Catalytic gasification methods, catalysts, applications of catalysts, and methods for preparing catalysts.

Abstract

This invention relates to catalytic gasification methods, catalysts, uses of catalysts, and methods for preparing catalysts, particularly catalysts for use in gasification methods of coke or coal alone or in mixtures, and methods for preparing said catalysts, which can be used to obtain higher levels of hydrogen and carbon monoxide, and which allow the conversion of coke into higher value-added byproducts (hydrogen-rich syngas). The invention also relates to methods for converting petroleum coke using catalysts according to the invention.

Description

[0001] This application is a divisional application of Chinese patent application filed on November 17, 2020, with application number “202080089856.4” and invention title “Catalytic Gasification Method, Catalyst, Use of Catalyst and Method for Preparing Catalyst”. The original application was the Chinese national phase application of international application PCT / BR2020 / 050478. Technical Field

[0002] This invention relates to a catalytic gasification method for coke or coal, alone or in mixtures. The gasification method uses a catalyst that allows coke to be converted into a higher value-added byproduct (hydrogen-rich syngas).

[0003] The present invention also relates to a method for obtaining the catalyst for use in the catalytic conversion process of petroleum coke, and the catalyst itself. Background Technology

[0004] As is well known, oil largely fueled industrial development in the early 19th century, and it remains a major energy source on Earth today. In fact, its finite nature, coupled with its significant economic value, makes it a key factor driving major geopolitical and socioeconomic changes around the world.

[0005] Petroleum can generally be described as an oily and flammable substance found at various depths underground. It is mainly composed of hydrocarbons, primarily a complex combination of aliphatic hydrocarbons, acyclic hydrocarbons, alicyclic hydrocarbons, and aromatic hydrocarbons.

[0006] The method of extracting oil from sediments is not practically applicable; it can only be used to maximize its energy potential after undergoing fractionation or separation of its components in a refinery.

[0007] Hydrocarbons are separated from oil refining by distillation and their impurities are removed in other processes, making it possible to extract a variety of products, including: diesel, gasoline, naphtha, kerosene, asphalt, lubricants, paraffin wax, liquefied petroleum gas, solvents, plastics and polymers, general tar and coke, more specifically petroleum coke (the primary target of the catalyst described in this patent).

[0008] Petroleum coke is composed of polymer chains with high molecular weight and high carbon concentration. Although coke products are considered a low-value-added byproduct, they can have value depending on their purity. There is a difference between metallurgical grade coke used in iron and steel metallurgy and anode grade coke used as raw material to manufacture anodes for the production of aluminum or titanium dioxide.

[0009] Currently, petroleum coke produced worldwide is consumed as fuel, primarily by refineries themselves. Refineries prioritize the use of low-value fuels within their furnaces to maximize the production and commercialization of other higher-value products.

[0010] Petroleum coke, considered a solid fuel, has a high calorific value, low ash content, low purchase cost, low volatile material content, high sulfur content, ash content containing heavy metals, and low combustion efficiency.

[0011] It should be emphasized that petroleum coke originates from delayed coking of low-value-added oil streams (high density, rich in sulfur and impurities). The properties of the resulting coke depend on the source of the oil and operating conditions, and in addition to increased viscosity, it may also contain significant amounts of sulfur and low-volatile components in its final composition.

[0012] Therefore, due to its unique properties, petroleum coke is considered an interesting alternative to coal. Its widespread availability in refineries makes it a viable and low-cost alternative, and petroleum coke produces gas, hydrogen, methane, and electricity through its gasification.

[0013] Furthermore, gasification can be defined as the conversion of organic matter into gaseous products through thermochemical reactions, involving amounts of steam, air, or oxygen below stoichiometry (the theoretical minimum for combustion).

