What are the current energy-saving technologies for ammonia synthesis?

Add a few more: 1. In the first stage of reforming the raw gas, the thin-walled HP conversion tube in the radiant section of the reformer remains unchanged. However, due to the high resistance drop, the lower section of the reforming tube is changed to a large-sized catalyst to reduce the resistance drop. ； Top burner replaced with low NOx burner ； Replace the heat exchange tube with a large convection section to increase the heat exchange area ； The second-stage reformer only replaces the burner ； Add an air compressor to meet the required air volume after capacity expansion. 2. The conversion process changes the conversion furnace from axial to axial-radial flow to improve the capacity of the conversion furnace. 3. Due to the increase in load during shift gas decarbonization, the absorption liquid is replaced with a new activator, and the bottom layer of the absorption tower and the regeneration tower are replaced with high-efficiency packing to meet the needs of the new load. 4. Synthetic gas compression The rotor of the high and low pressure cylinders of the syngas compressor is changed to a three-way flow impeller to improve the pumping capacity. A molecular sieve drying system was added to further purify the syngas and reduce energy consumption. In order to take full advantage of the addition of molecular sieves, the synthesis loop pipeline needs to be modified accordingly. 5 Synthesis Tower The internal parts of the synthesis tower are changed to cold shock internal heat exchange parts between the 3 bed sections in the Casale. Increase the heat exchanger, pump and other equipment of the ammonia and hydrogen recovery device. The above measures can increase production and save energy, and the implementation results are good. This post was last edited by qiwu9981 on 2008-9-11 21:15 ]

Energy saving while considering market needs: Synthetic ammonia and cohydrol go hand in hand. When the price of methanol is high, more methanol is used. When the price of fertilizer is high, more synthetic ammonia is used.

The following are the performance results of high-efficiency separation applications. Is your factory among them? Can you talk about the effect? \User Name Device Scale Purpose Equipment Specification Time Remarks Yongji Zhongxing Chemical Co., Ltd. 100,000 tons/year ammonia co-production 30,000 tons/year methanol methanol separator Φ1000 3/2006 Technical transformation of the second methanol system 30,000 tons/year methanol cycle machine outlet separator Φ1000 1/2007 Newly built methanol separation Φ1000 1/2007 Newly built 120,000 tons/year synthetic ammonia ammonia separator of Anyang Chemical Group Co., Ltd. Φ800 11/2006 Technical renovation of 60,000 tons/year methanol purified gas separator of Anyang Jiutian Fine Chemical Co., Ltd. Φ1000 2/2007 Technical renovation of methanol separator Φ1400 2/2007 Technical transformation of Yunnan Yunwei Group Zhanhua Chemical Co., Ltd. 120,000 tons/year ammonia co-production 30,000 tons/year methanol condensation tower lower ammonia separator Φ1000 10/2003 Technical transformation Yunnan Yunwei Group Dawei Coking Co., Ltd. 2 million tons/year coking production 200,000 tons/year methanol desulfurization tower outlet separator Φ4000 1/2007 Construction and renovation of ammonium sulfate outlet separator Φ4000 1/2007 Construction and renovation of benzene elution outlet separator Φ4000 1/2007 Construction and renovation of cycle machine outlet separator Φ2800 1/2007 Construction and renovation of methanol separator Φ3600 1/2007 Construction and renovation of 240,000 tons/year low-pressure methanol circulating gas outlet separator of Yunnan Yunwei Group Co., Ltd. Φ3800 2/2007 Design change: Supplementary gas oil-water separator Φ1600 2/2007 Design change: Low-pressure alcohol methanol separator Φ3800 2/2007 Design change: Compressor inlet separator Φ1000 2/2007 Design change: 240,000 tons/year ammonia co-production 60,000 tons/year methanolization methanol separator Φ1400 2/2007 Design change: Alkylation hydrocarbon separator Φ1400 2/2007 Design change of hydrocarbonized water separator Φ1400 2/2007 Design change of Yunnan Yunwei Group Co., Ltd. 200,000 tons/year acetic acid plant compressor outlet oil-water separator Φ1000 9/2007 Newly built Guangxi Liuzhou Chemical Co., Ltd. 240,000 tons/year ammonia co-production 60,000 tons/year methanol methanol separator Φ500 10/2007 Technical transformation of methanol separator Φ1000 10/2007 Technical transformation of 100,000 tons of methanol/year methanol separator Φ2200 11/2007 Design changes This post was last edited by qiwu9981 on 2008-6-11 22:59 ]

Use alcohol alkylation or alcohol alkylation instead of copper washing

Our company is the latest large-scale ammonia synthesis process. The energy saving is mainly reflected in the following aspects: 1. The gas turbine combustion exhaust gas is the combustion air of the furnace, with a temperature of about 420 degrees or more, 300T/H 2. Cryogenic purification technology 3. Combined ammonia cooler 4. Horizontal internal cooling synthesis tower 5. Decarbonization technology uses MDEA solution for removal 6. Release gas recovery system The above are just a few points.

