KR101133369B1 - Process for the preparation of clean fuel and aromatics from hydrocarbon mixtures catalytic cracked on fluid bed - Google Patents

Abstract

The present invention relates to a petroleum refining method for producing a variety of high-value clean petroleum products and aromatic products (Benzene / Toluene / Xylene), more specifically, low-pollution such as LPG, low sulfur diesel oil from fluidized bed catalytic cracking oil A method for efficiently producing petroleum products and aromatic products together.

Fluidized Bed Catalytic Cracking, LPG, Low Sulfur Diesel, Aromatic, BTX

Description

Process for the preparation of clean fuel and aromatics from hydrocarbon mixtures catalytic cracked on fluid bed

The present invention relates to a process for producing a variety of clean petroleum products and aromatic products having high value from the fluidized bed catalytic cracking oil, more specifically, distillation process, hydrodesulfurization / denitrification process of the oil from the fluidized bed catalytic cracking process And a low pollution petroleum product such as LPG, low sulfur diesel, and aromatic products (Benzene / Toluene / Xylene) by passing through a hydrocracking / dealkylation process.

Techniques for the efficient production of petrochemicals and their intermediates from fluidized bed catalytic cracking are well known:

(1) a process for preparing a reformate from a fluidized bed catalytic cracking gasoline via catalytic reforming and isolating it to produce an aromatic product;

(2) a process for producing a low sulfur diesel product from hydrobed catalytic cracking via hydrodesulfurization; And

(3) Process for producing low sulfur diesel, LPG and naphtha via hydrocracking from fluid bed catalytic cracking.

However, the above technique (1) is limited to the middle boiling point gasoline fraction having a low octane number in the fluidized bed catalytic cracking gasoline, and there is a problem that the production of LPG and low-sulfur diesel that increases demand is impossible.

The technique as described in (2) has the advantage that it can meet the demand of low-sulfur diesel by hydrodesulfurization alone or mixed with light gas oil produced in the atmospheric distillation step of crude oil alone or fluidized bed catalytic cracking. There was a problem that cannot be coped with the increasing demand for aromatic products.

The above-described technology (3) can cope with the increase in demand for low-sulfur diesel and LPG with high cetane number, and can produce naphtha, which is continuously increasing in demand, but it is not easy to control process severity. There is a problem in that it is not possible to flexibly cope with the stepwise reinforcement of the product, the hydrogen consumption is very large compared to the technique of (2) above, and the aromatic product cannot be manufactured.

It is an object of the present invention to provide a new process which is capable of efficiently producing a low pollution petroleum product, such as LPG, low sulfur diesel, and aromatic products, from a fluidized bed catalytic cracking fraction.

Still another object of the present invention is to provide a method of improving the efficiency of the alkylate manufacturing process, which is a satellite process of the shear fluidized bed catalytic cracking process, by utilizing LPG produced by the above method.

Still another object of the present invention is to provide a method of improving the efficiency of the entire process by efficiently producing hydrogen required for the hydrogenation reaction by utilizing the fuel gas emitted from the method.

In order to achieve the above object, a method for producing low-polluting petroleum products and aromatic products from the fluidized bed catalytic cracking oil according to the present invention comprises the steps of: (a) distilling the fluidized bed catalytic cracked oil to separate the effluent oil and the residual oil; (b) removing sulfur compounds and nitrogen compounds contained in the effluent oil by hydrodesulfurization / denitrification reaction of the effluent oil obtained in step (a); (c) converting the aromatic hydrocarbon compound in the effluent oil subjected to the hydrodesulfurization / denitrification reaction into an aromatic hydrocarbon mixture rich in benzene, toluene, and xylene through a hydrogenation dealkylation reaction, and LPG through a hydrocracking reaction. Hydrocracking / dealkylation step, converting to a rich non-aromatic hydrocarbon mixture; (d) separating and recovering fuel gas, LPG and aromatic products from the aromatic hydrocarbon mixture and LPG-rich non-aromatic hydrocarbon mixture produced in step (c), respectively; And (e) obtaining low sulfur diesel oil by hydrodesulfurization / denitrification of the residual oil obtained from step (a).