[0014] Regardless of the nature of the feedstock, the main elements constituting the hydrocarbon mixture—carbon, hydrogen, oxygen, and sulfur—are converted into thermodynamically stable substances: carbon monoxide, carbon dioxide, hydrogen, water, methane, hydrogen sulfide, and carbonyl sulfide, in proportions that vary depending on the process conditions (specifically, whether air or oxygen is used in the oxidation process).

[0015] Therefore, vaporization allows the conversion of non-vaporizable hydrocarbons, accompanied by the breaking of carbon-carbon bonds, which results in a single hydrocarbon, namely methane.

[0016] The most common raw materials used in the gasification process are coal, oil and their residues, natural gas, biomass, or mixtures thereof. The products obtained from syngas are used in a variety of applications, such as power generation, hydrogen production, methanol production, and liquid fuel synthesis.

[0017] In this manner, syngas obtained from the gasification of coal, petroleum coke, and refinery residues typically contains 25% to 30% H2 (volume / volume), 30% to 60% CO (volume / volume), 5% to 15% CO2 (volume / volume), and 2% to 3% H2O (volume / volume). Lower levels of CH4, H2S, N2, NH3, HCN, Ar, COS, Ni, and Fe are also found. The quantity and composition of the produced gases vary depending on the characteristics of the feedstocks used.

[0018] For the reaction to occur, typical processing temperatures range from 1600°C to 1350°C, and pressures can reach 150 kgf / cm². 2 (14.710 MPa). The basic reaction of the process is:

[0019]

[0020]

[0021]

[0022] In this case, it can be noted that the minimum amount of oxygen required for the reaction to occur is represented by equation (1), which states that 0.5 kmol / h of oxygen is required for every 1 kmol / h of carbon.

[0023] Carbon monoxide and hydrogen are the main products until all hydrocarbons are converted; then carbon dioxide and water are formed from the additional oxygen supplied. However, the order of the reactions remains uncertain. Some authors believe that CO2 and H2O are the main products.

[0024] According to equation (2), in order to prevent uncontrolled temperature rise, steam is sometimes added to undergo an endothermic reaction with hydrocarbons. This results in the formation of more hydrogen than is expected in equation (1).

[0025] The proportions of the components retained in the mixture are determined by equilibrium, which, in addition to the carbon monoxide oxidation reaction (7) and methane dry reforming (8), also includes water displacement (5), steam reforming (4), and the reaction from hydrogen sulfide to carbonyl sulfide (6), as follows:

[0026]

[0027]

[0028]

[0029]

[0030]

[0031] Equilibrium is established in reactors between 1500°C and 1350°C. Below 900°C, near equilibrium can only be reached with long residence times or the use of catalysts. Due to soot formation, the use of catalysts has not been commercially applied.

[0032] Therefore, oil residues, particularly petroleum coke, have become promising feedstocks for gasification processes, primarily due to their widespread availability in refineries. As key characteristics, petroleum coke is less reactive than coal, possessing lower carbon and volatile matter content, necessitating a high temperature of 1400°C to 1500°C for gasification. Furthermore, its high sulfur content necessitates additional steps to remove undesirable compounds such as H₂S, COS, and S₂.

[0033] Several strategies exist to improve and optimize the gasification process, including: air separation via membranes, novel gasifier configurations, hot gas purification, new solvents, membranes that enhance conversion rates in the shift reaction, hydrogen separation, and the application of catalysts in the process. Following this line of reasoning, the search for new catalysts could allow operation under milder conditions and / or with fewer byproducts, even reducing reaction temperature and energy consumption, leading to improved process efficiency.

[0034] Relevant literature describes how increasing the operating temperature improves the conversion rate of coke to CO2 (as a gasifying agent) and leads to a reduction in reaction time. Therefore, the higher the temperature, the shorter the time required for petroleum coke to convert into gaseous products. Furthermore, the conversion rate increases with increasing conversion rate and then decreases.

