circulating oil to be mixed with the coking feedstock into the heating unit.

[0066] According to the present invention, in some more preferred embodiments, a filter is further provided on the connection line between the distillation tower and the heating unit, for filtering all or part of the liquid product and introducing it into the heating unit as circulating oil; in some more preferred embodiments, a pump is provided on the inlet side of the heating unit, for introducing circulating oil and / or coking feedstock into the heating unit.

[0067] According to the present invention, the devices can be connected by pipelines as needed, and the pipelines can be cross-connected. It is understood that the heating wire can be set according to the required temperature. In addition, in order to avoid high-temperature heating directly heating the medium in the pipeline, the pipeline and the heating wire can use insulation materials as needed. No further details will be given here.

[0068] According to the present invention, in one embodiment, Figure 1 As shown, a method for utilizing styrene tar, the method comprises: Figure 1 The method is performed in a system comprising:

[0069] When the coke drum enters the coking period, under the conditions of the coking period, the coking raw material A is pressurized by the pump 4 and then enters the heating furnace 5 in the heating unit for heating. The styrene tar B is mixed with the coking raw material A heated by the heating furnace 5 and then introduced from the bottom of the coke drum V001 1 into the coke drum V001 1 for delayed coking reaction. The oil and gas generated by the delayed coking reaction in the coke drum V001 1 are discharged from the top of the tower and enter into a fractionation tower (not shown) for fractionation to obtain liquid products and gas products. The coke generated by the delayed coking reaction in the coke drum V001 1 remains in the coke drum V001 1; at the same time, according to the required circulation ratio, part or all of the liquid product is drawn out from the bottom of the distillation tower as the circulating oil D to circulate back to the inlet side of the heating unit, and after being filtered by the filter 3, it enters the pump 4 together with the coking raw material A for pressurization, and then continues to enter the heating furnace 5 in the heating unit to mix with the styrene tar B to continue the delayed coking reaction. After one coking operation cycle is completed, the feeding of styrene tar B and the coking raw material A is stopped, and after the pipeline is purged with steam, the generated coke is removed by switching the four-way valve, and the coke tower V001 1 is used for hydraulic decoking to remove the generated coke. At the same time, the coking tower V002 2 enters another coking period to carry out the delayed coking reaction.

[0070] The present invention will be described in detail below by way of examples. In the following examples,

[0071] The liquid product yield, gas product yield and coke product yield are obtained based on flow meter statistics.

[0072] The carbon residue of wax oil is obtained by testing with a carbon residue meter.

[0073] Example 1

[0074] like Figure 1As shown, a method for utilizing styrene tar comprises: when the coke tower V001 1 enters the coke-making period, under the conditions of the coke-making period, the coking raw material A (mixed residual oil raw material with a flow rate of 230 t / h) is pressurized to 3.5 MPa by a pump 4 and then enters the heating furnace 5 included in the heating unit and is heated to 485° C., styrene tar B (with a flow rate of 0.8 t / h) is mixed with the coking raw material A heated by the heating furnace 5 included in the heating unit and then introduced from the bottom of the coke tower V001 1 into the coke tower V001 1 for delayed coking reaction (operating temperature is 490° C., operating pressure is 0.11 MPa), the oil gas C generated by the delayed coking reaction in the coke tower V001 1 is discharged from the top of the tower and enters the fractionation tower (not shown) for fractionation to obtain liquid products and gas products, and the coke generated by the delayed coking reaction in the coke tower V001 1 remains in the coke tower V001 1 1; at the same time, the circulation ratio is set to 0.12, and the liquid product is drawn out from the bottom of the distillation tower (not shown) as the circulating oil D to circulate back to the inlet side of the heating unit, and after being filtered by the filter 3, it enters the pump 4 together with the supplementary coking raw material as the coking raw material to be pressurized to 3.5MPa, and then continues to enter the heating unit to be heated to 485℃ and mixed with styrene tar to continue the delayed coking reaction. After the end of an operation cycle of coking for 20h, the feeding of styrene tar and coking raw material is stopped, and after the pipeline is purged with steam, the generated coke is removed by switching the four-way valve, and the coke tower V001 1 is used for hydraulic decoking to remove the generated coke. At the same time, the coking tower V002 2 enters another coking period to carry out the delayed coking reaction.

[0075] After the test, it was found that after a coking operation cycle, there was no coking in the distillation tower and pipelines.

[0076] The obtained liquid products include gasoline with a fraction of 25-240°C, diesel with a fraction of 169-405°C, and wax oil with a fraction of 250-492°C.

[0077] The yield of liquid products, gas product yield, coke product yield, residual carbon in wax oil, and the form of coke are shown in Table 2.