According to the present invention, LPG, low-sulfur diesel and aromatic products can be efficiently produced together from the fractions of aromatic products and fluidized bed catalytic cracking processes containing almost no LPG. Can be adjusted via

In addition, by supplying the C4 fraction obtained in accordance with the present invention as a raw material of the alkylate production process, which is a satellite process of the fluidized bed catalytic cracking process, the overall efficiency of the fluidized bed catalytic cracking process can be improved, and the fuel gas produced by the process is the raw material of the hydrogen production process. By using it can maximize the improvement efficiency.

The method for producing low pollution petroleum products and aromatic products from the fluidized bed catalytic cracking oil according to the present invention comprises the steps of: (a) distilling the fluidized bed catalytic cracked oil to separate the effluent oil and the residual oil; (b) removing sulfur compounds and nitrogen compounds contained in the effluent oil by hydrodesulfurization / denitrification reaction of the effluent oil obtained in step (a); (c) converting the aromatic hydrocarbon compound in the effluent oil subjected to the hydrodesulfurization / denitrification reaction into an aromatic hydrocarbon mixture rich in benzene, toluene, and xylene through a hydrogenation dealkylation reaction, and LPG through a hydrocracking reaction. Hydrocracking / dealkylation step, converting to a rich non-aromatic hydrocarbon mixture; (d) separating and recovering fuel gas, LPG and aromatic products from the aromatic hydrocarbon mixture and LPG-rich non-aromatic hydrocarbon mixture produced in step (c), respectively; And (e) obtaining low sulfur diesel oil by hydrodesulfurization / denitrification of the residual oil obtained from step (a).

Here, the method also, at least a portion of the fuel gas recovered in the step (d) is put into a separate hydrogen production process and the hydrogen produced therefrom circulated in the steps (b), (c) and (e) It may further comprise the step of.

The method may further include supplying at least a portion of the C4 paraffinic hydrocarbon in the LPG recovered in step (d) as a raw material of the alkylate production process, which is a satellite process of the shear fluidized bed catalytic cracking process.

The catalyst of step (c) is at least one selected from the group consisting of mordenite, beta zeolite and ZSM-5 zeolite, 10 to 95% by weight zeolite having a molar ratio of silica or alumina of 200 to 90 and inorganic binder 5 to 90 It is preferable that the mixture is used as a carrier by mixing the weight%, and is prepared by supporting platinum / tin or platinum / lead on the mixed carrier.

According to another embodiment of the present invention, a process for producing low pollution petroleum products and aromatic products from the fluidized bed catalytic cracking oil according to the present invention comprises: (a) hydrogenated desulfurization / denitrification of the fluidized bed catalytic cracked oil contained in the oil; Removing the sulfur compound and the nitrogen compound; (b) a distillation separation step of distilling the hydrogenated desulfurization / denitrification fraction in step (a) to separate the effluent oil and the residual oil; (c) converting the aromatic hydrocarbon compound in the effluent oil into an aromatic hydrocarbon mixture rich in benzene, toluene and xylene via hydrodealkylation, and converting the non-aromatic hydrocarbon compound into LPG-rich nonaromatic hydrocarbon mixture through hydrocracking reaction. Converting, hydrocracking / dealkylation step; (d) separating and recovering fuel gas, LPG and aromatic products from the aromatic hydrocarbon mixture and LPG-rich non-aromatic hydrocarbon mixture produced in step (c), respectively; And (e) recovering the residual oil obtained from the step (b) as low sulfur diesel.

Here, the method further includes the step of circulating at least a portion of the fuel gas recovered in the step (d) into a separate hydrogen production process and circulating the hydrogen produced therefrom into steps (a) and (c). It may include.

