Method for converting industrial waste heat into low pressure steam to drive ammonia adsorption refrigeration

Abstract

The present application relates to the technical field of waste heat recycling, in particular to a method for converting industrial waste heat into low-pressure steam to drive ammonia adsorption refrigeration, comprising the following steps: Step 1: industrial waste heat collection and pretreatment, S1.1 waste heat classification collection: for different types of waste heat (slag waste heat, high-temperature flue gas, low-pressure steam, engine exhaust gas) in industrial production, special heat exchange devices are used for classification collection, wherein slag waste heat is recovered through indirect heat exchange devices; the present application efficiently recovers industrial low-grade waste heat and converts it into stable low-pressure steam of 0.3 MPa and above, and the waste heat utilization rate is increased to more than 85%; the refrigeration process does not consume high-grade energy, the main machine operates at zero cost, the comprehensive energy-saving rate is more than 77.8%, the annual electricity saving can reach 140,000 degrees per set, natural working substance ammonia is used as refrigerant, ammonia can be cyclically decomposed and compounded under natural conditions, and there is no greenhouse gas emission; fluorine-containing refrigerants such as freon are abandoned, atmospheric pollution is avoided from the source, and the green and low-carbon development trend is met.

Description

Technical Field

[0001] This invention relates to the field of waste heat recovery technology, specifically a method for converting industrial waste heat into low-pressure steam to drive ammonia adsorption refrigeration. Background Technology

[0002] Industrial production processes generate a large amount of low-grade waste heat (such as waste heat from steel plant slag, waste heat from cooling water in glass production lines, low-pressure steam from chemical plant reactors, and exhaust gas from oil and gas field combustion). This type of waste heat has a wide temperature range and huge emission volumes, but traditional treatment methods mostly involve direct discharge or simple heat exchange, resulting in a resource utilization rate of less than 30% and causing serious energy waste. Meanwhile, traditional refrigeration technologies have several core limitations:

[0003] High energy consumption and high emissions coexist: Compressor refrigeration relies on electricity or engine drive, resulting in high energy consumption and high operating costs, with an annual electricity saving rate of less than 20%; Freon and other fluorinated refrigerants are strong greenhouse gases, and long-term emissions will damage the atmospheric structure and cause environmental disasters, while their alternatives are more chemically stable and their environmental harm has a lag effect.

[0004] Limited applications of ammonia refrigeration: Traditional ammonia refrigeration equipment relies on electricity or engines and faces challenges in miniaturization. Its refrigeration temperature range is limited to -28~5℃, which cannot meet the needs of low-temperature refrigeration. At the same time, the system has poor sealing performance and insufficient corrosion resistance. When switching between high-temperature flue gas and cooling water, problems such as cross-contamination and control failure are prone to occur.

[0005] The disconnect between waste heat utilization and refrigeration technology: existing adsorption refrigeration technologies mostly use a single heat source, which cannot adapt to the fluctuating characteristics of industrial waste heat; unreasonable adsorbent formulations lead to severe powder spraying, and defects in generator structure make it easy for pipeline blockage to occur when flue gas, ammonia, and cooling water coexist, which restricts the efficient coupling of industrial waste heat and refrigeration systems.

[0006] High system maintenance costs and poor reliability: Traditional refrigeration equipment has many moving parts, requiring frequent and costly maintenance; adsorption refrigeration systems lack intelligent control mechanisms, cannot dynamically adjust their operating status based on waste heat parameters, and have insufficient fault warning and troubleshooting capabilities, affecting long-term stable operation.

[0007] Existing technologies have not yet formed an integrated technical solution of "efficient recovery of industrial waste heat - stable preparation of low-pressure steam - precise refrigeration by ammonia adsorption - intelligent control closed loop", making it difficult to balance energy utilization, refrigeration performance, environmental protection requirements and operational reliability. Therefore, a method of converting industrial waste heat into low-pressure steam to drive ammonia adsorption refrigeration is proposed. Summary of the Invention

[0008] In view of this, the present invention provides a method for converting industrial waste heat into low-pressure steam to drive ammonia adsorption refrigeration, so as to solve or alleviate the technical problems existing in the prior art, and at least provide a beneficial option.

