PETROLEUM PROCESSING AND PETROCHEMICALS

DEVELOPMENT OF AN INTEGRATED CATALYTIC REFORMING AND HYDROREFINING PROCESS FOR PRODUCING BIO-JET FUEL FROM BIO-OILS

2026, 57(5): 1-9.

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As a renewable resource that is expected to completely replace petroleum based jet fuel in the future, bio-jet fuel has become increasingly important to the aviation industry. At present, the production of jet fuel from bio-oil via HEFA technology has achieved industrial application. Aiming at the problems of complex pretreatment of raw materials and single component of jet fuel in the existing HEFA technology, based on the molecular structure characteristics of bio-oils, the molecular structure of fatty acid methyl ester was catalytically reformed on a special molecular sieve catalyst, so that it was partially converted into aromatics and naphthenes. The catalytic reforming index (CRI) was used to measure the degree of hydrogen transfer and cyclization reactions. Small scall experiments were carried out to obtain the middle distillate rich in aromatics and naphthenes. The middle distillate was hydrotreated to obtain the bio-kerosene rich in aromatics and naphthenes. The experimental results showed that after the fatty acid methyl ester was treated by the integrated technology of catalytic reforming and hydrofining, the yield of bio-jet fuel was more than 65%, the yield of light olefins was about 10%, the net calorific value of bio-jet fuel was 45 MJ/kg, the freezing point was less than -65 ℃, and its density was close to that of petroleum based jet fuel.

STUDY ON THE "REVERSE-ORDER" INTEGRATION FOR THE SEPARATION AND DESULFURIZATION OF FCC WET GAS AND NAPHTHA

2026, 57(5): 10-17.

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Based on the conventional processing flow where fluid catalytic cracking (FCC) wet gas and naphtha are first separated into dry gas, liquefied petroleum gas (LPG), and stabilized gasoline via the absorption-stabilization unit, followed by separate desulfurization. The dry gas is then treated with the alcohol amine method to remove hydrogen sulfide, while the LPG undergoes both the alcohol amine method for hydrogen sulfide removal and catalytic oxidation for mercaptan removal. The stabilized gasoline employs S Zorb adsorptive desulfurization technology to eliminate mercaptans, sulfides, and thiophenic sulfur compounds. A "reverse order" integrated technology was proposed, where FCC wet gas and naphtha first undergo integrated adsorptive desulfurization in two independent reactors, followed by a process similar to FCC absorption-stabilization separation flow, yielding refined dry gas, refined LPG, and refined gasoline. This "reverse order" integrated technology fully leverages the advantages of S Zorb's high desulfurization efficiency, low comprehensive energy consumption, and the high separation precision and mature technology of FCC absorption-stabilization unit. It enhances desulfurization efficiency, simplifies the production process, improves the separation precision and yield of refined gasoline, and reduces octane loss. After adopting the "reverse order" integrated technology, the refined gasoline yield increased by 0.9 percentage point, research octane number rose by 0.6, and the company's economic benefits improved obviously.

DEVELOPMENT AND APPLICATION OF SELECTIVE HYDROGENATION TECHNOLOGY FOR DEEP CATALYTIC CRACKING GASOLINE TO PRODUCE AROMATICS EXTRACTION FEEDSTOCK (RGTA)

2026, 57(5): 18-23.

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The selective hydrogenation technology for catalytic pyrolysis gasoline to produce aromatics-extraction feedstock (RGTA) was developed. A low-aromatics-saturation catalyst, RGA-1, was developed, compared with a reference catalyst it exhibits a markedly lower aromatics saturation while achieving deep denitrogenation. Commercial application results demonstrated that, as processing heavy catalytic pyrolysis gasoline feedstock with a sulfur mass fractions of 840 μg/g, a nitrogen mass fractions of 35.7 μg/g, an olefin mass fractions of 18.3%, and an aromatica mass fractions of 57.5%, the aromatics saturation rate of the hydrogenated product was 3.8%. The mass fractions of sulfur and nitrogen in the C₆—C₈ fraction of hydrogenated product were both less than 1.0 μg/g. The technology showed excellent selectivity, low aromatics saturation rate, stable long-term operation, and produces feedstock meeting the requirements for subsequent aromatic extraction units.

DEVELOPMENT AND APPLICATION OF COMBINED PROCESS OF EXTRACTIVE DISTILLATION AND HYDROGENATION OF REFINERY C₄

2026, 57(5): 24-31.