Lithium bromide cooling waste heat recovery technology: Recovery and conversion of waste heat cooling compressor section imported semi-water gas ； Waste heat is recovered at the outlet of the synthetic medium pot, and semi-water gas is imported from the cooling compressor. ； * * , Urea evaporation and condensation heat recovery increases the need for cooling capacity. 1. Application cases in fertilizer, coking, and thermal power plant industries: 1. Application cases in Fengxi Group’s refrigeration technology transformation and energy-saving project: ◆Need for refrigeration: A. Cooling of ammonia condensate gas of ammonia separation device B. Cooling of semi-water gas at the inlet of one section C. Cooling of raw gas before compressor intake D. Cooling of decarburized carbon propylene liquid E. Cooling of copper washing copper liquid needs to be cooled to achieve winter operating conditions ◆ Need for heating: A. One-stage heater (155℃) and two-stage heater (140℃) in the urea decomposition process B. One-stage evaporator (130℃) and two-stage evaporator (140℃) in the urea evaporation process ◆The meaning of waste heat is that under certain production process conditions, the energy that is not utilized in the system includes high-temperature waste gas waste heat, cooling medium waste heat, waste steam and waste water waste heat, high-temperature product chemical reaction waste heat, waste gas waste liquid and waste material waste heat, and high-pressure fluid waste heat, etc. ◆Waste heat in nitrogen fertilizer production A. High-temperature gas discharged from the bottom of the tower after reaction in the synthesis tower that needs to be cooled B. High-temperature hot water that needs to be cooled after heat exchange between the water cooler and the high-temperature gas discharged from the synthesis tower C. Hot desalted water generated during the urea synthesis process cycle absorption process D. Condensate generated from the steam used in the urea production process ◆ Fengxi Group waste heat utilization refrigeration process system diagram Waste heat source: Waste heat of steam condensate in urea production process: The waste hot water has been reduced from 130℃ to 68℃, the flow rate is 53.8t/h, and the heat released is 333×104kcal/h. The cooling capacity of the unit: Cold water is reduced from 12℃ to 7℃, flow rate is 500t/h, cooling capacity: 250×104kcal/h ◆Energy Savings: Utilizing the heat of the steam condensate in the urea production process, the hot water unit provides the low-temperature cold water required for the ammonia separation process and reduces the temperature of the raw gas, saving the electricity consumed to obtain cold water and increasing the production volume. ◆Actual usage and energy saving: (You can search for relevant authoritative media reports: Fengxi Group Refrigeration Technology Transformation) Fengxi Group installed heat exchange equipment and a hot water two-stage lithium bromide absorption chiller in front of the semi-desorbed hydrogen and nitrogen compressor. After being put into operation, there have been three results: First, the heat source of the urea condensate first meets the needs of the lithium bromide process and then is sent to the boiler, so that the heat energy is fully utilized. ； The second is to use the cold water generated by the lithium bromide refrigerator as the synthetic circulating cooling water to improve the synthetic ammonia separation effect, reduce the load of the ammonia cooling and ice machines, and significantly reduce the power consumption. ； Third, the raw gas temperature is reduced from 27 to 30°C to 11 to 13°C, the production fluctuation is small, the continuous operation level is improved, and the production increase effect is obvious. In the months of May to September, when the temperature is high, the production increase rate is 4.89%. In October, when the temperature is low, the production increase rate is 3% to 3.3%. The monthly output of synthetic ammonia is more than 400 tons, with a total investment of more than 3.5 million yuan, and an annual increase in income of more than 8 million yuan! 2. Henan Xinlianxin Chemical Waste Heat Refrigeration Application Case: waste heat source: Waste heat of thermal desalted water in urea production process: Circulating water drops from 110℃ to 75℃, flow rate: 143m3/h, heat release 5820KW unit cooling capacity: Cold water is reduced from 16℃ to 6℃, the flow rate: 350m3/h, cooling capacity 4070KW Energy saving: The ammonia synthesis process requires cooling water to ensure process temperature. The heat of the cooling water is used as the heat source of the refrigerator to obtain low-temperature cold water for cooling the urea process, which saves a large amount of high-grade energy consumed to obtain low-temperature cold water. Summary of case process characteristics: ◆ The temperature of waste (residual) heat changes greatly. During the production of synthetic ammonia and urea, the actual production process conditions and changes in output will cause fluctuations in the temperature of the waste heat source. This requires the lithium bromide absorption chiller to be able to adapt to changes in the heat source temperature to ensure that the unit can operate normally within a large fluctuation range of the heat source temperature. ◆ Large changes in cold water temperature and large temperature differences. During the production of synthetic ammonia and urea, actual production process conditions and changes in output will cause changes in the temperature of the cold water inlet and outlet. This also requires the unit to be able to adapt to normal operation within a large fluctuation range of cold water temperature. At the same time, taking into account factors such as reducing flow and reducing the electric power of the water pump, it is best to adopt a large temperature difference (temperature difference of 7°C to 15°C) design for the cold water system to achieve further energy saving. ◆ The operation of the unit must be adjusted according to changes in the working conditions of the process system. As the season and output change, the waste heat generated during the production of ammonia and urea and the cooling capacity requirements of the process system will change. Ordinary comfort air-conditioning refrigeration units can adjust the cooling capacity of the unit by controlling the driving heat source when the external cooling capacity changes. Part of the waste heat used by refrigerators in the nitrogen fertilizer industry, such as: The hot desalted water that needs to be cooled, the residual hot water from the water cooler, etc. cannot affect the flow and temperature changes due to changes in the cooling capacity of the unit. Therefore, the operation of the unit must adapt to the changing requirements of the production process. When the cooling capacity changes, the control system of the unit must be used to ensure that the process system will not be affected by refrigeration and always maintain normal operation. ◆ Special requirements for heat exchange tube materials and manufacturing processes. A large amount of ammonia in the nitrogen fertilizer production process is highly corrosive to traditional heat exchange material copper tubes. Therefore, lithium bromide absorption chillers used in the nitrogen fertilizer industry have special requirements for the selection of heat exchange tube materials. According to the actual conditions of the waste heat source, cold water system and cooling water system. It is necessary to consider the use of different heat exchange tubes for components such as the generator, evaporator, and absorption condensation. The manufacturing of the unit requires special production processes to ensure the sealing performance of the heat exchange tubes and tube sheets. 3. Urea production process heat pump energy-saving process system diagram waste heat source: Waste heat of desalted water from external heat transfer in urea production process: The waste hot water has been reduced from 110℃ to 80℃, the flow rate is 150t/h, and the heat released is 450×104kcal/h. The heating capacity of the unit: Hot water is heated from 120℃ to 140℃, flow rate is 100t/h, cooling capacity: 200×104kcal/h energy saving: Utilizing the heat of hot desalted water in the urea production process and providing hot water through the heat pump unit as the heat source in the urea evaporation process, it can save the consumption of low-pressure steam and reduce the cooling load of desalted water, saving 3 million yuan/year. 4. Shanxi Taiyuan Iron & Steel Group Co., Ltd. uses coke oven waste gas to circulate ammonia water waste heat as a cooling source.: In the iron and steel coking industry, the temperature of ammonia water in the coke oven waste gas cycle is 80°C. After heat exchange, 75°C hot water is obtained for cooling needs.: The coke oven gas intermediate cooling section purification process requires 16°C cold water and the return water is 23°C. Energy Savings: Utilize the heat of circulating ammonia water in the primary cooler to obtain low-temperature cold water through a hot water two-stage lithium bromide refrigeration unit, saving high-grade energy originally consumed to obtain cold water. economic analysis: To save steam, if a steam-type lithium bromide unit with a cooling capacity of 350×104kcal/h is used to satisfy the refrigeration of the process system, it will consume 4.8 tons/hour of steam. Annual operating cost of air cooler: 300,000 yuan. Using a heat pump unit can save operating costs (calculated based on 8,000 hours of annual operation): 4.8 tons/hour × 8,000 hours/year × 100 yuan/ton + 300,000 yuan = 4.14 million yuan/year

