Energy management and control method and device for synthetic ammonia production system

Abstract

The invention provides an energy management and control method and device for a synthetic ammonia production system. In the process of producing the liquid ammonia product by using the synthetic ammonia production system, first steam generated by the synthetic ammonia module during heat release in the process of producing the liquid ammonia product is recovered through the waste heat recovery module according to a preset control rule; power is supplied to the hydrogen production module, the hydrogen storage module and the ammonia synthesis module through the turbine generator set module based on first steam expansion power generation according to a preset control rule, and first hydrogen is provided for the ammonia synthesis module through the hydrogen production module; in the process that the turbine generator set module carries out first steam expansion power generation, corresponding second steam is recycled through a turbine steam extraction opening according to a preset control rule and the hydrogen amount of the first hydrogen; a dehydrogenation reactor in the hydrogen storage module is used for releasing and providing second hydrogen required by operation of the ammonia synthesis module based on the second steam. Therefore, gradient utilization of heat of the system is guaranteed, and hydrogen supply dynamic balance and energy efficient cooperation are achieved.

Description

TECHNICAL FIELD

[0001] The present specification belongs to the field of energy chemical industry and comprehensive utilization of renewable energy, and particularly relates to an energy management and control method and device for a synthetic ammonia production system. BACKGROUND

[0002] Currently, conventional synthetic ammonia industry usually provides raw materials and energy through fossil fuels, and a large amount of carbon dioxide is discharged during the process, and then synthetic ammonia is produced through an ammonia synthesis process. With the progress of technology, adjustment of energy structure and increasing pressure of carbon emission reduction, the future synthetic ammonia path based on green hydrogen gradually becomes the development direction in this field.

[0003] In the prior art, for example, Patent No. CN202310675830 proposes to directly couple the alkaline electrolysis hydrogen production and the synthetic ammonia process, but this scheme fails to solve the problem that the low-grade heat (such as hot water below 80℃) generated during the electrolysis process is difficult to effectively utilize. Another Patent No. CN202311236716 proposes to recycle heat through a molten salt heat storage device, which improves the energy utilization rate to a certain extent, but the overall system has high investment, low thermal efficiency, and poor dynamic adaptability.

[0004] In addition, in terms of hydrogen storage, the methylcyclohexane hydrogen storage system disclosed in Patent No. CN202310678683 requires a medium-high temperature steam of 280℃ or above in the dehydrogenation process, while the low-pressure steam after turbine power generation in the traditional synthetic ammonia system cannot directly meet this requirement, resulting in the need for additional heating equipment, which increases energy consumption and system complexity.

[0005] In summary, the current green synthetic ammonia system generally has the problem of uncoordinated heat flow grade and spatial and temporal distribution between the hydrogen production, hydrogen storage and synthetic ammonia subsystems, which is superimposed with the volatility of renewable energy, resulting in dynamic instability of the system heat balance. At the same time, the steam cascade utilization efficiency is insufficient, which also causes a lot of waste heat and cooling water consumption, and the heat management and coupling strategy needs to be optimized to solve the problem.

[0006] At present, there is no effective solution to the above problems. SUMMARY

[0007] The present specification provides an energy management method and device for a synthetic ammonia production system. The heat released during the reaction process of the synthetic ammonia module is converted into first steam by a waste heat recovery module, and introduced into a turbine generator set module for expansion power generation to provide the required power for the hydrogen production module, hydrogen storage module, and synthetic ammonia module, ensuring the continuous operation of the hydrogen production and synthesis reactions. During the first steam expansion process, second steam is obtained by steam extraction, which is used to drive the dehydrogenation reactor in the hydrogen storage module to release the second hydrogen, achieving dynamic adjustment of hydrogen supply, thereby ensuring the heat cascade utilization of the system while achieving dynamic balance of hydrogen supply and efficient energy collaboration.

[0008] The present specification provides an energy management method for a synthetic ammonia production system. The synthetic ammonia production system includes at least a hydrogen production module, a hydrogen storage module, a synthetic ammonia module, a waste heat recovery module, and a turbine generator set module. One end of the hydrogen production module is connected to the hydrogen storage module, and the other end is connected to the synthetic ammonia module. The synthetic ammonia module is connected to the waste heat recovery module. The waste heat recovery module is connected to the turbine generator set module. The turbine generator set module is connected to the hydrogen storage module. The method includes:

[0009] During the production of liquid ammonia products using the synthetic ammonia production system, the first steam generated by the synthetic ammonia module during heat release in the production of liquid ammonia products is recovered by the waste heat recovery module according to a predetermined control rule.

[0010] The turbine generator set module is used to generate power based on the first steam expansion according to a predetermined control rule, to provide power for the hydrogen production module, the hydrogen storage module, and the synthetic ammonia module, and to provide the first hydrogen to the synthetic ammonia module through the hydrogen production module.

[0011] During the first steam expansion power generation process of the turbine generator set module, the corresponding second steam is recovered through the turbine steam extraction port according to a predetermined control rule and the hydrogen amount of the first hydrogen.

[0012] The dehydrogenation reactor in the hydrogen storage module releases and provides the second hydrogen required for the operation of the synthetic ammonia module based on the second steam.

[0013] In one embodiment, the synthetic ammonia production system further includes a molten salt energy storage module and a power supply module. The molten salt energy storage module is used to store the heat released during the production of liquid ammonia products by the synthetic ammonia module. The power supply module is used to provide green electricity or grid electricity for the synthetic ammonia production system, and to jointly bear the system power demand with the turbine generator set module.

[0014] In one embodiment, the preset control rule is a control rule for dynamically controlling the recovery amounts of the first steam and the second steam, which is constructed based on an electricity balance relationship, a steam balance relationship, and a hydrogen balance relationship.

[0015] In one embodiment, the method further comprises:

[0016] According to the preset control rule, a first constraint condition based on an electricity balance relationship, a second constraint condition based on a steam balance relationship, and a third constraint condition based on a hydrogen balance relationship are constructed.

[0017] According to the preset control rule, a target cost function is constructed.

[0018] According to the first constraint condition, the second constraint condition, and the third constraint condition, the matching recovery amounts of the first steam and the second steam are determined by optimizing and solving the target cost function.

[0019] In one embodiment, the method further comprises:

[0020] An operating characteristic parameter of the synthetic ammonia production system is obtained; wherein the operating characteristic parameter comprises at least one of the following: synthetic ammonia production, unit synthetic ammonia reaction theoretical heat release, and waste heat recovery efficiency coefficient.

[0021] According to the operating characteristic parameter, the recovery amount of the first steam is determined.

[0022] In one embodiment, the method further comprises:

[0023] An operating characteristic parameter of the synthetic ammonia production system is obtained; wherein the operating characteristic parameter comprises at least one of the following: hydrogen amount required by the synthetic ammonia module, hydrogen amount of the first hydrogen provided by the hydrogen production module.

[0024] According to the operating characteristic parameter, the steam extraction flow required by the turbine generator set is determined.

[0025] According to the steam extraction flow, the recovery amount of the second steam of the turbine generator set module is determined.

