Amount Of Coke Research Articles

The rational mode of nut coke charging into the blast furnace by compact trough-type charging device

The laboratory research on the 1:5 scale physical model of a trough-type bell-less charging device (BLCD) resulted in the rational mode of nut coke charging into the BLCD hopper together with sinter and pellets. This rational mode provides the highest uniformity coefficient of its entering the furnace throat area. The amount of nut coke in the BLCD hopper was at rates of 100, 550 and 1000 kg per 16 tons batch for an actual furnace. In this study, a three-factor Box-Behnken experimental design was used. The following factors have been considered: the sequence of nut coke charging into the hopper, the degree of charge gate opening, and nut coke consumption per feeding. The mathematical description of the output parameter is given by a second-degree polynomial. The significance of each coefficient of the equation resulted from experimental data processing was determined by Student’s t test. The position of nut coke in the centre of the raw material mass in the BLCD hopper resulted in the highest uniformity coefficient and reached 0.85. We investigated the influence of the charging sequence of sinter, quartzite, ore, pellets and nuts into the BLCD hopper on the furnace performance and blast furnace processing during three periods of experienced heats lasting 8–9 days in one of the blast furnaces with a compact trough-type BLCD at Magnitogorsk Iron and Steel Works OJSC (MMK). We evaluated the drainage ability of the hearth on several factors: the amount of slag remaining in the furnace after discharging, the time interval from the start of discharging until the slag occurrence and slag viscosity. In the first period, when nut coke was positioned on the bottom of the BLCD hopper, the amount of slag, remaining in the furnace, was 0.38 of the ladle. When nut coke was charged into the BLCD hopper last (period 2), the amount of slag increased to 0.44 showing the deterioration in the drainage property of the hearth. In the third period, when nut coke was positioned in the centre of the raw material mass, the amount of slag decreased to 0.31 of the ladle that resulted in the improved filtration of melting liquid products through the coke packed bed. The deterioration in the filtering ability of the coke packing in the second period, compared to the first one, was followed by decreased coefficient of the replacement rate of coke by nut coke from 0.64 to 0.59 kg/kg. In the third period, improved penetrability of the coke packing was followed by an increased coefficient of the replacement of coke by nut coke to 0.85 kg/kg. Indicators of the furnace performance intensity according to their types, the drag coefficient of charge by zones and the reduction degree with reducing agents corresponded to the results obtained.

Effect of potassium addition on bimetallic PtSn/θ-Al2O3 catalyst for dehydrogenation of propane to propylene

PtSn/θ-Al2O3 catalysts with different amounts of K (0.14, 0.22, 0.49, 0.72, and 0.96 wt%) are prepared to investigate the K effects on the PtSn catalyst in propane dehydrogenation (PDH). KPtSn catalyst with 0.xx wt% K, 0.5 wt% Pt and 0.75 wt% Sn is designated as xx-KPtSn. PDH was performed at 873 K and a gas hourly space velocity (GHSV) of 53,000 mL/gcat h. The temperature-programmed desorption (NH3-TPD), temperature-programmed reduction (TPR) and CO chemisorption of the KPtSn catalysts with K added revealed the potassium addition blocked the acid sites, promoted the reduction of Sn oxide and decreased the Pt dispersion. The formations of cracking products and higher hydrocarbons on acid sites were suppressed by the K effect of blocking the acid sites. In contrast, K addition at more than 0.72 wt% rather increased cracking products and the amount of coke, resulting in the severe deactivation of catalysts. The high cracking products on the KPtSn catalysts with the high amount of K should not be related to the acid sites, because the acid sites were monotonously decreased with an increase in the amount of K. Instead, the potassium affected the characteristics of PtSn. The interaction between Pt and Sn could be weakened by enriching the reduced Sn, because the K component promoted the reduction of Sn oxide in the TPR experiments. Therefore, the 14-KPtSn catalyst with the low amount of K exhibits the highest stability and selectivity among the prepared KPtSn catalysts due to the compromise of the advantageous (blocking the acid sites) and bad (weakening the interaction between Pt and Sn) effects of the K addition in PDH.

