Yield Of Diesel Fraction Research Articles

Utilization of waste tires in the process of thermal cracking of vacuum gas oil

The process of thermal cracking of vacuum gas oil (VGO) with the addition of 10% tire crumb at a temperature of 500 °C and feed rate of 1 h- ¹ was studied. In the course of the study experiments were carried out, which showed that the introduction of tire crumb into the composition of VG promotes the acceleration of conversion of the heavy fraction of VG. Addition of 10% of tire crumb has a positive effect on the cracking process, which is expressed in the increase in the yield of diesel fraction by weight by 2%. Analysis of the material balance of the thermal cracking process of crushed tire crumb shows that under these conditions tire crumb was poorly subjected to thermal transformation. The yield of gasoline fraction and light gas oil fraction in the catalyst composition was only 1% and 7.4% by weight, respectively. The conversion of tire crumb into light fractions including gas oil reached 20.5%. Addition of 10% by weight of tire crumb to the composition of vacuum gas oil increases the yield of gasoline and diesel fractions (light gas oil fractions), while reducing the amount of heavy gas oil. The increase in the yield of diesel fraction is 4% by weight, and the total conversion of blended feedstock reaches 59.5%. Thus, the addition of tire crumb to the composition of vacuum gas oil practically does not affect the total conversion, but increases the yield of light gas oil. This allows us to conclude that the introduction of tire crumb contributes to a more efficient conversion of heavy fractions of vacuum gas oil. After hydrotreating process the obtained diesel and gasoline fractions can be successfully used as components of automotive fuels. Thus, the addition of tire crumb to the thermal cracking process of vacuum gas oil not only improves the conversion of heavy fractions, but also increases the yield of valuable products such as diesel fuel, which is important for the refining industry.

Catalytic advances in vacuum gas oil hydrocracking

Hydrocracking still maintains the pivotal role in the industry owing to the production of highly demanded transportation fuels. Having comprised pretreatment of VGO, comparative research onrecent catalysts, this review paper provides athorough picture about all consecutive steps in the hydrocracking process of vacuum gasoil. Discussing recovery of VGO from vacuum residue with minimum sulfur content, the focus was put on the catalyst characterizations and their influence on the conversion of VGO, the yield of middle distillate, gasoline as well asnaphtha. Both zeolite and amorphous catalysts have undergone a comparative analysis interms of their hydrocracking properties as well as catalytic activities during provided conditions. The article also examines the process of hydrocracking of vacuum gas-oil from Baku oils with the participation of modified aluminosilicate catalyst containing Ni, Mo to obtain high-quality raw materials for environmentally friendly diesel fuel and catalytic cracking process. The hydrocracking process of vacuum gas-oil conducted at 3-8 MPa pressure, 400-450 °C temperature range, in a flow-type Hungarian unit with a reactor capacity of 200 ml. During the investigations of temperature on hydrocracking process it was revealed that, when temperature rises from 400 to 460 °С the yield of diesel fraction increases from 35 to 50% wt. The yield of gasoline fraction constitutes 0-6% wt. and the produce of residue fraction decreases from 65% to 45%. With increasing of temperature from 400 °C to 450 °C the amount of sulphur decreases from 0.01% to 0.005% in composition of diesel fraction. Keywords: vacuum gasoil; hydrocracking; diesel fraction; alumosilicate; catalyst; hydrodesulfurization.

Sustainable Diesel from Pyrolysis of Unsaturated Fatty Acid Basic Soaps: The Effect of Temperature on Yield and Product Composition.

The production of sustainable diesel without hydrogen addition remains a challenge for low-cost fuel production. In this work, the pyrolysis of unsaturated fatty acid (UFA) basic soaps was studied for the production sustainable diesel (bio-hydrocarbons). UFAs were obtained from palm fatty acids distillate (PFAD), which was purified by the fractional crystallization method. Metal hydroxides were used to make basic soap composed of a Ca, Mg, and Zn mixture with particular composition. The pyrolysis reactions were carried out in a batch reactor at atmospheric pressure and various temperatures from 375 to 475 °C. The liquid products were obtained with the best yield (58.35%) at 425 °C and yield of diesel fraction 53.4%. The fatty acids were not detected in the pyrolysis liquid product. The gas product consisted of carbon dioxide and methane. The liquid products were a mixture of hydrocarbon with carbon chains in the range of C7 and C20 containing n-alkane, alkene, and iso-alkane.