[0035] The reaction behavior observed in the gasification of coke with CO2 is due to the fact that temperature affects the graphitization process of petroleum coke during gasification. In this context, it is noteworthy that coke, compared to coal, possesses high crystallinity and a high structural composition, which are ideal conditions for the formation of graphitic carbon as temperature increases.

[0036] Another point described in the professional literature concerns the effect of lignin on the gasification of petroleum coke. Lignin is highly reactive due to the presence of alkaline substances and its high surface area. The description points out that the mixture of coke and lignin provides optimization for the reactivity of the coke because it promotes close contact between the substances during the grinding process; therefore, the proximity of the alkaline substances present in lignin will accelerate the gasification of petroleum coke.

[0037] Regarding patent literature, document US20150299588 describes the gasification reaction of coke with a catalyst impregnated in coal in the presence of steam. The proposed catalyst consists of coal and potassium, with a catalyst-to-coke ratio of 1:1, exhibiting a conversion rate of 88.4%. The reaction is carried out in an argon atmosphere at temperatures ranging from 700°C to 900°C.

[0038] Document US20070083072 describes an alkali metal catalyst for coke gasification. The catalyst is selected from the following substances: Na₂CO₃, K₂CO₃, Rb₂CO₃, LiCO₃, CsCO₃, NaOH, KOH, RbOH, or CsOH. The coke is pre-impregnated with a mixture of fresh and recycled solutions. The reaction is carried out in a temperature range of 580°C to 816°C. The conversion rate is up to 97%, producing methane, carbon dioxide, carbon monoxide, and hydrogen, the latter two of which are recovered during the process.

[0039] Document US6585883 relates to the removal or reduction of coke in a fluidized bed coking unit. In this process, alkoxylated or non-alkoxylated oxide catalysts containing cerium, titanium, and zirconium are proposed; cobalt oxides, vanadium oxides, and silver oxides; metal carbonates, alkali metal hydroxides, and alkaline earth metal hydroxides; mixtures of Group VIII transition metal oxides, cerium vanadium oxides, and potassium chloride; or Cu-KV-Cl catalysts or mixtures thereof, these solutions being pre-impregnated in the coke. In this description, the reaction occurs at 500°C to 700°C.

[0040] Document US20090165380 describes the gasification of coke using steam and a catalyst composed of an alkali metal hydroxide and one or more other alkali metals, with the catalyst impregnated in the coke, producing methane, hydrogen, carbon monoxide, and other larger hydrocarbons. The coke gasification is carried out at 700°C.

[0041] Document CN108587687 discloses a method for gasifying petroleum coke using a catalyst, the method comprising mechanical mixing, impregnation or direct spraying of a magnesium-based catalyst, wherein the following can be used as examples: MgO, MgCl2, MgSO4 and Mg(NO3)2.

[0042] Alternatively, document CN108641752 relates to a method for optimizing the gasification reaction of petroleum coke using the following catalysts: CaO, ZrO2, Ba2TiO4, Li2O, Li2ZrO3, Li2SiO3, and Li4SiO4, which significantly increases the gasification reaction rate and reduces the reaction time required.

[0043] As can be seen from this disclosure, the prior art describes catalysts that have the function of improving and optimizing processes in practice; however, all instances involve a step prior to the reaction in which the catalytic phase must be mixed with or impregnated in coke, or still impregnated in coal, to obtain a mixture of the catalytic phase and coke. This step needs to be repeated because the material must be resupplyed to the process as the coke is consumed.

[0044] Therefore, there is still a need to describe a catalyst that can optimize the process without requiring a previous mixing or coke impregnation stage to form the catalyst with each new coke supply; in this way, it is intended to disclose a conventionally described catalyst that is not consumed with the coke and does not require resupply in a highly correlated manner with the coke, but only requires replacement of losses, which reduces the number of steps and thus lowers the cost of the process.

