The Aromatization Properties of Nano-HZSM-5 Catalyst

Abstract

In this article, the influence of reaction conditions on the aromatization over nano-HZSM-5 zeolite catalyst was investigated. The experimental results showed that nano-HZSM-5 catalyst has the best aromatization properties under the optimal conditions: reaction temperature 430°C, reaction pressure 0.3 MPa, and liquid hourly space velocity 1 h^?1. At the optimal operational conditions, the conversion of olefins in the feedstock was 76.15%. Aromatics yield and the content of olefins, content of aromatics, and content of isoparaffins in liquid product were up to 84.98%, 12.11%, 39.58%, and 35.23%, respectively.     

Reducing Olefins Content of FCC Gasoline Using a NANO-HZSM-5 Catalyst

The study of reducing olefins properties on nano-HZSM-5 catalyst was investigated with a continuous fixed reactor using fraction of fluid catalytic cracking gasoline (75N120°C). The experimental results showed that nano-HZSM-5 catalyst has the best reducing olefins properties under the optimal conditions: temperature 430°C, pressure 0.3 MPa, and liquid hourly space velocity 1 h^-1, and the content of olefins in the feed stock decreased to 12.11% and dropped 31 percentage points. The yield of liquid product, the content of aromatics, and the content of isoalkane in liquid product are up to 84.98%, 39.58%, and 35.23% respectively.     

The Aromatization Properties of Nano-HZSM-5 Catalyst

In this article, the influence of reaction conditions on the aromatization over nano-HZSM-5 zeolite catalyst was investigated. The experimental results showed that nano-HZSM-5 catalyst has the best aromatization properties under the optimal conditions: reaction temperature 430°C, reaction pressure 0.3 MPa, and liquid hourly space velocity 1 h^-1. At the optimal operational conditions, the conversion of olefins in the feedstock was 76.15%. Aromatics yield and the content of olefins, content of aromatics, and content of isoparaffins in liquid product were up to 84.98%, 12.11%, 39.58%, and 35.23%, respectively.     

Influence of ZnO and P2O5 Content on Modified HZSM-5 on Aromatization of FCC Gasoline

Abstract

Catalytic properties of different content of ZnO and P₂O₅ supported on HZSM-5 zeolites were studied in the conversion of FCC gasoline (75°C–120°C) into aromatic hydrocarbons with a temperature of 430°C, a liquid hourly space velocity of 1.0 hr^?1, and a pressure of 0.1 MPa. In the reaction, when the contents of ZnO and P₂O₅ are 2% and 4%, respectively, Zn-P/HZSM-5 showed the highest selectivity and activity to aromatic hydrocarbons and conversion of olefins. The content of aromatics in the liquid product and the yield of aromatics reached as high as 94.53%, 68.87%, and 51.74%, respectively.     

Aromatization of FCC Gasoline Over Modified HZSM-5 Catalyst

Abstract

Zinc and phosphorus incorporated HZSM-5 catalyst was prepared by adopting incipient wet co-impregnation (Zn-P/HZSM-5). Zn-P/HZSM-5 catalyst exhibited the lowest acidity but the highest aromatization activity with stable performance in the studied period of 16 hr. The process conditions on aromatization reaction and the coke deactivation mechanism of Zn-P/HZSM-5 catalyst were studied on a small-scale, fixed bed reactor using FCC naphtha (75–120°C). The weight contents of ZnO and P₂O₅ were 2% and 4%, respectively. Results showed that Zn-P/HZSM-5 catalyst under a temperature of 450°C, liquid hourly space velocity of 1.0 h^?1, and pressure of 0.1 MPa, the conversions of olefins and alkanes are 96.77% and 88.94%, respectively, the contents of olefins, aromatics in liquid product are 6.79% and 74.57%, respectively. Carbon deposition was the major reason for catalyst deactivation due to the catalyst's good performance as a fresh catalyst after regeneration. All of the blending products fitted the standards of Chinese gasoline.     

The Aromatization of Different FCC Naphtha Fractions over a P-Zn/HZSM-5 Catalyst

Abstract

The aromatization reaction performance of P-Zn/HZSM-5 catalyst was investigated on a fixed bed reactor using five fluid catalytic cracked (FCC) gasoline fractions (<100°C, 50°C–100°C, <120°C, 75°C–120°C, and full fraction) as feedstock, and the effect of feedstock on aromatization is discussed. The results showed that the activity and stability of P-Zn/HZSM-5 catalyst for the aromatization of the 50°C–100°C fraction were high in definite reaction conditions. After 16 hr, the content of olefin and aromatics in liquid product were 5.23 and 79.9%, respectively. The liquid product of low olefin and high aromatics was obtained. The distribution of benzene, toluene, and xylene in liquid product of 50°C–100°C fraction was investigated during aromatization, and the result showed that the toluene content was maximum among the three aromatics contents, the benzene content was minimum at the beginning of the reaction, xylene content became maximum, and benzene was still minimum after reacting for 20 hr. The content of C₉ ⁺ aromatics increased at the first stage of the reaction and then decreased with the increasing reaction time.     

