Applied Petrochemical Research最新文献

Ethylene glycol dry reforming (EGDR) was investigated for the first time on 10% Co/Al₂O₃ and 3% Ce–10% Co/Al₂O₃ catalysts at stoichiometric feed composition under atmospheric pressure and 923–998?K for syngas production. Catalysts were characterized using BET, H₂-TPR, XRD and Raman spectroscopy measurements. The addition of Ce promoter eased the reduction of Co₃O₄ with lower reduction temperature and enhanced metal dispersion. Ce promotion also improved EGDR performance by increasing reactant conversions, syngas yields and reducing undesirable methane formation. The conversion of ethylene glycol and H₂ yield reached up to 71.7% and 69.3%, respectively.

The water–gas shift reaction plays a major role in ammonia and hydrogen plant design and operation. Good performance of the shift catalysts, and attainment of a close approach to equilibrium and, hence, minimization of the CO slip from the catalyst system is critical to the efficient and economic operation of the plant and ensures maximum hydrogen production from the hydrocarbon feedstock. Excessive drying out of catalyst during first reduction was studied to identify its influence on the catalyst during normal operation.

Demulsification of highly aqueous waste oil is difficult to complete by a single process efficiently. The dewatering-type hydrocyclone is used as the unit body and includes the high-voltage electrode to realize demulsification and dewatering ability of the coupling of high-voltage electric and swirling centrifugal fields in waste oil emulsion efficiently. This study considers the influence of heating temperature on demulsification in coupled field. Thus, a heat-strengthening double-field demulsification process is proposed. Specifically, the effect of heat strengthening on demulsification, dewatering, and separation of double-field coupled by numerical simulation and experimental methods was investigated. The temperatures of heat-strengthening were 60?°C, 65?°C, 70?°C, and 75?°C. The results show that the separation efficiency predicted by numerical simulation are in good agreement with the experimental results. And the heat-strengthening can effectively enhance the separation effect of two fields and improve the efficiency of the oil–water separation of industrial waste oil. When the heating temperature is raised from 60 to 65?°C, and from 65 to 70?°C, the separation efficiency increases by approximately 4.1% and 6.7%, respectively.

Energy consumption is a significant issue in operation design for low-cost sustainable production and is accomplished by heat integration giving overall environmental advantages via reducing carbon emissions. Heat recovery is a beneficial tool that determines the minimum cooling and heating demand through recovery and re-use of energy within the process. Thus in this study, process of heat recovery and energy consumption of the fluidized catalytic cracking (FCC) is investigated to recover most of the external energy and reducing the environmental effect in addition to maximizing the productivity with minimum overall cost of the process. Where the performance of the FCC units plays a major role on the overall economics of refinery plants and improvement in operation or control of FCC units, it will result in dramatic economic benefits. The heat integration process is done based on experimental information from pilot scale, mathematical modeling developed and commercial process reported in our earlier study.

This research project focuses on the development of catalysts for syngas production by synthesizing Ni–Co bimetallic catalyst using aluminum oxide (Al₂O₃) and magnesium oxide (MgO) as the catalyst support. Ni/Al₂O₃ (CAT-1), Ni–Co/Al₂O₃ (CAT-2) and Ni–Co/Al₂O₃–MgO (CAT-3) nanocatalysts were synthesized by sol–gel method with citric acid as the gelling agent, and used in the dry reforming of methane (DRM). The objective of this study is to investigate the effects of Al₂O₃ and MgO addition on the catalytic properties and the reaction performance of synthesized catalysts in the DRM reactions. The characteristics of the catalyst are studied using field emission scanning electron microscope (FESEM), Brunauer–Emmett–Teller (BET), X-ray powder diffraction (XRD), transmission electron microscopy, H₂-temperature programmed reduction, CO₂-temperature programmed desorption and temperature programmed oxidation analysis. The characteristics of the catalyst are dependent on the type of support, which influences the catalytic performances. FESEM analysis showed that CAT-3 has irregular shape morphology, and is well dispersed onto the catalyst support. BET results demonstrate high surface area of the synthesized catalyst due to high calcination temperature during catalysts preparation. Moreover, the formation of MgAl₂O₄ spinel-type solution in CAT-3 is proved by XRD analysis due to the interaction between alumina lattice and magnesium metal which has high resistance to coke formation, leading to stronger metal surface interaction within the catalyst. The CO₂ methane dry reforming is executed in the tubular furnace reactor at 1073.15?K, 1?atm and CH₄/CO₂ ratio of unity to investigate the effect of the mentioned catalysts. Ni–Co/Al₂O₃–MgO gave the highest catalyst performance compared to the other synthesized catalysts owning to the strong metal–support interaction, high stability and significant resistance to carbon deposition during the DRM reaction.

