Hydrocracking of Heavy Vacuum Gas Oil with Petroleum Wax

: Petroleum heavy vacuum gas oil (HVGO) containing 10 wt.% of petroleum wax was hydrocracked at 390–430 ◦ C and under the pressure of 18 MPa over a Ni W/amorphous silica-alumina catalyst in a continuous-ﬂow ﬁxed-bed reactor. The hydrocracking of a reference feed (neat HVGO) was carried out under the same reaction conditions. The physico-chemical properties of primary products obtained via laboratory atmospheric-vacuum distillation (heavy naphtha, middle distillates and distillation residue) were evaluated. Most products prepared from the mixed feedstock had a similar or lower density and sulfur content than the products obtained from the hydrocracking of the neat HVGO. The heavy naphtha fractions obtained from mixed feedstock contained slightly more n -alkanes and iso -alkanes and less naphthenes and aromatics. Similarly, middle distillates obtained from the mixed feedstock contained slightly more n -alkanes and less aromatics and had cetane index higher by up to 2 units.


Introduction
Declining crude oil reserves together with the constantly increasing consumption of fossil fuels (diesel, gasoline, kerosene, etc.) and increasing emissions of greenhouse gases and other pollutants have prompted the increased global awareness of the new socioeconomic and environmental challenge [1,2]. Consequently, research activities focused on the utilization of alternative and more preferably renewable energy resources are widely supported. At the current level of the state-of-the-art, liquid fuels are an indispensable energy carrier for the transportation sector due to the existing infrastructure (fuel distribution as well as engine technology) and their high energy density. The need for other carbon sources to produce liquid fuels can be satisfied only partially by renewable resources that can be converted directly into liquid transportation fuels, i.e., vegetable oils and fats (lipids) for biodiesel or hydrotreated vegetable oil (HVO) [3,4] and sugars for ethanol production [5]. Indirect routes of producing liquid transportation fuels from biomass offer a significantly larger potential particularly due to the abundance of lignocellulosic biomass and waste materials.
For the enhancement of liquid fuels production, several types of cracking processes (thermal cracking, catalytic cracking and hydrocracking) [6][7][8] are commonly applied. The hydrocracking of petroleum heavy vacuum gas oil (HVGO) is a commonly used process for the production of high-quality liquid fuels for vehicles and jet planes. The co-processing of heavy-vacuum gas oil with a high-molecular paraffinic feedstock can provide the additional intensification of the production of these high-quality liquid fuels. In consideration of the actual technological potential, the processing of the "synthetic" wax from Fischer-Tropsch synthesis (FTS) or the "natural" petroleum wax from the dewaxing process is possible [9].

Results and Discussion
The distillation curves of heavy vacuum gas oil (HVGO), petroleum wax (PW) and the mixed feedstock obtained via simulated distillation are presented in Figure 1. While the HVGO was entirely composed of components boiling above 400 • C, the PW contained approximately 40 wt.% of the fraction boiling below 400 • C. From the other point of view, even though the heaviest components of the PW boiled below 550 • C, the HVGO contained ca. 10 wt.% of the fraction boiling above 550 • C. As expected, the addition of the PW to the HVGO shifted the distillation curve of the mixed feedstock to lower values.
Catalysts 2022, 12, x FOR PEER REVIEW 3 of 14 middle distillate (diesel) and hydrocracking residue, as well as on their composition and properties using a commercial hydrocracking catalyst.