Unpowered ammonia recovery technology. Lithium bromide refrigeration technology. Power-saving technology that places the two working numbers of conversion and decarbonization in one section of the compressor. High-efficiency ammonia separation to reduce imported ammonia and improve ammonia separation technology. Washing technology of gas after alcoholization.

1. The original fixed-bed intermittent gas generation furnace adopts oxygen-rich continuous gas generation. 2. The original gas furnace jacket was changed to a thermal oil jacket. 3. Remove the jacket and replace with a heat-resistant lining. 4. Change all gas production and hydraulic valves to seat plate valves. 5. The gas outlet method of the gas generator is changed to ejection. 6. Synthetic ammonia is combined with methanol, nitrogen-rich gas is used to synthesize ammonia, and water gas is used to remove methanol. 7. Methanol synthesis purge gas is used to synthesize ammonia. 8. The cooling between synthesis, compression and distillation adopts air cooling + water cooling.

Our factory is conducting a feasibility study on oxygen enrichment. According to rough calculations by the design unit, the energy consumption per ton of ammonia has dropped by 1GJ.

7. Methanol synthesis purge gas is used to synthesize ammonia. eddy-8280103, this friend, is there CO/CO2 in the methanol purge gas? Is it feasible?

Lithium bromide refrigeration technology is mainly used in the field of air conditioning. Is it suitable for use in the ammonia synthesis process?

I have a small-scale ammonia synthesis device in my workshop. In terms of energy saving, I have the following points:: 1. The PSA purge gas enters the reformer for combustion ； 2. The purification part adopts MDEA decarbonization process ； 3. Chi-gas recovery ； 4. Flash gas recovery ； 5. Condensate recovery from low-variation gas process ； 6. Pump circulating water recovery. The most important thing is the German Linde design adopted in my workshop, which recovers waste heat below 80 degrees.

The latest KBR process eliminates the need for methanation and cold boxes, greatly reducing investment and pipeline pressure drop.

Ultrafiltration device, used for syngas purification, oil and water and other impurities and ammonia separation, decarbonization system filtration, etc.； Oil-free lubrication, used in compressors, etc.

Lithium bromide refrigeration unit is used in gas main pipe； Pressure Swing Adsorption Hydrogen Recovery ； Alcohol alkylation replaces copper washing process

Lithium bromide refrigeration technology can be used in the field of air conditioning and is also suitable for use in the ammonia synthesis process. The solvent cooler for propylene carbonate decarburization of Hebei Zhengyuan Fertilizer Co., Ltd. uses lithium bromide refrigeration technology to cool PC lean liquid and reduce the temperature to below 10°C, with very good effect.

Lithium bromide units are currently being used by more and more fertilizer companies, with obvious energy-saving effects.

The gas-generating slag is sent to the circulating fluidized bed boiler for burning.

The reforming furnace adopts thin-walled reforming furnace； Blast furnace feed water pump switched to turbine drive ； Large unit seal oil waste oil recovery ； Carbon dioxide compressor inlet condensate recovery and distillation ； Large units adjust the fresh steam/extraction steam ratio to optimize the unit's working conditions so that the unit works close to the optimal operating point. ； Increase the temperature of the reforming furnace, increase the air volume of the second-stage furnace, reduce the water-to-carbon ratio, adjust the purge gas volume, and optimize the inert gas content and hydrogen-to-nitrogen ratio of the synthesis tower.