The method may further include supplying at least a portion of the C4 paraffinic hydrocarbon in the LPG recovered in step (d) as a raw material of the alkylate production process, which is a satellite process of the shear fluidized bed catalytic cracking process.

The catalyst of step (c) is at least one selected from the group consisting of mordenite, beta zeolite and ZSM-5 zeolite, 10 to 95% by weight zeolite having a molar ratio of silica or alumina of 200 to 90 and inorganic binder 5 to 90 It is preferable that the mixture is used as a carrier by mixing the weight%, and is prepared by supporting platinum / tin or platinum / lead on the mixed carrier.

The fluidized bed catalytic cracking fraction used in the present invention is preferably a hydrocarbon mixture having a boiling point of 170 to 360 ° C. According to the present invention, from a fluidized bed catalytic cracking fraction containing less than 2% by mass of aromatic products (BTX), such as benzene, toluene and xylene, and containing no LPG, at least 15% by mass of aromatic products and at least 12% by mass of LPG It can be produced efficiently with low sulfur diesel, and the production yield of each product can be adjusted according to the production needs.

The distillation separation process of the present invention separates the fluidized bed catalytic cracking oil used as a raw material according to the boiling point range so that light oil is used to produce fuel gas, LPG and aromatic products, and heavy oil is used as low sulfur diesel. For the purpose, preferably, the light fraction is composed of a hydrocarbon having a boiling point of 170 ~ 220 ℃, the heavy fraction is composed of a hydrocarbon having a boiling point of 220 ~ 360 ℃.

In the present invention, the hydrodesulfurization / denitrification reaction process produces a low pollution hydrocarbon fuel with very low generation of SOx and NOx, and maintains the activity of the catalyst used in the subsequent hydrocracking / dealkylation process. As a step for removing sulfur compounds and nitrogen compounds, which are included impurities, it proceeds by reacting the oil with hydrogen in the presence of a catalyst for the hydrogenation reaction.

As the catalyst used for the hydrogenation reaction, any of the well-known catalysts generally used for the hydrogenation desulfurization / desorption reaction can be used. In particular, it is preferable to use a catalyst in which NiMo, CoMo and the like are supported on alumina.

Hydrogenation desulfurization / denitrification reaction process of the present invention is the hydrogen partial pressure of 10 ~ 50 kg / cm ^{2, the amount} of hydrogen of 50 ~ 400 Nm ³ / kl, the space velocity (LHSV) of 0.1 ~ 10 h ^-1 , 200 ~ 400 ℃ It is preferable to proceed under the conditions of the reaction temperature. These conditions are suitable for the hydrogenation of the feed oil to remove impurities such as sulfur and nitrogen, so that the naphtha component is added to the final product when the severity of the condition is increased so that some of the oil is cracked. It may be included as.

In the process according to the invention, the hydrodesulfurization / denitrification can be carried out after or before the distillation separation process. When the hydrodesulfurization / desorption reaction process is located at the end of the distillation separation process, the effluent distilled off the oil of the fluidized bed catalytic decomposition process is hydrodesulfurized / denitrated, and the hydrodesulfurization / desorption process is located at the front end of the distillation separation process. In this case, the oil from the fluidized bed catalytic cracking reaction process is directly hydrodesulfurized / denitrated, and then separated into a light oil and a heavy oil.

In the former case, the hard oil and the heavy oil must be hydrodesulfurized / denitrated, respectively. In the latter case, the entire oil is separated by hydrodesulfurization / denitrification and separated to achieve the desired purpose with a simple process configuration. There is an advantage.

In the present invention, the hydrocracking / dealkylation process uses fuel oil, liquefied petroleum gas (LPG) and aromatics by reacting with hydrogen in the presence of a catalyst as a feedstock using highly refined oil as a feedstock in the hydrodesulfurization / desulfation process at the front end. It is a process for obtaining a product.