Study the pressure effect on hydrocracking process of vacuum gasoil

The paper presents the results of study on the pressure effect on hydrocracking process of vacuum gasoil from the mixture of Baku oils with the presence of aluminosilicate catalyst modified Ni, Mo. Hydrocracking of vacuum gasoil in the presence of aluminosilicate catalyst, modified Ni, Mo has been carried out in 3−8 MPa pressure in the temperature interval of 400−450 оС with the speed of 0.7−2.0 h-1 on Hungarian unit with reactor capacity in 200 ml. The pressure effect on the hdyrocracking process has been studied in the diapason of 3-8 MPa. It was defined that while the pressure is increasing from 3 to 5 MPa, the yield of diesel fraction also increases from 35 to 44 % mass. The pressure increase from 5 to 8 MPa increases the yield of diesel fraction for 48 %, i.e. the growth of only for 4 % is observed. It was considered practical to conduct hydrocracking process in 5MPa, as the pressure increase from 5 to 8 MPa leads to the significant increase of capital expenses.

Hydrocracking vegetable oil on borate-containing catalysts: Effect of nature of support

The structure, texture, and acid properties of platinum catalysts on oxide (Al2O3, ZrO2, ZrO2–Al2O3) and borate-containing supports (B2O3–Al2O3, B2O3–ZrO2) are studied. The catalysts are tested in the process of hydrocracking sunflower-seed oil at 380°C, 4.0 MPa, and a weight stock feed rate of 1.0 h–1. It has been found that aluminum oxide (A) contains the γ-Al2O3 phase, zirconium dioxide (Z) includes 85 and 15 rel. % of the monoclinic (M) and tetragonal (T) phases, respectively, while zirconium dioxide with the addition of 2.5 wt % Al2O3 (ZA) comprises 14 and 86 rel. % of the M–ZrO2 and T–ZrO2 phases, respectively. The B2O3–Al2O3 (BA) and B2O3–ZrO2 (BZ) systems modified with boron oxide (20 wt %) are X-ray amorphous. A Pt/BA catalyst differs from a Pt/A catalyst, while a Pt/BZ catalyst has a larger specific surface area and acidity than Pt/Z and Pt/ZA catalysts and contains Bronsted acidic centers (BACs) along with Lewis acidic centers (LACs). Only LACs are present on the surface of Pt/A, Pt/Z, and Pt/ZA catalysts. The LAC/BAC ratio in Pt/BA and Pt/BZ catalysts is 0.3 and 1.0, respectively. All the catalysts provide complete oil conversion to give C5+ hydrocarbons with a yield of 81.7–87.3 wt %. Pt/A catalyzes mainly decarboxylation and hydrogenation–dehydration reactions, while Pt/Z and Pt/ZA provide decarboxylation. The yield of diesel fraction reaches 71.8–73.9 wt % with an n-alkane content of 94.0–95.9 wt %. One-stage oil hydrocracking with the prevalence of hydrodecarbonylation and hydrogenation–dehydration reactions occurs on Pt/BA and Pt/BZ catalysts for 20 h to give the yield of the diesel fraction of at least 81.4 and 74.4 wt % and the total content of iso-alkanes and cycloalkanes of at least 28.3 and 60.7 wt %, respectively.

Conversion of triglycerides to fuel hydrocarbons over a Pt–Pd–Al–HMS catalyst

The hydroconversion of rapeseed oil fatty acid triglycerides (TGs) over a mesoporous platinum–palladium aluminosilicate catalyst has been studied. It has been shown that, in a temperature range of 250–375°C at a hydrogen pressure of 60 atm, the TGs undergo complete deoxygenation and the resulting products undergo isomerization. Under optimum process conditions, the diesel fraction yield is 94%. The resulting fraction can be used as an environmentally safe fuel component.

Hydrothermal liquefaction of freshwater and marine algal biomass: A novel approach to produce distillate fuel fractions through blending and co-processing of biocrude with petrocrude

Biocrude was produced from Tetraselmis sp. – a marine alga and Arthrospira platensis – a fresh water alga using hydrothermal liquefaction (HTL) process. Considering the constraints in cultivating algae for replacing 100% petrocrude, this study evaluated the option of blending and co-processing algal biocrude with petrocrude. Biocrudes obtained from algal strains cultivated in fresh water and sea water were blended with petrocrude at 10% concentration and the characteristics were studied using FT-IR and CNS SIMDIST. True Boiling Point (TBP) distillation was carried out to assess yields and properties of distillates of blended biocrudes. Biocrudes obtained from both algae were light crudes and the blended crudes recorded distillate yields of 76–77wt%. The yield of light naphtha fraction of biocrude blends was 29–30%; whereas the yield of diesel fraction was about 18%. This study proposes blending and co-processing of algal biocrude with petrocrude to produce drop-in biofuels.

