Can anyone tell me the specific ingredients of NB113 medium temperature conversion catalyst?

B113-2 Carbon Monoxide High Temperature Shift Catalyst Instruction Manual 1 1 Product Introduction B113-2 Carbon Monoxide High Temperature Shift Catalyst is produced using advanced technology, using Fe2O3 as the active component, Cr2O3 as the additive, and adding an appropriate amount of other additives. The catalyst is suitable for energy-saving carbon monoxide conversion processes in ammonia synthesis, hydrogen production and other devices under low steam-to-gas ratio conditions. B113-2 catalyst is a new generation of energy-saving catalyst produced using the latest international technology. This catalyst not only fully possesses the characteristics of the B113 catalyst such as high operating intensity, wide operating temperature range, good low-temperature activity, low sulfur content in the body, no need to specially arrange the sulfur release time, and good steam condensation resistance, it is more suitable for use under low steam-to-gas ratio process conditions, and can effectively inhibit the occurrence of Fischer-Tropsch reaction. B113-2 catalyst is used to convert carbon monoxide in hydrogen-rich gas flow under low steam-gas ratio conditions, and generate more hydrogen through the following reaction: CO+H2O=CO2+H2+41.19kJ/mol and hydrogen is also purified. B113-2 catalyst has two outstanding characteristics: First, there is almost no change in the apparent volume of the catalyst particles during the reduction process, which ensures the strength and long life of the catalyst after reduction, and the anti-vapor condensation performance is very obvious. Second, the catalyst has high selectivity and high activity at low temperature, and the side reaction products of ammonia, methane or ethane are significantly reduced. 2 Product physical and chemical properties 2.1 Catalyst appearance Ⅰ Ⅱ Dimensions (mm): Φ9×5～7 Φ6×3～6 Shape: Plane Cylinder Plane Cylinder Color: Dark brown Dark brown 2.2 Physical properties Bulk density (kg/l): 1.38～1.45 Radial strength (N/cm): ≥250 Specific surface (m2/g): 80 wear (%): ≤10 Boiling water resistance: 8～2～0 2.3 Chemical composition Fe2O3 (%): ≥74 Cr2O3 (%): ≥7 graphite (%): ≤3 Additives (%): Appropriate weight loss on burning (%): ≤10S(%): ≤0.025 Cl (%): ≤0.010 B113-2 Carbon Monoxide High Temperature Shift Catalyst Instruction Manual 2 3 Product Quality Index Project Index (HT Standard) Activity (CO conversion rate %): ≥45 Radial strength (N/cm): ≥250S(%): ≤0.025 Cl (%): ≤0.010 wear (%): ≤10 4 Product use 4.1 Use conditions B113-2 catalyst operating pressure is 0.1~8.0MPa, operating temperature is 300~500℃, steam/dry gas ≥0.35, operating airspeed is 500~5000h-1, and the service life is expected to be more than three years. The B113-2 catalyst has excellent resistance to steam condensation. After drying with process gas under accident conditions, the strength of the catalyst does not decrease, the bed resistance does not increase, and the catalyst can still maintain the activity before the accident. 4.2 Filling 1) The filling quality of the catalyst is directly related to the air flow distribution, resistance reduction and catalyst performance of the high-variability furnace bed layer, so great attention should be paid to this work. 2) In order to ensure the filling quality, choose a sunny day and avoid contamination by oil, dust and chemical substances. 3) Confirm that the quality of the high-variable furnace is qualified, that the furnace is dry and free of other debris, and that the filling lines for refractory balls, wire mesh, grate plates and catalysts are marked on the inner wall of the furnace. 4) Carefully sieve the catalyst through a 4×4mm mesh to remove dust and debris generated during transportation. 5) First, install Φ25mm refractory balls to the furnace bottom to a predetermined height, then install Φ12mm refractory balls 100~200mm on top, lay a layer of stainless steel mesh, and then install the catalyst. 6) Slowly lift the catalyst to the top of the furnace and slowly pour it into a funnel or chute connected to a canvas bag. The catalyst flows into the furnace from the mouth of the canvas bag. Someone in the furnace needs to hold the mouth of the canvas bag and constantly move the position of the discharge port to raise the level of the catalyst surface. The method of stacking and then raking is not allowed. The free fall height of the catalyst shall not exceed 0.6 meters. Furnace operators should step on wooden boards and never step directly on the catalyst. 