[0009] The technical solution of this invention is implemented as follows: a method for converting industrial waste heat into low-pressure steam to drive ammonia adsorption refrigeration, comprising the following steps:

[0010] Step 1: Industrial Waste Heat Collection and Pretreatment

[0011] S1.1 Waste Heat Classification and Collection: For different types of waste heat in industrial production (slag waste heat, high-temperature furnace flue gas, low-pressure steam, engine exhaust gas), a special heat exchange device is used for classified collection. Slag waste heat is recovered through an indirect heat exchange device, high-temperature furnace flue gas is introduced into the heat exchange system after dust removal and desulfurization pretreatment, and low-pressure steam is directly connected to the steam buffer tank.

[0012] S1.2 Waste heat parameter control: Waste heat parameters are monitored in real time through flow regulating valve and temperature sensor to control the waste heat temperature to be stable at 120~200℃ and the flow fluctuation range to ≤±10%, so as to ensure the stability of subsequent steam preparation.

[0013] Step 2: Low-pressure steam preparation and stabilization

[0014] S2.1 Waste heat-water heat exchange: The pretreated industrial waste heat is introduced into a heat exchanger to exchange heat with deionized water. The heat exchange pressure is controlled at 0.3~0.8MPa and the heat exchange temperature is 130~180℃ to heat the deionized water to saturated low-pressure steam.

[0015] S2.2 Steam pressure stabilization treatment: The generated low-pressure steam is introduced into a buffer tank with a pressure compensation device. The steam pressure is maintained at 0.3MPa or above through the linkage of a pressure sensor and a regulating valve. The steam flow rate is controlled at 0.3 to 1.67 tons / h to meet the heat source requirements of the adsorption refrigeration system.

[0016] Step 3: Start-up and circulation operation of the ammonia adsorption refrigeration system

[0017] S3.1 System Pretreatment: The generator (containing three units A, B, and C) of the adsorption refrigeration unit is filled with an optimized formula adsorbent (composed of metal oxide composites) and ammonia refrigerant is injected to ensure that the mass ratio of adsorbent to ammonia is 2.66:1; the flue gas, ammonia, and cooling water inside the generator are isolated and sealed through a water seal structure.

[0018] S3.2 Desorption-condensation process: The low-pressure steam after pressure stabilization is introduced into generator unit A to heat the adsorbent to the desorption temperature of 80~120℃. The complex between the adsorbent and ammonia undergoes reversible decomposition, releasing high-temperature and high-pressure ammonia gas. The ammonia gas enters the condenser and is cooled to 30~40℃ by cooling water, condensing into liquid ammonia, which is stored in the liquid ammonia storage tank.

[0019] S3.3 Evaporation-Refrigeration Process: Liquid ammonia is throttled and depressurized by the expansion valve, and converted into mist-like low-temperature and low-pressure ammonia. It enters the evaporator to exchange heat with the medium to be cooled (water or air). After absorbing heat, it evaporates into gaseous ammonia, achieving refrigeration in the range of -40~20℃. Cold water or cold air is obtained at the outlet of the evaporator.

[0020] S3.4 Adsorption-Regeneration Process: Gaseous ammonia enters generator unit B, which is in a cooled state, and is adsorbed by the adsorbent at 30~50℃, reforming the complex; at the same time, generator unit A stops supplying low-pressure steam and supplies cooling water to cool to the adsorption temperature; generator unit C starts the desorption-condensation process according to the above procedure; the three units switch sequentially according to the program to achieve continuous refrigeration cycle.

[0021] Step 4: Intelligent Control and Operation Maintenance

[0022] S4.1 Real-time monitoring: Data such as waste heat parameters, steam pressure / flow rate, refrigeration temperature / cooling capacity, and adsorbent status are collected through a sensor array and transmitted to the digital monitoring platform;

[0023] S4.2 Dynamic Control: Based on monitoring data, the waste heat exchange flow rate, steam pressure, cooling water flow rate, and generator switching cycle are intelligently adjusted to ensure stable operation of the refrigeration system; when waste heat parameters fluctuate, the heat storage device is activated to compensate for heat and maintain stable cooling capacity.