纳米HZSM-5沸石催化剂上催化裂化轻汽油的芳构化

利用小型固定床加压反应器在纳米 HZSM-5沸石催化剂上进行了流化催化裂化(FCC)轻汽油(馏出温度小于等于85℃的馏分)的芳构化反应。实验结果表明,在反应温度为360～400℃、反应压力为1.0～3.0 MPa、重时空速为1.0～4.0 h~(-1)、V(H_2)∶V(原料)为260、反应时间48 h 的条件下,FCC 轻汽油中的 C_5~+烯烃转化率为39.11%～97.92%,产物中芳烃净增量为2.59%～19.05%,说明 FCC 轻汽油可在纳米 HZSM-5沸石催化剂上有效进行芳构化反应。汽油收率低和催化剂失活快是 FCC轻汽油在纳米 HZSM-5沸石催化剂上进行芳构化反应需要解决的两个主要问题。对纳米 HZSM-5沸石催化剂进行必要的改性处理及脱除原料中的二烯烃杂质呵以改进 FCC 轻汽油芳构化催化剂的性能。     

Catalytic co-cracking of waste polypropylene and residual fuel oil

Abstract

Industrial waste polypropylene (PP) homopolymer and residual fuel oil (RFO) were pyrolyzed together in presence of catalyst ZSM-5 under the atmospheric pressure with different mixing ratios of the feedstocks. The experiments were carried out in a batch reactor at two different temperatures of 500?°C and 600?°C with the blended mixture (PP/RFO) to catalyst (ZSM-5) ratio of 4:1. The effects of blending ratios between the two feedstocks and temperature with respect to the yield of the products oil, gas, and residual coke were determined. The optimum blending ratio of PP and RFO with respect the higher quantity yield of liquid product was found to be 1:1 at 500?°C. The percentages of liquid fuel, gas, and coke were observed to be 74.8%, 10.2%, and 15% at 500?°C.     

Investigation of the Operating Conditions on Decreasing FCC Gasoline Olefin Content by GOR-Q Catalyst

Abstract

Based on a fixed-fluid-bed reactor and a GOR-Q catalyst, the influence of process parameters on decreasing gasoline olefin content was studied. The results show that the catalyst had an obvious effect on the decreasing gasoline olefins. A higher catalyst-to-oil ratio, lower weighted hourly space velocity, and lower reactor temperature give rise to lower gasoline olefin content. The reduction of fluid catalytic cracking (FCC) gasoline olefin content is achieved by decreasing olefins of low carbon number. Reaction temperature under 520°C and catalyst-to-oil ratio = 7.0 for a GOR-Q catalyst are advantageous for decreasing olefin content of FCC gasoline.     

EVALUATION OF GUARD BED MATERIALS FOR HYDROFINISHING USED LUBE OILS

ABSTRACT

The objective of this study was to survey several types of guard bed materials for their use in hydrotreating used motor oils. The feedstock originated from numerous automobile drainings and was first reclaimed at the National Institute of Petroleum and Energy Research. The effectiveness of the four different guard bed materials was determined by studying product, guard bed and catalyst properties. The candidate guard bed materials were all tested in experiments using a commercial hydrotreating catalyst in a standard, packed bed reactor. A temperature of 325^°C (617^°F), a pressure of 4583 kPa (665 psi), a liquid hourly space velocity of 1 h^?1, and hydrogen flow rate of 748 std. M³/m³ of oil (4200 SCF/BBL) were maintained throughout each of the experimental runs. Though all of the experimental runs, except the activated clay, produced an acceptable base stock color, the greatest improvement in all properties resulted from the use of the activated carbon. The activated carbon also proved to be the most protective of the catalyst bed. The only two materials that gave undersirable results were the activated clay and the alumina spheres.     

Conditions for nonhydrodewaxing reaction of hydrocracking tail oil

Hydrocracking tail oil is used in hydrogenation modification in the hydrocracking process and is an ideal material to produce lube-based oil. Through investigating the effect of operation conditions on properties of dewaxing products under atmospheric pressure, the optimum operation conditions are that reaction temperature is 360°C, volume space velocity is 1.0 h^?1, and distillation temperature is 140°C. Under the optimum condition, the yield of liquid products is higher, and the flash point, pour point, and viscosity of white oil are stable and meet the factory product requirements. Especially, properties of alkane and white oil change little when reaction time is 20 h, which indicates that HZSM-5/Al₂O₃ has better stability. When HZSM-5 molecular sieve catalyst was loaded by pseudo-boehmite, HZSM-5/Al₂O₃ catalyst activity and stability improved and became more beneficial to nonhydrodewaxing reaction of hydrocracking tail oil.     