7) After the catalyst is installed, rake the surface flat, cover it with a layer of stainless steel mesh, and then install a 100-200mm thick Raschig ring and grate plate. When it is confirmed that the catalyst filling quality is qualified and there are no foreign objects in the furnace, the furnace should be closed. Blow with air or inert gas until there is no dust at the furnace outlet. 8) Safety precautions: In order to prevent harmful gases in the reactor and dust in the catalyst from affecting people, personnel entering the furnace during the filling process must wear long-tube gas masks and adopt forced air supply protection measures. 4.3 Temperature Rising and Reduction 4.3.1 Temperature Rising The heating medium can be air, nitrogen, superheated steam, natural gas or process gas and other gases. 1) If dry air is used to heat up, the maximum temperature of the catalyst bed should be strictly controlled below 150°C (pressure ≤ 0.7Mpa), and then use other heating media to continue heating. 2) If superheated steam is used to raise the temperature, the temperature can be directly raised to 220°C, and then process gas can be used to raise the temperature. B113-2 Carbon Monoxide High Temperature Shift Catalyst Instruction Manual 3 3) If natural gas is used as the heating medium, the bed temperature shall not exceed 204°C to prevent hydrocarbons from cracking and depositing carbon. 4) In a pressurized continuous conversion system using naphtha as raw material, ammonia cracking gas is usually used to raise the temperature and then process gas is used to continue heating and reduction. 5) In the pressurized continuous conversion of natural gas as raw material, it is best to use nitrogen to raise the temperature to 180°C, then use superheated steam to raise the temperature to 220°C, and use process gas to continue raising the temperature. 6) The catalyst bed temperature rise rate is ≤80℃/h, and the medium space velocity is 200~300h-1. 4.3.2 Reduction B113-2 catalyst is provided in the form of Fe2O3 and must be reduced to Fe3O4 to have catalytic effect. The B113-2 catalyst is heated to about 200°C by any of the methods proposed above. In the presence of water vapor and reducing gas is introduced, there will be an obvious reduction reaction.: 3Fe2O3+CO=2Fe3O4+CO2+50.79kJ/mol 3Fe2O3+H2=2Fe3O4+H2O+9.62kJ/mol If there is no water vapor, excessive reduction reaction will occur: Fe3O4+4CO=3Fe+4CO2+14.8kJ/mol Fe3O4+H2=3Fe+4H2O-149.92kJ/mol The generation of metallic iron will promote methanation reaction and CO disproportionation reaction: CO+3H2=CH4+H2O+206.28kJ/mol 2CO=CO2+C+172.5kJ/mol The above two reactions will release a large amount of heat, which can easily cause the catalyst to overheat or sinter. Therefore, when the temperature of the catalyst bed rises above 200°C, reducing dry gas is not allowed to be used to increase the temperature. According to thermodynamic data, when the bed temperature is 400°C, PH2/(PH2+PH2O)<0.86 or PCO/(PCO+PH2O)<0.34 can prevent the formation of metallic iron. For devices using natural gas as raw material, reformed gas can be used directly for reduction. In a device using naphtha as raw material, while using ammonia cracking gas to reduce the first-stage reformer catalyst, the hypervariable catalyst is also reduced to a considerable extent. In the early stage of reduction, the inlet temperature of the catalyst bed should be kept at 250°C for at least 2 hours. Otherwise, the temperature at the bottom of the catalyst bed may rise too fast. The temperature rise rate is not allowed to exceed 20°C/h. If the temperature rises too fast, the inlet temperature should be lowered. If the temperature rise is too slow, the inlet temperature should be gradually increased at a rate of 10°C/h. In any case, the inlet temperature at this stage should not exceed 300°C.℃ ； In the early stage of reduction, trial gas distribution can also be used to avoid unnecessary losses caused by bed temperature rise. When the operating pressure of the high-variable furnace is 0.5~2MPa, the space velocity is >200h-1, and the furnace inlet temperature is controlled at 300~370°C (it can be raised to 370°C~420°C at the end of the reduction), the B113-2 catalyst can be successfully and completely reduced after 6 to 8 hours of reduction. B113-2 catalyst, the sulfur content in the body is usually between 150 and 200PPm, and it is easily released. Practice has shown that while the catalyst is reduced, trace amounts of sulfur in the bulk are also reduced and released in the form of H2S, so there is no need to arrange the sulfur release time separately. When the bed temperature of the B113-2 catalyst reaches 220°C, H2S has begun to relax. In order to track the sulfur release of the catalyst body, sulfur analysis must be done immediately after the conversion gas is conducted in the high-variable furnace, otherwise it will be difficult to obtain H2S analysis data. B113-2 catalyst is easy to reduce, and trace amounts of sulfur are easily released. For a pressurized continuous conversion system using natural gas as raw material, when the carbon monoxide content in the high-variable furnace outlet gas remains unchanged and meets the design requirements, it means that the catalyst has been reduced and the high-variable furnace outlet gas can be fed into the low-variable furnace. After that, the load can be gradually increased and the furnace temperature and pressure can be slowly adjusted to normal operating conditions. 