Hydrocracking of vacuum gas oil in the presence of catalysts NiMo/Al2O3–amorphous aluminosilicates and NiW/Al2O3–amorphous aluminosilicates

Supported nickel–molybdenum and nickel–tungsten hydrocracking catalysts prepared using a support that consists of 70% Al2O3 and 30% amorphous aluminosilicate were characterized by nitrogen and mercury porosimetry, IR spectroscopy of adsorbed CO, and high-resolution electron microscopy. The catalytic tests in hydrocracking of vacuum gas oil containing 3.39% sulfur showed that the nature of the hydrogenating component (NiMo or NiW) only slightly influences the vacuum gas oil conversion and the diesel fraction yield, but noticeable influences the properties of the diesel fraction obtained. The catalyst NiMo/Al2O3–amorphous aluminosilicates, compared to NiW/Al2O3–amorphous aluminosilicates, ensures lower sulfur content in the diesel fraction obtained, whereas the catalyst NiW/Al2O3–amorphous aluminosilicates allows obtaining a diesel fraction with lower content of polyaromatic compounds.

Silica-alumina based nickel-molybdenum catalysts for vacuum gas oil hydrocracking aimed at a higher diesel fraction yield

Nickel-molybdenum hydrocracking catalysts based on amorphous silica-aluminas (ASAs) with Si/Al = 0.3–1.5 have been prepared using chemicals and methods available for catalyst plants. The acidic properties of the ASA surface have been investigated by IR spectroscopy of adsorbed CO, and it has been demonstrated that the Si/Al ratio has an effect on the concentration and strength of Bronsted and Lewis acid sites in the ASA. The catalysts have been characterized by low-temperature nitrogen adsorption and transmission electron microscopy, and it was found that the Si/Al ratio in the ASA has a considerable effect on the textural properties of the catalysts and only a slight effect on the particle size of the sulfide active component. The catalysts have been tested in vacuum gas oil hydrocracking in a laboratory-scale high-pressure flow reactor under typical industrial hydrocracking conditions. The highest diesel fraction yield (>60 wt % at 400°C) has been obtained with the catalyst based on the Si/Al = 0.9 ASA, which has the strongest Bronsted acid sites. With the catalysts based on the Si/Al = 0.3 and 1.5 ASAs, the diesel fraction yield is much lower. This may be due to the lower concentration and strength of acid sites in these catalysts and their smaller specific surface area. The NiMo catalyst based on Si/Al ≈ 0.9 ASA is recommended for industrial use in refineries aimed at obtaining the maximum possible yield of low-sulfur, high-cetane, diesel fuels.

Vacuum Pyrolysis of Waste Tires by Continuously Feeding into a Conical Spouted Bed Reactor

The continuous pyrolysis of waste tires under vacuum conditions (25 and 50 kPa) has been studied in a pilot plant equipped with a conical spouted bed reactor and operating with continuous feed at 425 and 500 °C. The effects of vacuum on product distribution and properties have been studied. The main effect of vacuum is an increase in the diesel fraction yield of the liquid product. A remarkable yield of isoprene has been obtained operating under vacuum, reaching yields of higher than 7 wt %. Moreover, a positive effect on the quality of the residual carbon black has been observed, given that a decrease in pore blockage gives way to higher surface areas of the carbon blacks obtained. The results show that vacuum operation does not limit the good perspectives for waste tire valorization by pyrolysis in a conical spouted bed, and energy requirements for heating the inert gas and the condensation section are significantly reduced.

Influence of FCC catalyst steaming on HDPE pyrolysis product distribution

A commercial FCC catalyst based on a zeolite active phase has been used in the catalytic pyrolysis of HDPE. The experimental runs have been carried out in a conical spouted bed reactor provided with a feeding system for continuous operation. Different treatments have been applied to the catalyst to improve its behaviour. This paper deals with the optimization of catalyst steaming and pyrolysis temperature in order to maximize the production of diesel-oil fraction. The performance of the fresh catalyst has been firstly studied at 500 °C. This catalyst gives way to 52 wt% gas yield, 35 wt% light liquid fraction and a low yield of C 10 + fraction (13 wt%). After mild steaming (5 h at 760 °C) the results show a significant improvement in product distribution. Thus, gas yield decreases to 22 wt%, the yield of light liquid is similar to that of the fresh one (38 wt%), whereas the yield of the desired C 10 + fraction increases to 38 wt%. Nevertheless, the best results have been obtained when a severe steaming is applied to the catalyst (8 h at 816 °C) and pyrolysis temperature is reduced to 475 °C. There is a significant reduction in the gaseous fraction (8 wt%). The light liquid fraction has also been reduced to 22 wt%, but the yield of diesel fraction increases to 69 wt%. Moreover, the deactivation of the catalyst has also been studied under the optimum conditions.