DEEP DESULPHURISATION OF A DIESEL BLEND IN A PILOT PLANT TRICKLE BED REACTOR

ABSTRACT

A pilot plant investigation was conducted to study the influence of hydrotreating conditions on conversion and characteristics of diesel blend and to determine the severity of operating conditions required to meet the proposed product specifications for diesel fuel in India. A typical diesel blend derived from various refinery streams with sulphur content of 2·06 wt% was hydrodesulphurised over a commercial NiO-MoO₃/Al₂O₃ catalyst in a pilot plant trickle bed reactor. The experiments were conducted at 300–370°C, 30–50 kg/cm², 2·0 3·0 hr^-1 liquid hourly space velocity and constant H₂/oil ratio of 185 m³/m³. The data showed that the diesel blend could be hydrotreated to meet revised product specifications of 0·25 wt% sulphur, 46 cetane number by increasing the severity of operation. The cetane number and aromatic saturation were limited by thermodynamic equilibrium at temperatures above 360°C. The influence of temperature was found to be more pronounced than that of pressure in the range of operating conditions studied.     

An Orthogonal Method for Aromatization Reactions of Shenghua FCC Gasoline

Abstract

Using a confined fluidized bed reactor and aromatization catalysts (LBO-A and LBO-16), the aromatization performance of Shenghua fluid catalytic cracking (FCC) gasoline has been studied in an orthogonal method. The experimental results reveal that the optimum reaction condition for the light oil yield was reaction temperature 420°C, WHSV 40 h^?1, mass ratio catalyst to oil 4 and 75% LBO-A and 25% LBO-16; the optimum reaction condition for aromatics amount in the light oil was reaction temperature 420°C, WHSV 30 h^?1, mass ratio catalyst to oil 5 and 65% LBO-A and 35% LBO-16, the olefin content is remarkably reduced from about 54.7% to 12.8% and 8.7% (by mass), respectively, at the same time the reaction mechanism of aromatization reaction is put forward based on the experimental result.     

BEHAVIOR OF SHALE OIL JET FUELS AT VARIABLE SEVERITIES

ABSTRACT

Catalytic hydro processed ahale oil jet fuels In the USA were characterized and compared with petroleum Jet fuel to demonstrate their possibility as a conventional Jet fuel substitute. The shale oils (Geoklnetica, Occidental, Faraho and Tosco II) were hydrotreated in a 0.0508m ID by 1.524m long reactor containing Ni/MO/A1203 catalyst. The fractionated hydrogenated shale oila at Jet fuel ranges (120-300^°C) were analyzed for composition and physical properties. The increasing hydroprocessing severity proport1nally decreased nitrogen, sulfur, olefins, and aromaticB, and increased hydrogen content. The nitrogen content even at high severity conditions was considerably higher than that of conventional Jet fuel. Sulfur and olefin contents were lower at all severities. The heat of combustion and the physical properties, except the freezing point, were comparable to petroleum Jet fuels. The yields of Jet fuels increased proportionally to increased severity. The study showed that high severity hydroprocessing gave better performance in processing shale oils to Jet fuels.     

Hydrotreating of gasoline and diesel oil fractions over modified alumina/zeolite catalysts

This paper deals with hydrotreating of straight-run gasoline (SRG) and diesel oil fractions (DOF) over new Ni (Co) containing alumina/zeolite catalysts, modified by transition metals (W and Mo) with the addition of P and Ce elements. In hydrotreating of the DOF, the CoO-WO₃-CAR catalyst has the highest hydrodesulphurization activity that reaches 97.2% at 400?°C, P?=?4MPa and V?=?2h^?1. Moreover, increasing of pressure until 5?MPa leads to reducing of the sulfur content up to 0.0007%. The greatest decrease in the pour (?58.9?°C) and the cloud (?56.7?°C) points during the hydrotreating of the DOF is observed using the NiO-MoO₃-CAR catalyst. The octane number of SRG after hydrotreating over the NiO-MoO₃-CAR catalyst rises up to 88.6. Obtained results clearly show that using synthesized catalysts, motor fuel with Euro-5 standard could be obtained.     

EFFECTS OF HYDROTREATING COKER LIGHT GAS OIL ON FUEL QUALITY

ABSTRACT

Coker light gas oil (LGO) derived from Athabasca bitumen was hydrotreated in a fixed bed reactor using two commercial NiO-MoO₃/Al₂0₃ catalysts. The effect of temperature on product quality was investigated in a pilot plant between 330 and 390 °C at 12.4 MPa, space velocity of 0.5 Ir1 and 700 liter of hydrogen per liter of coker LGO (L/L). The product quality was monitored by ^I3C NMR spectroscopy, elemental analysis, density and distillation techniques.

