A process for the preparation of heavy aromatics

Abstract

This invention discloses a method for preparing heavy aromatics. Under naphtha catalytic reforming conditions, naphtha is contacted with a catalyst, and the products are separated. The active component of the catalyst is a nickel-gallium alloy, and the catalyst support is a boron-modified SBA-15 molecular sieve. The mass of the nickel-gallium alloy active component is 8-12% of the support mass, and the atomic mass ratio of Ni to Ga in the nickel-gallium alloy is 1-3:1. Boron accounts for 15-25% of the mass of the boron-modified SBA-15 molecular sieve. The synergistic effect of nickel and gallium on the nickel-gallium alloy catalyst facilitates the aromatization reaction of hydrocarbons in naphtha. A suitable Ni-Ga ratio can improve the heavy aromatic selectivity of the aromatic products. The boron-modified SBA-15 molecular sieve can improve the stability of the catalyst, enabling it to maintain good structural stability and activity at high temperatures.

Description

Technical Field

[0001] This invention relates to the field of aromatic hydrocarbon production technology, and in particular to a method for preparing heavy aromatic hydrocarbons. Background Technology

[0002] Heavy aromatics are a general term for aromatic compounds with 9 or more carbon atoms (C9). They are primarily C9 and C10 aromatics produced as byproducts in petroleum and coal processing. Heavy aromatics mainly originate from catalytic reforming units in oil refineries, cracked gasoline and ethylene tar from ethylene plants, and coal tar from high-temperature coal coking. With the rapid development of my country's petroleum and coal processing industries, the production of heavy aromatic oils has increased significantly. The composition of heavy aromatics is very complex; according to reports, there are more than 100 components. Although the content of each component varies with production process parameters and actual operating conditions, the main components and their contents remain relatively stable. For example, reformed aromatics contain approximately 40% pseudotrimethylbenzene, 30% methylethylbenzene, and mesitylene and mesitylene, all of which are valuable organic chemical raw materials.

[0003] Catalytic reforming is one of the main processes in petroleum refining, primarily used to convert naphtha into reformate rich in aromatics and to produce hydrogen as a byproduct. The manufacturing process of heavy aromatics mainly includes the following steps: (1) Raw material pretreatment: The raw material is pretreated by desulfurization, denitrification, and dehydration to ensure the smooth progress of subsequent reactions; (2) Cracking reaction: Under high temperature and the action of a catalyst, the raw material undergoes a cracking reaction to generate small molecule hydrocarbons and hydrogen; (3) Aromatization reaction: The small molecule hydrocarbons generated by the cracking reaction undergo an aromatization reaction under the action of an acidic catalyst to generate aromatics and hydrogen; (4) Fractionation: The reaction products are separated by a fractionation tower to obtain heavy aromatic products with different boiling points; (5) Product refining: The heavy aromatic products are refined to remove impurities and moisture to obtain qualified products. The core technology of catalytic reforming is its catalyst. Since the reforming reaction mainly includes dehydrogenation, isomerization, and cracking reactions, the reforming catalyst must have dual functions. Industrially, platinum-based reforming catalysts typically employ a combination of noble metal Pt-Re and Pt-Sn active components with halide-modified alumina supports. Platinum forms the dehydrogenation active center, promoting dehydrogenation and hydrogenation reactions, while the acidic support provides acidic centers, promoting carbocation reactions such as isomerization and cracking. However, platinum-based reforming catalysts are expensive and have poor adaptability to reforming feedstocks, which generally require pretreatment. Therefore, developing alternative platinum-based reforming catalysts is of paramount importance. By developing novel catalysts, the yield of specific substances in the cracking products can be selectively increased. Summary of the Invention

[0004] In view of this, the present invention proposes a method for preparing heavy aromatic hydrocarbons to solve the above problems.

[0005] The technical solution of this invention is implemented as follows:

[0006] A method for preparing heavy aromatics includes the following steps: under naphtha catalytic reforming reaction conditions, contacting naphtha with a catalyst to separate the products; wherein the active component of the catalyst is a nickel-gallium alloy, and the catalyst support is a boron-modified SBA-15 molecular sieve.

[0007] Preferably, the mass of the nickel-gallium alloy, the active component of the catalyst, is 8-12% of the mass of the support.