Thorough study of the effect of metal-incorporated SAPO-34 molecular sieves on catalytic performances in MTO process

SAPO-34 and MeAPSO-34s (Me=Fe, Co, Ni, La and Ce) molecular sieves were synthesized and used as catalysts for conversion of methanol to light olefins. X-ray diffraction, scanning electron microscopy, nitrogen adsorption–desorption inductively coupled plasma mass spectrometry, Fourier transform infrared spectroscopy and temperature programmed desorption techniques were used to characterize the synthesized catalysts. Thermogravimetric analysis was used to investigate the amount of coke deposited on the spent catalysts during the reaction. The synthesized MeAPSO-34s had the same chabazite topology structure, while metal incorporation gave rise to the different micropore area and acidity. All the SAPO-34 and MeAPSO-34 molecular sieves were very active and selective catalyst for light olefins production. Metal incorporation improved the catalyst lifetime and favored the ethylene and propylene product. Concerning the yield of light olefins at 425°C and 1bar, NiAPSO-34 favored ethylene production and CeAPSO-34 and LaAPSO-34 were helpful for propylene production. Light olefins yield decreased with time on stream for all the samples; although, this decrease rate is lower for MeAPSO-34 than for the parent SAPO-34. The catalyst lifetime increased in an order as follows: Ce->La->Co->Ni->Fe->SAPO-34. The rare earth modified catalysts exhibited lower methanation than parent SAPO-34 and transition metal modified catalysts.

Prereforming of n-tetradecane over Ce-promoted 50 wt% Ni/MgO–Al2O3 catalyst with high coke resistance

The effect of Ce-promotion on 50 wt% Ni-based catalysts during the prereforming of n-tetradecane and its optimum content were investigated. The Ni catalyst was synthesized by deposition–precipitation method. Next, various amounts of Ce (0–13 wt%) were loaded on the Ni catalyst by impregnation. The characteristics of the prepared catalysts were analyzed by XRD, H2-TPR, BET, BJH, and H2-chemisorption analyses. The prepared catalysts were tested under the prereforming conditions (temperature = 400 °C, GHSV = 3000 h−1, and S/C = 3 and 4). The Ni catalyst was easily deactivated under the following conditions: temperature = 400 °C, GHSV = 3000 h−1, and S/C = 4. The stability of all Ce-promoted Ni catalysts was improved as compared to that of the Ni catalyst. Among the Ce-promoted catalysts, 5 wt% Ce/50 wt% Ni/MgO–Al2O3 catalyst showed excellent stability even under the severe condition of S/C = 3. SEM, TEM, and TG analyses were performed in order to identify the main factor responsible for the rapid deactivation of the Ni catalyst. In the case of 0Ce/50Ni, Ni particles were encapsulated by many folds of coke and it was related to the rapid catalyst deactivation. However, after Ce promoted on the Ni catalyst, the thickness of the coke layers and the number of encapsulated Ni particles decreased and the deposited amount of coke on the catalyst also decreased.

Syngas Production via Steam–CO2 Dual Reforming of Methane over LA-Ni/ZrO2 Catalyst Prepared by l-Arginine Ligand-Assisted Strategy: Enhanced Activity and Stability

A highly dispersed supported nickel catalyst (LA-Ni/ZrO2), synthesized by a facile l-arginine ligand-assisted incipient wetness impregnation (LA-IWI) approach, demonstrates much superior catalytic activity and exceptional stability for steam–CO2 dual reforming of methane in comparison with the classical Ni/ZrO2 catalyst by the IWI method. The origin of the enhanced activity and stability of the developed LA-Ni/ZrO2 catalyst as well as the role of the Ni–{(l-Arg)} complex as the Ni precursor is revealed by employing diverse characterization techniques including X-ray diffraction (XRD), N2 adsorption (BET), transmission electron microscopy (TEM), H2 temperature-programmed reduction (H2-TPR), Fourier transform infrared spectroscopy (FT-IR), Raman spectroscopy (Raman), CO chemisorption, temperature-programmed hydrogenation (TPH), and thermogravimetric analysis (TGA). The superior catalytic activity of the developed LA-Ni/ZrO2 catalyst to the classical Ni/ZrO2 can be ascribed to the higher Ni dispersion, intensified Ni–support interaction, the enlarged oxygen vacancies, as well as the increased t-ZrO2 content and enhanced reducibility of NiO led by oxygen vacancies. More interestingly, although a larger amount of coke depositing on the spent LA-Ni/ZrO2 catalyst in comparison with that on the spent Ni/ZrO2 can be observed by TGA and TPH measurement, the developed LA-Ni/ZrO2 illustrates much higher catalytic stability to Ni/ZrO2, ascribed to the superior thermal sintering resistance of Ni nanoparticles and the different coke morphologies confirmed by TEM images led by intensified interaction of Ni and the ZrO2 support. The much superior catalytic activity and stability of the developed LA-Ni/ZrO2 catalyst endows it to be a promising candidate for syngas production with diverse H2/CO ratios via steam–CO2 dual reforming of methane.