Results and Discussion
The distillation curves of heavy vacuum gas oil (HVGO), petroleum wax (PW) and the mixed feedstock obtained via simulated distillation are presented in Figure 1. While the HVGO was entirely composed of components boiling above 400 °C, the PW contained approximately 40 wt.% of the fraction boiling below 400 °C. From the other point of view, even though the heaviest components of the PW boiled below 550 °C, the HVGO contained ca. 10 wt.% of the fraction boiling above 550 °C. As expected, the addition of the PW to the HVGO shifted the distillation curve of the mixed feedstock to lower values. Basic physiochemical properties of the HVGO, PW and the mixed feedstock used for the hydrocracking are presented in Table 1. The composition of the PW was determined via the GC-MS method showed that it was composed of ca. 88 wt.% of acyclic (predominantly unbranched) alkanes, 11 wt.% of alkylnaphthenes and less than 1 wt.% of other hydrocarbons. In comparison with the FTS waxes, the PW thus contained a higher proportion of the other hydrocarbons group than n-alkanes [2]. On the other hand, the content of aromatic components was very low, which supports the assumption of the PW and FTS wax similarity. The differences in the chemical composition of these two types of wax were thus considered as almost negligible and their manner during the hydrocracking should be very similar as well.  Basic physiochemical properties of the HVGO, PW and the mixed feedstock used for the hydrocracking are presented in Table 1. The composition of the PW was determined via the GC-MS method showed that it was composed of ca. 88 wt.% of acyclic (predominantly unbranched) alkanes, 11 wt.% of alkylnaphthenes and less than 1 wt.% of other hydrocarbons. In comparison with the FTS waxes, the PW thus contained a higher proportion of the other hydrocarbons group than n-alkanes [2]. On the other hand, the content of aromatic components was very low, which supports the assumption of the PW and FTS wax similarity. The differences in the chemical composition of these two types of wax were thus considered as almost negligible and their manner during the hydrocracking should be very similar as well.
The density of the PW was significantly lower than the density of the HVGO which can be attributed to the lower distillation profile and the absence of aromatic structures in PW. On the other hand, its pour point was higher in comparison with HVGO. It can be associated with the chemical nature of the PW composed predominantly of saturated straight chain paraffins. The PW was sulfur and nitrogen free, which affected its overall elemental composition, so the dominant elements were carbon and hydrogen only. On the other hand, significant proportions of sulfur and nitrogen were detected in the HVGO and thus in the mixture feedstock as well.
The primary liquid products of the hydrocracking were characterized by their density at 25 • C and refractive index at 50 • C to operatively monitor the composition changes during the hydrocracking. The representative values of these parameters are given in Table 2 together with liquid feedstock conversion, liquid products yield and elemental composition.  The yield of the primary liquid products decreased with an increasing reaction temperature. The influence of the PW addition to the feedstock was less significant, especially at 390 • C where the difference between products from both feedstocks was almost negligible. The application of the higher reaction temperatures caused a moderate increase in the liquid product yield from the feedstock containing the PW. The increasing reaction temperature was followed by the increasing conversion of the feedstock to the products with the required boiling range, i.e., below 360 • C. The addition of the PW to the feedstock led to a mild conversion reduction. Although it was possible to observe a slight density reduction caused by the addition of the PW to the feedstock, the differences between the density of the primary products decreased strongly with the increasing reaction temperature caused by the increasing conversion.
The decrease in the refractive index (RI) of primary liquid products with an increasing reaction temperature was evident. The decreasing RI was caused by the decreasing content of heterocompounds and aromatics and cracking of long-chain paraffins into shorter ones. For example, the refractive indexes of n-nonane, n-decane and n-dodecane at temperature 35 • C are 1.3989, 1.4062 and 1.4154, respectively [29]. The refractive index can therefore be used as a parameter for the fast and operative monitoring of the hydrocracking process.
As expected, the more severe reaction conditions lead to deeper desulfurization and denitrogenation (Table 2). This observation is in accordance with the results of Halmenschlager et al. [28] who hydrocracked the mixture of HVGO and petroleum wax at a pressure of 9.5 MPa and the temperature range of 330-410 • C. The primary products obtained from the feedstock containing PW at the reaction temperatures of 390 and 410 • C had a lower sulfur and nitrogen content than similar products obtained from the neat HVGO. On the other hand, the content of sulfur and nitrogen in products obtained at a temperature of 430 • C was almost the same. This is probably due to the reaction of hydrogen sulfide and ammonia with alkenes formed as intermediates of hydrocracking of wax at a higher reaction temperature (430 • C) into aliphatic sulfur and nitrogen compounds (e.g., mercaptanes, sulfides, amines). For example, the direct hydrosulfurization and hydroamination of ethylene by hydrogen sulfide and ammonia on zeolites was described by Kalló et al. [30] and Deeba et al., respectively [31]. Nevertheless, in the industrial process, these sulfur and nitrogen compounds are easily eliminated by the hydrorefining catalyst at the end of the catalyst bed.