An advanced grid system design was developed to capture accurately the effects of geometrically complex features such as geological features (faults, pinch outs and inclined beddings) and well-related phenomenon (multilateral wells of general orientation) in triangular coordinates. Modeling these effects can have significant impact on the accuracy of the simulation and prediction of reservoir performance as well as reservoir fluid flow using conventional grid designs. The finite difference method provides additional difficulty in capturing geological features in typical reservoir flow and grid model simulators. Hence, the orthogonal collocation method was used for simulating multiphase reservoir flow equations in triangular curvilinear coordinates (left[ {xi left( r right),xi left( theta right),xi left( z right)} right]) of domain [0,1] that were derived from Cartesian coordinates (left( {x,y,z} right)). This was to accommodate general three-dimensional deviated wells and complex reservoir geometry for multiphase flow of hydrocarbon in complex reservoir formations. Based on preliminary field data obtained from multinational oil and gas operator in Nigeria, the proposed model was used to predict saturation, production and petroleum productivity with time and distance in a MATLAB environment. The simulated plots revealed that pressure is parabolic at the center of the reservoir with coordinates (xi (r) =0.4257), reflecting the impact of geological features in the pressure and production flow performance.

The increasing rate of accumulation of plastic waste (PW) is quite disturbing to the world, particularly in developing nations due to its non-biodegradable nature and inadequate waste management practices. The need to properly manage this waste and utilize the potential and chemical energy value that can be derived from this waste justifies the encouragement and employment of newer and better recycling methods and technology of these wastes. Therefore, this has led us to explore the catalytic pyrolysis of plastic waste using zeolite Y synthesized from kaolin deposit in Covenant University, Sango Ota, Ogun state of Nigeria. A stainless steel packed bed reactor was used in the cracking of low-density polyethylene (LDPE) plastic wastes into liquid fuel components at a temperature of 300?℃ using zeolite Y catalyst. The liquid fuel obtained from the catalytic pyrolysis was analyzed using GC–MS. Fifty compounds were identified, which revealed the presence of mostly alkenes and aromatics in the hydrocarbons range of C₈–C₂₉. This is made up of 56% of gasoline fractions range of C₆–C₁₂, 26% of diesel and kerosene fractions range C₁₃–C₁₈, and 10% of fuel oil range C₁₈–C₂₃, while 8% is residual fuel range greater than C₂₄.

This paper reports the production of syngas from two types of O₂-assisted dry reforming of propane, namely oxidative (O₂-dosed) dry reforming (ODR) and dry (CO₂-dosed) partial oxidation (DPOX). Reaction runs were conducted over alumina-supported bimetallic Co–Ni promoted with CeO₂ at 120?kPa and 793–893?K. Ceria promotion improved the carbon deposition resilience of the Co–Ni catalyst. Physicochemical attributes were obtained from liquid N₂ adsorption, H₂ chemisorption and temperature-programmed desorption runs for NH₃, CO₂, CH₄ and C₃H₈. Rate behavior under ODR, DPOX and pure dry reforming could be described consistently with empirical models that are structurally similar to Langmuir–Hinshelwood type relations. Inferences from these models allowed the postulation of the same overall reaction network for the three types of reactions albeit with variation in rate-controlling steps depending on the different product species. On the whole, DPOX seemed to be a superior option for the manufacturing of syngas for downstream olefin FT production due to reduced variability in the H₂:CO ratio and the closeness to unity (0.72–0.95) of the exiting syngas over the range of O₂ partial pressure used.

An extensive literature review of the mechanistic modeling of n-heptane and cyclohexane pyrolysis was carried out. It was shown that Rice–Kossiakoff free radical theory does not adequately account for product distributions of n-heptane pyrolysis in the high conversion regime. Secondary reactions of alpha higher olefins and di-olefins accounted for the major products (ethene, propene and 1-butene) of n-heptane pyrolysis. Predicted product distributions (CH₄, C₂H₄, C₃H₆, 1-C₄H₈ and 1,3-C₄H₆) of n-heptane pyrolysis showed very good agreement with experimental data. The product distributions of cyclohexane pyrolysis in the high conversion regime were rationalized and adequately accounted for using decomposition reactions of cyclohexyl bi-radicals followed by secondary reactions of major primary products such as C₃H₆ and 1,3-C₄H₆. The latter expanded mechanism can be used to model cyclohexane pyrolysis in the high conversion regime. Rate parameters (pre-exponential factors and activation energy) for each of the elementary reactions of n-heptane mechanistic model were either obtained from the literature or estimated using thermochemical parameters. The use of steady state approximation in mathematical modeling of n-heptane pyrolysis led to erroneous results.