[0008] Preferably, the mass of the nickel-gallium alloy, the active component of the catalyst, is 10% of the mass of the support.

[0009] Preferably, the mass ratio of Ni to Ga in the active component of the catalyst, the nickel-gallium alloy, is 1-3:1.

[0010] Preferably, the mass ratio of Ni to Ga in the active component of the catalyst, the nickel-gallium alloy, is 2:1.

[0011] Preferably, the boron element in the boron-modified SBA-15 molecular sieve accounts for 15-25% of the mass of the SBA-15 molecular sieve.

[0012] Preferably, the boron element in the boron-modified SBA-15 molecular sieve accounts for 20% of the mass of the SBA-15 molecular sieve.

[0013] Preferably, the catalyst is prepared as follows: nickel nitrate hexahydrate, gallium nitrate nonahydrate, and ammonium borate are dissolved in a three-necked flask, and ammonia is added dropwise to adjust the pH to 10-11. After the reaction is complete, SBA-15 powder is added to the flask, and the mixture is stirred and aged at 40-50°C for 6-8 hours. The solution is then heated to 90-100°C, and the remaining ammonia is evaporated until the pH reaches 6-7. Heating is then stopped, and the solution is filtered, washed, dried, calcined at 500°C for 6-8 hours, pressed into tablets, sieved to 60-80 mesh, and placed in a fixed bed for activation with high-purity hydrogen before use.

[0014] Preferably, the naphtha catalytic reforming reaction conditions are: temperature 450-550℃, pressure 0.8-1.0MPa, and liquid feed volume hourly space velocity (VHSV) of 1-2 h⁻¹. -1 The hydrogen / oil volume ratio is 600-1000.

[0015] Preferably, the reaction conditions for the alkylation of pseudotrimethylbenzene and methanol to produce heavy aromatics are: temperature 500°C, pressure 0.9 MPa, and liquid feed volume hourly space velocity (VHSV) of 1.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is 800.

[0016] Compared with the prior art, the beneficial effects of the present invention are as follows:

[0017] (1) The present invention provides a method for preparing heavy aromatics, which is to obtain heavy aromatics by naphtha catalytic reforming reaction. The catalyst used is composed of nickel gallium alloy and the catalyst support is boron modified SBA-15 molecular sieve. The heavy aromatics (C10-C12) in the reaction product have high selectivity.

[0018] (2) Boron modification can improve the acidity of SBA-15 molecular sieve, which is crucial for the decomposition and reorganization of long-chain alkanes into heavy aromatics in naphtha. The modified catalyst is more likely to promote these reactions, improving the activity and selectivity of the reaction and helping to increase the yield of the target product. Boron-modified SBA-15 molecular sieve can improve the stability of the catalyst, enabling it to maintain good structural stability and activity at high temperatures. Under the high-temperature reaction conditions of naphtha catalytic reforming, the carbon deposition rate is low. The stability of the catalyst is crucial for long-term operation and maintaining product quality.

[0019] (3) The synergistic effect of nickel and gallium elements on nickel-gallium alloy catalysts helps hydrocarbons in naphtha to undergo aromatization reactions, thereby improving the selectivity of aromatic products. The ratio of nickel to gallium in nickel-gallium alloy catalysts also affects the selectivity. Different nickel-gallium ratios will lead to different catalytic activities and heavy aromatic selectivity. Detailed Implementation

[0020] To better understand the technical content of this invention, specific embodiments are provided below to further illustrate the invention.

[0021] Unless otherwise specified, the experimental methods used in the embodiments of this invention are all conventional methods.

[0022] Unless otherwise specified, all materials and reagents used in the embodiments of this invention are commercially available.

[0023] Example 1

[0024] A one-pot method was used to prepare Ni-Ga / B-SBA-15 catalyst (10 wt% nickel-gallium alloy loading, Ni to Ga mass ratio 1:1). 2.48 g of nickel nitrate hexahydrate, 1.83 g of cobalt gallium nitrate nonahydrate, and 10.56 g of ammonium borate were dissolved in a three-necked flask. A 20 wt% ammonia solution was added dropwise to the flask until the pH reached 10.5. After complete reaction, 10 g of SBA-15 powder was added to the flask, and the mixture was stirred and aged at 45 ± 5 °C for 6 h. The solution was heated to 95±5℃, and the remaining ammonia was evaporated until the pH reached 6-7. Heating was then stopped, the solution was filtered, washed, and dried in an oven for 12 hours. After calcination at 500℃ for 6 hours, the solution was pressed into tablets, sieved to 60-80 mesh, and placed in a fixed bed. The tablets were then heated to 400℃ and activated with high-purity hydrogen before use. This product was designated as 10% Ni-Ga / B-SBA-15, i.e., a boron-modified SBA-15 molecular sieve supported on a NiGa alloy catalyst, with Ni and Ga loadings of 5wt% each. Boron accounted for 20% of the mass of the boron-modified SBA-15 molecular sieve.