[0045] To address this problem, the present invention proposes a catalyst that optimizes the coke gasification process and reduces costs by eliminating the coke pretreatment step used to introduce catalytic activity and by employing low-cost metals and supports. Eliminating the aforementioned steps means that it is not necessary to mix the catalyst with the coke or pre-impregnate the catalyst in the coke. It should be further emphasized that, compared to currently described methods, the method described in this application produces high-value-added syngas with a high concentration of hydrogen at a very low processing cost. Summary of the Invention

[0046] This invention relates to a catalyst for converting organic matter, particularly petroleum coke, into gaseous products (gasification) via a thermochemical reaction, involving amounts of steam, air, or oxygen in substoichiometric quantities. Regardless of the nature of the feedstock, the primary conversion elements are carbon monoxide, carbon dioxide, hydrogen, water, methane, hydrogen sulfide, and carbonyl sulfide.

[0047] According to one aspect of the invention, three catalysts are proposed: Fe / SiO2-NO3 derived from nitrates, Fe / SiO2-Cl derived from chlorides, or Fe / SiO2-SO4 derived from sulfates. The invention proposes the preferred use of the Fe / SiO2-Cl catalyst, which achieves complete conversion in 4 hours, compared to the 6 hours required in thermal gasification and reactions using catalysts Fe / SiO2-NO3 and Fe / SiO2-SO4.

[0048] According to the same principle, compared to a purely thermal reaction without a catalyst, the Fe / SiO2-Cl catalyst reduces the reaction time at the same temperature. When compared to existing technologies, the application of this catalyst produces higher levels of H2, promoting the conversion of petroleum coke into a higher value-added byproduct (hydrogen-rich syngas). Attached Figure Description

[0049] The invention will now be described in more detail with reference to the accompanying drawings, which illustrate examples of embodiments thereof in an illustrative manner and without limiting the scope of the invention. In the drawings, the following are present:

[0050] - Figure 1The conversion of petroleum coke as a function of time is shown in thermal gasification and catalytic gasification at 800 °C using Fe / SiO2 catalysts prepared from chlorides, nitrates and sulfates.

[0051] - Figure 2 The molar composition of the gasifier output stream (on an anhydrous and nitrogen-free basis) is shown in a test conducted at 800 °C using a Fe / SiO2-Cl catalyst.

[0052] - Figure 3 The molar composition of the vaporizer output streams using the Fe / SiO2-Cl catalyst at 800 °C, 750 °C, and 700 °C is shown (on anhydrous and nitrogen-free conditions). Detailed Implementation

[0053] This invention relates to a catalytic gasification method for petroleum coke, coal, or mixtures thereof to produce hydrogen-rich syngas. The use of a catalyst provides milder conditions for processing the aforementioned feedstock. Furthermore, the catalyst required in this invention can be supplied together with the material to be processed, without the need for an impregnation step in the coke or pre-mixing with the coke or other materials.

[0054] The catalytic gasification method proposed in this invention is carried out through the following steps:

[0055] a) Loading the reactor with a catalyst, an inert material, or a mixture of both;

[0056] b) Fluidize the bed loaded in step (a) at an air flow rate of 10 Nl / min at room temperature;

[0057] c) Heat the fluidized bed from room temperature to 800°C at a rate of 20°C / min; d) Begin introducing steam into the system heated in step (c);

[0058] e) After the gasification temperature is reached and the temperature of the bed and the system stabilizes, petroleum coke is introduced.

[0059] f) Inject the gas from the vaporizer from step (e) into the chromatograph;

[0060] g) Cool the system under an airflow;

[0061] h) Unload the bed;

[0062] i) The bed, cyclone separator and filter unloaded in weighing step (h);

[0063] j) Perform mass balancing of the unit.

[0064] In one aspect of the invention, a reactor bed is loaded with 1 kg of silica and 1 kg of catalyst for the catalytic gasification of petroleum coke or coal. Conversely, in thermal gasification, the reactor is loaded with 2 kg of silica (which is inert).