[0026] According to the recovery amount of the second steam, the hydrogen amount of the second hydrogen released by the dehydrogenation reactor in the hydrogen storage module is determined.

[0027] In one embodiment, the method further comprises:

[0028] An operating characteristic parameter of the synthetic ammonia production system is obtained; wherein the operating characteristic parameter comprises at least one of the following: power generation amount of the turbine generator set module, power consumption amount of the hydrogen production module, power consumption amount of the hydrogen storage module, and power consumption amount of the synthetic ammonia module.

[0029] According to the operation characteristic parameter, an external power supply required by the synthetic ammonia production system is determined.

[0030] The present specification provides an energy management device of a synthetic ammonia production system, applied to a synthetic ammonia production system, the synthetic ammonia production system at least comprising: a hydrogen production module, a hydrogen storage module, a synthetic ammonia module, a waste heat recovery module, a turbine generator set module; one end of the hydrogen production module is connected with the hydrogen storage module, and the other end is connected with the synthetic ammonia module; the synthetic ammonia module is connected with the waste heat recovery module; the waste heat recovery module is connected with the turbine generator set module; the turbine generator set module is connected with the hydrogen storage module; the device comprises:

[0031] A first steam determination module is configured to, in a process of producing liquid ammonia products by using the synthetic ammonia production system, recover, according to a preset control rule, first steam generated by the synthetic ammonia module in a heat release process of producing the liquid ammonia products through the waste heat recovery module;

[0032] A first hydrogen determination module is configured to, according to a preset control rule, use the turbine generator set module to generate power based on the first steam expansion, supply power to the hydrogen production module, the hydrogen storage module and the synthetic ammonia module, and provide first hydrogen to the synthetic ammonia module through the hydrogen production module;

[0033] A second steam determination module is configured to, in a process of the turbine generator set module generating power based on the first steam expansion, recover corresponding second steam through a turbine steam extraction port according to a preset control rule and a hydrogen amount of the first hydrogen;

[0034] A second hydrogen determination module is configured to use a dehydrogenation reactor in the hydrogen storage module to release and provide second hydrogen required for operation of the synthetic ammonia module based on the second steam.

[0035] The present specification also provides an electronic device comprising a processor and a memory for storing processor-executable instructions, the processor executing the instructions to implement an energy management method of a synthetic ammonia production system.

[0036] The present specification also provides a computer-readable storage medium having computer instructions stored thereon, the instructions being executed to implement an energy management method of a synthetic ammonia production system.

[0037] Based on the energy management method of the synthetic ammonia production system provided in the specification, applied to the synthetic ammonia production system, the synthetic ammonia production system at least comprises: a hydrogen production module, a hydrogen storage module, a synthetic ammonia module, a waste heat recovery module, a turbine generator set module; one end of the hydrogen production module is connected with the hydrogen storage module, the other end is connected with the synthetic ammonia module; the synthetic ammonia module is connected with the waste heat recovery module; the waste heat recovery module is connected with the turbine generator set module; the turbine generator set module is connected with the hydrogen storage module; the method comprises: in the process of producing liquid ammonia product by using the synthetic ammonia production system, according to the preset control rule, the first steam generated by the synthetic ammonia module in the process of producing liquid ammonia product is recovered through the waste heat recovery module; according to the preset control rule, the turbine generator set module is used to generate electricity based on the first steam expansion, to supply power to the hydrogen production module, the hydrogen storage module and the synthetic ammonia module, and to provide the first hydrogen to the synthetic ammonia module through the hydrogen production module; in the process of first steam expansion of the turbine generator set module, according to the preset control rule and the hydrogen amount of the first hydrogen, the corresponding second steam is recovered through the turbine steam extraction port; the second hydrogen required for the operation of the synthetic ammonia module is released and provided by using the dehydrogenation reactor in the hydrogen storage module based on the second steam. In this way, the heat released in the reaction process of the synthetic ammonia module is converted into first steam by the waste heat recovery module, and introduced into the turbine generator set module for expansion power generation, to provide the required power for the hydrogen production module and the synthetic ammonia module, to ensure the continuous operation of the hydrogen production and synthesis reaction; the second steam is obtained by steam extraction during the first steam expansion, and is used to drive the dehydrogenation reactor in the hydrogen storage module to release the second hydrogen, to realize the dynamic adjustment of hydrogen supply, so as to realize the dynamic balance of hydrogen supply and the efficient cooperation of energy while ensuring the heat cascade utilization of the system. BRIEF DESCRIPTION OF DRAWINGS

[0038] In order to more clearly illustrate the embodiments of the specification, the drawings required in the embodiments will be briefly introduced as follows. The drawings in the following description are only some embodiments described in the specification, and other drawings can be obtained by those skilled in the art without creative labor on the basis of these drawings.

[0039] Figure 1 is a flowchart of an energy management method of a synthetic ammonia production system provided by an embodiment of the specification;

[0040] Figure 2 is a schematic diagram of the structure of an electronic device provided by an embodiment of the specification;

[0041] Figure 3 is a schematic diagram of the structure of an energy management device of a synthetic ammonia production system provided by an embodiment of the specification;

[0042] Figure 4 is a whole flow schematic diagram of another energy management method of a synthetic ammonia production system provided by an embodiment of the present specification;

[0043] Figure 5 is a steam balance schematic diagram provided by an embodiment of the present specification. DETAILED DESCRIPTION

[0044] In order for those skilled in the art to better understand the technical solutions in the present specification, the technical solutions in the embodiments of the present specification will be clearly and completely described below in conjunction with the drawings in the embodiments of the present specification. Obviously, the described embodiments are only part of the embodiments of the present specification, not all. Based on the embodiments in the present specification, all other embodiments obtained by those skilled in the art without creative labor should be within the scope of protection of the present specification.

[0045] The current green synthetic ammonia system generally faces the problems of heat grade mismatch and low energy coupling efficiency, which are specifically manifested as follows: the low-temperature heat byproduct of water electrolysis for hydrogen production is difficult to effectively match the high-temperature heat release of the synthetic ammonia reaction, the low-pressure steam remaining in the traditional steam turbine system cannot meet the medium-high temperature heat load required by the organic liquid dehydrogenation, resulting in additional electric heating to supplement energy and aggravating energy consumption; at the same time, the heat flow mismatch in time and space among the hydrogen production, hydrogen storage and synthetic ammonia subsystems, combined with the fluctuation of renewable energy input, easily causes the system heat balance instability, steam cascade utilization rate decline and cooling resource waste, and it is urgent to build a multi-energy coupling and efficient collaborative heat management optimization mechanism to realize the stable and low-carbon operation of the green synthetic ammonia system.

[0046] In view of the root causes of the above problems, the present specification converts the heat released in the reaction process of the synthetic ammonia module into first steam through a waste heat recovery module, and introduces a turbine generator set module for expansion power generation to provide the required power for the hydrogen production module and the synthetic ammonia module, thereby ensuring the continuous operation of the hydrogen production and synthesis reaction; the second steam is obtained by steam extraction during the expansion of the first steam, and is used to drive the dehydrogenation reactor in the hydrogen storage module to release the second hydrogen, thereby realizing the dynamic adjustment of hydrogen supply, so as to realize the dynamic balance of hydrogen supply and the efficient collaboration of energy while ensuring the cascade utilization of system heat.