[0025] Example 2

[0026] A one-pot method was used to prepare Ni-Ga / B-SBA-15 catalyst (10 wt% nickel-gallium alloy loading, Ni to Ga mass ratio of 2:1). 1.63 g of nickel nitrate hexahydrate, 2.42 g of cobalt gallium nitrate nonahydrate, and 10.56 g of ammonium borate were dissolved in a three-necked flask. A 20 wt% ammonia solution was added dropwise to the flask until the pH reached 10.5. After complete reaction, 10 g of SBA-15 powder was added to the flask, and the mixture was stirred and aged at 45 ± 5 °C for 6 h. The solution was heated to 95±5℃, and the remaining ammonia was evaporated until the pH reached 6-7. Heating was then stopped, the solution was filtered, washed, and dried in an oven for 12 hours. After calcination at 500℃ for 6 hours, the solution was pressed into tablets, sieved to 60-80 mesh, and placed in a fixed bed. The tablets were then heated to 400℃ and activated with high-purity hydrogen before use. This product was designated as 10% Ni2-Ga / B-SBA-15, i.e., a boron-modified SBA-15 molecular sieve supported on a NiGa alloy catalyst. The Ni and Ga loadings were 6.6wt% and 3.3wt%, respectively, with boron accounting for 20% of the mass of the boron-modified SBA-15 molecular sieve.

[0027] Example 3

[0028] A one-pot method was used to prepare Ni-Ga / B-SBA-15 catalyst (10 wt% nickel-gallium alloy loading, Ni to Ga mass ratio of 3:1). 3.71 g of nickel nitrate hexahydrate, 0.92 g of cobalt gallium nitrate nonahydrate, and 10.56 g of ammonium borate were dissolved in a three-necked flask. A 20 wt% ammonia solution was added dropwise to the flask until the pH reached 10.5. After complete reaction, 10 g of SBA-15 powder was added to the flask, and the mixture was stirred and aged at 45 ± 5 °C for 6 h. The solution was heated to 95±5℃, and the remaining ammonia was evaporated until the pH reached 6-7. Heating was then stopped, the solution was filtered, washed, and dried in an oven for 12 hours. After calcination at 500℃ for 6 hours, the solution was pressed into tablets, sieved to 60-80 mesh, and placed in a fixed bed. The tablets were then activated with high-purity hydrogen at 400℃ and left to use. This product was designated as 10% Ni3-Ga / B-SBA-15, i.e., a boron-modified SBA-15 molecular sieve supported on a NiGa alloy catalyst. The Ni and Ga loadings were 7.5wt% and 2.5wt%, respectively, with boron accounting for 20% of the mass of the boron-modified SBA-15 molecular sieve.

[0029] Example 4

[0030] A Ni-Ga / B-SBA-15 catalyst (8 wt% nickel-gallium alloy loading, Ni to Ga mass ratio 2:1) was prepared using a one-pot method. 1.34 g of nickel nitrate hexahydrate, 1.94 g of cobalt gallium nitrate nonahydrate, and 10.56 g of ammonium borate were dissolved in a three-necked flask. A 20 wt% ammonia solution was added dropwise to the flask until the pH reached 10.5. After complete reaction, 10 g of SBA-15 powder was added to the flask, and the mixture was stirred and aged at 45 ± 5 °C for 6 h. The solution was heated to 95±5℃, and the remaining ammonia was evaporated until the pH reached 6-7. Heating was then stopped, the solution was filtered, washed, and dried in an oven for 12 hours. After calcination at 500℃ for 6 hours, the solution was pressed into tablets, sieved to 60-80 mesh, and placed in a fixed bed. The tablets were then activated with high-purity hydrogen at 400℃ and left to use. This product was designated as 8% Ni2-Ga / B-SBA-15, i.e., a boron-modified SBA-15 molecular sieve supported on a NiGa alloy catalyst. The Ni and Ga loadings were 5.33wt% and 2.67wt%, respectively, with boron accounting for 20% of the mass of the boron-modified SBA-15 molecular sieve.