The data showed that coker LGO can be hydrotreated using nickel-molybdenum catalysts at 350 °C, 0.5 h¹, 12.4 MPa and 700 L/L to meet the diesel product specifications, namely, 0.5 wt % sulfur, 20% aromatics and cetane index of 40. The cetane index improvement and aromatic saturation, which are affected by thermodynamic equilibrium at temperature higher than 370?°C, could reach 29 and 86% respectively. The cetane improvement was attributed to aromatic saturation and hydrocracking with hydrogen consumption ranging from 215-340 L/L. The Ketjenfine KF-840 catalyst was found slightly better performance than Procatalyse HR-348 catalyst.     

Production of Lubricating Base Oil Using a Moist SiO2/γ-Al2 O3 Catalyst

Abstract

The catalyst SiO₂/γ-Al₂ O₃ treated by micro-wetness air to produce lubricating base oil was studied in this article. The satisfactory reaction temperature, the treatment temperature, and the proper content of active composition was researched. Under the best reaction conditions with a reaction temperature of 170°C, a reaction pressure at 6.0 Mpa, the volume velocity at 0.5 h^?1. The polymerization of α-olefin was performed at a microreactor and produced lubricating base oil with the kinetic viscosity at 38.19 mm² · s^?1, the bromine number at 5.78 g(Br) · (100 g)^?1, and the pour point at ?43.0°C. Then the structure of the catalyst was determined by Brunauer, Emmett and Teller (BET) technology. The result shows that when the optimal micro-wetness air was 45°C, the reaction temperature was 800°C, and the amount of active composition was 12%, and the catalyst has high catalytic activity and wide market prospect.     

Olefin Reduction of FCC Naphtha Using β-zeolite Catalyst in the Absence of Hydrogen

Abstract

In order to fulfill the requirement of environmental protection, experimentation of reducing FCC gasoline olefin content and optimization of the process operating conditions were studied in a small fixed vector. Under the action of a macroporous molecular sieve catalyst, which consists of active composition of Ni and Mo metal in β-zeolite supporter, when the reaction temperature was 140°C, reaction pressure was 2.0 MPa, and space velocity was 1.0 h^?1–2.0 h^?1, aromatization reactions, isomerization reactions, and hydrogen transfer reactions happened, so that the olefin, benzene, and arene in product gasoline were no more than 35%, 2.5%, and 40%, respectively. The octane number of petroleum is slightly increased. And it overcomes the disadvantage of losing octane by hydrogenation process. The catalyst could be regenerated using a multi-cycle with an average running cycle of about 96 hr. The results show that the process reaction condition is relaxation, process is non-hydrogenation, process flow is simple, technical and economic target is advanced, benefit is high, and cost is low.     

直馏汽油非临氢改质技术的工业应用

摘要扬州石油化工厂20 kt／a直馏汽油非临氢改质装置的运行结果表明,石油化工科学研究院开发的RGw-l型直馏汽油非临氢改质催化剂的活性、选择性高,单程运转周期大于70 d,再生后反应性能完全恢复。改质反应产品收率高,干气产率小于2％。产品品质好,改质后汽油RoN提高30个单位以上,烯烃质量分数小于2％,是汽油降烯烃的优质调合组分;副产液化气的烷烃体积分数达95％以上,可以作为车用液化气。该催化剂还可用于含ct烯烃原料的改质。为直馏汽油和c。馏分的升值利用及炼油厂汽油降烯烃开辟了一条新途径。     

HYDROLIQUEFACTION OF TEXAS LIGNITE IN COAL- AND PETROLEUM-DERIVED SLURRY OILS

ABSTRACT

Hydroliquefaction of Texas lignite (68.5%. C daf) was conducted in a batch autoclave under hydrogen in a coal–derived slurry oil at 90 bar initial pressure for temperatures of 380–460^° C and residence time of 15–60 minutes, or a vacuum distillate from petroleum at 435^° C for 60 minutes and initial H₂–pressure of 60–150 bar, or a vacuum residue from the same petroleum at 435 and 460^° C for 60 minutes and initial H₂–pressure of 90–150 bar or tetralin at 435^°C, 60 minutes and 90 bar initial H₂–pressure. Red mud plus sodium sulfide were added as a catalyst for all experiments. Lignite conversion ranged from 50 to 83%. The products were separated into gases, residue, asphaltenes, oils B,P. above 200^° C, oils B.P. below 200^° C. Total liquid products from coal reached 57% in coal-derived slurry-oil, 56% in vacuum distillate and 64% in vacuum residue at optimum conditions with 32% of product oil B.P. below 200^° C in vacuum distillate and 24% in vacuum residue. When coprocessing lignite with vacuum residue at 120 bar initial pressure, 435^°C and 60 minutes residence time the total mass balance presented an oil yield of 73%. with 32% boiling below 200^°C.