Hydrogen generation by ethanol steam reforming over Rh/Al2O3 and Rh/CeZrO2 catalysts: A comparative study

Rhodium (Rh) catalysts supported over Al2O3 and CeZrO2 were developed and their activity towards hydrogen generation through ethanol steam reforming (ESR) was compared. Reforming reactions were performed over a range of temperatures (450 °C–600 °C) and feed flow rates (0.1, 0.2 and 0.3 mL min−1) at a constant ethanol-to-water molar ration of 1:6. Although complete ethanol conversion could be effected, the H2 selectivity was found to be higher for Rh/CeZrO2 catalyst (62.9%) as compared to Rh/Al2O3 (59.3%) under optimized reaction conditions. The average exit flow rate was relatively higher for Rh/CeZrO2 catalyst (263 mL min−1) as compared to Rh/Al2O3 catalyst (236 mL min−1). In-situ Diffuse Reflectance Infrared Fourier Transform Spectroscopy (DRIFTS) revealed the underlying mechanism responsible for better performance of Rh/CeZrO2 catalyst over Rh/Al2O3 catalyst. Rh/CeZrO2 catalyst was found to facilitate the decomposition of acetate intermediates, through carbonates at lower temperatures. On the other hand, over Rh/Al2O3, reaction proceeds through formation of both acetate as well as formate species both of which decompose at much higher temperatures. The amount of coke deposited was also lower in case of Rh/CeZrO2 catalyst (6.75 mmol gcatalyst−1) than over Rh/CeZrO2 catalyst (10.57 mmol gcatalyst−1).

Dry Reforming of Methane over Mg-Co-Al Mixed-Oxides Catalysts: Effect of Mg Content and Reduction Conditions

Mg-Co-Al mixed oxides were synthesized by the precipitation method and evaluated for dry reforming of methane. The samples were characterized by thermal techniques (TGA/DTA, NH3-TPD, H2-TPR, and TPO), specific surface area, and X-ray diffraction (XRD). Activity runs were conducted at atmospheric pressure, temperatures between 400 and 550°C, a CH4/CO2 molar ratio of 1, and a space velocity of 6000 NmL CH4/g/h. The partial substitution of Co with Mg increased the surface area and thermal stability and changed the reducibility and acid-base properties of the samples. These modifications led to a higher activity for dry reforming of methane for the catalyst with Mg/Co = 0.5, primarily due to its enhanced thermal stability. However, its higher activity was followed by higher amounts of coke. The different activation procedures highlighted Co3O4 as the main active phase rather than the Co-mixed oxides. Therefore, milder activation temperatures are required to properly reduce the Co3O4 phase and avoid sintering.

Reactions of Mixture of Oxygenates Found in Pyrolysis Vapors: Deoxygenation of Hydroxyacetaldehyde and Guaiacol Catalyzed by HZSM-5

Pyrolysis is a promising thermochemical process to convert lignocellulosic biomass to renewable biofuel. Much research has been conducted on the catalytic upgrading of either vapors derived from whole biomass scale or on individual model oxygenates. However, not many studies investigated the upgrading and deoxygenation of a mixture of several oxygenates. In this study, we use a combination of techniques to probe the reactions of guaiacol and hydroxyacetaldehyde (HAA) on HZSM-5, their diffusion inside the zeolite catalyst pores, and the extractable products. The techniques we used included several NMR methods, gas chromatography, and thermogravimetric analysis coupled with Fourier transform infrared spectroscopy (TGA-FTIR). In nitrogen at 280 °C with HZSM-5 catalyst, HAA decomposes, cyclizes to form aromatics and phenolic compounds, as well as produces coke. Under the same conditions, guaiacol neither reacts nor forms coke. When the two molecules are present together at 280 °C, their reaction pathways are independent of each other. For HAA at 480 °C, the quantity of aromatics produced is much higher than at 280 °C. At 480 °C guaiacol forms mostly substituted phenolics, BTEX type molecules, and coke. When guaiacol and HAA are mixed together at 480 °C, the amount of coke formed is slightly higher while the aromatics produced in the form of toluene, naphthalene, and their substituted compounds are substantially higher than that can be predicted by simple summation of products in individual cases. After reactions with guaiacol alone or a mixture containing both guaiacol and HAA, the available micropore surface area decreased to zero, indicating plugging of the pores or blocking of pore entrance. However, in both cases the guaiacol and phenolics can be desorbed in an N2 atmosphere at a relatively low temperature range of 100–200 °C. Diffusion measurements indicate that size has a large effect on the pore diffusion coefficients of different oxygen molecules. After coke forms on the catalyst the diffusion coefficients of larger molecules such as guaiacol are affected more significantly than diffusion of small molecules such as water and methanol.