If you want to know whether it saves energy, first learn* Here are the energy consumption calculation methods. Statistical methods for synthetic ammonia energy consumption. 1. Statistical principles for synthetic ammonia energy consumption. 1. Indicator system for synthetic ammonia energy consumption statistics.: ①Natural gas consumption per unit of synthetic ammonia (cubic meters/ton) ； ②Electricity consumption per unit of ammonia synthesis (kWh/ton) ； ③Standard raw coal consumption per unit of synthetic ammonia (kg standard coal/ton) (converted into standard coal based on 7000 kcal/kg) ； ④Standard fuel coal consumption per unit of synthetic ammonia (kg standard coal/ton) (converted into standard coal based on 7000 kcal/kg) ； ⑤Comprehensive energy consumption per unit of synthetic ammonia (kg standard coal/ton) (converted into standard coal based on 7000 kcal/kg) ； 2. The energy consumption of synthetic ammonia refers to the amount of energy actually consumed or necessary for the production of synthetic ammonia products. It should neither be omitted nor repeated. Therefore, when calculating energy consumption, not only the consumption of the production system but also the consumption of the auxiliary and ancillary production systems should be included. 3. Single energy consumption refers to the amount of energy actually purchased and consumed to produce synthetic ammonia, such as: ① Although the foamed coal purchased at the same time as the lump coal is not put into the furnace, it is a component of the purchased raw coal and should be counted in the consumption of raw coal. However, the unused foam coal can be deducted from the comprehensive energy consumption when exported. ② The energy output during the production of ammonia (such as coke return, carbon return, foam coal, combustible gas, etc.), because it is different from the state when it is put into the system, should not be deducted from the input single energy consumption, but should be included in the output energy item of the comprehensive energy consumption. 4. The foamed coal screened from the burned returned coke, returned charcoal, and lump coal will no longer be repeatedly counted into raw materials or fuel consumption. 5. The energy consumed by necessary safety and environmental protection measures in the production of synthetic ammonia should be included in each individual consumption. like: Sulfur recovery, oil recovery, sewage treatment, etc. 6. Multiple users sharing raw gas, public works (steam, energy-consuming working fluids, etc.) as well as joint alcohol, joint alkali, and joint power enterprises should reasonably share the consumption of various energy sources. 7. The energy output by the synthetic ammonia system to the outside world for use by other products or devices should be included in the output energy and deducted from the comprehensive energy consumption. For waste gas, waste liquid, waste residue, etc. in the synthetic ammonia system that are not recycled, are not measured and have no measured calorific value, and are not used for energy reuse (such as for road construction, building houses, etc.), they shall not be included in the output energy. 2. Calculation method of synthetic ammonia energy consumption index Calculation formula of 1 unit of synthetic ammonia consumption of natural gas 1.1: Natural gas consumption per unit of synthetic ammonia (cubic meters/ton) =10000×Total natural gas consumption of synthetic ammonia (10,000 cubic meters)/Synthetic ammonia production (tons) 1.2 Sub-item: The total amount of natural gas consumed by synthetic ammonia includes raw gas used for gas production, natural gas used for heating reformer tubes and auxiliary boilers, and natural gas used for steam boilers. Using oil field gas, coke oven gas, and refinery gas to produce ammonia, the calculation method is the same. 1.3 Parent term: Synthetic ammonia output (see Section 6 Synthetic ammonia output) (omitted below). . 2. Power consumption per unit of synthetic ammonia 2.1 Calculation formula Power consumption per unit of synthetic ammonia (kWh/ton) = 10000 × Total power consumption of synthetic ammonia (10,000 kilowatt-hours) / Synthetic ammonia production (tons) 2.2 Sub-items: Total power consumption for ammonia synthesis The total power consumption for ammonia synthesis includes the power consumption of the ammonia production system and auxiliary and ancillary production systems as well as the loss within the boundary. Measured by electricity meter. 2.2.1 The total power consumption for ammonia synthesis should include: 2.2.1.1 Electricity is used for each process of raw material yard, warehouse transportation (coal, coke, oil, gas), pretreatment (raw coal crushing, coal briquettes, etc.), gas generation, purification, compression, ammonia synthesis, ice machine, ammonia storage and auxiliary boiler. The above-mentioned processes use electricity for workshop lighting, safety ventilation, heating, air conditioning, exhaust cooling, workshop offices, analysis and testing, and baking motors. 2.2.1.2 Electricity consumption for planned overhaul, medium repair, minor repair and accident shutdown (such as lifting, welding) and the power consumed by ignition, oven, heating, hot standby, replacement, etc. during start-up and shutdown caused by maintenance (including overhaul). 2.2.1.3 The amount of electricity consumed in the preparation, extraction and transportation of various energy-carrying working fluids (such as primary water, circulating water, chemical soft water, deoxygenated water, oxygen, nitrogen, compressed air, etc.) consumed in the synthesis of ammonia. 2.2.1.4 Electricity consumption of three wastes treatment in the synthetic ammonia production process (sulfur recovery, oil recovery, sewage treatment, etc.). 2.2.1.5 Industrial boilers consume electricity (such as induced draft fans, blowers, water supply, cooling circulating water pumps, etc.). If the boiler supplies steam to other products at the same time, the amount of steam consumed in the production of ammonia should be reasonably allocated to the power consumption of ammonia. 