[0047] Referring to Figure 1As shown, the embodiment of the present specification provides an energy management method of a synthetic ammonia production system, wherein the method is specifically applied to the server side. In specific implementation, it is applied to a synthetic ammonia production system, which at least includes: a hydrogen production module, a hydrogen storage module, a synthetic ammonia module, a waste heat recovery module, a turbine generator set module; one end of the hydrogen production module is connected with the hydrogen storage module, and the other end is connected with the synthetic ammonia module; the synthetic ammonia module is connected with the waste heat recovery module; the waste heat recovery module is connected with the turbine generator set module; the turbine generator set module is connected with the hydrogen storage module; the method can include the following contents:

[0048] S101: In the process of producing liquid ammonia products by using the synthetic ammonia production system, according to the preset control rule, the first steam generated by the synthetic ammonia module in the process of heat release in producing liquid ammonia products is recovered through the waste heat recovery module;

[0049] S102: According to the preset control rule, the turbine generator set module is used to generate electricity based on the first steam expansion, to supply power to the hydrogen production module, the hydrogen storage module and the synthetic ammonia module, and to provide the first hydrogen to the synthetic ammonia module through the hydrogen production module;

[0050] S103: In the process of first steam expansion of the turbine generator set module, according to the preset control rule and the hydrogen amount of the first hydrogen, the corresponding second steam is recovered through the turbine extraction port;

[0051] S104: The second hydrogen required for the operation of the synthetic ammonia module is released and provided by using the dehydrogenation reactor in the hydrogen storage module based on the second steam.

[0052] The turbine generator set can be an extraction condensing turbine generator set, which has an extraction function and can extract part of the medium-pressure steam as the second steam through the extraction port arranged in the middle section of the turbine during the first steam expansion process, so as to provide a heat source for the dehydrogenation reaction under the premise of ensuring the efficiency of turbine power generation, and realize dynamic balance adjustment of heat and power supply.

[0053] The dehydrogenation reactor can be a dehydrogenation reaction device of heat-driven liquid organic hydrogen storage material, which is designed to release the stored hydrogen under a certain heat source input, and the heat source is provided by the second steam, which is used to release the hydrogen elements in the organic liquid into the second hydrogen available for the synthetic ammonia reaction through the catalytic dehydrogenation reaction, so as to realize the precise matching between the hydrogen storage-hydrogen release process and the demand for hydrogen for ammonia production.

[0054] In some embodiments, the synthetic ammonia production system further comprises a data monitoring module and a control module; wherein the data monitoring module comprises sensors, data storage, transmission and display devices of the synthetic ammonia production system for detecting, storing, transmitting and displaying production data such as temperature, pressure, flow rate, etc.; the control module comprises various valves and control methods related to software and hardware devices set in the synthetic ammonia production system, for automatically adjusting the opening degree of the valve according to the monitoring data and scheduling instructions to ensure stable transmission of materials.

[0055] Further, the synthetic ammonia production system further comprises an energy control module for dynamically coordinating the steam distribution strategy of the turbine generator set according to the type of hydrogen storage module and the real-time running state of the system, realizing the hierarchical utilization of waste heat resources and energy optimization scheduling, and realizing real-time monitoring and scheduling of system energy flow. When the hydrogen storage module is a gaseous hydrogen storage type, no steam is needed to provide dehydrogenation, and all the byproduct steam of synthetic ammonia enters the turbine generator set for expansion power generation to supply power for the hydrogen production module and the synthetic ammonia module; when the hydrogen storage module is a liquid or solid hydrogen storage type, its dehydrogenation process needs medium-pressure steam heating, and the energy control module calculates the steam extraction flow rate according to the hydrogen demand, dehydrogenation heat load and first steam production to control the turbine to extract steam at the medium-pressure section to meet the heating demand, and the remaining steam continues to be used for power generation. The turbine generator set can be a full-condensing turbine, an extraction-condensing turbine, an extraction-injection turbine or a back-pressure turbine, etc., and the energy control module determines the steam extraction strategy according to the turbine characteristics to realize dynamic balance of hydrogen storage heating and power generation.

[0056] In some embodiments, the first steam generated by the synthetic ammonia module during heat release in the production of liquid ammonia products is recovered by the waste heat recovery module according to a preset control rule, and in specific implementation, can include:

[0057] S1: monitoring the liquid ammonia production of the synthetic ammonia module, and when the liquid ammonia production reaches a preset threshold, obtaining the unit ammonia production heat release value and the waste heat recovery coefficient of the synthetic ammonia module;

[0058] S2: calculating the effective heat that can be converted into steam during the heat release process of the synthetic ammonia module according to the current liquid ammonia production, the unit ammonia production heat release value and the waste heat recovery coefficient; and based on the effective heat and the latent heat parameter of the first steam, calculating the production of the first steam;

[0059] S3: controlling the waste heat recovery module to heat the condensed water under the condition of the effective heat to generate the first steam with the corresponding production.

[0060] For example, in a certain production cycle, the daily ammonia production of the synthetic ammonia module is 50 tons, the unit ammonia production reaction heat release is 285 kJ / mol, and the system can obtain about 6 tons / hour of first steam through heat conversion according to the waste heat recovery efficiency of 60% and the water vaporization latent heat. The steam is introduced into the turbine generator set to expand and generate electricity, and at the same time provides a steam extraction heat source for the subsequent dehydrogenation of the hydrogen storage module.

[0061] In the above manner, the first steam is efficiently generated by using the exothermic reaction heat of the synthetic ammonia module, the energy recovery and reuse of the reaction heat are realized, the overall energy efficiency of the system is improved, the dependence on external heating devices is reduced, and the stable operation of the hydrogen storage module and the power generation module is ensured, thereby effectively promoting the energy self-balancing and low-carbon operation of the synthetic ammonia production process.

[0062] In some embodiments, the turbine generator set module is used to generate electricity based on the expansion of the first steam according to the preset control rule, to supply power to the hydrogen production module, the hydrogen storage module and the synthetic ammonia module, and to provide the first hydrogen to the synthetic ammonia module through the hydrogen production module. In specific implementation, it can include:

[0063] S1: determining the steam power available for turbine expansion power generation according to the real-time parameters of the first steam generated by the waste heat recovery module, including pressure, temperature and flow;

[0064] S2: controlling the turbine generator set module to introduce the first steam into the turbine for isentropic expansion to drive the generator to output electric energy;

[0065] S3: monitoring the real-time power demand of the hydrogen production module, the hydrogen storage module and the synthetic ammonia module;

[0066] S4: under the condition that the power generation capacity of the turbine generator set module meets the total power demand of the hydrogen production module, the hydrogen storage module and the synthetic ammonia module, supplying power to the hydrogen production module to realize water electrolysis reaction to generate the first hydrogen, and controlling the hydrogen storage module to supply the first hydrogen to the synthetic ammonia module as needed.