[0031] Example 5

[0032] A Ni-Ga / B-SBA-15 catalyst (Ni-gallium alloy loading of 12 wt%, Ni to Ga mass ratio of 2:1) was prepared using a one-pot method. 1.96 g of nickel nitrate hexahydrate, 2.90 g of cobalt gallium nitrate nonahydrate, and 10.56 g of ammonium borate were dissolved in a three-necked flask. A 20 wt% ammonia solution was added dropwise to the flask until the pH reached 10.5. After complete reaction, 10 g of SBA-15 powder was added to the flask, and the mixture was stirred and aged at 45 ± 5 °C for 6 h. The solution was heated to 95±5℃, and the remaining ammonia was evaporated until the pH reached 6-7. Heating was then stopped, the solution was filtered, washed, and dried in an oven for 12 hours. After calcination at 500℃ for 6 hours, the solution was pressed into tablets, sieved to 60-80 mesh, and placed in a fixed bed. The tablets were then activated with high-purity hydrogen at 400℃ and left to use. This product was designated as 12% Ni2-Ga / B-SBA-15, i.e., a boron-modified SBA-15 molecular sieve supported on a NiGa alloy catalyst. The Ni and Ga loadings were 8wt% and 4wt%, respectively, with boron accounting for 20% of the mass of the boron-modified SBA-15 molecular sieve.

[0033] Example 6

[0034] A Ni-Ga / B-SBA-15 catalyst (Ni-gallium alloy loading of 10 wt%, Ni to Ga mass ratio of 2:1) was prepared using a one-pot method. 1.63 g of nickel nitrate hexahydrate, 2.42 g of cobalt gallium nitrate nonahydrate, and 7.92 g of ammonium borate were dissolved in a three-necked flask. A 20 wt% ammonia solution was added dropwise to the flask until the pH reached 10.5. After complete reaction, 10 g of SBA-15 powder was added to the flask, and the mixture was stirred and aged at 45 ± 5 °C for 6 h. The solution was heated to 95±5℃, and the remaining ammonia was evaporated until the pH reached 6-7. Heating was then stopped, the solution was filtered, washed, and dried in an oven for 12 hours. After calcination at 500℃ for 6 hours, the solution was pressed into tablets, sieved to 60-80 mesh, and placed in a fixed bed. The tablets were then activated with high-purity hydrogen at 400℃ and left to use. This product was designated as 10% Ni2-Ga / B-SBA-15, i.e., a boron-modified SBA-15 molecular sieve supported on a NiGa alloy catalyst. The Ni and Ga loadings were 6.6wt% and 3.3wt%, respectively, with boron accounting for 15% of the mass of the boron-modified SBA-15 molecular sieve.

[0035] Example 7

[0036] A one-pot method was used to prepare Ni-Ga / B-SBA-15 catalyst (10 wt% nickel-gallium alloy loading, Ni to Ga mass ratio of 2:1). 1.63 g of nickel nitrate hexahydrate, 2.42 g of cobalt gallium nitrate nonahydrate, and 13.2 g of ammonium borate were dissolved in a three-necked flask. A 20 wt% ammonia solution was added dropwise to the flask until the pH reached 10.5. After complete reaction, 10 g of SBA-15 powder was added to the flask, and the mixture was stirred and aged at 45 ± 5 °C for 6 h. The solution was heated to 95±5℃, and the remaining ammonia was evaporated until the pH reached 6-7. Heating was then stopped, the solution was filtered, washed, and dried in an oven for 12 hours. After calcination at 500℃ for 6 hours, the solution was pressed into tablets, sieved to 60-80 mesh, and placed in a fixed bed. The tablets were then activated with high-purity hydrogen at 300℃ and left to use. This product was designated as 10% Ni2-Ga / B-SBA-15, i.e., a boron-modified SBA-15 molecular sieve supported on a NiGa alloy catalyst. The Ni and Ga loadings were 6.6wt% and 3.3wt%, respectively, with boron accounting for 25% of the mass of the boron-modified SBA-15 molecular sieve.