2.2.1.6 The power consumption of machinery, electricity, instrument repair and metal processing, as well as the power consumption of workshop lighting, ventilation, cooling, and workshop offices, should be reasonably allocated according to the actual maintenance and processing workload of the synthetic ammonia production system. 2.2.1.7 Enterprises that synthesize ammonia alcohol, joint alkali, UMC and ammonium bicarbonate production should reasonably share the electricity they consume. 2.2.1.8 Add ice machine and canning electricity for commercial liquid ammonia. 2.2.1.9 Other electricity consumption for ammonia production. 2.2.2 The total power consumption of ammonia synthesis does not include: 2.2.2.1 Electricity for expansion and technical measures projects. 3 units of synthetic ammonia consume standard raw coal (converted into standard coal based on 7000 kcal/kg) 3.1 Calculation formula: Standard raw coal consumption per unit of synthetic ammonia (kg/ton) = 1000×Total amount of standard raw coal consumption for synthetic ammonia (tons)/Synthetic ammonia production (tons) 3.2 Sub-item: The total amount of standard raw coal for synthetic ammonia consumption (tons) = the sum of each batch (tons) 3.2.1 The physical raw coal (or coke) refers to the coal put into the gas furnace (anthracite lump coal, coke, pellets, bituminous coal, lignite, etc.). When lump coal is used as the raw material, it includes the foamed coal screened out before entering the furnace. The actual weighing value shall prevail. 3.2.2 The application-based low heating value refers to: The thermal effect when the water vapor in the complete combustion product still exists in the gaseous state under certain temperature conditions. Application base low calorific value = high calorific value measured by oxygen bomb instrument - amount of steam generated by combustion × heat of steam condensation 3.2.3 Principle of apportionment and deduction 3.2.3.1 When the gas emitted during the production of synthetic ammonia is recovered and used as fuel (such as storage tank gas, blown gas, etc.), it cannot be deducted from the sub-item. ； 3.2.3.2 Returned coke (returned charcoal) will no longer be counted as consumption, and those that are not returned to the furnace will not be deducted. 3.2.3.3 If the process gas used in the synthetic ammonia production process is used as raw material for other products and the synthetic ammonia co-produces other products, the raw coal consumption should be reasonably allocated. (For joint alcohol, joint alkali, and UMC, see the energy consumption apportionment method for synthetic ammonia and co-produced methanol, the method for apportioning energy consumption for synthetic ammonia and co-produced alkali, and the method for apportioning the energy consumption of synthetic ammonia and co-produced ammonia) 4 units of synthetic ammonia consume standard fuel coal (based on 7000 kcal/kg converted into standard coal) 4.1 Calculation formula: Standard fuel coal consumption per unit of synthetic ammonia (kg/ton) = Total amount of standard fuel coal consumption for synthetic ammonia (kg)/Synthetic ammonia production (tons) 4.2 sub-item: The total amount of standard fuel coal for synthetic ammonia consumption (kg) = the sum of each batch (kg) 4.2.1 Application-based low calorific value (same as 5.2.2) 4.2.2 The total amount of standard fuel coal for synthetic ammonia consumption mainly refers to the fuel coal used to generate steam to meet the steam consumption of the synthetic ammonia production system and auxiliary and ancillary production systems. The amount of purchased steam should be converted into standard fuel coal according to the enthalpy value of the incoming plant and boiler efficiency. 4.2.2.1 The steam consumption of the production system includes the steam used in the production and start-up and stop processes of gas production, purification, compression, ammonia synthesis, ice machine and ammonia storage (including large, medium and minor repair and start-up), as well as the steam used for the above-mentioned process equipment, pipeline insulation and workshop, analysis and testing, workshop office heating, etc. 4.2.2.2 The steam consumption of auxiliary and ancillary production systems includes all heating steam for briquette manufacturing, deoxygenated water preparation, raw materials, fuel storage and pretreatment, briquette workshop, self-contained boiler room and mechanical, electrical, instrument repair workshops and the above workshop offices, as well as replacement and purging steam for planned major, medium and minor repairs and accident repairs, as well as steam for safety production, three wastes treatment, and environmental protection processes. 4.2.2.3 When the steam is only used for synthetic ammonia, the consumption of fuel coal or steam will be included in the consumption of synthetic ammonia. ； When steam is used for multiple products, the fuel coal consumption should be reasonably allocated. (For the consumption apportionment of co-hydrol, co-alkali and co-power, please refer to the energy consumption apportionment method for synthetic ammonia and co-produced methanol, the energy consumption apportionment method for synthetic ammonia and co-produced alkali, and the apportionment method for synthetic ammonia and co-produced power) 4.2.2.4 The returned charcoal, slag, coal gangue, and foamed coal screened from lump coal mixed with the boiler are not included in the fuel consumption, and the returned charcoal picked up from the boiler burning residue is not deducted from the consumption. 