The catalyst used in the process is at least one selected from the group consisting of mordenite, beta zeolite and ZSM-5 zeolite, 10 to 95 wt% zeolite having a molar ratio of silica / alumina of 200 or less and inorganic binder 5 to 90 Mix by weight to use as a carrier. And 0.01 to 0.5 parts by weight of platinum and tin or lead on the basis of the total weight of the mixed carrier, and 0.1 to 5.0 parts by weight of tin, and 0.02 to 5.0 parts by weight of lead. Support.

The catalyst allows the hydrodealkylation, transalkylation and hydrocracking reactions of the feedstock to occur in at least one reactor in the reaction zone.

In the present invention, the hydrodesulfurized / denitrated fraction containing aromatic and non-aromatic components is introduced into the hydrocracking / dealkylation reactor at a space velocity (WHSV) of 0.5 to 10 h ⁻¹ , and a temperature of 250 to 600 ° C. Reacts under pressure ranges of 5 to 50 atmospheres.

In the hydrocracking / dealkylation reactor, hydrocracking dealkylation of aromatic components and hydrocracking of non-aromatic components are carried out in the presence of the above reaction conditions and catalysts. Fuel gas, liquefied petroleum gas, benzene, Aromatic components such as toluene and xylene are obtained.

Meanwhile, the unconverted fraction of the hydrocracking / dealkylation reaction may be mixed with the heavy fraction in the fluidized bed catalytic cracking fraction which has undergone the hydrodesulfurization / denitrification process to be produced in the form of low sulfur diesel.

Hereinafter, with reference to the accompanying drawings will be described in more detail with respect to the present invention.

1 and 2 are process diagrams schematically illustrating specific examples of producing LPG, low sulfur diesel and aromatic products together from fluidized bed catalytic cracking fractions according to the present invention, respectively.

Referring to FIG. 1, the oil S1 produced in the fluidized bed catalytic cracking process is introduced into the distillation separation process U1, and the light oil is separated into the effluent oil S2, and the heavy oil is separated into the residual oil S3.

The effluent oil (S2) is reacted with hydrogen (S4) in the presence of a catalyst in the hydrogenation desulfurization / denitrification process (U2) to remove the sulfur compound and nitrogen compounds as catalyst poisoning components, the treated oil (S5) is hydrogenated at the rear end Fed to the cracking / dealkylation process (U3) and then reacted with hydrogen (S4) in the presence of a catalyst to convert to fuel gas (S6), LPG (S7), aromatic product (S8) and unconverted fraction (S9); and Are separated.

Meanwhile, the residual oil (S3) separated in the distillation separation process (U1) is supplied to the hydrodesulfurization / denitration reaction process (U4) and reacted with hydrogen (S4) in the presence of a catalyst to produce low sulfur diesel (S10) having a low sulfur content. At least a portion of the unconverted fraction (S9) produced in the hydrocracking / dealkylation process (U3) may be prepared as a low-sulfur diesel (S11) in a mixed form.

Referring to Figure 2, the oil (S1) produced in the fluidized bed catalytic cracking process is introduced into the hydrodesulfurization / denitrification process (U20) to react with hydrogen (S4) in the presence of a catalyst to remove a large amount of sulfur compounds and nitrogen compounds (S20), the oil (S20) is introduced into the distillation separation process (U21) and the light oil is separated into the oil (S21), heavy oil is separated into the residual oil (S22), respectively. The operating condition of the hydrogenation desulfurization / desorption reaction step (U20) is that the sulfur compound and the nitrogen compound contained in the effluent oil (S21) of the distillation separation step (U21) are used in the subsequent hydrocracking / dealkylation step (U22). It is advisable to adjust the temperature so as to be within the allowable limits of the catalyst.