The distillation profiles of the primary hydrocracking products were more affected by the reaction temperature than by the feedstock composition ( Table 3). As expected, the increasing reaction temperature shifted the distillation curves of the primary products downward to the lower boiling points and increased the yield of light fractions. On the other hand, differences between the distillation profiles of two products obtained at the same reaction temperature from various feedstocks were negligible. The data presented in Figure 2 show that the yields of the light fractions (gases + light naphtha) and distillation fractions (heavy naphtha and middle distillates) increased with an increasing reaction temperature of hydrocracking. As the rate of cracking was rather low at the reaction temperature of 390 • C, considerable amounts of heavy naphtha were obtained only by hydrocracking at 410 and 430 • C. The products obtained from the mixed feedstock yielded slightly less than a middle distillate and slightly more distillation residue then the products obtained from the neat HVGO.
The heavy naphtha fractions obtained from hydrocracking at 430 • C had slightly lower distillation curves than the heavy naphthas obtained from hydrocracking at 410 • C. There were no significant differences between heavy naphthas obtained from different raw materials. Some other physico-chemical properties of the heavy naphthas are shown in Table 3. A high reaction temperature and the presence of the petroleum wax in the feedstock reduced the density of the obtained heavy naphthas, but the influence of the reaction temperature was much greater. The contents of sulfur and nitrogen were comparable for all samples with regard to their relatively low values. On the other hand, the slightly higher content of sulfur and nitrogen in products obtained at a temperature of 430 • C was probably caused by the presence of aliphatic sulfur and nitrogen compounds formed during the hydrocracking. The reaction temperature also influenced the group-type composition of the heavy naphthas. The greatest effect was observed in the content of cycloalkanes (Figure 3), which represented the major group of all heavy naphthas. The content of cycloalkanes decreased by more than 4 wt.% when the reaction temperature was increased from 410 to 430 • C. The intensive opening of the naphthenic ring and subsequent formation of n-alkanes or iso-alkanes was, therefore, not observed. The opening of the naphthenic ring during hydrotreating requires strong hydrogenolytic functionality provided by noble metals [32]. The differences in cycloalkanes content between the naphthas obtained from the neat HVGO and mixed raw material were negligible. The content of aromatic hydrocarbons also slightly decreased with an increase in the reaction temperature. The naphthas obtained from raw material containing PW had a lower content of aromatics than the naphthas originating from neat HVGO. This could be attributed to the absence of aromatic hydrocarbons in the petroleum wax. On the other hand, the content of n-alkanes and iso-alkanes in products was higher at a higher reaction temperature, which is a consequence of the more extensive cracking and cleaving of aliphatic side-chains from alkyl-cycloalkanes and alkyl-aromatics. The addition of the PW into the feedstock caused a moderate increase in the content of n-alkanes and iso-alkanes of approx. 1 wt.%. The heavy naphtha fractions obtained from hydrocracking at 430 °C had slight lower distillation curves than the heavy naphthas obtained from hydrocracking at 410 ° There were no significant differences between heavy naphthas obtained from differe raw materials. Some other physico-chemical properties of the heavy naphthas are show in Table 3. A high reaction temperature and the presence of the petroleum wax in t feedstock reduced the density of the obtained heavy naphthas, but the influence of t reaction temperature was much greater. The contents of sulfur and nitrogen were comp rable for all samples with regard to their relatively low values. On the other hand, t slightly higher content of sulfur and nitrogen in products obtained at a temperature of 4 °C was probably caused by the presence of aliphatic sulfur and nitrogen compoun formed during the hydrocracking. The reaction temperature also influenced the grou type composition of the heavy naphthas. The greatest effect was observed in the conte of cycloalkanes (Figure 3), which represented the major group of all heavy naphthas. T content of cycloalkanes decreased by more than 4 wt.% when the reaction temperatu was increased from 410 to 430 °C. The intensive opening of the naphthenic ring and su sequent formation of n-alkanes or iso-alkanes was, therefore, not observed. The openin of the naphthenic ring during hydrotreating requires strong hydrogenolytic functionali provided by noble metals [32]. The differences in cycloalkanes content between the nap thas obtained from the neat HVGO and mixed raw material were negligible. The conte of aromatic hydrocarbons also slightly decreased with an increase in the reaction tempe ature. The naphthas obtained from raw material containing PW had a lower content All middle distillates obtained from primary hydrocracking products had a similar distillation profile and their composition corresponded to that of diesel fuel. Table 4 shows physico-chemical properties of the analyzed middle distillates. Both products obtained from hydrocracking at 390 • C had the same density. The density of the middle distillates decreased with an increasing reaction temperature. Furthermore, density was influenced by the type of the feedstock to a greater extent than kinematic viscosity. The products obtained from the feedstock containing the PW had a lower density than those originating from the neat HVGO. The sulfur and nitrogen content in middle distillates showed a similar trend to primary liquid products. The content of sulfur and nitrogen increased slightly at the highest tested reaction temperature of 430 • C compared to the temperature of 410 • C. This is probably due to the presence of aliphatic sulfur and nitrogen compounds formed during the hydrocracking which can be easily hydrotreated on the hydrotreating catalyst placed at the end of the hydrocracking unit [5,6].  