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In order to solve the problem of insufficient utilization of C4 resources as high-value chemicals in refineries, the coupling process of alkane/olefin extractive distillation and low reaction temperature rise hydrogenation process was proposed, and the C4 resources in a refinery were classified and utilized. The pinch technology is applied to optimize the heat exchange process, and realize the normal production and shutdown of the heating furnace, which can greatly save steam consumption by using low-temperature heat. The 600 kt/a unit built by this technology has been successfully started up at one time, the maximum reactor load can reach 120%, the purity (mass fraction) of isobutane product is 99.9% with sulfur mass fraction less than 0.5 μg/g, the purity of n-butane product is 97% with sulfur mass fraction less than 0.5 μg/g, the purity of rich butene is 95%, the actual energy consumption is significantly lower than the design value, and the unit operates stably. It shows that the technology realizes the effective utilization of C4 resources in refineries and creates higher benefits for enterprises.

STUDY ON CONDITIONS OF CLAY TREATING OF PARAFFIN WAX

2026, 57(5): 32-35.

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The technological process and characteristics of clay treatment to refine paraffin wax are introduced. The effects of different clays are compared. The optimal clay for the treatment of deoiled wax is selected, and its most suitable reaction conditions are studied. The experimental results show that: when the clay addition amount is 2.0%（w）, the contact temperature is 110 ℃, and the contact time is 50 min, the clay produced by Manufacturer A achieves the best effect. For the No.66 wax feedstock produced by a refinery, under the conditions of a clay addition of 4.0%,a contact temperature of 110 ℃ and a contact time of 50 min , the Saybolt color of product can reach ＋2, and clay treatment significantly improves the color of the wax feedstock.Using the clay-treated wax as the feedstock for hydrofining, under the process conditions of a reaction pressure of 8.0 MPa, a reaction temperature of 260 °C, a liquid hourly space velocity of 0.9 h^-1 and a hydrogen-to-wax volume ratio of 300, the Saybolt color of the hydrofined product can reach above +25, and the photo-stability (color number per SH/T 0403) can reach 7, meeting the specification requirements for semi-refined wax.

THE FCC SLURRY MEDIUM-PRESSURE HYDROUPGRADING - DISTILLATE CUTTING COMBINED PROCESS FOR PREPARING RUBBER PLASTICIZERS

2026, 57(5): 36-43.

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Taking the catalytic cracking (FCC) slurry from a certain petrochemical company as the raw material, a combined process of hydroupgrading and distillate cutting is employed. The test results show that the optimal process conditions for hydroprocessing are as follows:a reaction temperature of 320 ℃,a reaction pressure of 8 MPa,a volumetric space velocity of 0.6 h^-1, and a hydrogen-to-oil volume ratio of 1000.The distillation fractionation of the hydrogenation product is carried out, and the fraction between 400 ℃ and 540 ℃ can be used as a high-quality aromatic rubber plasticizer.The yield of this product is 37.53%, the CA (thepercentage of carbon atoms on the aromatic ring to the total number of carbon atoms) is 21.92%, and the mass fraction of PCA is 2.90%.The product properties all comply with the standards of GB/T 33322 for product A1820.The comparative analysis of the Fourier transform infrared spectroscopy (FT-IR) and nuclear magnetic resonance hydrogen spectroscopy (¹H-NMR) spectra of the products revealed that most of the polycyclic aromatic hydrocarbons in the feedstock oil underwent side-chain hydrogenation cracking and hydrogenation saturation reactions, converting into short-side-chain alkane molecules, and the product structure gradually became stable.

DISCUSSION ON ADDING ETHANE FEEDSTOCK CASE FOR A NEW ETHYLENE PLANT

2026, 57(5): 44-48.

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A new 1.0Mt/a ethylene plant adopts SINOPEC′s proprietary ethylene technology(CBL+LECT),with naphtha serving as the base operating conditions.It is planned to purchase 130kt/a of high-quality ethane as cracking feedstock. Without changing the annual ethylene production capacity of 1.0Mt/a, the plant intends to integrate an ethane operating conditions. Compared with the base case, the total ethylene plant feedstock in the ethane case decreases by 208.6kt/a, and the ethylene yield increases by 2.57 percentage points.This study estimates the changes in equipment load and potential bottlenecks in the compression and separation unit under the ethane operating conditions. It also explores the directions for adjustments in ethane storage and preheating. According to calculations, under ethane-based operation, the loadratio/temperatureratio difference for the CFT and the intermediate reboiler in the ethylene tower increases by 26% and 23% respectively; the recycled ethane volume rises by 25%.It is necessary to carry out the design of increasing the corresponding equipment load capacity to realize the processing of purchased ethane feedstock.