The effluent oil (S21) is reacted with hydrogen (S4) in the presence of a catalyst in the hydrocracking / dealkylation process (U22) to fuel gas (S6), LPG (S7), aromatic product (S8) and unconverted fraction (S9) ) And are separated.

Meanwhile, the residual oil (S22) separated in the distillation separation process (U21) may be made of low-sulfur diesel (S23) mixed with at least a portion of the unconverted fraction (S9) produced in the hydrocracking / dealkylation process (U22). Can be.

Figure 3 is a process diagram further comprising the step of supplying butane produced by using the method according to the invention as a raw material of the alkylate production process, a satellite process of the fluidized bed catalytic cracking process.

Butane (S31), which is a C4 component of LPG produced by the method according to the present invention, is partially mixed with general mixed butane (S35) and supplied as a raw material of the alkylate manufacturing process (U31). Only propane (S30) can be separated and recovered.

In the present invention, the butane produced in the hydrocracking / dealkylation process (U3) has a higher ratio of isobutane to normal butane in its constituents compared to the general mixed butane (S35), which is why the fluidized bed catalytic cracking process By supplying the raw material of the alkylate manufacturing process (U31) generally adopted as the satellite process of (U30), the efficiency of the alkylate manufacturing process (U31) can be improved. That is, when the isobutane is contained in the raw material of an alkylate manufacturing process compared with normal butane which does not participate in an alkylate manufacturing reaction, the magnitude | size of the separation apparatus required for the separation of normal butane (S34) and an alkylate (S33). May be minimized, and this may bring about an effect of improving the efficiency of the alkylate manufacturing process (U31).

Figure 4 is a part of the fuel gas (S6) obtained according to the present invention as a raw material of the hydrogen production process (U40), hydrogen (S4) produced through the hydrogen production process (U40) hydrogenated desulfurization / It is a process chart which further includes supplying to denitrification reaction process (U2, U4) and hydrocracking / dealkylation process (U3).

In the method according to the present invention, since the fuel gas (S6) conversion-separated in the hydrocracking / dealkylation process (U3) is made of methane, ethane, and the like having a relatively small carbon number, it is used as a raw material of the hydrogen production process (U40). It can be used to supply the hydrogen required for hydrodesulfurization / denitrification and hydrocracking / dealkylation processes. Since the fuel gas (S6) produced by the method according to the invention contains almost no olefin and hydrogen sulfide components, in the hydrogen production process (U40), it is possible to simplify the pretreatment step for removing the sulfur compound, Accordingly, there is an advantage that can reduce the investment cost of commercial plants.

3 and 4 are based on the case where the distillation separation process (U1) is located at the front end of the hydrodesulfurization / desorption reaction process (U2, U4) as shown in FIG. 1, but after the hydrodesulfurization / desorption as shown in FIG. The same applies to the case of distillation separation.

Hereinafter, the present invention will be described in more detail with reference to the following examples, which are for illustrative purposes only and are not intended to limit the scope of the present invention.

Example  One

According to the method of the present invention, as shown in Table 1 below, the boiling point of the fluidized bed catalytic cracking oil is a raw material having a boiling range of 160 to 300 ° C., which is distilled off under atmospheric pressure, and the boiling point falls within a range of 160 to 220 ° C. The oil and the boiling point were prepared in two kinds of oil belonging to the range of 220 ~ 300 ℃.

The physical properties, compositions, and yields of the fluidized bed catalytic cracking oil may be different according to the type of raw material of the fluidized bed catalytic cracking process and the operating conditions of the process, and thus, the scope of the present invention is not limited thereto.

Example  2

Hydrodesulfurization / denitrification was carried out in the presence of a catalyst on the effluent oil shown in Table 1 of Example 1. One of the desulfurization catalyst groups that are already commercially applied was selected, and desulfurization / desorption reaction experiments were performed while adding hydrogen in a fixed bed high pressure reactor, and the experimental conditions and the results are shown in Table 2 below. Depending on the group of commercially applicable desulfurization catalysts, the reaction conditions and the properties of the reaction products may be somewhat changed, and thus, the scope of the present invention is not limited thereto.