4.2.2.5 The steam by-product of the ammonia production process is for the system's own use and is not included in the consumption. The steam vented or exported will not be deducted from the fuel coal consumption. Comprehensive energy consumption for 5 units of synthetic ammonia production 5.2 Calculation formula: Comprehensive energy consumption per unit of synthetic ammonia production (kg standard coal/ton) (converted into standard coal based on 7000 kcal/kg) = unit synthetic ammonia consumption of natural gas (converted into standard coal) + unit unit synthetic ammonia consumption (converted into standard coal) + unit unit synthetic ammonia consumption standard raw coal + unit unit synthetic ammonia consumption standard fuel coal - unit unit synthetic ammonia consumption energy output (converted into standard coal) 5.2.1 Unit unit synthetic ammonia consumption of natural gas (kg standard coal/ tons) = natural gas consumption per unit of synthetic ammonia (cubic meter/ton) (converted to standard state) × low calorific value of natural gas (kcal/standard meter3)/7000 (kcal/kg) 5.2.1.1 Natural gas consumption per unit of ammonia synthesis is the same as Section 1 5.2.1.2 The low calorific value of gas energy sources such as natural gas can be calculated based on the gas composition analysis results. Low calorific value = (2579×H2%) + (3018×CO%) + (5585×H2S%) + (8555×CH4%) + (15226×C2H6%) + (21795×C3H8%) + (28338×C4H10%) + (34890×C5H12%) + (14107×C2H4%) + (20541×C3H6%) + (27111×C4H8%) + (33528×C5H10%) (kcal/standard meter3). 5.2.2 Power consumption per unit of ammonia synthesis (kg standard coal/ton) = Power consumption per unit of ammonia synthesis (kWh/ton) × 0.1229 kg standard coal/kWh 5.2.2, Power consumption per unit of ammonia synthesis is the same as Section 2 5.2.2.2 0.1229 kg standard coal/kWh = 860 (kcal/kWh)/7000 (kcal/kg) 5.2.3 Standard raw coal consumption per unit of synthetic ammonia is the same as Section 3. 5.2.4 Standard fuel coal consumption per unit of synthetic ammonia is the same as Section 4. 5.2.5 Energy output per unit of synthetic ammonia (converted into standard coal at 7000 kcal/kg) 5.2.5.1 Ammonia output energy refers to the energy output by the ammonia system to the outside world for use by other products or devices. For waste gas, waste liquid, waste residue, etc. in the synthetic ammonia system that are not recycled, are not measured and have no measured calorific value, and are not used for energy reuse (such as for road construction, building houses, etc.), they shall not be included in the output energy. 5.2.5.2 Calculation regulations for converting output energy into standard coal: (1) When synthetic ammonia blowout gas, relaxation gas, and analytical gas are used as energy (raw materials, fuel) for other products or devices (including use as civil fuel gas), the calorific value is calculated based on the measured fuel gas composition (the calculation method is the same as 5.2.1.2 ). (2) The materials discharged from synthetic ammonia gas production (foamed coal, coal ash, coke ash, slag, etc.) are indeed used as energy for other products or devices (such as making briquettes, briquettes, firing bricks, etc.) and are converted into standard coal according to the measured low calorific value (7000 kcal/kg). (3) If the waste heat (residual pressure) of the ammonia synthesis system is used to generate electricity and steam, and the output electricity and steam are used by other products or devices, the electricity is converted according to 0.1229 kg standard coal/kWh, and the steam is converted according to the enthalpy value under the temperature and pressure parameters when it leaves the boundary area. (4) Use the waste heat in the production of synthetic ammonia to preheat materials (or production water) for use by other products or devices (according to the recovery of heat energy). The calculation formula for recovering heat energy is: Q = D×C× (T out - T in) where: D - the amount of material to be preheated (kg) C - is the specific heat of the material to be preheated (kcal/kg·degree) T out, T in - is the temperature at which the material to be preheated exits and enters the ammonia synthesis system ； 6 Synthetic ammonia output Synthetic ammonia output is calculated based on physical quantity and is not 100% pure product. Ammonia production includes: Usage of each ammonia unit in the factory ； Amount of liquid ammonia sold ； Self-consumption in the production process of synthetic ammonia (for purification and desulfurization) ； The amount of ammonia recovered from the purge gas of the ammonia tank and the blown gas of the synthesis tower (based on the recycled product based on the ammonia content discounted by 100%) ； Synthetic ammonia production does not include: The amount of ammonia used by the ice machine (loss) ； Ammonia content in ammonia recovered from purification and ammonia desulfurization ； The ammonia water coming out of the carbonization cleaning tower and recovery tower contains ammonia. Synthetic ammonia output should be measured by instrument ； If the enterprise does not install a liquid ammonia meter, the synthetic ammonia output will be calculated based on the final nitrogen-containing product output. Cancel the ammonia tank liquid level meter measurement method and calculate the synthetic ammonia production based on the ammonia consumption quota accounting method of ammonia processing products. 6.1 Instrument measurement: When measuring the liquid ammonia output with an instrument, the liquid ammonia must be decompressed in the intermediate tank to analyze the gas dissolved in the liquid ammonia, and temperature and pressure compensation must be performed to ensure accurate measurement. When an enterprise has both a total ammonia meter and sub-meters for each user, ammonia production must be balanced with usage, and artificial differences between large production and small usage are not allowed. 6.1.1 The total ammonia meter is installed in front of the ammonia warehouse: Synthetic ammonia output (tons) = value recorded in the total ammonia table + the amount of ammonia recovered by blowing, analyzing, and venting gas. 6.1.2 The total ammonia meter is installed behind the ammonia library: Synthetic ammonia output (tons) = the value recorded in the total ammonia table + the amount of self-consumption ammonia + the amount of commercial liquid ammonia + the amount of ammonia recovered from blown, analyzed, and vented gases + (ending inventory of ammonia tanks - beginning inventory of ammonia tanks). 