[0037] Comparative Example 1

[0038] The difference between this example and Example 2 is that the catalyst support in this example is SBA-15 molecular sieve, which is not modified with ammonium borate. The Ni-Ga / SBA-15 catalyst (nickel-gallium alloy loading of 10wt%, mass ratio of Ni to Ga of 2:1) is prepared by one-pot method. The catalyst preparation method is basically the same as that in Example 2.

[0039] Comparative Example 2

[0040] The difference between this example and Example 2 is that this example does not contain gallium. That is, the Ni / B-SBA-15 catalyst (nickel loading of 10 wt%) is prepared by a one-pot method. The catalyst preparation method is basically the same as that in Example 2.

[0041] Comparative Example 3

[0042] The difference between this example and Example 2 is that this example uses a one-pot method to prepare the Ni-Ga / B-SBA-15 catalyst (nickel-gallium alloy loading of 10wt%, Ni to Ga mass ratio of 5:1), and the catalyst preparation method is basically the same as that in Example 2.

[0043] Comparative Example 4

[0044] The difference between this example and Example 2 is that in this example, the SBA-15 molecular sieve is replaced with the ZSM-5 molecular sieve, and Ni-Ga / B-ZSM-5 is prepared by a one-pot method. The catalyst preparation method is basically the same as in Example 2.

[0045] Comparative Example 5

[0046] The difference between this example and Example 2 is that this example uses a one-pot method to prepare the Ni-Zn / B-SBA-15 catalyst (nickel-zinc alloy loading of 10wt%, Ni and Zn mass ratio of 2:1), and the catalyst preparation method is basically the same as that in Example 2.

[0047] Comparative Example 6

[0048] The difference between this example and Example 2 is that this example uses a one-pot method to prepare the Ni-Cu / B-SBA-15 catalyst (nickel-copper alloy loading of 10wt%, Ni and Cu mass ratio of 2:1), and the catalyst preparation method is basically the same as that in Example 2.

[0049] Experimental Example 1

[0050] The specific surface area and pore properties of the catalysts prepared in Examples 1-7 and Comparative Examples 1-6 were tested using the low-temperature nitrogen adsorption-desorption isotherm method, and the results are shown in Table 1.

[0051] Table 1

[0052] Example 1 350 0.48 Example 2 352 0.50 Example 3 353 0.51 Example 4 357 0.53 Example 5 345 0.44 Example 6 359 0.49 Example 7 339 0.41 Comparative Example 1 332 0.32 Comparative Example 2 351 0.47 Comparative Example 3 354 0.49 Comparative Example 4 324 0.30 Comparative Example 5 348 0.43 Comparative Example 6 351 0.45

[0053] As shown in Table 2, the catalysts provided in Examples 1-7 of this invention have a large specific surface area and pore volume. A larger specific surface area provides more active sites, increasing the contact area between reactants and the catalyst, thereby improving the reaction rate and catalytic activity. A larger mesopore volume provides larger diffusion channels, facilitating mass transfer between reactants and products, promoting the diffusion and dispersion of carbon deposits, slowing down carbon deposition, and thus extending the catalyst's lifespan. Comparison of the results of Comparative Example 1 and Examples 2, 6, and 7 shows that at low boron content, the pore volume of boron-modified molecular sieves typically increases. This is because borate ions can expand the pore size through interaction with the silicon-oxygen bonds in the molecular sieve framework. However, with further increases in boron content, the arrangement of borate ions may lead to pore closure, thereby reducing the pore volume. A higher active metal loading in the catalyst results in a greater number of active sites, potentially enhancing its catalytic activity. However, a high metal loading also typically reduces the specific surface area and pore volume of the catalyst. Comparing Comparative Example 4 and Example 2, it can be seen that the boron-modified SBA-15 molecular sieve has a larger specific surface area and pore volume than the boron-modified ZSM-5 molecular sieve, and the boron modification effect is more obvious.