[0065] In another aspect of the invention, it should be emphasized that after the bed is fluidized and a temperature of 500°C is reached, steam is introduced into the system, wherein the liquid pump is calibrated to a supply rate of 5 ml / min.

[0066] In another aspect, when the gasification temperature in the system is reached, bed stabilization occurs and petroleum coke is introduced at a rate of 0.366 kg / h.

[0067] In another aspect, it should be emphasized that, five minutes after the start of solids supply, the gas from the vaporizer is injected into an online chromatograph to determine its composition. A sample of the gas stream is injected every thirty minutes. After all the coke material has been supplied, injection continues until no CO and H2 products are detected, indicating the end of vaporization.

[0068] Once gasification is complete and room temperature is reached, the bed is unloaded, and the unloaded bed, cyclone separator, and filter are weighed. Depending on the situation, weighing is performed to determine if any particles are carried away from the bed, from the petroleum coke, or from the coal.

[0069] One aspect of the catalytic gasification method should be emphasized: the method produces hydrogen-rich syngas.

[0070] In another aspect of the catalytic gasification method, the method allows the reaction to occur under mild conditions and at a higher conversion rate.

[0071] In addition to the aspects mentioned above, the catalyst is supplied to the system without impregnation in coke, coal or other similar materials and without pre-mixing with the charge.

[0072] A second variant of the invention relates to a method for preparing a catalyst for catalytic gasification, described in several related aspects, including the following preparation steps:

[0073] a) Weigh 100g of carrier (quartz sand);

[0074] b) Weigh the iron salts to obtain the desired iron content % (by weight);

[0075] c) Add 150 ml of water to the iron salt;

[0076] d) Add the prepared solution to the quartz sand;

[0077] e) Let stand for 16 hours;

[0078] f) Allow the solution to evaporate slowly;

[0079] g) Dry in an oven at 100°C for 16 hours;

[0080] h) Calcine at 550℃ for 5 hours.

[0081] In this variant, the catalyst is prepared via a slurry method, in which a defined mass of support is mixed with a solution constituting the desired metal concentration to form a suspension. The resulting suspension is then allowed to stand, followed by drying and calcination.

[0082] In all variations of the invention, the raw material used to obtain hydrogen-rich syngas is preferably petroleum coke with a maximum particle size of 177 μm. However, the catalyst can be used for coal gasification.

[0083] The catalyst mentioned in the foregoing variations of the present invention is also required to be an innovative product. In this way, the catalyst obtained for catalytic gasification comprises:

[0084] a) Carrier, preferably quartz sand;

[0085] b) Group VIII transition metals;

[0086] c) Calcine the compound at 550°C for 5 hours.

[0087] It should be emphasized that in this third variant of the invention, the catalyst for catalytic gasification comprises a Group VIII transition metal, namely iron. Three forms of catalyst are claimed in this invention: FeSiO2-Cl, FeSiO2-NO3, and a third, FeSiO2-SO4.

[0088] Among the types mentioned, FeSiO2-Cl exhibits a reduction in conversion time and an increase in CO2 and H2 levels compared to thermal conversion. Therefore, the FeSiO2-Cl catalyst for catalytic gasification allows catalytic gasification to occur under milder conditions and at a higher petroleum coke conversion rate, in a manner similar to that of coal.

[0089] In another way, catalysts for catalytic gasification have additional advantages because they are supplied to the system without impregnation in coke, coal or other similar materials and without pre-mixing with the feed, thereby reducing processing steps, processing time and energy consumption.

[0090] Therefore, the catalytic gasification method for petroleum coke or coal has been optimized and improved using catalysts for catalytic gasification, resulting in high-value-added hydrogen-rich syngas. Furthermore, due to the materials used and the preparation method, it is a low-cost catalyst.