[0078] Example 2

[0079] According to the method of Example 1, the difference is

[0080] The flow rate of mixed residual oil raw material is 250t / h, and the flow rate of styrene tar is 1t / h; the operating temperature is 495℃, the operating pressure is 0.11MPa, the circulation ratio is 0.12, and the operating cycle is 18h;

[0081] After the test, it was found that after a coking operation cycle, there was no coking in the distillation tower and pipelines.

[0082] The yield of liquid products, gas product yield, coke product yield, residual carbon in wax oil, and the form of coke are shown in Table 2.

[0083] Example 3

[0084] The method of Example 1 is different from that of Example 1:

[0085] The flow rate of mixed residual oil raw material is 200t / h, and the flow rate of styrene tar is 0.5t / h; the operating temperature is 485℃, the operating pressure is 0.12MPa, the circulation ratio is 0.15, and the operating cycle is 20h;

[0086] After the test, it was found that after a coking operation cycle, there was no coking in the distillation tower and pipelines.

[0087] The yield of liquid products, gas product yield, coke product yield, residual carbon in wax oil, and the form of coke are shown in Table 2.

[0088] Example 4

[0089] The method of Example 1 is different from that of Example 1:

[0090] The flow rate of styrene tar is 4 t / h.

[0091] After the test, it was found that after an operation cycle of coking, there was slight coking in the distillation tower and pipelines.

[0092] The yield of liquid products, gas product yield, coke product yield, residual carbon in wax oil, and the form of coke are shown in Table 2.

[0093] Example 5

[0094] The method of Example 1 is different from that of Example 1:

[0095] The flow rate of styrene tar is 0.1 t / h.

[0096] After the test, it was found that after an operation cycle of coking, there was slight coking in the distillation tower and pipelines.

[0097] The yield of liquid products, gas product yield, coke product yield, residual carbon in wax oil, and the form of coke are shown in Table 2.

[0098] Example 6

[0099] The method of Example 1 is different from that of Example 1:

[0100] The coking raw material enters the heating unit and is heated to 480°C; after being filtered through the filter, it enters the pump together with the coking raw material and is pressurized to 3.5MPa, and then continues to enter the heating unit and is heated to 480°C.

[0101] After the test, it was found that after a coking operation cycle, there was no coking in the distillation tower and pipelines.

[0102] The yield of liquid products, gas product yield, coke product yield, residual carbon in wax oil, and the form of coke are shown in Table 2.

[0103] Example 7

[0104] The method of Example 1 is different from that of Example 1:

[0105] The coking raw materials enter the heating unit and are heated to 500°C; after being filtered through the filter, they enter the pump together with the coking raw materials and are pressurized to 3.5MPa, and then continue to enter the heating unit and are heated to 500°C.

[0106] After the test, it was found that after a coking operation cycle, there was no coking in the distillation tower and pipelines.

[0107] The yield of liquid products, gas product yield, coke product yield, residual carbon in wax oil, and the form of coke are shown in Table 2.

[0108] Comparative Example 1

[0109] A method for utilizing styrene tar, the method comprising: when a coke drum enters a coke-generating period, under the conditions of the coke-generating period, a coking raw material (mixed residual oil raw material with a flow rate of 240 t / h) and styrene tar (with a flow rate of 0.8 t / h) are mixed, pressurized to 3.5 MPa by a pump, and then enter a heating furnace 55 included in a heating unit, heated to 485° C., and then introduced from the bottom of the coke drum into the coke drum for delayed coking reaction (operating temperature of 490° C., operating pressure of 0.12 MPa), the oil and gas generated by the delayed coking reaction in the coke drum are discharged from the top of the tower and enter a fractionation tower for fractionation to obtain liquid products and gas products, and the coke generated by the delayed coking reaction in the coke drum is retained in the coke drum; at the same time, The fixed circulation ratio is 0.12, and the circulating oil is drawn out from the bottom of the distillation tower and circulated back to the inlet side of the heating unit. After being filtered by the filter, the materials mixed with the coking raw material (the flow rate of the mixed residual oil raw material is 240t / h) and styrene tar (the flow rate is 0.8t / h) enter the pump together and are pressurized to 0.7MPa. After that, they continue to enter the heating unit to be heated to 485℃ and mixed with styrene tar to continue the delayed coking reaction. After an operation cycle of coking for 20h, the feeding of styrene tar and coking raw materials is stopped, and after the pipeline is purged with steam, the four-way valve is switched and hydraulic decoking is used in the coke tower to remove the generated coke. At the same time, the coke tower enters another coking period for delayed coking reaction.

[0110] After the test, it was found that after an operation cycle of coking, a lot of coking was deposited in the distillation tower and pipelines.

[0111] The obtained liquid products include gasoline with a fraction of 25-245°C, diesel with a fraction of 169-398°C, and wax oil with a fraction of 262-405°C.

[0112] The yield of liquid products, the yield of gas products, the yield of coke products, the residual carbon of wax oil, and the form of coke are shown in Table 2.