[0054] Experimental Example 2

[0055] A 200 mL apparatus was loaded with 50 mL of catalyst. The catalysts prepared in Examples 1-7 and Comparative Examples 1-6 were evaluated using desulfurized and refined straight-run naphtha as feedstock. The catalysts were tested using naphtha (composition as follows: 38.5 wt% n-alkanes, 35 wt% isoalkanes, 21 wt% cycloalkanes, and 5.5 wt% aromatics) at 500 °C, 0.9 MPa, a hydrogen-to-oil volume ratio of 800, and a space velocity of 1.5 h⁻¹. -1 Catalytic reforming reaction test was conducted on the catalyst under the reaction conditions, with a cumulative reaction time of 168 h (one week). The reaction product entered a water cooler and was separated into gas and liquid phases. The gas and liquid phases were measured and their composition was analyzed. The content of heavy aromatic hydrocarbons in the target product was statistically analyzed. The results are shown in Table 2.

[0056] Table 2

[0057]

[0058] Table 2 shows that the boron-modified SBA-15 supported nickel-gallium alloy catalysts prepared in Examples 1-7 of this invention exhibit good heavy aromatics selectivity and anti-carbon deposition performance in naphtha catalytic reforming. Comparing the results of Examples 1-3 and Comparative Examples 2 and 3, it is clear that the Ni / Ga mass ratio has a significant impact on the heavy aromatics selectivity. Combining the results of Examples 2 / 6 / 7 and Comparative Example 1, it is evident that the B content affects the quality of the modified SBA-15 molecular sieve. Appropriate B addition can improve thermal stability and anti-carbon deposition performance; too little B will affect its effectiveness, while excessive B content may clog the pore structure of the SBA-15 molecular sieve, reducing the active surface area and the number of available active sites, thereby reducing catalytic activity and selectivity. In Comparative Examples 5 and 6, replacing the nickel-gallium alloy with nickel-zinc and nickel-copper alloys significantly reduced the heavy aromatics selectivity and the catalyst's anti-carbon deposition performance. In Comparative Example 4, replacing the SBA-15 molecular sieve with ZSM-5 molecular sieve resulted in a certain degree of decrease in both conversion selectivity and anti-carbon deposition performance.

[0059] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the protection scope of the present invention.

Claims

1. A process for the production of heavy aromatics, characterized by, The process includes the following steps: under naphtha catalytic reforming reaction conditions, naphtha is contacted with a catalyst to separate the products; the active component of the catalyst is a nickel-gallium alloy, and the catalyst support is a boron-modified SBA-15 molecular sieve. The mass of the nickel-gallium alloy, the active component of the catalyst, is 8-12% of the mass of the support. The atomic mass ratio of Ni to Ga in the active component of the catalyst, the nickel-gallium alloy, is 1-3:1; In the boron-modified SBA-15 molecular sieve, boron accounts for 15-25% of the mass of the SBA-15 molecular sieve.

2. The process for the preparation of heavy aromatics according to claim 1, characterized in that, The mass of the nickel-gallium alloy, the active component of the catalyst, is 10% of the mass of the support.

3. The method for preparing heavy aromatics according to claim 1, characterized in that, The active component of the catalyst, the nickel-gallium alloy, has an atomic mass ratio of Ni to Ga of 2:

1.

4. The method for preparing heavy aromatics according to claim 1, characterized in that, In the boron-modified SBA-15 molecular sieve, boron accounts for 20% of the mass of the SBA-15 molecular sieve.

5. The method for preparing heavy aromatics according to claim 1, characterized in that, The catalyst is prepared as follows: nickel nitrate hexahydrate, gallium nitrate nonahydrate, and ammonium borate are dissolved in a three-necked flask. Ammonia water is added dropwise to adjust the pH to 10-11. After the reaction is complete, SBA-15 powder is added to the flask and stirred and aged at 40-50℃ for 6-8 hours. The solution is heated to 90-100℃, and the remaining ammonia water is evaporated until the pH is 6-7. Heating is then stopped, and the solution is filtered, washed, dried, calcined at 500℃ for 6-8 hours, pressed into tablets, sieved to 60-80 mesh, and placed in a fixed bed. After activation with high-purity hydrogen, it is ready for use.

6. The method for preparing heavy aromatics according to claim 1, characterized in that, The naphtha catalytic reforming reaction conditions are: temperature 450-550℃, pressure 0.8... 1.0 MPa, liquid feed volumetric hourly space velocity is 1-2 h⁻¹ 1 The hydrogen / oil volume ratio is 600-1000.

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