[0067] Based on the above embodiments, the turbine generator set module is controlled to generate electricity based on the expansion of the first steam, and the load demand of the hydrogen production module and the synthetic ammonia module is preferentially met, thereby realizing efficient conversion and cascade utilization of heat energy to electric energy.

[0068] In some embodiments, during the process of the turbine generator set module generating electricity by expanding the first steam, the corresponding second steam is recovered through the turbine extraction port according to the preset control rule and the hydrogen amount of the first hydrogen. In specific implementation, it can include:

[0069] S1: obtaining a target hydrogen amount required by a current synthetic ammonia module, and a hydrogen amount of the first hydrogen provided by the hydrogen production module, and calculating a hydrogen amount of the second hydrogen required by the hydrogen storage module to be supplemented; S2: calculating a heat load required by the dehydrogenation reactor according to the hydrogen amount of the second hydrogen and a unit heat load of the dehydrogenation reactor in the hydrogen storage module; S3: determining a steam flow required for steam extraction according to the heat load and a unit enthalpy value of the first steam; S4: controlling the steam extraction valve of the turbine generator set module to perform steam extraction operation at a corresponding expansion stage, and extracting a corresponding flow of the second steam for providing the dehydrogenation reactor for heating reaction.

[0070] In this way, by extracting part of the steam of the intermediate stage as the second steam in the turbine expansion power generation process, not only the heat load demand of the dehydrogenation reactor is met, and the heat energy supply for the organic liquid hydrogen storage module is realized, but also the influence on the heat energy utilization of the final condensing stage is avoided, the hierarchical utilization of waste heat resources is effectively realized, and the system thermal-electric-hydrogen coupling efficiency and the continuity of hydrogen supply are improved.

[0071] Based on the above embodiment, the heat released in the reaction process of the synthetic ammonia module is converted into the first steam by the waste heat recovery module, and introduced into the turbine generator set module for expansion power generation, to provide the required power for the hydrogen production module and the synthetic ammonia module, and to ensure the continuous operation of the hydrogen production and synthesis reactions; the second steam is obtained by steam extraction during the expansion of the first steam, and is used to drive the dehydrogenation reactor in the hydrogen storage module to release the second hydrogen, to realize dynamic adjustment of hydrogen supply, so as to ensure the hierarchical utilization of system heat, and realize dynamic balance of hydrogen supply and efficient energy cooperation.

[0072] In some embodiments, the synthetic ammonia production system further comprises a molten salt energy storage module and a power supply module, the molten salt energy storage module is used to store the heat released in the production of liquid ammonia products by the synthetic ammonia module, and the power supply module is used to provide green electricity or grid electricity for the synthetic ammonia production system, and to jointly bear the system electricity demand with the turbine generator set module.

[0073] Among them, the above-mentioned synthetic ammonia production system has the characteristics of fluctuating production, which is that the output of renewable energy power generation fluctuates with environmental conditions, and then leads to dynamic changes in the amount of hydrogen produced by water electrolysis, the hydrogen storage and release rate of the hydrogen storage module, and the synthetic ammonia load.

[0074] In specific implementation, the following can be included: during operation of the ammonia synthesis module, the heat release load generated by the ammonia synthesis reaction is monitored; when the heat recovered by the waste heat recovery module exceeds the current first steam demand, the waste heat recovery module is controlled to direct part of the high-temperature heat carrier into the molten salt energy storage module; the molten salt energy storage module includes a high-temperature molten salt medium and a heat exchange unit, the high-temperature heat carrier exchanges heat with the molten salt medium and is heated, achieving heat storage; in a subsequent system heat demand scenario, the molten salt energy storage module is controlled to release the stored heat, providing a supplemental steam source for the turbine generator set module or providing heat for the dehydrogenation reactor of the hydrogen storage module.

[0075] By introducing the molten salt energy storage module into the system, high-temperature heat is stored when the ammonia synthesis reaction releases excess heat, and the stored heat is released in an orderly manner when the system heat demand increases or power generation is insufficient, improving the system thermal energy regulation capability and time shift utilization efficiency, achieving dynamic matching between heat supply and ammonia production load, and effectively avoiding waste of excess heat.

[0076] In some embodiments, the preset control rule is a control rule for dynamically controlling the recovery amounts of the first steam and the second steam, which is constructed based on power balance relationship, steam balance relationship, and hydrogen balance relationship.

[0077] By constructing the control rule based on the three balance relationships of power, steam, and hydrogen, the first steam and the second steam are linked and regulated, so that the system can stably output the hydrogen, power, and heat required for ammonia synthesis under different load changes, improving the waste heat utilization efficiency and the overall operation efficiency of the system, and avoiding the problem of unstable operation caused by local excess heat or hydrogen shortage.

[0078] In some embodiments, the method, in specific implementation, can further include the following:

[0079] S1: according to the preset control rule, constructing a first constraint condition based on power balance relationship, a second constraint condition based on steam balance relationship, and a third constraint condition based on hydrogen balance relationship;

[0080] S2: according to the preset control rule, constructing a target cost function;

[0081] S3: according to the first constraint condition, the second constraint condition, and the third constraint condition, determining the recovery amounts of the first steam and the second steam by optimizing and solving the target cost function.

[0082] The first constraint condition can include power supply of the first steam expansion power generation, electricity consumption of the hydrogen production module, and electricity consumption of the synthetic ammonia module. The second constraint condition can include the first steam, the second steam, and liquid ammonia production of the synthetic ammonia module. The third constraint condition can include the hydrogen amount of the first hydrogen, the hydrogen amount of the second hydrogen, and the hydrogen amount required by the synthetic ammonia module.

[0083] Specifically, a first constraint condition based on the power supply of the first steam expansion power generation, the electricity consumption of the hydrogen production module, and the electricity consumption of the synthetic ammonia module is constructed. A second constraint condition based on the first steam, the second steam, and the liquid ammonia production of the synthetic ammonia module is constructed. A third constraint condition based on the hydrogen amount of the first hydrogen, the hydrogen amount of the second hydrogen, and the hydrogen amount required by the synthetic ammonia module is constructed. A target cost function is constructed based on the first constraint condition, the second constraint condition, and the third constraint condition. The first steam recovery amount and the second steam recovery amount that match the constraint conditions are determined by optimizing and solving the target cost function.

[0084] For example, during the operation of a certain synthetic ammonia device, it is monitored that the current synthetic ammonia production is 10 tons / hour, the total required hydrogen amount is 20000 The electrolytic water hydrogen production module provides the first hydrogen of 15000 The remaining hydrogen is supplemented by the dehydrogenation reactor. At the same time, the three constraint conditions are constructed according to the liquid ammonia production, the dehydrogenation reactor heat load, the available capacity of the first steam, and the power consumption data. The target cost function is optimized and solved to determine that the first steam recovery amount is 30 t / h and the second steam recovery amount is 12 t / h.

[0085] Based on the above embodiment, by constructing the multi-dimensional constraint relationship of power balance, steam balance, and hydrogen balance, and optimizing and solving the target cost function, the accurate matching and distribution of the first steam and the second steam can be realized, so that the heat, electricity, and hydrogen resources in the system operation are dynamically coordinated and comprehensively utilized, thereby improving the overall energy efficiency and reducing the operation cost.