4.4 Recommended daily operating indicators of B113-2 catalyst for normal operation are as follows:: Temperature of process gas entering the high-variable furnace (°C): 300～360 B113-2 Carbon Monoxide High Temperature Shift Catalyst Instruction Manual 4 Daily operating temperature (℃): 340～500 steam/dry gas: ≥0.35 airspeed (h-1): 500~700 when below 0.7MPa, 900~2000 when 0.7~2.0MPa, 5000 when 5.0MPa. Users can determine the operating temperature index according to their respective process conditions. The lower limit can be selected at the initial stage of use, and the operating temperature can be gradually increased as the use time goes by. When the furnace inlet temperature is 320°C and steam/dry gas = 0.3, the catalyst activity will not change significantly during short-term operation. Normal operation can also be maintained when the hot spot is at 470°C. But when used at higher temperatures, activity will be affected. In order to ensure and extend the service life of the catalyst, the catalyst should be protected from sudden changes in temperature and pressure. It is recommended that the temperature change speed is <60℃/h and the pressure change speed is <0.3MPa/h. Sulfur, chlorine, silicon, phosphorus, oils, inorganic salts, etc. can deactivate or inactivate the catalyst, and should be avoided from being brought into the furnace through the process gas. In order to ensure the activity of the catalyst, it is recommended that the operating temperature be 25°C higher than the dew point. 4.4.1 Shutdown If the shutdown occurs due to power outage, water cutoff, raw material gas cutoff or other reasons, if the time is short, the raw material gas and steam should be cut off first, the inlet and outlet valves of the high-variable furnace should be closed, and the heat and pressure should be maintained. Wait until the process is normal before introducing qualified process gas. If the shutdown time is long, the system should be depressurized and nitrogen should be used to maintain positive pressure. It is strictly forbidden for the catalyst to come into contact with air or oxygen, otherwise the reduced catalyst will oxidize rapidly and cause the catalyst to burn out due to overtemperature. Catalyst cooling method: If oxidation cooling is used, steam (space speed greater than 500h-1) can be used to lower the bed temperature to 200°C, and then add 2.4% air (equivalent to 0.5% oxygen) for oxidation, and gradually increase the amount of air until the bed temperature stops rising. In order to protect the equipment, the maximum temperature during oxidation should be controlled below 400°C. When the furnace temperature drops to 120°C, the steam can be stopped and air alone is used to cool it to normal temperature. If the catalyst is not removed and will be used in the future, it is best to use the following cooling method:: Chemical plants with inert gas can first use steam to lower the bed temperature to below 200°C, and then use inert gas (such as nitrogen) circulation to cool down to below 50°C. If natural gas is used for cooling, the natural gas can only be cut in when the bed temperature is below 150°C. 4.4.2 Start-up If the catalyst is maintained at temperature and pressure with reducing gas, and the bed temperature is lower than 280°C during start-up, nitrogen or superheated steam can be used to raise it to 280°C first, and then the reformed gas can be introduced. For large-scale ammonia synthesis plants, the high-change furnace is connected in series with the conversion system. 4.5 Catalyst unloading The highly variable catalyst in the reduced state is very easy to oxidize and catch fire. If it is unloaded, it is best to use low-pressure steam to cool it to the lowest possible temperature, then use natural gas or other inert gas to cool it to below 50°C, and then soak it in water to passivate the catalyst and bring it to room temperature. Douse the dry catalyst with water at any time during the unloading process, and transport it out of the factory, taking care to prevent spontaneous combustion.