[0024] S4.3 Fault Early Warning and Handling: Through data analysis, early warnings are provided for faults such as adsorbent aging, pipeline blockage, and seal failure, and troubleshooting procedures are automatically triggered to ensure continuous system operation;

[0025] Step 5: Cooling capacity output and multi-scenario adaptation

[0026] S5.1 Direct Cooling Output: Based on the application scenario requirements, the cooling capacity generated by the evaporator is directly supplied to cold storage, air conditioning, ice-making equipment, etc. The ice-making system can achieve a daily production of 5 tons or more of flake ice.

[0027] S5.2 Cold Storage and Mobile Cooling: Ice storage is achieved through ice storage tanks, supporting cross-seasonal cold storage and delayed cooling; it is compatible with mobile cooling vehicles to achieve zero-consumption transportation cooling, with a charging and cold storage time of 30 minutes and a cold removal time of 90 minutes.

[0028] Further preferred, the preparation method of the optimized adsorbent formulation in step S3.1 is as follows: zinc oxide and aluminum oxide are mixed in a mass ratio of 3:2, 5% to 8% of modifier (titanium ester coupling agent) is added, and the mixture is prepared by high-temperature calcination (500~600℃) and granulation (particle size 50~100μm), thus avoiding the powder spraying problem of traditional formulations.

[0029] In a further preferred embodiment, the water seal structure described in step S3.1 includes a sealing cavity, an elastic sealing element, and an automatic control valve, which can achieve dynamic sealing when switching between high-temperature flue gas and cooling water, and has a corrosion resistance level of C4 or above, thus solving the problems of thermal deformation and gas leakage.

[0030] Further preferably, the special heat exchange device mentioned in step S1.1 is designed for different types of waste heat: slag waste heat adopts an immersion heat exchange device, high-temperature furnace flue gas adopts a shell and tube heat exchanger, and low-pressure steam adopts a plate heat exchanger, with a heat exchange efficiency ≥85%.

[0031] More preferably, the conductivity of the deionized water in step S2.1 is ≤10μS / cm to avoid scaling in the heat exchanger affecting the heat exchange efficiency.

[0032] More preferably, the expansion valve in step S3.3 has a throttling accuracy of ±0.1MPa to ensure that the ammonia mist has a uniform particle size and that the refrigeration temperature fluctuation is ≤±2℃.

[0033] More preferably, the switching cycle of the three units of the generator in step S3.4 is 10 to 15 minutes, and automatic switching is achieved by a PLC controller to ensure continuous cooling.

[0034] More preferably, the sensor array in step S4.1 includes a temperature sensor (accuracy ±0.5℃), a pressure sensor (accuracy ±0.01MPa), a flow sensor (accuracy ±1%), and an adsorbent state sensor, with a data acquisition frequency of 1 time / minute.

[0035] Further preferably, the ice-making system described in step S5.1 is designed with a cooling capacity of 24,000 kcal / h and an evaporation temperature of -18°C, which meets the needs of industrial ice making and ice supply for agricultural markets.

[0036] The embodiments of the present invention have the following advantages due to the adoption of the above technical solutions:

[0037] I. This invention efficiently recovers low-grade industrial waste heat and converts it into stable low-pressure steam at 0.3 MPa and above, increasing the waste heat utilization rate to over 85%. The refrigeration process does not require the consumption of high-grade energy, the main unit operates at zero cost, the comprehensive energy saving rate reaches over 77.8%, and the annual electricity saving can reach 140,000 kWh / set. It uses ammonia, a natural working fluid, as a refrigerant, which can be cyclically decomposed and recombined under natural conditions, with no greenhouse gas emissions. It eliminates fluorinated refrigerants such as Freon, avoiding air pollution at its source, and conforms to the trend of green and low-carbon development.

[0038] Second, the refrigeration temperature range of this invention is extended to -40~20℃, breaking through the temperature limitations of traditional ammonia refrigeration, and can meet the needs of multiple scenarios such as ice making, cold storage, air conditioning, and low-temperature chilled water; the refrigeration capacity covers tens of watts to tens of thousands of watts, and is suitable for different application scenarios such as small refrigeration equipment, large cold storage, and cold chain transportation.