[0086] In some embodiments, the energy management method of the synthetic ammonia production system further includes realizing dynamic production scheduling optimization of the whole system by constructing a multi-energy flow coupling mathematical model. Specifically, the energy management module first establishes the following constraint conditions based on the system operation state parameters:

[0087] The first constraint condition is used to represent the power balance relationship between the power supply of the turbine generator set based on the first steam expansion power generation and the total electricity demand of the hydrogen production module, the hydrogen storage module, and the synthetic ammonia module.

[0088] A second constraint condition is used to represent a steam supply-demand balance relationship among the first steam production, the second steam extraction amount, and the liquid ammonia production of the ammonia synthesis module.

[0089] A third constraint condition is used to represent a hydrogen balance relationship among the first hydrogen, the second hydrogen, and the hydrogen required by the ammonia synthesis module.

[0090] On the basis of the constraint conditions, a production scheduling optimization function with the optimal system economy as the target is constructed, and a multi-energy flow coupling mathematical model is established. Through an optimization solving algorithm, the optimal inflow, outflow, and accumulation of power, hydrogen, and steam of each module in the target period are obtained, and dynamic adjustment of system operation parameters is realized to ensure that the whole system realizes maximum energy efficiency and minimum production cost under fluctuating energy input conditions.

[0091] In some embodiments, the method, when implemented, can further include the following:

[0092] S1: Obtain the operation characteristic parameters of the ammonia synthesis production system; wherein the operation characteristic parameters include at least one of the following: ammonia production, unit ammonia reaction theoretical heat release, and waste heat recovery efficiency coefficient;

[0093] S2: Determine the recovery amount of the first steam according to the operation characteristic parameters.

[0094] In some embodiments, the adjusting of the recovery amount of the second steam according to the operation characteristic parameters, when implemented, can include:

[0095] S1: Calculate the effective heat available for steam conversion according to the operation characteristic parameters;

[0096] S2: Determine the production of the first steam according to the effective heat;

[0097] S3: Determine the extraction flow of the turbine generator set according to the production of the first steam and the heat supply load of the dehydrogenation reactor in the hydrogen storage module;

[0098] S4: Determine the recovery amount of the second steam of the turbine generator set module according to the extraction flow.

[0099] Based on the above embodiments, by dynamically adjusting the recovery amount of the second steam based on the operation characteristic parameters, the system can flexibly adapt to the heat load demand under different working conditions, enhance the adjustability of the heat source of the dehydrogenation reactor, and improve the stability of the supply of synthetic hydrogen. At the same time, it avoids waste of heat energy and realizes reasonable allocation of steam energy.

[0100] In some embodiments, the method, when implemented, can further include the following:

[0101] S1: Obtain an operation characteristic parameter of the synthetic ammonia production system; wherein the operation characteristic parameter comprises at least one of the following: a hydrogen amount required by the synthetic ammonia module, a hydrogen amount of the first hydrogen provided by the hydrogen production module;

[0102] S2: Determine a steam extraction flow rate required by the turbine generator set according to the operation characteristic parameter;

[0103] S3: Determine a recovery amount of the second steam of the turbine generator set module according to the steam extraction flow rate;

[0104] S4: Determine a hydrogen amount of the second hydrogen released by a dehydrogenation reactor in the hydrogen storage module according to the recovery amount of the second steam.

[0105] Specifically, the operation characteristic parameter of the synthetic ammonia production system is obtained, wherein the operation characteristic parameter comprises the hydrogen amount required by the synthetic ammonia module and the hydrogen amount of the first hydrogen provided by the hydrogen production module; in the case that the hydrogen amount required by the synthetic ammonia module is greater than the hydrogen amount of the first hydrogen, the steam extraction flow rate required by the turbine generator set is determined according to the operation characteristic parameter; the recovery amount of the second steam of the turbine generator set module is determined according to the steam extraction flow rate; and the hydrogen amount of the second hydrogen released by the dehydrogenation reactor in the hydrogen storage module is determined according to the recovery amount of the second steam.

[0106] For example, in a certain operation period, if it is monitored that the hydrogen amount required by the synthetic ammonia module is 1800 , and the hydrogen amount of the first hydrogen provided by the current hydrogen production module is only 1400 , then the difference is 400 . The system calculates the required heat load as 1.2 GJ / h based on a preset dehydrogenation reaction heat load coefficient and a unit steam enthalpy value, and then determines that the turbine needs to extract 1.5 tons / h of medium-pressure steam as the second steam. The control system adjusts the turbine steam extraction ratio accordingly, and controls the dehydrogenation reactor to release 400 of the second hydrogen.

[0107] Based on the above embodiment, by dynamically calculating the steam extraction flow rate based on the hydrogen demand, and regulating the steam extraction behavior of the turbine generator set, the dehydrogenation reactor is ensured to stably operate under the condition of heat energy matching, and the response ability and overall coordination of the hydrogen supply chain are improved.

[0108] In some embodiments, the method can further include the following when implemented:

[0109] S1: Obtain an operation characteristic parameter of the synthetic ammonia production system; wherein the operation characteristic parameter comprises at least one of the following: a power generation amount of the turbine generator set module, an electricity consumption amount of the hydrogen production module, an electricity consumption amount of the hydrogen storage module, and an electricity consumption amount of the synthetic ammonia module;

[0110] S2: determining an external power supply required by the synthetic ammonia production system according to the operation characteristic parameter.

[0111] The external power supply can include a wind power generation system, a photovoltaic power generation system, a regional power grid power supply device, and other energy sources. The power supply object can cover electrolytic water hydrogen production equipment in the hydrogen production module, dehydrogenation heating devices in the hydrogen storage module, ammonia compressors, ammonia condenser circulating fans, cold ammonia pumps, liquid ammonia storage and transportation equipment, and PLC units and sensor power supply circuits of the control system. By introducing a multi-source external power supply mechanism, the operation stability and energy scheduling flexibility of the system can be improved, ensuring the continuous and stable operation of each key device in the case of insufficient steam capacity or fluctuating power generation capacity, and achieving dynamic response to power supply and demand balance and multi-source coupling optimization.