Example  3

LPG and aromatic products were prepared by hydrocracking / dealkylation of the reaction product obtained in Example 2 above.

Mordenite having a molar ratio of silica / alumina and 20 was mixed with aqueous solution of H ₂ PtCl ₆ and SnCl ₂ in the process of forming a mixed carrier using gamma alumina as a binder, and the mordenite content of the carrier except platinum and tin was 75 It was made to be the weight%. Platinum and tin were formed to have a diameter of 1.5 mm and a length of 10 mm by carrying 0.05 parts by weight and 0.5 parts by weight, respectively, based on 100 parts by weight of the binder, dried at 200 ° C. for 12 hours, and then fired at 500 ° C. for 4 hours. Catalyst was prepared. The reaction was performed using a fixed bed reaction apparatus (370 ° C., partial pressure of hydrogen 30 kg / cm ² , molar ratio 5.3 of H ₂ / HC (hydrocarbon), WHSV 1.0 hr ⁻¹ ), and representative yield structures are shown in the following table. Same as 3.

Yield (% by weight) Example 3 H2 -2.68 C1 + C2 14.35 C3 29.37 C4 6.72 C5 + non-aromatic component 3.81 benzene 4.81 toluene 13.38 Ethylbenzene 0.52 Xylene 13.29 C9 + aromatic component 16.43

Example  4

In addition to the above Example 3 using a fixed bed reaction apparatus for more than 330 hours reaction experiments (370 ℃, hydrogen partial pressure 30 kg / cm ² , H ₂ / HC (hydrocarbon) molar ratio 5.3, WHSV 1.0hr ^-1 ) continuously It was confirmed that the yield structure was maintained stably even after the reaction time elapsed, and the trend of the yield structure change according to the reaction time is shown in FIG. 5.

Example  5

Hydrogenation desulfurization / denitrification was carried out in the presence of a catalyst on the residual oil shown in Table 1 of Example 1. Desulfurization catalyst was selected from the group of commercially applied desulfurization catalyst, the desulfurization / denitrification reaction experiment was carried out while adding hydrogen in a fixed bed high pressure reactor, the experimental conditions and the results are shown in Table 4. Depending on the group of commercially applicable desulfurization catalysts, the reaction conditions and the properties of the reaction products may be somewhat changed, and thus, the scope of the present invention is not limited thereto.

Example  6

For the raw material shown in Table 1 of Example 1, a hydrodesulfurization / denitrification reaction was performed in the presence of a catalyst. After combining two selected from the group of desulfurization catalyst already commercially applied, the desulfurization / denitrification reaction experiment was carried out while adding hydrogen in a fixed bed high pressure reactor, the experimental conditions and the results are shown in Table 5 below. Depending on the group of commercially applicable desulfurization catalysts, the reaction conditions and the properties of the reaction products may be somewhat changed, and thus, the scope of the present invention is not limited thereto.

Example  7

Hydrogen desulfurization / denitrified fluidized bed catalytic cracking oil in the presence of hydrogen and a catalyst according to Example 6 according to the method of the invention as shown in Table 6 as a raw material of the boiling point range of 160 ~ 300 ℃ as a raw material, it is atmospheric pressure By distillation under the conditions, the boiling point was prepared in two kinds of oil belonging to the range of 160 ~ 220 ℃ and boiling point belonging to the range of 220 ~ 300 ℃.

The physical properties, compositions, and yields of the fluidized bed catalytic cracking oil may be different according to the type of raw material of the fluidized bed catalytic cracking process and the operating conditions of the process, and thus, the scope of the present invention is not limited thereto.

Example  8

The reaction product obtained in Example 7 was prepared through hydrocracking / dealkylation to prepare LPG and aromatic products.