All middle distillates obtained from primary hydrocracking products had a similar distillation profile and their composition corresponded to that of diesel fuel. Table 4 shows physico-chemical properties of the analyzed middle distillates. Both products obtained from hydrocracking at 390 °C had the same density. The density of the middle distillates decreased with an increasing reaction temperature. Furthermore, density was influenced by the type of the feedstock to a greater extent than kinematic viscosity. The products obtained from the feedstock containing the PW had a lower density than those originating from the neat HVGO. The sulfur and nitrogen content in middle distillates showed a similar trend to primary liquid products. The content of sulfur and nitrogen increased slightly at the highest tested reaction temperature of 430 °C compared to the temperature of 410 °C. This is probably due to the presence of aliphatic sulfur and nitrogen compounds formed during the hydrocracking which can be easily hydrotreated on the hydrotreating catalyst placed at the end of the hydrocracking unit [5,6].
The increase in the reaction temperature from 390 to 410 °C favorably influenced the cetane index (CI), but further increasing the reaction temperature to 430 °C did not lead to additional improvement in this parameter. All middle distillates obtained from the feedstock containing PW had a higher cetane index than those obtained from the neat   The increase in the reaction temperature from 390 to 410 • C favorably influenced the cetane index (CI), but further increasing the reaction temperature to 430 • C did not lead to additional improvement in this parameter. All middle distillates obtained from the feedstock containing PW had a higher cetane index than those obtained from the neat HVGO (Table 4). Low temperature properties of middle distillates were excellent-the cloud point of all tested samples was lower than −25 • C (Table 4). Small differences not exceeding 3 • C are not significant.
The middle distillates contained approximately 5 to 8 wt.% of n-alkanes (Figure 4). Their content increased with an increase in the reaction temperature of hydrocracking. All distillates obtained from the feedstock containing the PW had a higher content of n-alkanes than those obtained from pure HVGO, the difference slightly increased with an increasing reaction temperature. The middle distillates contained approximately 5 to 8 wt.% of n-alkanes (Figure 4). Their content increased with an increase in the reaction temperature of hydrocracking. All distillates obtained from the feedstock containing the PW had a higher content of n-alkanes than those obtained from pure HVGO, the difference slightly increased with an increasing reaction temperature.  Correspondingly, all middle distillates obtained from the mixed feedstock contained a lower content of aromatic hydrocarbons than those originating from the neat petroleum  Correspondingly, all middle distillates obtained from the mixed feedstock contained a lower content of aromatic hydrocarbons than those originating from the neat petroleum raw material (HVGO). The dependence of the content of aromatics on the reaction temperature showed a minimum at 410 • C. This could be explained by the influence of temperature on reaction equilibrium. The formation of aromatic hydrocarbons is preferred at high reaction temperatures, even though the reaction mixture contains excess hydrogen, thereby promoting de-aromatization at mild temperatures and sufficient residence times. This hypothesis was confirmed by calculations of the theoretical composition of an equilibrium reaction mixture resulting from the hydrogenation of naphthalene with hydrogen (at 1000 L/L hydrogen/feed volume ratio and 18 MPa). Equilibrium conditions were considered such that the minimum Gibbs energy was attained. Figure 5 shows the effect of temperature on the equilibrium composition of the reaction mixture with an apparent increase in the naphthalene concentration at elevated temperatures. It can be concluded that the optimum reaction temperature is a compromise between the reaction kinetics of hydrogenation reactions and the equilibrium composition of a reaction mixture.
(at 1000 L/L hydrogen/feed volume ratio and 18 MPa). Equilibrium conditions were considered such that the minimum Gibbs energy was attained. Figure 5 shows the effect of temperature on the equilibrium composition of the reaction mixture with an apparent increase in the naphthalene concentration at elevated temperatures. It can be concluded that the optimum reaction temperature is a compromise between the reaction kinetics of hydrogenation reactions and the equilibrium composition of a reaction mixture. Although the content of other hydrocarbon groups was not determined directly, it can be expected that a major part of the middle distillates was composed of iso-alkanes and cycloalkanes. The highest yield of them, i.e., approximately 84 wt.%, was reached at 410 °C.