[0112] As can be seen from the above, the energy management method of the synthetic ammonia production system provided by the embodiments of the present specification is applied to a synthetic ammonia production system, which at least includes a hydrogen production module, a hydrogen storage module, a synthetic ammonia module, a waste heat recovery module, and a turbine generator set module. One end of the hydrogen production module is connected to the hydrogen storage module, and the other end is connected to the synthetic ammonia module. The synthetic ammonia module is connected to the waste heat recovery module. The waste heat recovery module is connected to the turbine generator set module. The turbine generator set module is connected to the hydrogen storage module. The method includes: during the production of liquid ammonia products by the synthetic ammonia production system, recovering first steam generated by the synthetic ammonia module during heat release in the production of liquid ammonia products through the waste heat recovery module according to a predetermined control rule; using the turbine generator set module to generate power based on the first steam expansion to supply power to the hydrogen production module, the hydrogen storage module, and the synthetic ammonia module, and providing first hydrogen to the synthetic ammonia module through the hydrogen production module according to the predetermined control rule; during the first steam expansion power generation of the turbine generator set module, recovering corresponding second steam through a turbine steam extraction port according to the hydrogen amount of the first hydrogen and the predetermined control rule; and using a dehydrogenation reactor in the hydrogen storage module to release and provide second hydrogen required for the operation of the synthetic ammonia module based on the second steam. In this way, the heat released during the reaction process of the synthetic ammonia module is converted into first steam by the waste heat recovery module, and introduced into the turbine generator set module for expansion power generation to provide the required power for the hydrogen production module and the synthetic ammonia module, ensuring the continuous operation of the hydrogen production and synthesis reaction. The second steam is obtained by steam extraction during the first steam expansion, and is used to drive the dehydrogenation reactor in the hydrogen storage module to release the second hydrogen, achieving dynamic adjustment of hydrogen supply, thereby ensuring the heat cascade utilization of the system while achieving dynamic balance of hydrogen supply and efficient energy collaboration.

[0113] Referring to Figure 2As shown, the embodiment of the present specification further provides a specific electronic device, wherein the electronic device comprises a network communication port 201, a processor 202 and a memory 203, and the above structures are connected through internal cables so that each structure can perform specific data interaction.

[0114] The network communication port 201 can be specifically used for recovering, according to a preset control rule, first steam generated when the synthesis ammonia module releases heat in the process of producing liquid ammonia products, through the waste heat recovery module, in the process of producing liquid ammonia products by using the synthetic ammonia production system.

[0115] The processor 202 can be specifically used for supplying power, according to a preset control rule, to the hydrogen production module, the hydrogen storage module and the synthesis ammonia module by using the turbogenerator module based on first steam expansion power generation, and providing first hydrogen to the synthesis ammonia module through the hydrogen production module; in the process of first steam expansion power generation by the turbogenerator module, recovering corresponding second steam through a turbine steam extraction port according to a preset control rule and a hydrogen amount of the first hydrogen; and releasing and providing, by using a dehydrogenation reactor in the hydrogen storage module, second hydrogen required for operation of the synthesis ammonia module based on the second steam.

[0116] The memory 203 can be specifically used for storing a corresponding instruction program.

[0117] Based on the above method, the related structure performance of the electronic device can be effectively utilized, the data processing speed of the electronic device can be improved, and an energy management and control method of a synthetic ammonia production system can be efficiently realized.

[0118] In the embodiment, the network communication port 201 can be a virtual port that can send or receive different data by being bound with different communication protocols. For example, the network communication port can be a port responsible for web data communication, can be a port responsible for FTP data communication, and can be a port responsible for mail data communication. In addition, the network communication port can also be an entity communication interface or a communication chip. For example, it can be a wireless mobile network communication chip such as GSM, CDMA, etc.; it can also be a Wifi chip; and it can also be a Bluetooth chip.

[0119] In the present embodiment, the processor 202 can be implemented in any suitable manner. For example, the processor can take the form of a microprocessor or processor and computer readable medium storing computer readable program code (e.g. software or firmware) executable by the (micro)processor, logic gates, switches, an application specific integrated circuit (ASIC), a programmable logic controller and embedded microcontroller, etc. The present description is not limited in this regard.

[0120] In the present embodiment, the memory 203 can comprise a hierarchy, in a digital system, anything that can hold binary data is a storage medium; in an integrated circuit, a circuit that has the function of storing data without physical form is also called a memory, such as RAM, FIFO, etc.; in a system, a storage device with physical form is also called a memory, such as a memory stick, a TF card, etc.

[0121] The embodiment of the present description also provides a computer readable storage medium based on the energy management method of the synthetic ammonia production system. The computer readable storage medium is applied to a synthetic ammonia production system, and the synthetic ammonia production system at least comprises a hydrogen production module, a hydrogen storage module, a synthetic ammonia module, a waste heat recovery module, and a turbine generator set module. One end of the hydrogen production module is connected with the hydrogen storage module, and the other end is connected with the synthetic ammonia module. The synthetic ammonia module is connected with the waste heat recovery module. The waste heat recovery module is connected with the turbine generator set module. The turbine generator set module is connected with the hydrogen storage module. The method comprises the following steps: in the process of producing liquid ammonia products by using the synthetic ammonia production system, according to a preset control rule, the waste heat recovery module recovers first steam generated by the synthetic ammonia module when the synthetic ammonia module produces liquid ammonia products; according to a preset control rule, the turbine generator set module is used to generate electricity based on the first steam expansion, to supply power to the hydrogen production module, the hydrogen storage module and the synthetic ammonia module, and to provide first hydrogen to the synthetic ammonia module through the hydrogen production module; in the process of the turbine generator set module generating electricity based on the first steam expansion, according to a preset control rule and the hydrogen amount of the first hydrogen, the turbine extraction port recovers corresponding second steam; the dehydrogenation reactor in the hydrogen storage module is used to release and provide second hydrogen required for the operation of the synthetic ammonia module based on the second steam.

[0122] In the embodiment, the storage medium includes, but is not limited to, a random access memory (RAM), a read-only memory (ROM), a cache, a hard disk drive (HDD), or a memory card. The storage medium can be used to store computer program instructions. The network communication unit can be an interface configured according to a standard of a communication protocol, and used for network connection communication.

[0123] In the embodiment, the program instructions stored in the computer-readable storage medium specifically implement functions and effects, which can be explained by comparing with other embodiments, and will not be described here.

[0124] Referring to Figure 3 At the software level, the embodiment of the present specification also provides an energy management device of a synthetic ammonia production system, applied to the synthetic ammonia production system, wherein the synthetic ammonia production system at least includes a hydrogen production module, a hydrogen storage module, a synthetic ammonia module, a waste heat recovery module, and a turbine generator set module; one end of the hydrogen production module is connected with the hydrogen storage module, and the other end is connected with the synthetic ammonia module; the synthetic ammonia module is connected with the waste heat recovery module; the waste heat recovery module is connected with the turbine generator set module; and the turbine generator set module is connected with the hydrogen storage module; and the device specifically can include the following structure modules:

[0125] A first steam determination module 301 is configured to, in a process of producing liquid ammonia products by using the synthetic ammonia production system, recover, according to a preset control rule, first steam generated by the synthetic ammonia module in the process of producing the liquid ammonia products and releasing heat through the waste heat recovery module;

[0126] A first hydrogen determination module 302 is configured to, according to a preset control rule, use the turbine generator set module to generate electricity based on the first steam expansion, supply power to the hydrogen production module, the hydrogen storage module, and the synthetic ammonia module, and provide first hydrogen to the synthetic ammonia module through the hydrogen production module;

[0127] A second steam determination module 303 is configured to, in the process of the turbine generator set module generating electricity based on the first steam expansion, recover corresponding second steam through a turbine steam extraction port according to a preset control rule and a hydrogen amount of the first hydrogen;

[0128] A second hydrogen determination module 304 is configured to use a dehydrogenation reactor in the hydrogen storage module to release and provide second hydrogen required for operation of the synthetic ammonia module based on the second steam.