Pre-reforming of n-tetradecane over Ni/MgO–Al2O3 catalyst: effect of added potassium on the coke resistance

We investigated the pre-reforming of n-tetradecane (C14H30) over the K-promoted 50 wt% Ni/MgO–Al2O3 catalyst and also analysed the coke resistance. The 50 wt% Ni/MgO–Al2O3 catalysts were prepared by the deposition–precipitation method and 1–5 wt% of potassium was added to the catalyst using the impregnation method. The catalysts were characterized by ICP, XRD, H2-chemisorption, H2-TPR, and BET. The pre-reforming of n-tetradecane was performed under the reaction conditions of S/C = 4.0, GHSV = 3000 h−1, and 400–450 °C. The Ni crystallite size increased, whereas the Ni dispersion and surface area of catalysts decreased with increasing amounts of K. The 50 wt% Ni/MgO–Al2O3 showed large amounts of coke deposition compared to the K-promoted catalysts. It was found that the K addition over 50 wt% Ni/MgO–Al2O3 catalyst was beneficial for coke removal by promoting the coke gasification. A 1 wt%K/50 wt% Ni/MgO–Al2O3 catalyst showed stable activity during pre-reforming at S/C = 4.0, GHSV = 3000 h−1, and 400 °C. Furthermore, it had the lowest amount of surface coke, as observed by SEM, TEM, and TG analysis.

Dual coke deactivation pathways during the catalytic cracking of raw bio-oil and vacuum gasoil in FCC conditions

Coke deposition pathways have been studied during the fluid catalytic cracking of bio-oil, vacuum gasoil (VGO) and a blend of the previous two (80wt% VGO and 20wt% bio-oil), under realistic riser conditions of the fluid catalytic cracking (FCC) unit, using a commercial catalyst at 500°C and contact times of 1.5–10s. Amount and composition of soluble and insoluble coke in dichloromethane have been analyzed using a set of techniques (TPO, FTIR, 13C NMR, XPS, Raman, GC–MS and MALDI-TOF MS, among others). The relationship of coke deposition with its composition and the reaction medium has allowed us to set two pathways of coke formation: (i) heavy hydrocarbon pathway tend to form ordered polycondensed aromatic nanostructures; whereas (ii) oxygenate pathway tend to form a lighter fraction of coke containing oxygen, less ordered and more aliphatic coke. A synergy between the two pathways have been verified due to the lower coke deposition of the blend compared to the individual components, and this has been explained in terms of (i) attenuation of the heavy hydrocarbon pathway caused by the steam contained or originated from the bio-oil, and (ii) the hydride transfer from hydrocarbons to the precursors of the oxygenate pathway.

Hydrogen Production by High Density Polyethylene Steam Gasification and In-Line Volatile Reforming

Steam gasification (900 °C) of high density polyethylene (HDPE) in a conical spouted bed reactor (CSBR) followed by steam reforming in a fixed bed reactor (Ni commercial catalyst) has been carried out. The effect reforming temperature in the 600–700 °C range has on product yields and gas composition as well as on the amount and nature of the coke deposited on the catalyst has been studied. The reforming leads to a full transformation of C2+ hydrocarbons and tar. The maximum H2 yield is obtained at 700 °C (36 wt % by mass unit of HDPE in the feed, which accounts for 83 wt % of the maximum H2 yield according to stoichiometry), with CH4 conversion being 94% and the coke amount deposited on the Ni catalyst being minimum (3.3 wt % by mass unit of HDPE in the feed). The syngas obtained by reforming at 700 °C has a H2/CO volumetric ratio of 6 and is suitable for hydrogenation reactions and further valorization to produce H2.