[0039] Third, this invention features an innovative water seal structure and a new adsorbent formula, completely solving the problems of sealing, corrosion prevention, thermal deformation, and powder spraying. The system has no moving parts, requires no maintenance, has a long service life, and its operating cost is only less than 25% of that of compressor refrigeration. The investment payback period is shortened to about one year. It integrates a digital economy support system to monitor operating data in real time, intelligently adjust parameters, provide fault warnings and troubleshooting, and can adapt to the fluctuating characteristics of industrial waste heat. It supports multiple modes such as delayed refrigeration, intermittent refrigeration, and ice storage refrigeration, and can achieve lossless cold storage across seasons.

[0040] The above overview is for illustrative purposes only and is not intended to be limiting in any way. In addition to the illustrative aspects, embodiments, and features described above, further aspects, embodiments, and features of the invention will become readily apparent from the accompanying drawings and the following detailed description. Attached Figure Description

[0041] To more clearly illustrate the technical solutions in the embodiments of this application or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0042] Figure 1 This is a flowchart of the method of the present invention. Detailed Implementation

[0043] In the following description, only certain exemplary embodiments are briefly described. As those skilled in the art will recognize, the described embodiments can be modified in various ways without departing from the spirit or scope of the invention. Therefore, the drawings and description are considered to be exemplary in nature and not restrictive.

[0044] The embodiments of the present invention will now be described in detail with reference to the accompanying drawings.

[0045] like Figure 1 As shown, this embodiment of the invention provides a method for converting industrial waste heat into low-pressure steam to drive ammonia adsorption refrigeration, comprising the following steps:

[0046] Step 1: Industrial Waste Heat Collection and Pretreatment

[0047] S1.1 Waste Heat Classification and Collection: For different types of waste heat in industrial production (slag waste heat, high-temperature furnace flue gas, low-pressure steam, engine exhaust gas), a special heat exchange device is used for classified collection. Slag waste heat is recovered through an indirect heat exchange device, high-temperature furnace flue gas is introduced into the heat exchange system after dust removal and desulfurization pretreatment, and low-pressure steam is directly connected to the steam buffer tank.

[0048] S1.2 Waste heat parameter control: Waste heat parameters are monitored in real time through flow regulating valve and temperature sensor to control the waste heat temperature to be stable at 120~200℃ and the flow fluctuation range to ≤±10%, so as to ensure the stability of subsequent steam preparation.

[0049] Step 2: Low-pressure steam preparation and stabilization

[0050] S2.1 Waste heat-water heat exchange: The pretreated industrial waste heat is introduced into a heat exchanger to exchange heat with deionized water. The heat exchange pressure is controlled at 0.3~0.8MPa and the heat exchange temperature is 130~180℃ to heat the deionized water to saturated low-pressure steam.

[0051] S2.2 Steam pressure stabilization treatment: The generated low-pressure steam is introduced into a buffer tank with a pressure compensation device. The steam pressure is maintained at 0.3MPa or above through the linkage of a pressure sensor and a regulating valve. The steam flow rate is controlled at 0.3 to 1.67 tons / h to meet the heat source requirements of the adsorption refrigeration system.

[0052] Step 3: Start-up and circulation operation of the ammonia adsorption refrigeration system

[0053] S3.1 System Pretreatment: The generator (containing three units A, B, and C) of the adsorption refrigeration unit is filled with an optimized formula adsorbent (composed of metal oxide composites) and ammonia refrigerant is injected to ensure that the mass ratio of adsorbent to ammonia is 2.66:1; the flue gas, ammonia, and cooling water inside the generator are isolated and sealed through a water seal structure.

[0054] S3.2 Desorption-condensation process: The low-pressure steam after pressure stabilization is introduced into generator unit A to heat the adsorbent to the desorption temperature of 80~120℃. The complex between the adsorbent and ammonia undergoes reversible decomposition, releasing high-temperature and high-pressure ammonia gas. The ammonia gas enters the condenser and is cooled to 30~40℃ by cooling water, condensing into liquid ammonia, which is stored in the liquid ammonia storage tank.