Some properties of the heaviest products, i.e., atmospheric residues, are shown in Table 5 to provide information about the hydrocracking products. From the point of view of raw material for hydrocracking, the products obtained from the mixed feedstock had a lower density and a slightly higher pour point. The dependence of sulfur and nitrogen content on the reaction temperature is the same as heavy naphtha and the middle distillate and is caused by the formation of aliphatic sulfur and nitrogen compounds during hy- Although the content of other hydrocarbon groups was not determined directly, it can be expected that a major part of the middle distillates was composed of iso-alkanes and cycloalkanes. The highest yield of them, i.e., approximately 84 wt.%, was reached at 410 • C.
Some properties of the heaviest products, i.e., atmospheric residues, are shown in Table 5 to provide information about the hydrocracking products. From the point of view of raw material for hydrocracking, the products obtained from the mixed feedstock had a lower density and a slightly higher pour point. The dependence of sulfur and nitrogen content on the reaction temperature is the same as heavy naphtha and the middle distillate and is caused by the formation of aliphatic sulfur and nitrogen compounds during hydrocracking, especially at higher reaction temperatures. The distillation curves of the residues shifted to the lower boiling points with an increasing reaction temperature of the hydrocracking and with the presence of the PW in the feedstock.

Characteristics of the Feedstocks
Heavy vacuum gas oil (HVGO), obtained as a primary product of the oil vacuum distillation carried out at petroleum refinery ORLEN Unipetrol RPA (Litvínov, Czech Republic), was used as a basic feedstock for the hydrocracking. The HVGO was used as a feedstock for the reference experiments and as a major component for preparation of a mixed feedstock. The mixed feedstock was composed of 90 wt.% of the HVGO and 10 wt.% of the petroleum wax (PW), as obtained from the petroleum refinery dewaxing process. Its composition was determined using gas chromatograph equipped with mass spectrometer Focus (Thermo Electron Corporation, Waltham, MA, USA). Both components were blended at the temperature of 80 • C and homogenised. The components as well as the mixed feedstock were analysed by simulated distillation (SIMDIST). The analysis was carried out using a TRACE GC ULTRA (Thermo Fisher Scientific, Waltham, MA, USA) gas chromatograph equipped with an on-column injector, oven cryogenic cooling system and a capillary column Agilent (Santa Clara, CA, USA) J&W WCOT Ulti-metal (5 m × 0.53 mm i.d.: film thickness 0.17 µm). The refractive index of the HVGO, PW and the mixed feedstock was analysed using an Abbe-2WAJ Refractometer (PCE Instruments UK, Southampton, UK).

Hydrocracking
Hydrocracking of the feedstocks was performed in a bench-scale flow reactor equipped with a salt-bath heating system. The dimensions of the reactor were 614 mm (length) and 30 mm (inner diameter). A thermoprobe with an outer diameter of 9 mm was used, in which three thermocouples measuring temperature in the catalyst bed were located. The thermoprobe was placed in the centre of the reactor. The reactor was loaded with 90 g of the commercial amorphous-alumina-silica-supported Ni-W catalyst. A fresh catalyst was used for each type of feedstock. The catalyst was diluted in the volume of 1:1 with an inert, silicon carbide (size 0.1 mm) to ensure proper hydrodynamic conditions over the catalyst bed. SiC (size 1-2 mm) was placed in the reactor below and on the top of the catalyst bed. SiC in the lower part of the reactor (i.e., below the catalyst bed) ensured that the catalyst bed was located in the isothermal zone of the reactor. SiC in the upper preheating part of the reactor (i.e., above the catalyst bed) helped in the good mixing of the feedstock and hydrogen, before entering the catalyst bed. A standard catalyst-activation procedure using hydrogen sulfide was used. A certain amount of time was devoted to the stabilization of the catalyst activity. The temperature inside the reactor was monitored by means of three thermocouples. Adjustable positions of these thermocouples corresponded to the top, middle and bottom of the catalyst bed. A tempered feedstock container was placed on scales and thus the actual and average feed rates were recorded. The feedstock flow rate was kept at 72 g·h −1 , which corresponds to a weight hourly space velocity (WHSV) of 0.8 h −1 . A constant hydrogen flow rate of 72 Ndm 3 ·h −1 was controlled by a mass flow controller. The feedstocks (HVGO and the mixture of HVGO and 10 wt.% of petroleum wax) were hydrocracked at the reaction temperatures of 390, 410 and 430 • C under a hydrogen pressure of 18 MPa. The obtained primary liquid products were cooled down and collected in sealed vessels. In order to quickly assess the chemical composition changes, the refractive index of the primary products using an Abbe-2WAJ Refractometer (PCE Instruments UK, Southampton, UK) was determined.