[0091] Example

[0092] As can be seen from the tests conducted, the catalyst is prepared via a slurry method, which involves adding a solution with a desired metal concentration to a defined mass of support. The resulting suspension is allowed to stand, then dried and calcined. The steps used for preparation are as follows:

[0093] a) Weigh 100g of carrier (quartz sand);

[0094] b) Weigh the iron salt to the desired iron content % (by weight);

[0095] c) Add 150 ml of water to the iron salt;

[0096] d) Add the prepared solution to the quartz sand;

[0097] e) Let stand for 16 hours;

[0098] f) Allow the solution to evaporate slowly;

[0099] g) Dry in an oven at 100°C for 16 hours;

[0100] h) Calcine at 550℃ for 5 hours.

[0101] The coke used in the tests was ground and particle size classified using a set of sieves. The fraction with a maximum particle size of 177 μm was collected and stored. Table 1 shows the composition of the various catalysts prepared, as determined by X-ray fluorescence (FRX).

[0102] Table 1 – Composition of several catalysts prepared by FRX.

[0103]

[0104] Figure 1 The conversion rate of petroleum coke as a function of gasification time is shown at a temperature of 800 °C when using a Fe / SiO2 catalyst prepared using chloride, sulfate, and nitrate. For comparison purposes, coke conversion rate curves obtained by thermal gasification in the absence of a catalyst are included.

[0105] Blank tests and tests to evaluate the conversion effectiveness of various catalysts were conducted using the following methods:

[0106] a) Loading a reactor bed, which may contain 2 kg of silica (thermal gasification test) or 1 kg of silica and 1 kg of catalyst (catalytic gasification test);

[0107] b) Fluidize the bed at a flow rate of 10 Nl / min at room temperature;

[0108] c) Heat the bed from room temperature to 800°C at a rate of 20°C / minute;

[0109] d) When the temperature reaches 500°C, begin introducing steam into the system and calibrate the liquid pump to a supply rate of 5 mL / min;

[0110] e) Once the desired gasification temperature is reached, wait for stabilization. Once the bed temperature stabilizes, begin introducing petroleum coke at a rate of 0.366 kg / hour.

[0111] f) Five minutes after the start of solids supply, inject gas from the gasifier into an online chromatograph to determine its composition. Inject a sample of the gas stream every thirty minutes. After all coke material has been supplied, continue injection until no CO and H2 products are detected, indicating the end of gasification; g) Cool the system under an air stream, and once room temperature is reached, unload and weigh the bed. Also weigh the cyclone separator and filter to determine if particles have been carried away from the bed or from the petroleum coke, thus ensuring the mass balance of the closed unit.

[0112] Following the tests, it was observed that the Fe / SiO2 catalyst prepared from sulfate exhibited performance similar to that observed in thermal gasification. This result can be explained by considering that the iron content incorporated into the silica is lower when sulfate is used as the metal source compared to other cases. This information is confirmed by Table 1.

[0113] When using nitrates as the iron source to prepare catalysts, the content of iron incorporated is higher than that of the other two, but in this case, the conversion rate of petroleum coke is not significantly improved compared with thermal gasification. In particular, the catalysts prepared from nitrates exhibit similar performance to those prepared from sulfates until the performance of the catalysts prepared from nitrates begins to decline after about 100 minutes, even for thermal gasification.

[0114] The use of the Fe / SiO2-Cl catalyst appears to have affected the gasification kinetics of petroleum coke, as complete conversion was achieved in 4 hours compared to the 6 hours required in thermal gasification and in reactions using Fe / SiO2-NO3 and Fe / SiO2-SO4 catalysts.

[0115] Figure 2 The molar composition of the gasifier output stream (on an anhydrous and nitrogen-free basis) is shown in tests conducted at 800 °C using a Fe / SiO2-Cl catalyst. Higher CO2 and H2 contents were obtained in experiments using the Fe / SiO2-Cl catalyst, as... Figure 2 As shown in the figure. This result indicates that, in addition to effectively reducing the total gasification time, the catalyst also greatly promotes the gas-water displacement reaction, thus increasing the hydrogen yield.