THE CHALLENGES AND OPTIMIZATION MEASURES FOR HIGH-LOAD OPERATION OF DIESEL HYDROTREATING UNIT

2026, 57(5): 49-54.

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The diesel hydrotreating unit encountered constraints in capacity enhancement and stable operation under high-load conditions. Through detailed analysis of process conditions and equipment operations, key bottlenecks were identified: insufficient hydrogen supply, catalyst activity decline, ammonium salt crystallization corrosion in high-pressure heat exchangers, overloading of heating furnaces, and inadequate cooling capacity of air coolers. To address these limitations, targeted optimization measures were implemented including hydrogen purity improvement, feedstock property control, boundary condition operation optimization, periodic professional flushing of heat exchangers, enhanced air cooler efficiency, and refined heating furnace operation parameters. After implementing these measures, the purity of mixed fresh and recycled hydrogen in the hydroprocessing unit increased from 88.9% and 83.5% to above 90% and above 85%, respectively. The new hydrogen consumption decreased by 5% to 10%, the process parameter edge control rate approached 90%, the reactor temperature was stably controlled at around 315℃, andthe decline trend of catalyst activity was significantly slowed down. Simultaneously, the heat exchange efficiency of the high-pressure heat exchanger, the cooling effect of the air cooler, and the thermal efficiency of the furnace were significantly improved. These improvements jointly ensured the stable operation of the unit under high load and brought about significant economic benefits.

STUDY ON THE DISTRIBUTION OF SULFUR TYPES IN HYDROGENATED ATMOSPHERIC RESIDUE AND ITS COKING PRODUCTS

2026, 57(5): 55-61.

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Through analyzing the properties and compositional structures of atmospheric residue (AR) at different hydrodesulfurization (HDS) depths, the influence of HDS depth on the characteristics of hydrotreated AR and the distribution of sulfur-bearing compound types was investigated. The results indicate that with increasing HDS depth, the aromaticity of hydrotreated AR decreases, while the number of alkyl substituents on aromatic rings in its molecular constituents increases. The predominant sulfur-containing compounds in hydrotreated AR are identified as S1, S2, S1O1, and N1S1-type species. As HDS depth increases, the relative abundances of these major sulfur compounds decline, and sulfur compounds are found to be more readily removed than nitrogen compounds. The most abundant sulfur compound in hydrotreated AR is S1, 90% of which resides in the >500?°C narrow distillation fraction and is primarily composed of benzothiophene- and dibenzothiophene-type structures. Coking test results reveal that with increasing HDS depth, the yields of coking gas, gasoline, diesel, and wax oil fractions from residue coking rise progressively—among which the yield of coking wax oil increases most significantly—while the yield of petroleum coke declines. Concurrently, the sulfur content proportion in coking gas and petroleum coke decreases, whereas the sulfur content proportion in liquid coking products increases.

MODEL ESTABLISHMENT AND RESEARCH OF THE ADSORPTIVE SEPARATION PROCESS FOR NORMAL C₅ AND C₆ PARAFFINS

2026, 57(5): 62-69.

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Under the conditions of an adsorption temperature of 140 ℃ and an adsorption pressure of 2.0 MPa, the static adsorption method was employed to investigate the saturated adsorption capacity and adsorption equilibrium constants of different concentrations of C₅–C₉ n-paraffins on the adsorbent. The dynamic breakthrough curve method was used for data fitting to obtain the mass transfer coefficients of each component on the adsorbent. Based on these parameters, a n-C₅and n-C₆ adsorption pulse test model was established. The model was validated through multi-component pulse experiments, with relative deviations between simulated and experimental values being less than 3%, indicating the reliability of both the model and the regressed parameters. Finally, an adsorption separation process model for C₅ and C₆ n-paraffins was developed to examine the effect of different numbers of adsorption beds on separation performance. The results show that the separation performance improves as the number of beds increases. However, when the number of beds reaches 12 or more, the improvement in separation performance becomes relatively small. Considering both investment costs and operational convenience, the optimal number of beds was determined to be 12.

STUDY ON CHEMICAL HYDROGEN CONSUMPTION IN HIGH-GRAVITY MICROBUBBLE-ENHANCED DIESEL HYDROFINING PROCESS

2026, 57(5): 70-77.