Processing and Analysis of Products
A small part of all collected products was kept for the further analysis while the main portions were fractionated via distillation to obtain heavy naphtha (boiling range 100-200 • C), middle distillates (boiling range 200-360 • C) and residue (boiling range above 360 • C). A distillation apparatus (Fischer scientific, Waltham, MA, USA) with a SPAL-TROHR HMS 500 spiral column (Fischer scientific, Waltham, MA, USA) with 90 theoretical trays was used for the fractionation. The heavy naphtha fractions were obtained via atmo-spheric distillation using the following parameters: reflux of 1:1, the maximum temperature in the distillation flask of 320 • C and the maximum temperature on the head of the distillation column of 200 • C. The middle distillates were obtained via vacuum distillation using the same reflux ratio, a pressure of 70 Pa, while the maximum temperature at the head of the column was 149 • C.
Three different gas chromatographic methods were used for the evaluation of the hydrocracking products. The SIMDIST method was always applied on all primary hydrocracking products and on all products obtained by their distillation.
The results of the SIMDIST analysis of the primary products were used for the calculation of the conversion (X 360 ) and the yield (Y 360 ) as follows: (1) where: X 360 : conversion to products having b. p. < 360 • C, wt. %. The heavy naphtha fractions and middle distillates were characterized in accordance with the ASTM D2887 method. The group-type analysis of naphtha samples was determined using an Agilent 6890 gas chromatograph (Agilent, Santa Clara, CA, USA) equipped with a split/splitless injector and a capillary column Agilent HP-PONA (50 m × 0.2 mm i.d.; film thickness 0.5 µm). All naphtha components were identified, quantified and assigned to the corresponding hydrocarbon group (n-alkanes, iso-alkanes, cycloalkanes, aromatics). The content of n-alkanes in the middle distillates was determined using a gas chromatograph Agilent 6890 (Agilent, Santa Clara, CA, USA) equipped with a split/splitless injector and a capillary column HP-ULTRA 1 (12 m × 0.32 mm i.d.; film thickness 0.52 µm). The content of n-alkanes was calculated as a sum of area percentage of all n-alkane peaks present in the chromatogram. The values obtained by this determination are not absolute, so they were used for comparison only. The determination of aromatic hydrocarbons in the middle distillates was performed using an HPLC system (Shimadzu, Kyoto, Japan) equipped with a refractometric detector and a Supelcosil column (St. Louis, MO, USA) LC-NH2-NP NP (25 cm × 4.6 mm i.d.; particle size 5 µm). This analysis was performed according to the EN 12916 standard test method.
The elemental composition of the selected samples and raw materials was determined using a Vario EL III (Elementar, Langenselbold, Germany) analyzer (determination of carbon and hydrogen) and TS-100/TN-100 (Mitsubishi, Tokyo, Japan) analyzer (determination of sulfur and nitrogen). The other properties, i.e., density (DMA 4000-Anton Paar, Graz, Austria), kinematic viscosity (SVM 3000-Anton Paar, Graz, Austria), water content (Coulometer WTK-Diram, Prague, Czech Republic), flash point (PMA 5-Anton Paar, Graz, Austria), cloud point and pour point (NTE 450-Normalab, Valliquerville, France) were determined using suitable standard test methods designated for petroleum products. The cetane index of middle distillates was calculated according to ISO 4264 method. Distillation data required for this calculation were obtained from API correlation proposed in the method ASTM D2887.

Conclusions
Hydrocracking of the neat heavy vacuum gas oil (HVGO) and its mixture with 10 wt.% petroleum wax at reaction temperatures 390; 410 and 430 • C and a pressure of 18 MPa was carried out. Although the addition of the petroleum wax (PW) to the feedstock led to mild conversion reduction, the quality of the primary liquid products obtained from