Comparison Between Ceria–Zirconia and Alumina as Supports for Oxidative Steam Reforming of Biodiesel

The objective of the study is to illustrate the advantages with using ceria–zirconia instead of promoted alumina as support for rhodium-based catalysts in oxidative steam reforming of biodiesel. The evaluation is based on long-term oxidative steam reforming experiments where the stability and durability of the catalysts are evaluated. The durability and fuel conversion of the two catalysts were comparable. However, the H2 yield of the ceria–zirconia supported catalyst was 10 % higher than for the catalyst supported on promoted alumina after 65 h on stream. Included are also measurements of the acidity of the catalysts, where it was concluded that the promoted alumina catalyst was significantly more acidic. The acidity of the materials could then be related to the amount of coke deposited, where the amount of coke on the alumina catalyst was almost five times higher after 50 h of operation compared to the ceria–zirconia catalyst.

Efficient Transformation of Anisole into Methylated Phenols over High‐Silica HY Zeolites under Mild Conditions

AbstractTransformation of anisole (methoxybenzene), a typical component of bio‐oil, into phenol and methylated phenols was studied over HY zeolites with framework Si/Al ratios of 5, 15, 25, and 35. It was demonstrated that the amounts of Brønsted acid and Lewis acid sites, the ratio of Lewis acid and Brønsted acid sites, and the textural properties of the zeolites were all crucial parameters that influenced the catalytic performance. The Brønsted acid and Lewis acid sites of the zeolites catalyzed the reaction cooperatively and efficiently promoted the transmethylation. The hierarchical channel system with fully open micropore–mesopore connectivity was favorable to reduce the amount of coke generated.

Supercritical water treatment of oil sludge, a viable route to valorize waste oil materials

Treatment of oil sludge generated from a pilot-scale upgrading process plant using supercritical water (SCW) was studied in detail to ascertain alternate ways of valorizing. SCW is a highly active agent, providing a suitable medium for converting heavy residues into lighter fuel compounds. Various operating conditions such as temperature and reaction time were investigated in this study; the results showed that a considerable amount of valuable oil and gas compounds can be recovered from the waste feedstock (up to ∼18.6wt% recovery). The gas produced was a hydrogen and methane-rich stream, which potentially can be utilized as fuel. In addition, the quantity of oil produced was significant considering the source feed, and rich in valuable saturate and aromatic hydrocarbons. Simulated distillation showed the oil contained mainly naphtha and light gasoil. It was concluded that a high reaction temperature and severity accelerated the product recovery yields, although the amount of coke generated increased. To address the current literature debate regarding the role of water and whether or not hydrogen is supplied from water, a detailed oxygen element balance was performed. The results proved that hydrogen is mainly supplied from hydrocarbon materials and not from water. Moreover, water acted as an excellent dispersant and solvent in the recovery of light compounds from heavy molecules through various radical reactions.

Kinetic Study on Catalytic Cracking of Rubber Seed (Hevea brasiliensis) Oil to Liquid Fuels

Reaction kinetics of catalytic cracking of rubber seed oil to liquid fuels has been investigated. The reac-tion was performed with sulfuric acid as catalyst at temperatures of 350-450 oC and the ratio of oil-catalyst of 0-2 wt.% for 30-90 minutes. Kinetics was studied using the model of 6-lump parameters. The parameters were rubber seed oil, gasoline, kerosene, diesel, gas, and coke. Analysis of experimen-tal data using regression models to obtain reaction rate constants. Activation energies and pre-exponential factors were then calculated based on the Arrhenius equation. The simulation result illus-trated that the six-lump kinetic model can well predict the product yields of rubber seed oil catalytic cracking. The product has high selectivity for gasoline fraction as liquid fuel and the smallest amount of coke. The constant indicates that secondary reactions occurred in diesel products compared to gaso-line and kerosene. The predicted results indicate that catalytic cracking of rubber seed oil had better be conducted at 450 oC for 90 minutes using 0.5 wt.% catalyst. © 2015 by Authors, Published by BCREC Group. This is an open access article under the CC BY-SA License (https://creativecommons.org/licenses/by-sa/4.0)

Coke-resistant Ni@SiO2 catalyst for dry reforming of methane

Nanostructured Ni@SiO2 core–shell catalyst is prepared from nickel oxide nanoparticles by a facile method. Calcination of as-synthesized core–shell nanoparticles creates a micro/meso-porous structure in the amorphous silica shell. The catalytic performance of core–shell catalyst toward dry reforming of methane was first evaluated in a thermogravimeter coupled with a mass spectrometer. Coking is negligible in a reforming period of 40h on stream at 850°C, while more than 0.32gcokegcat−1 is produced on a commercial Ni-based reforming catalyst in 6.4h at the same reforming condition. Dry reforming was also performed in a continuous flow, fixed-bed reactor at 750°C. Characterization of spent catalyst further confirms that Ni@SiO2 catalyst has high coke-resistance for dry reforming. The amount of coke deposited on the core–shell catalyst in 24.5h is 0.012gcokegcat−1.