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A high-gravity (HiGee) microbubble upward-flow liquid-phase hydrogenation reactor was utilized for the hydroprocessing of blended diesel feedstock. Under a operating conditions of 8 MPa pressure and a hydrogen-to-oil volume ratio of 150, the contents of sulfides, nitrides and aromatic compounds in the hydrogenation products were quantified at different axial positions of the reactor. Hydrogen consumption associated with hydrodesulfurization (HDS), hydrodenitrogenation (HDN) and aromatics saturation (HDA) reactions was calculated via the chemical equation method, followed by the establishment of a hydrogen consumption kinetic model. Results showed that at the initial reaction stage, the HiGee microbubble process exhibited distinct superiority in sulfide and nitride removal; however, its hydrogen consumption was higher than that of the conventional process, with HDA hydrogen consumption accounting for a substantial proportion of the total hydrogen consumption. As the reaction proceeded, the discrepancy in hydrogen consumption between the two processes gradually narrowed. Kinetic analysis revealed slightly lower apparent activation energies and higher reaction rate constants for all reactions in the microbubble process compared with the conventional process, confirming its enhanced reaction kinetics. With rising reaction temperature, the hydrogen consumption of all reactions increased overall for both liquid-phase hydrogenation processes. However, the mass transfer advantage of the microbubble process diminished with increasing temperature, leading to a progressive reduction in its hydrogen?consumption difference relative to the conventional process. By effectively enlarging the gas-liquid mass transfer area, the HiGee microbubble technology intensifies the hydrogenation process and improves hydrogen utilization efficiency, providing a theoretical foundation for the optimization and industrial application of diesel liquid-phase hydrogenation processes.

RESEARCH ON NANO-CERIA-SYNERGIZED CATALYTIC CRACKING CATALYST FOR ENHANCING LIGHT OLEFIN PRODUCTION

2026, 57(5): 78-85.

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To explore the application potential of nanoscale cerium oxide (nano-CeO2) in catalytic cracking processes for enhancing light olefin yield, this study conducted experiments on a fixed fluidized-bed reactor, a continuous-feed pilot-scale unit, and a commercial 350 kt/a catalytic cracking unit. Results from the small-scale tests showed that loading nano-CeO2 onto the catalyst increased light olefin yield, with a more pronounced enhancement observed at lower reaction temperatures. An optimal loading range was identified; beyond this range, the promotional effect gradually diminished. Pilot-scale trials demonstrated that, at a theoretical nano-CeO2 loading of 3 760 μg/g on the catalyst, light olefin yield increased by 3.60 percentage points and conversion rose by 1.87 percentage points. Validation on the industrial unit further confirmed the feasibility and effectiveness of this approach. Characterization by pyridine adsorption Fourier-transform infrared spectroscopy (Py-IR) and ammonia temperature-programmed desorption (NH3-TPD) revealed that the incorporation of nano-CeO2 increased both Br?nsted acid site density and the amount of medium-strong acid sites on the catalyst. This promoted carbocation formation and subsequent cracking reactions, thereby enhancing feedstock conversion and light olefin yield.

PREPARATION OF Pd₄S/Al₂O₃ CATALYST AND ITS CATALYTIC PERFORMANCE IN ANTHRAQUINONE HYDROGENATION TO HYDROGEN PEROXIDE

2026, 57(5): 86-91.

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As a green oxidant, hydrogen peroxide is predominantly produced via the anthraquinone process, which currently faces the core challenge of unsatisfactory catalytic performance using traditional palladium-based catalysts. To address this, this work focuses on the construction of the Pd₄S active phase and investigates its performance in the anthraquinone hydrogenation for hydrogen peroxide production. Using PdSO₄ as a precursor, a Pd₄S/Al₂O₃ catalyst was successfully prepared via high-temperature H2 reduction. Structural characterization (XRD, XPS, CO-IR, etc.) reveals that the introduction of S atoms alters the coordination environment of Pd atoms, resulting in more isolated active sites. Meanwhile, the electronic interaction between Pd and S significantly modulates the electron density of Pd, enhancing the adsorption and activation capacity of the carbonyl group in the anthraquinone molecule during the reaction, thereby effectively improving both activity and selectivity. In the anthraquinone hydrogenation reaction, the Pd₄S/Al₂O₃ catalyst exhibits excellent catalytic performance, achieving a hydrogenation efficiency of 16.4 g/L within 60 minutes, which represents an approximately 34% improvement compared to the conventional Pd/Al₂O₃ catalyst. This study provides a new strategy of synergistic electronic and geometric modulation for the development of high-performance anthraquinone hydrogenation catalysts.