[0116] If it is possible Figure 3 The results show the molar composition of the vaporizer output stream in tests conducted at 800°C, 750°C, and 700°C (on anhydrous and nitrogen-free conditions). This data demonstrates that... Figure 3 In the additional tests cited, the conversion rate decreased at lower temperatures, and the gasification time to reach final conversion gradually increased. On the other hand, the conversion rate observed at 750°C was close to the pure thermal conversion rate without a catalyst, such as... Figure 1 As shown. Therefore, it can be noted that in the presence of the catalyst of the present invention, a lower temperature is required to achieve a conversion rate comparable to that of a purely thermal reaction, thereby reducing the energy consumption of the entire process.

[0117] It should be noted that although the invention has been described with reference to the accompanying drawings, those skilled in the art may make modifications and adjustments as appropriate, provided that they are within the scope of the invention as defined herein.

[0118] The following content corresponds to the original claims in the parent application and is incorporated herein as part of the specification:

[0119] 1. A catalytic gasification method, characterized in that it includes the following steps:

[0120] a) Loading the reactor bed;

[0121] b) Fluidize the bed loaded in step (a) at an air flow rate of 10 Nl / min at room temperature;

[0122] c) Heat the fluidized bed from room temperature to 800°C at a rate of 20°C / min;

[0123] d) Begin introducing steam into the system heated in step (c);

[0124] e) After the gasification temperature is reached and the temperature of the bed and the system stabilizes, petroleum coke is introduced.

[0125] f) Inject the gas from the vaporizer from step (e) into the chromatograph;

[0126] g) Cool the system under an airflow;

[0127] h) Unload the bed;

[0128] i) Weighing the bed, cyclone separator and filter unloaded in step (g);

[0129] j) Perform mass balancing of the unit.

[0130] 2. The catalytic gasification method according to item 1, characterized in that when catalytic gasification of petroleum coke, coal or a mixture thereof is carried out, the reactor bed is loaded with a mixture of catalyst and inert material in a ratio of 10:90, wherein the ratio of the mixture of catalyst and inert material is preferably selected as 50:50 of silica and catalyst.

[0131] 3. The catalytic gasification method according to item 1, characterized in that after reaching a temperature of 300°C to 700°C, preferably 500°C, steam is introduced by a liquid pump calibrated to a supply rate of 5 ml / min or matching the size of the parts of the equipment used.

[0132] 4. The catalytic gasification method according to item 1, characterized in that after the gasification temperature is reached, bed stabilization occurs, and petroleum coke is introduced at a rate of 0.366 kg / h or a rate matching the mass of the parts and raw materials of the equipment used.

[0133] 5. The catalytic gasification method according to item 1, characterized in that the method produces high-value-added hydrogen-rich syngas.

[0134] 6. The catalytic gasification method according to item 1, characterized in that the method allows the reaction to occur under mild conditions and at a higher conversion rate.

[0135] 7. The catalytic gasification method according to item 1, characterized in that the catalyst is supplied to the method without a pre-impregnation step or without pre-mixing with the feed.

[0136] 8. A method for preparing a catalyst for catalytic gasification, characterized by the following preparation steps:

[0137] a) Weigh 100g of carrier (quartz sand);

[0138] b) Weigh the iron salts to obtain the desired iron content % (by weight);

[0139] c) Add 150 ml of water to the iron salt;

[0140] d) Add the prepared solution to the quartz sand;

[0141] e) Let stand for 16 hours;

[0142] f) Allow the solution to evaporate slowly;

[0143] g) Dry in an oven at 100°C for 16 hours;

[0144] h) Calcine at 550℃ for 5 hours.

[0145] 9. The method for preparing a catalyst for catalytic gasification according to item 8, characterized in that the catalyst is prepared by a slurry method.