[0113] Table 2

[0114]

[0115] It can be seen from the results in Table 1 that the styrene tar utilization method of the present invention not only has a good liquid product yield, but also has low residual carbon in the wax oil in the liquid product, and can obtain coke with high practical value, and can reduce coking in the distillation tower and pipeline.

[0116] The preferred embodiments of the present invention are described in detail above, but the present invention is not limited thereto. Within the technical concept of the present invention, the technical solution of the present invention can be subjected to a variety of simple modifications, including the combination of various technical features in any other suitable manner, and these simple modifications and combinations should also be regarded as the contents disclosed by the present invention and belong to the protection scope of the present invention.

Claims

1. A method for utilizing styrene tar, characterized in that: The method includes: When the coke drum enters the coking period, the styrene tar is mixed with the heated coking raw materials and introduced into the coke drum from the bottom of the coke drum for delayed coking reaction; Among them, the conditions during the coking period include: an operating temperature of 480-500°C.

2. The method according to claim 1, wherein: The coking feedstock includes one or more of mixed residual oil, catalytic slurry oil and deoiled asphalt mixed feedstock; and / or The temperature of the heated coking raw material is greater than 482°C, preferably 485-495°C.

3. The method according to claim 1 or 2, wherein: The conditions during the coking period also include: an operating pressure of 0.1-0.18 MPa, preferably 0.1-0.12 MPa; and / or The amount of styrene tar is 0.01-2 wt %, preferably 0.1-0.5 wt % of the coking raw material.

4. The method according to any one of claims 1 to 3, wherein: The flow rate of the coking raw material is 150-250 t / h, preferably 200-240 t / h; and / or The flow rate of the styrene tar is 0.01-3 t / h, preferably 0.2-1 t / h.

5. The method according to any one of claims 1 to 4, wherein: From switching the feed to filling the coke tower and changing the tower is a coking operation cycle, and a coking operation cycle is 18-24 hours, preferably 20-24 hours.

6. The method according to any one of claims 1 to 5, wherein: The method further includes: The oil and gas generated by the delayed coking reaction in the coke tower is discharged from the top of the tower and enters the fractionation tower for fractionation to obtain liquid products and gas products; and / or The coke generated by the delayed coking reaction in the coke drum remains in the coke drum; Preferably, the liquid product comprises one or more of gasoline, diesel, wax oil, dry gas, liquefied gas and petroleum coke; and / or Coke includes sponge coke and / or shot coke; More preferably, the circulation ratio during the delayed coking reaction is 0-0.4, preferably 0.1-0.15, wherein the circulation ratio refers to the ratio of the flow rate of part or all of the circulating oil mixed with the coking feedstock to the flow rate of the coking feedstock, wherein the circulating oil is the liquid product; More preferably, part or all of the circulating oil is filtered before being mixed with the coking feedstock.

7. The method according to claim 6, wherein: Gasoline including a fraction between 25 and 250°C; and / or Diesel oil includes a fraction having a temperature of 169-405°C; and / or Wax oil includes the fraction at 250-630°C.

8. The method according to any one of claims 1 to 7, wherein: The method further comprises: completing a coking operation cycle in the coke drum, optionally using steam to purge the pipeline, and then decoking; Preferably, the decoking method is hydraulic decoking; More preferably, the hydraulic decoking pressure is 32-35 MPa.

9. A styrene tar utilization system, characterized in that: The system includes: A coking raw material supply unit, used for supplying coking raw materials into the system; A styrene tar supply unit, used for supplying styrene tar into the system; A heating unit, the heating unit comprising a heating furnace for heating the coking raw material, Coke unit, used for delayed coking reaction of styrene tar and heated coking raw materials; Wherein, the coke unit includes one or at least two parallel coke towers; the outlet side of the coking raw material supply unit is connected to the inlet side of the heating unit; the outlet side of the heating unit and the outlet side of the styrene tar supply unit are respectively connected to the bottom of the coke tower.

10. The system according to claim 9, wherein: The outlet side of the heating unit and the outlet side of the styrene tar supply unit are connected to the bottom of the coke drum through a four-way valve; and / or The system also includes a fractionation tower for fractionating the oil and gas generated by the delayed coking reaction to obtain liquid products and gas products; Preferably, the top of the coke tower is connected to a fractionation tower; and / or The fractionation tower is provided with a discharge port for drawing out liquid products and gas products; More preferably, the fractionation tower is connected to the inlet side of the heating unit for introducing all or part of the liquid product as circulating oil to be mixed with the coking feedstock into the heating unit; More preferably, a filter is provided on the connection line between the fractionation tower and the heating unit, for filtering all or part of the liquid product and introducing it into the heating unit as circulating oil; and / or The inlet side of the heating unit is provided with a pump for introducing circulating oil and / or coking raw materials into the heating unit.

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