OPTIMIZATION OF PRODUCT QUALITY AND FEED OVER-VAPORIZATION RATE IN THE MAIN FRACTIONATION SYSTEM OF HYDROCRACKING UNIT

2026, 57(5): 92-101.

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The main fractionation system is the primary energy-consuming unit of the hydrocracking unit, where the feed over-vaporization rate and product separation degree directly affect unit operation and energy consumption. Based on this, a rigorous mechanistic model constructed using PRO/Ⅱ software was employed to simulate the entire process of the main fractionation system in a hydrocracking unit. The results revealed that the feed over-vaporization rate determines the top cooling load of the main fractionation column, the furnace heat load, the bottom steam injection rate, and the heat load of the jet fuel/diesel side-line column. The heat load of the diesel side-line column and the furnace load showed weak correlation with the separation degree δ₁ between jet fuel and crude gasoline. The heat load of the jet fuel side-line column was largely unaffected by the separation degree δ₂ between diesel and jet fuel. Subsequently, a 4-5-7 structure BP neural network surrogate model was established to optimize the main fractionation system, with the objective function being the minimization of annualized total cost. The genetic algorithm was used to solve for the optimal combination of feed over-vaporization rate and product separation degree. The results indicated that the optimal feed over-vaporization rate is 40.67%, and the optimal product separation degrees δ₁ and δ₂ are -0.06 ℃ and -0.64 ℃, respectively. Under these optimal conditions, the main fractionation system can increase economic benefits by 6.669 million Yuan per year.

RESEARCH ON THE APPLICATION OF LARGE MODEL TECHNOLOGY IN PRODUCTION OPTIMIZATION OF REFINING AND PETROCHEMICAL INDUSTRY

2026, 57(5): 102-113.

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Large model technology serves as the core technical engine driving the transformation of the refining and chemical industry toward "zero-carbon, efficient, and intelligent" development. Its capabilities in multi-modal integration, data-driven decision-making, and dynamic optimization can address the pain points and challenges in the full-chain management and control of the industry. To clarify the adaptability and empowerment path of large model technology for the industry's transformation, this paper systematically sorts out its three-stage evolution from theoretical foundation to scenario deepening, focuses on analyzing the technical implementation logic and value creation mechanism of large model technology in core links such as safe production, production optimization, and equipment maintenance, quantitatively evaluates the cost reduction and efficiency improvement effects of large models combined with typical industry cases, and centers on the business pain points of PetroChina Yunnan Petrochemical Company. Furthermore, it puts forward intelligent optimization schemes for key scenarios including crude oil procurement, unit processing, and equipment anti-corrosion, as well as prospects for digital twin projects. The research shows that large model technology can effectively improve operational efficiency and risk management capabilities by reconstructing the industry's decision-making and management paradigms, thereby providing technical support and paradigm innovation for the intelligent transformation of the refining and chemical industry.

DETERMINATION OF CHLORINE CONTENT IN PYROLYSIS OIL DERIVED FROM WASTE PLASTICS

2026, 57(5): 114-119.

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Two methods, namely monochromatic wavelenth dispersive X-ray fluorescence spectrometry(MWDXRF) and microcoulometry, were used to measure the chlorine content in pyrolysis oil from waste plastics. The effects of sample homogeneity, matrix influence, and coexistence of multiple elements on the measurement results were investigated. The application effects of the two methods in different laboratories were also verified. The results show that when using the MWDXRF method, the influence on the test results of the chlorine element is relatively small when the sulfur mass fraction in the sample is less than 0.5% and the oxygen mass fraction is less than 5%. When using the microcoulometry method, the influence of sulfur element on the chlorine element can be ignored when the sulfur mass fraction is less than 2%. The detection limits of the two methods are 3 μg/g and 0.3 mg/L ,respectively, and the spiked recovery rates are between 92% and 106%. During the actual measurement process, the microcoulometry method is subject to interference from brominated flame retardants present in the waste plastic pyrolysis oil. The test result actually represents the total halogen content in the waste plastic pyrolysis oil, so the measured value is higher than that obtained using the MWDXRF method.The two methods provides reliable data support for the development of low-impurity oil production technology from waste plastics.

APPLICATION OF LIBS TECHNOLOGY IN THE RAPID ANALYSIS OF CATALYTIC MATERIALS

2026, 57(5): 120-124.

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