6.1.3 When the ammonia output is taken as the sum of the ammonia metering tables of each user: Including the recorded value of self-use ammonia and commercial liquid ammonia + the amount of ammonia recovered by blowing, analyzing, and venting gas) + (ending inventory of ammonia tanks - beginning inventory of ammonia tanks). The amount of ammonia recovered from blown, analyzed, and relaxed gases refers to the amount of ammonia recovered from the blowing gas from the synthesis tower, the analytical gas from the intermediate tank, and the relaxed gas from the ammonia tank that are recycled into the system for use or sale. 6.2 Calculate the synthetic ammonia production based on the final nitrogen-containing product. When calculating synthetic ammonia production based on final nitrogen-containing products, urea, ammonium bicarbonate, * The ammonia utilization rate of various solid chemical fertilizers such as aoan, sulfate, ammonium chloride, and concentrated nitric acid is 92%. ； The ammonia utilization rate of ammonia is 96%. Synthetic ammonia production [tons] = commercial liquid ammonia amount (tons) + self-use ammonia amount (tons) + [qualified solid fertilizer containing 100% nitrogen (tons) + unqualified solid fertilizer containing 100% nitrogen (tons)] × 1.32161 + ×1.04167 + where: 1.32161 = 1 /0.82245 /0.92 0.82245 is the molecular weight of nitrogen divided by the molecular weight of ammonia, which is the theoretical nitrogen content of ammonia. 1.04167 = 1 /0.96 6.2.1 The amount of commercial liquid ammonia is based on the bottling or loading amount. 6.2.2 Amount of ammonia for self-use. When each user has an ammonia meter, the amount of ammonia for self-use shall be based on the value recorded on the meter. ； When each user does not have a meter for measurement, the regulations and calculation formula for self-use ammonia are as follows:: (a) The amount of self-used ammonia for copper washing method is 0.5% of the total ammonia amount. The amount of self-used ammonia for copper washing (tons) = synthetic ammonia production × 0.5%. (b) The amount of self-used ammonia for changing from alkali washing to ammonia washing after copper washing is 0.5% of the total ammonia amount. The amount of self-used ammonia for alkali washing to ammonia washing (tons) = synthetic ammonia production × 0.5%. (c) The self-used ammonia amount for desulfurization process is 1% of the total ammonia amount. Amount of self-used ammonia for desulfurization (tons) = synthetic ammonia output 6.2.3 The amount of ammonia in ammonia solution includes: Qualified agricultural ammonia and industrial ammonia produced directly by recycling the synthesis tower blowout gas, intermediate tank analysis gas, and ammonia tank relaxation gas also include unqualified ammonia that contains more than 10% ammonia and has been sold. ； The amount of ammonia deaminated does not include: ammonia water recovered from purification (copper washing), desulfurization, ammonia water from the carbonization cleaning tower and recovery tower, nor does it include self-use ammonia water (purification) for copper washing and desulfurization, and discharged qualified or unqualified ammonia water. 6.3 Determination of ammonia output when using multiple raw materials to produce synthetic ammonia Enterprises that use multiple raw materials to produce synthetic ammonia should break down the synthetic ammonia output by raw materials when reporting the total synthetic ammonia output. The determination of the output of synthetic ammonia produced from various raw materials should be determined according to the gas production volume of various raw materials and their effective gas components in the total ammonia amount. The calculation formula: Synthetic ammonia output produced from a certain raw material = Total synthetic ammonia output × 7 Nitrogen fertilizer output Nitrogen fertilizer is a chemical fertilizer made by chemical methods that contains nitrogen, a nutrient element for crops. The main types of nitrogen fertilizers are urea, ammonium bicarbonate, ammonium chloride, anhydrous sulfate, * aoan, lime nitrogen, ammonia, etc., as well as compound fertilizers containing nitrogen, such as nitric acid phosphate fertilizer and ammonium phosphate fertilizer. The pure amount should be converted into 100% of the actual nitrogen content to calculate the yield. Nitrogen fertilizer yield (100% nitrogen reduction) is the sum of the qualified physical quantity of each nitrogen fertilizer variety multiplied by the actual nitrogen content (%). If the active ingredient content is expressed by dry basis analysis, the water should be deducted from the actual amount when calculating, and then multiplied by the actual analyzed dry basis content. Calculation methods for main varieties of nitrogen fertilizers: 7.1 Urea (scientific name: carbonyl diammonium, NH2CONH2) converted into pure nitrogen yield Urea (converted nitrogen 100%) = sum of each batch 7.2 Ammonium bicarbonate (NH4HCO3) converted into pure nitrogen yield ammonium bicarbonate (reduced nitrogen 100%) = sum of each batch 7.3 Ammonium chloride (NH4CL) converted into pure nitrogen yield ammonium chloride (reduced nitrogen 100%) = sum of each batch 7.4 * Ao acid an (NH4NO3) converted into pure nitrogen yield * ao acid an (nitrogen 100%) = sum of each batch. 7.6 Lime nitrogen (scientific name: calcium cyanamide CaCN2) converted into pure nitrogen yield Lime nitrogen (condensed 100% nitrogen) = sum of each batch 7.7 Ammonia water (NH4OH) converted into pure nitrogen yield ammonia water (condensed 100% nitrogen) = sum of each batch 7.8 Compound (mixed) fertilizer converted into pure nitrogen yield Nitrogen-containing compound (mixed) fertilizer calculates the nitrogen fertilizer yield, where the nitrogen comes from liquid ammonia or urine (( Whether it is purchased from outside or produced in-house), pure nitrogen (100%) must be converted into nitrogen fertilizer production. Nitrogen comes from the non-repeated calculation of nitrogen fertilizer production of finished nitrogen fertilizers (urea, ammonium chloride, ammonium bicarbonate, anhydrous sulfate, etc.).