[0055] S3.3 Evaporation-Refrigeration Process: Liquid ammonia is throttled and depressurized by the expansion valve, and converted into mist-like low-temperature and low-pressure ammonia. It enters the evaporator to exchange heat with the medium to be cooled (water or air). After absorbing heat, it evaporates into gaseous ammonia, achieving refrigeration in the range of -40~20℃. Cold water or cold air is obtained at the outlet of the evaporator.

[0056] S3.4 Adsorption-Regeneration Process: Gaseous ammonia enters generator unit B, which is in a cooled state, and is adsorbed by the adsorbent at 30~50℃, reforming the complex; at the same time, generator unit A stops supplying low-pressure steam and supplies cooling water to cool to the adsorption temperature; generator unit C starts the desorption-condensation process according to the above procedure; the three units switch sequentially according to the program to achieve continuous refrigeration cycle.

[0057] Step 4: Intelligent Control and Operation Maintenance

[0058] S4.1 Real-time monitoring: Data such as waste heat parameters, steam pressure / flow rate, refrigeration temperature / cooling capacity, and adsorbent status are collected through a sensor array and transmitted to the digital monitoring platform;

[0059] S4.2 Dynamic Control: Based on monitoring data, the waste heat exchange flow rate, steam pressure, cooling water flow rate, and generator switching cycle are intelligently adjusted to ensure stable operation of the refrigeration system; when waste heat parameters fluctuate, the heat storage device is activated to compensate for heat and maintain stable cooling capacity.

[0060] S4.3 Fault Early Warning and Handling: Through data analysis, early warnings are provided for faults such as adsorbent aging, pipeline blockage, and seal failure, and troubleshooting procedures are automatically triggered to ensure continuous system operation;

[0061] Step 5: Cooling capacity output and multi-scenario adaptation

[0062] S5.1 Direct Cooling Output: Based on the application scenario requirements, the cooling capacity generated by the evaporator is directly supplied to cold storage, air conditioning, ice-making equipment, etc. The ice-making system can achieve a daily production of 5 tons or more of flake ice.

[0063] S5.2 Cold Storage and Mobile Cooling: Ice storage is achieved through ice storage tanks, supporting cross-seasonal cold storage and delayed cooling; it is compatible with mobile cooling vehicles to achieve zero-consumption transportation cooling, with a charging and cold storage time of 30 minutes and a cold removal time of 90 minutes.

[0064] In one embodiment, the preparation method of the optimized adsorbent formulation in step S3.1 is as follows: zinc oxide and aluminum oxide are mixed in a mass ratio of 3:2, 5% to 8% of modifier (titanium ester coupling agent) is added, and the mixture is prepared by high-temperature calcination (500~600℃) and granulation (particle size 50~100μm), thus avoiding the powder spraying problem of traditional formulations.

[0065] In one embodiment, the water seal structure in step S3.1 includes a sealing cavity, an elastic seal, and an automatic control valve, which can achieve dynamic sealing when switching between high-temperature flue gas and cooling water, and has a corrosion resistance level of C4 or above, solving the problems of thermal deformation and gas leakage.

[0066] In one embodiment, the dedicated heat exchange device in step S1.1 is designed for different types of waste heat: slag waste heat adopts an immersion heat exchange device, high-temperature furnace flue gas adopts a shell and tube heat exchanger, and low-pressure steam adopts a plate heat exchanger, with a heat exchange efficiency of ≥85%.

[0067] In one embodiment, the conductivity of the deionized water in step S2.1 is ≤10μS / cm to avoid scaling in the heat exchanger affecting the heat exchange efficiency.

[0068] In one embodiment, the throttling accuracy of the expansion valve in step S3.3 is ±0.1MPa, ensuring that the particle size of the ammonia mist is uniform and the refrigeration temperature fluctuation is ≤±2℃.

[0069] In one embodiment, the switching cycle of the three units of the generator in step S3.4 is 10 to 15 minutes, and automatic switching is achieved through a PLC controller to ensure continuous cooling.

[0070] In one embodiment, the sensor array in step S4.1 includes a temperature sensor (accuracy ±0.5℃), a pressure sensor (accuracy ±0.01MPa), a flow sensor (accuracy ±1%), and an adsorbent state sensor, with a data acquisition frequency of 1 time / minute.