The Kinetic Analysis of Coke Formation Under Differential Air-oil Ratio During High Pressure Air Injection

For studying the heavy oil property change during high pressure air injection process, constant temperature oxidation tube experiments have been finished to study the influence of air-oil ratio on the oxidation process with thermoanalysis methods. The results presented an increasing amount of formation coke was contained with the air-oil ratio increment. When the air-oil ratio reached 200:1, the oxidation process was promoted and the oxide was identified as “coke” with smell. Based on the Arrhenius method, it indicated the air concentration has positive influences on the coke deposition conducive to form and sustain stable combustion front.

Catalytic Pyrolysis of Biomass-Derived Compounds: Coking Kinetics and Formation Network

A deactivation study of ZSM-5 in heterogeneous catalysis during the pyrolysis of a biomass-derived compound has been carried out. Experiments were performed in a gas–solid reactor with an online weighting system at varied temperatures, weight hourly space velocities, and partial pressures. Real-time catalyst weight monitoring during the catalytic conversion of furan as a main intermediate of biomass fast pyrolysis can be realized. The coke amount increased from 3.48% at a temperature of 300 °C to 9.81% at 700 °C and then declined slightly at 800 °C. The catalyst weight increment included active carbon species confined in the catalysts and inert carbon species of large unsaturated carbon molecules, which were defined as active coke and inert coke, respectively. Differentiation curves among displayed coke amount, active coke, and inert coke were described. Active coke accumulated quickly at the early stage; meanwhile, inert coke was dominant for its suppression on the catalysis reaction at the later stage, ...

Evaluation of Co, La, and Mn promoted Rh catalysts for autothermal reforming of commercial diesel: Aging and characterization

In this study, three bimetallic catalysts are evaluated for autothermal reforming (ATR) of fuels (1wt.% Rh and 6wt.% X (X=Co, La or Mn) supported on high-surface area CeO2–ZrO2). The catalysts are aged for approximately 35h and carefully characterized both as fresh and aged materials. The objective is to illuminate the changes in material properties after time on stream as well as the differences among the materials. The changes in material properties are evaluated by H2-TPR, BET surface area analysis, TEM, SEM, and STEM. The material’s tendency to coke is investigated by TPO analysis.The three materials exhibit promising initial activity. However, the Co-promoted sample decreases sharply in activity after 25h of operation. Meanwhile, the other two materials display a more stable activity throughout the evaluated time. The deactivation of the Co-promoted material could be linked to the high amount of coke deposited during operation. Based on the results from the activity evaluation and characterization, the material promoted with lanthanum displays the most promising results. The addition of lanthanum resulted in a catalyst that was both stable and had high activity, even though a low rhodium loading is used. The material also shows superior thermal resistance compared to the other two materials. In addition, the tendency to coke is significantly lower compered to the other materials, which is especially beneficial when dealing with ATR of complex fuels.

Ironmaking System Including Coproduction of Carbon-Loaded Iron Oxide and Reformed Coke Oven Gas by Chemical Vapor Infiltration Process

Ironmaking system including coproduction of carbon-loaded iron oxide and reformed coke oven gas (COG) using coal tar, limonite ore, and waste heat is proposed to solve resource and energy problems in steelworks. In the proposed system, limonite ore, which is a low-grade iron ore with combined water, is first dehydrated to obtain a mesoporous solid. Then, during the chemical vapor infiltration, iron ore reduction, and reforming processes, the tar contained in the COG is deposited, leaving carbon in the mesopores of the ore. The ore is reduced by the COG and the tar is reformed by the combined sensible heat of the slag and COG, which acted as a heat source with the ore as a catalyst. The purpose of this study is to estimate the feasibility of the proposed system by process simulation using the Gibbs free energy minimization technique from the viewpoints of (1) the amount of coke required in steelworks, (2) the total chemical exergy of reformed COG, (3) the mass fraction of carbon deposited on carbon-loaded prereduced iron ore, and (4) available supplies of heat from the coke oven system to other systems under the reasonable assumptions given. The results of the analysis showed that, compared to the conventional ironmaking process, the proposed system can help decrease coke requirements by 9.62 % and increase the total chemical exergy by 14.2 %.