[0129] In some embodiments, when the device is implemented, the synthetic ammonia production system further comprises a molten salt energy storage module and a power supply module, the molten salt energy storage module is used to store the heat released during the production of liquid ammonia product by the synthetic ammonia module, and the power supply module is used to provide green electricity or grid electricity for the synthetic ammonia production system, and the turbine generator set module jointly undertakes the system power demand. In some embodiments, when the device is implemented, the preset control rule is a control rule for dynamically controlling the recovery amount of the first steam and the second steam, which is constructed based on the power balance relationship, the steam balance relationship and the hydrogen balance relationship.

[0130] In some embodiments, when the device is implemented, it further comprises: according to the preset control rule, constructing a first constraint condition based on the power balance relationship, a second constraint condition based on the steam balance relationship, and a third constraint condition based on the hydrogen balance relationship; according to the preset control rule, constructing a target cost function; according to the first constraint condition, the second constraint condition and the third constraint condition, determining the matching recovery amount of the first steam and the recovery amount of the second steam by optimizing the target cost function.

[0131] In some embodiments, when the device is implemented, it further comprises: obtaining the operating characteristic parameters of the synthetic ammonia production system; wherein the operating characteristic parameters include at least one of the following: synthetic ammonia production, unit synthetic ammonia reaction theoretical heat release and waste heat recovery efficiency coefficient; according to the operating characteristic parameters, determining the recovery amount of the first steam.

[0132] In some embodiments, when the device is implemented, it further comprises: obtaining the operating characteristic parameters of the synthetic ammonia production system; wherein the operating characteristic parameters include at least one of the following: the amount of hydrogen required by the synthetic ammonia module, the amount of hydrogen provided by the hydrogen production module; according to the operating characteristic parameters, determining the steam extraction flow required by the turbine generator set; according to the steam extraction flow, determining the recovery amount of the second steam of the turbine generator set module; according to the recovery amount of the second steam, determining the hydrogen amount of the second hydrogen released by the dehydrogenation reactor in the hydrogen storage module.

[0133] In some embodiments, when the device is implemented, it further comprises: obtaining the operating characteristic parameters of the synthetic ammonia production system; wherein the operating characteristic parameters include at least one of the following: the power generation of the turbine generator set module, the power consumption of the hydrogen production module, the power consumption of the hydrogen storage module and the power consumption of the synthetic ammonia module; according to the operating characteristic parameters, determining the external power supply required by the synthetic ammonia production system.

[0134] It should be noted that the units, devices or modules and the like illustrated in the above embodiments can be implemented by computer chips or entities, or by products with certain functions. For the convenience of description, the above devices are described as various modules with functions. Of course, in the implementation of the present specification, the functions of each module can be implemented in the same software and / or hardware, or the modules implementing the same function can be implemented by a combination of sub-modules or sub-units. The above described device embodiments are only illustrative, for example, the division of the units is only a logical function division, and in actual implementation, there can be another division method, for example, the units or components can be combined or integrated into another system, or some features can be ignored or not executed. Another point is that the coupling or direct coupling or communication connection between the units or devices shown or discussed can be indirect coupling or communication connection through some interfaces, devices or units, which can be electrical, mechanical or other forms.

[0135] As can be seen from the above, based on the energy management device of the synthetic ammonia production system provided in the embodiments of the present specification, the heat released in the reaction process of the synthetic ammonia module is converted into first steam by the waste heat recovery module, and introduced into the turbine generator set module for expansion power generation to provide the required power for the hydrogen production module and the synthetic ammonia module, ensuring the continuous operation of the hydrogen production and synthesis reaction; in the first steam expansion process, the second steam is obtained by steam extraction, and is used to drive the dehydrogenation reactor in the hydrogen storage module to release the second hydrogen, realizing dynamic adjustment of hydrogen supply, so as to realize dynamic balance of hydrogen supply and efficient synergy of energy while ensuring the heat cascade utilization of the system.

[0136] In one specific scenario example, the energy management method and device of the synthetic ammonia production system provided in the present specification can be applied, the heat released in the reaction process of the synthetic ammonia module is converted into first steam by the waste heat recovery module, and introduced into the turbine generator set module for expansion power generation to provide the required power for the hydrogen production module, the hydrogen storage module and the synthetic ammonia module, ensuring the continuous operation of the hydrogen production and synthesis reaction; in the first steam expansion process, the second steam is obtained by steam extraction, and is used to drive the dehydrogenation reactor in the hydrogen storage module to release the second hydrogen, realizing dynamic adjustment of hydrogen supply, so as to realize dynamic balance of hydrogen supply and efficient synergy of energy while ensuring the heat cascade utilization of the system. The specific implementation process can include the following contents.

[0137] The green ammonia synthesis system mainly comprises three core subsystems, namely, a hydrogen production module, a hydrogen storage module, and an ammonia synthesis module. Each subsystem comprises specific device components and cooperatively operates in the overall process. The hydrogen production module adopts an electrolytic cell as a core device, and water is electrolyzed into hydrogen and oxygen by driving with electric energy. When the electrolytic cell is working, water molecules react on the electrode surface under the driving of a direct current power supply, oxygen is generated at the anode, and hydrogen is generated at the cathode. The conversion efficiency of the electrolytic cell directly determines the hydrogen production rate and quality, and a high-efficiency electrolytic cell can stably produce high-purity hydrogen under low energy consumption. To ensure stable operation of the electrolysis working condition, the hydrogen production module further comprises a power supply subsystem, a cooling subsystem, and a gas separation unit, which are respectively used for power supply, temperature control, and hydrogen and oxygen separation and purification operations to ensure that the hydrogen quality meets the subsequent reaction requirements.

[0138] The hydrogen storage module is configured with a hydrogenation reactor and a dehydrogenation reactor. The hydrogenation reactor is used for hydrogenation reaction of hydrogen output by the hydrogen production module and an organic liquid, so that hydrogen is stored in the organic liquid in the form of a chemical bond, which is usually carried out at a set temperature, pressure, and catalyst participation. The dehydrogenation reactor releases the second hydrogen used in the ammonia synthesis module by heating the hydrogenated organic liquid to release hydrogen when hydrogen is needed. The dehydrogenation temperature is usually between 100-300°C. The setting of this module significantly improves the hydrogen storage and transportation flexibility and the hydrogen regulation and control ability of the whole system.

[0139] The ammonia synthesis module is the core of the system, which mainly realizes the catalytic synthesis reaction of hydrogen and nitrogen to generate liquid ammonia products. The compressor, the synthesis reactor, and the waste heat recovery device are arranged inside. The compressor is used to pressurize the raw gas to meet the process requirements, improve the reaction rate and yield. In the reactor, hydrogen and nitrogen generate ammonia gas under the action of high temperature, high pressure and catalyst. The waste heat recovery device is used to recover the high-quality heat energy released by the synthesis reaction and generate high-pressure steam, and the steam pressure range can reach 10-120 bar. In addition to being used for turbine power generation, the recovered first steam can also be extracted according to the control rules to generate the second steam for the dehydrogenation reactor in the hydrogen storage module, thereby realizing the cascade utilization and closed-loop recovery of heat energy.