[0071] In one embodiment, the ice-making system in step S5.1 is designed with a cooling capacity of 24,000 kcal / h and an evaporation temperature of -18°C, which meets the needs of industrial ice making and ice supply for agricultural markets.

[0072] The above description is merely a specific embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Any person skilled in the art can easily conceive of various variations or substitutions within the technical scope disclosed in the present invention, and these should all be included within the scope of protection of the present invention. Therefore, the scope of protection of the present invention should be determined by the scope of the claims.

Claims

1. A method for converting industrial waste heat into low pressure steam to drive ammonia adsorption refrigeration, characterized in that: Includes the following steps: Step 1: Industrial Waste Heat Collection and Pretreatment S1.1 Waste Heat Classification and Collection: For different types of waste heat in industrial production (slag waste heat, high-temperature furnace flue gas, low-pressure steam, engine exhaust gas), a special heat exchange device is used for classified collection. Slag waste heat is recovered through an indirect heat exchange device, high-temperature furnace flue gas is introduced into the heat exchange system after dust removal and desulfurization pretreatment, and low-pressure steam is directly connected to the steam buffer tank. S1.2 Waste heat parameter control: Waste heat parameters are monitored in real time through flow regulating valve and temperature sensor to control the waste heat temperature to be stable at 120~200℃ and the flow fluctuation range to ≤±10%, so as to ensure the stability of subsequent steam preparation. Step 2: Low-pressure steam preparation and stabilization S2.1 Waste heat-water heat exchange: The pretreated industrial waste heat is introduced into a heat exchanger to exchange heat with deionized water. The heat exchange pressure is controlled at 0.3~0.8MPa and the heat exchange temperature is 130~180℃ to heat the deionized water to saturated low-pressure steam. S2.2 Steam pressure stabilization treatment: The generated low-pressure steam is introduced into a buffer tank with a pressure compensation device. The steam pressure is maintained at 0.3MPa or above through the linkage of a pressure sensor and a regulating valve. The steam flow rate is controlled at 0.3 to 1.67 tons / h to meet the heat source requirements of the adsorption refrigeration system. Step 3: Start-up and circulation operation of the ammonia adsorption refrigeration system S3.1 System Pretreatment: The generator (containing three units A, B, and C) of the adsorption refrigeration unit is filled with an optimized formula adsorbent (composed of metal oxide composites) and ammonia refrigerant is injected to ensure that the mass ratio of adsorbent to ammonia is 2.66:1; the flue gas, ammonia, and cooling water inside the generator are isolated and sealed through a water seal structure. S3.2 Desorption-condensation process: The low-pressure steam after pressure stabilization is introduced into generator unit A to heat the adsorbent to the desorption temperature of 80~120℃. The complex between the adsorbent and ammonia undergoes reversible decomposition, releasing high-temperature and high-pressure ammonia gas. The ammonia gas enters the condenser and is cooled to 30~40℃ by cooling water, condensing into liquid ammonia, which is stored in the liquid ammonia storage tank. S3.3 Evaporation-Refrigeration Process: Liquid ammonia is throttled and depressurized by the expansion valve, and converted into mist-like low-temperature and low-pressure ammonia. It enters the evaporator to exchange heat with the medium to be cooled (water or air). After absorbing heat, it evaporates into gaseous ammonia, achieving refrigeration in the range of -40~20℃. Cold water or cold air is obtained at the outlet of the evaporator. S3.4 Adsorption-Regeneration Process: Gaseous ammonia enters generator unit B, which is in a cooled state, and is adsorbed by the adsorbent at 30~50℃, reforming the complex; at the same time, generator unit A stops supplying low-pressure steam and supplies cooling water to cool to the adsorption temperature; generator unit C starts the desorption-condensation process according to the above procedure; the three units switch sequentially according to the program to achieve continuous refrigeration cycle. Step 4: Intelligent Control and Operation Maintenance S4.1 Real-time monitoring: Data such as waste heat parameters, steam pressure / flow rate, refrigeration temperature / cooling capacity, and adsorbent status are collected through a sensor array and transmitted to the digital monitoring platform; S4.2 Dynamic Control: Based on monitoring data, the waste heat exchange flow rate, steam pressure, cooling water flow rate, and generator switching cycle are intelligently adjusted to ensure stable operation of the refrigeration system; when waste heat parameters fluctuate, the heat storage device is activated to compensate for heat and maintain stable cooling capacity. S4.3 Fault Early Warning and Handling: Through data analysis, early warnings are provided for faults such as adsorbent aging, pipeline blockage, and seal failure, and troubleshooting procedures are automatically triggered to ensure continuous system operation; Step 5: Cooling capacity output and multi-scenario adaptation S5.1 Direct Cooling Output: Based on the application scenario requirements, the cooling capacity generated by the evaporator is directly supplied to cold storage, air conditioning, ice-making equipment, etc. The ice-making system can achieve a daily production of 5 tons or more of flake ice. S5.2 Cold Storage and Mobile Cooling: Ice storage is achieved through ice storage tanks, supporting cross-seasonal cold storage and delayed cooling; it is compatible with mobile cooling vehicles to achieve zero-consumption transportation cooling, with a charging and cold storage time of 30 minutes and a cold removal time of 90 minutes.