The catalyst was prepared in the same manner as in Example 3, and the reaction was carried out using a fixed bed reaction apparatus (370 ° C., hydrogen partial pressure of 30 kg / cm ² , molar ratio of H ₂ / HC (hydrocarbon) 5.3, WHSV 1.0 hr). ^-1 ) was performed, and typical yield structures are shown in Table 7 below.

Yield (% by weight) Example 8 H2 -2.44 C1 + C2 13.92 C3 27.62 C4 6.55 C5 + non-aromatic component 3.40 benzene 5.17 toluene 14.01 Ethylbenzene 0.54 Xylene 14.12 C9 + aromatic component 17.11

1 is a process schematic showing one embodiment according to the present invention.

2 is a process schematic showing yet another embodiment according to the present invention.

3 is a process schematic showing yet another embodiment according to the present invention.

4 is a process schematic showing yet another embodiment according to the present invention.

5 is a graph showing the yield change of each product over time when producing LPG, low sulfur diesel, aromatic products by the method according to the present invention.

<Explanation of symbols for the main parts of the drawings>

U1, U21: distillation separation process

U2, U4, U20: Hydrogen Desulfurization / Denitrification Process

U3, U22: Hydrocracking / Dealkylation Process

U30: Fluidized Bed Catalytic Cracking Process

U31: Alkylate Manufacturing Process

U40: Hydrogen Manufacturing Process

Claims (4)

(a) distilling the fluidized bed catalytic cracking fraction to separate the effluent and the residual oil; (b) removing sulfur compounds and nitrogen compounds contained in the effluent oil by hydrodesulfurization / denitrification reaction of the effluent oil obtained in step (a); (c) converting the aromatic hydrocarbon compounds in the effluent oil subjected to the hydrodesulfurization / denitrification to an aromatic hydrocarbon mixture rich in benzene, toluene, and xylene through hydrodealkylation, and the LPG-rich mixture of the nonaromatic hydrocarbon compounds by hydrocracking. Hydrocracking / dealkylation step, converting to non-aromatic hydrocarbon mixture; (d) separating and recovering fuel gas, LPG and aromatic products from the aromatic hydrocarbon mixture and LPG-rich non-aromatic hydrocarbon mixture produced in step (c), respectively; And (e) obtaining low sulfur diesel oil by hydrodesulfurization / denitrification of the residual oil obtained in step (a). (a) removing the sulfur compound and nitrogen compound contained in the oil by hydrodesulfurization / denitrification of the fluidized bed catalytic cracking oil; (b) distilling the hydrogenated desulfurization / denitrification fraction in step (a) to separate the effluent and the residual oil; (c) converting the aromatic hydrocarbon compound in the effluent oil into an aromatic hydrocarbon mixture rich in benzene, toluene and xylene via hydrodealkylation, and converting the non-aromatic hydrocarbon compound into an LPG-rich nonaromatic hydrocarbon mixture through hydrocracking. Hydrocracking / dealkylation step; (d) separating and recovering fuel gas, LPG and aromatic products from the aromatic hydrocarbon mixture and LPG-rich non-aromatic hydrocarbon mixture produced in step (c), respectively; And (e) recovering LPG, low sulfur diesel and aromatic products from fluidized bed catalytic cracking fraction comprising recovering the bottom oil obtained from step (b) as low sulfur diesel. The fluidized bed catalytic cracking fraction according to claim 1 or 2, further comprising the step of separating the butane component in the recovered LPG and feeding it to a process for producing an alkylate from a separate fluidized bed cracked fraction. Process for producing LPG, low sulfur diesel and aromatic products. The method of claim 1 or 2, further comprising the step of supplying all or part of the recovered fuel gas to a hydrogen production process for producing hydrogen for use in the hydrodesulfurization / denitrification process and the hydrocracking / dealkylation process. A process for producing LPG, low sulfur diesel and aromatic products from fluidized bed catalytic cracking fractions.

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