[0146] 10. The method for preparing a catalyst for catalytic gasification according to item 8, characterized in that the catalyst is prepared with a solution having a desired metal concentration at a defined support mass.

[0147] 11. The method for preparing a catalyst for catalytic gasification according to item 8, characterized in that the catalyst is prepared by forming a suspension, allowing it to stand, and then drying and calcining it.

[0148] 12. The method for preparing a catalyst for catalytic gasification according to item 8, characterized in that the raw material used is preferably petroleum coke, wherein the maximum particle size is 177 μm.

[0149] 13. A catalyst for catalytic gasification obtained by the method according to claims 8 to 12, characterized in that it comprises:

[0150] a) Carrier, preferably quartz sand;

[0151] b) Group VIII transition metals;

[0152] c) The compound is calcined at 400°C to 700°C, preferably at 550°C, for a duration ranging from 2 to 10 hours, and more preferably within 5 hours.

[0153] 14. The catalyst for catalytic gasification according to claim 13, characterized in that the group VIII transition metal includes iron.

[0154] 15. The catalyst for catalytic gasification according to item 13, characterized in that the catalyst can be of the following types: Fe / SiO2-NO3 and Fe / SiO2-SO4.

[0155] 16. The catalyst for catalytic gasification according to claim 13, characterized in that it is used for the catalytic gasification of petroleum coke, coal and mixtures thereof, wherein the preferred raw material is petroleum coke.

[0156] 17. The catalyst for catalytic gasification according to item 13, characterized in that it allows catalytic gasification to occur under milder conditions and at a higher conversion rate of petroleum coke and coal.

[0157] 18. The catalyst for catalytic gasification according to item 13, characterized in that the catalyst is supplied to the method without a pre-impregnation step or without pre-mixing with the charge.

[0158] 19. The use of the catalyst according to any one of items 13 to 18, characterized in that it is used for the optimization and improvement of a catalytic gasification method for petroleum coke, coal or a mixture of both, wherein coke is the preferred raw material.

[0159] 20. The use of the catalyst according to item 19 is characterized in that it produces hydrogen-rich syngas with high added value.

Claims

1. A method for preparing a catalyst for catalytic gasification, characterized by the following preparation steps: a) Weigh 100 g of the carrier, wherein the carrier is quartz sand; b) Weigh the iron salts to obtain the desired iron content by weight (%). c) Add 150 ml of water to the iron salt; d) Add the prepared solution to the quartz sand; e) Let stand for 16 hours; f) Allow the solution to evaporate slowly; g) Dry in an oven at 100°C for 16 hours; h) Calcination at 550℃ for 5 hours The catalyst is a Fe / SiO2-Cl catalyst derived from chloride.

2. The method for preparing a catalyst for catalytic gasification according to claim 1, characterized in that the catalyst is prepared with a solution having a desired metal concentration at a defined support mass.

3. The method for preparing a catalyst for catalytic gasification according to claim 1, characterized in that the raw material used is petroleum coke, wherein the maximum particle size is 177 μm.

4. A catalyst for catalytic gasification obtained by the method according to any one of claims 1 to 3, characterized in that it comprises: a) Quartz sand; b) Iron; The catalyst is a catalyst in the form of FeSiO2-Cl.

5. The catalyst for catalytic gasification according to claim 4, characterized in that it is used for the catalytic gasification of petroleum coke, coal, or a mixture of both.

6. The catalyst for catalytic gasification according to claim 4, characterized in that it is used for the catalytic gasification of petroleum coke.

7. The catalyst for catalytic gasification according to claim 4, characterized in that the catalyst is supplied to the method without a pre-impregnation step or without pre-mixing with the charge.

8. Use of the catalyst according to any one of claims 4 to 7, characterized in that it is used for the optimization and improvement of a catalytic gasification method for petroleum coke, coal, or a mixture thereof.

9. The use of the catalyst according to claim 8, characterized in that it produces hydrogen-rich syngas with high added value.

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