2. The method of claim 1, wherein the industrial waste heat is converted into low pressure steam to drive ammonia adsorption refrigeration. The optimized adsorbent formulation described in step S3.1 is prepared by mixing zinc oxide and aluminum oxide in a mass ratio of 3:2, adding 5% to 8% of a modifier (titanium ester coupling agent), and then calcining at high temperature (500 to 600°C) and granulating (particle size 50 to 100 μm) to avoid the powder spraying problem of traditional formulations.

3. The method of claim 1, wherein the industrial waste heat is converted into low pressure steam to drive ammonia adsorption refrigeration. The water seal structure described in step S3.1 includes a sealing cavity, an elastic sealing element, and an automatic control valve, which can achieve dynamic sealing when switching between high-temperature flue gas and cooling water, and has a corrosion resistance level of C4 or above, solving the problems of thermal deformation and gas leakage.

4. The method of claim 1, wherein the industrial waste heat is converted into low pressure steam to drive ammonia adsorption refrigeration. The special heat exchange device mentioned in step S1.1 is designed for different types of waste heat: slag waste heat adopts an immersion heat exchange device, high-temperature furnace flue gas adopts a shell and tube heat exchanger, and low-pressure steam adopts a plate heat exchanger, with a heat exchange efficiency of ≥85%.

5. The method of converting industrial waste heat into low pressure steam to drive ammonia adsorption refrigeration according to claim 1, characterized in that: The conductivity of the deionized water mentioned in step S2.1 is ≤10μS / cm to avoid scaling in the heat exchanger, which would affect the heat exchange efficiency.

6. The method of converting industrial waste heat to low pressure steam to drive ammonia adsorption refrigeration of claim 1, wherein: The expansion valve described in step S3.3 has a throttling accuracy of ±0.1MPa, ensuring that the ammonia mist has a uniform particle size and that the refrigeration temperature fluctuation is ≤±2℃.

7. The method of converting industrial waste heat to low pressure steam to drive ammonia adsorption refrigeration of claim 1, wherein: The switching cycle of the three units of the generator in step S3.4 is 10 to 15 minutes, and automatic switching is achieved through the PLC controller to ensure continuous cooling.

8. The method for converting industrial waste heat into low-pressure steam to drive ammonia adsorption refrigeration according to claim 1, characterized in that: The sensor array mentioned in step S4.1 includes a temperature sensor (accuracy ±0.5℃), a pressure sensor (accuracy ±0.01MPa), a flow sensor (accuracy ±1%), and an adsorbent state sensor, with a data acquisition frequency of 1 time / minute.

9. The method for converting industrial waste heat into low-pressure steam to drive ammonia adsorption refrigeration according to claim 1, characterized in that: The ice-making system described in step S5.1 is designed with a cooling capacity of 24,000 kcal / h and an evaporation temperature of -18°C, which meets the needs of industrial ice making and ice supply for agricultural markets.

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