[0140] The system further comprises a turbine generator set mainly composed of a steam turbine and a generator, which can be selected from an extraction condensing turbine, a back pressure turbine or a full condensing turbine, and is flexibly configured according to the system load demand. The module receives the first steam output by the waste heat recovery module, drives the turbine to rotate and drives the generator to generate electricity. For extraction or back pressure turbine, a part of steam can be extracted as second steam in a certain pressure difference range, which is directly delivered to the dehydrogenation reactor as a heat source, avoiding inefficient electric heating and improving the energy utilization rate of the system.

[0141] The hydrogen flow path is as follows: after hydrogen production in the electrolyzer, the hydrogen is purified by the gas separation module and sent to the hydrogenation reactor to react with the organic liquid to form a hydrogen storage organic liquid. When needed, the liquid is sent to the dehydrogenation reactor to release hydrogen for use in the ammonia synthesis module. The steam flow path is as follows: the heat generated by the reactor is recovered by the waste heat recovery module to generate first steam, which drives the turbine generator set to generate electricity. Part of the steam forms second steam at the extraction port to heat the dehydrogenation reactor, and the rest continues to expand to generate electricity and is condensed into water to form a closed loop water-steam cycle.

[0142] Electric energy is provided in the system by the generator set to supply part of the load power, and the rest of the power can be supplemented by external renewable energy systems (such as wind turbines, photovoltaic modules, energy storage devices) to ensure stable operation of the system under fluctuating energy. In addition, the system is equipped with various valves, sensors and control systems to monitor and adjust the operating parameters such as gas flow rate, pressure, temperature in real time, and realize closed-loop optimal control of operating parameters.

[0143] Through the above-mentioned cooperation between modules, the system not only realizes the integrated operation of electrolytic hydrogen production, chemical hydrogen storage and green ammonia synthesis process, but also optimizes the temporal and spatial coupling relationship of heat, electricity and hydrogen three energy carriers, effectively improving the energy efficiency and the economy, flexibility and green attributes of the system operation.

[0144] In addition, various valves, sensors and control systems are provided in the system to adjust parameters such as flow rate, pressure and temperature of substances, ensuring accurate control of the connection between devices and the flow of substances according to the actual needs of the system. For example, flow regulating valves are installed on the hydrogen and steam transmission pipelines, and sensors are used to monitor the flow rate and pressure in real time. The control system automatically adjusts the opening of the valve according to the monitoring data to ensure stable transmission of substances.

[0145] The time-varying load characteristics of the flexible ammonia synthesis system are one of its distinctive features, which are mainly caused by the coupling mechanism of multi-source input and dynamic load, and are particularly prominent in the operation of the power generation link, hydrogen production module and ammonia synthesis module.

[0146] From the perspective of power supply path, the fluctuation mainly comes from the instability of renewable energy supply, such as wind energy, photovoltaic energy and other energy forms, whose output power is greatly affected by the spatial and temporal distribution of natural resources. Photovoltaic power generation system depends on the intensity and duration of irradiation, and has high output capacity during the period of sufficient sunlight, while its output capacity significantly decreases or even becomes zero during the period of low irradiation such as night or cloudy days. Wind energy system also shows similar characteristics, and its output power has strong non-stationarity due to the limitation of wind speed and its fluctuation. The power fluctuation of such energy supply end directly affects the stable operation of the downstream hydrogen production module and ammonia synthesis module, affecting the system's ability to operate stably.

[0147] The hydrogen production module relies on electricity to drive the electrolysis unit to generate hydrogen, so power fluctuations can cause power adjustment at the hydrogen production end. When the power supply is sufficient, the electrolytic cell can run at full capacity, achieving high hydrogen production efficiency; otherwise, in the state of low power supply, the power output of the electrolytic cell decreases, and the hydrogen production rate also decreases. In addition, the performance of the electrolysis unit itself may degrade due to factors such as operating time, thermal management, or system failure, further causing fluctuations in hydrogen supply capacity.

[0148] The operating load of the ammonia synthesis module is also subject to fluctuation risks. The module needs to maintain a stable reaction environment within a certain temperature, pressure, and hydrogen-nitrogen ratio parameter range, and any supply disturbance at the hydrogen or nitrogen raw material end can cause fluctuations in ammonia production load. On the one hand, as mentioned above, fluctuations in the output of the hydrogen production module can cause discontinuity in the hydrogen supply end; on the other hand, the running deviation of the air separation subsystem (if provided) or the raw gas ratio control equipment can also affect the stability of the nitrogen supply. In addition, the demand for liquid ammonia products in downstream industries (such as agriculture, fertilizer, chemical industry, etc.) fluctuates periodically, and changes in market demand will also force capacity adjustment, thereby causing fluctuations in the load of the ammonia synthesis module.

[0149] The above-mentioned dynamic fluctuations coupled with multiple factors pose significant challenges to the comprehensive scheduling and energy-quality balance of green ammonia synthesis systems. The system needs to maintain energy closure, material closure, and power matching under the conditions of power fluctuations, steam flow fluctuations, and dynamic changes in hydrogen supply. For example, in the case of a sudden drop in power generation, which leads to a decrease in the ability of water electrolysis to produce hydrogen, the hydrogen supply strategy of the hydrogen storage module needs to be coordinated in real time, and the operating parameters of the ammonia synthesis module need to be adjusted in conjunction to ensure that the target hydrogen flow does not be interrupted. At the same time, the system also needs to have a fast response capability to complete the dynamic reconstruction of the heat and power coupling path within a short time scale, ensuring the continuity of product quality and the economy and safety of system operation.

[0150] In some embodiments, hydrogen balance is a key component of material balance in green ammonia synthesis systems, involving the dynamic relationship between hydrogen production, storage, and consumption. In this system, the main source of hydrogen is water electrolysis, which decomposes water into hydrogen and oxygen through an electrolytic cell. The main consumption paths of hydrogen include two aspects: one is used for ammonia synthesis reaction, and the other is involved in organic liquid hydrogen storage process.

[0151] The hydrogen balance relationship can be expressed as:

[0152]

[0153] wherein, is the mass of hydrogen produced by water electrolysis at time t (unit: kg / h); is the mass of hydrogen released from the hydrogen storage module at time t (unit: kg / h); is the mass of hydrogen desorbed in the organic liquid at time t (unit: kg / h); is the mass of hydrogen required for the synthesis of ammonia reaction at time t (unit: kg / h).

[0154] There is a certain quantitative correspondence between the production and consumption of hydrogen. In the synthesis of ammonia reaction, the consumption of hydrogen is proportional to the production of ammonia, which can be expressed as:

[0155]

[0156] wherein, is the hydrogen consumption coefficient required for the synthesis of each ton of ammonia (unit: ), and its typical value range is 1980 ≤ n ≤ 2200; is the production of ammonia at time t (unit: t / h).

[0157] In actual operation, due to the influence of power generation fluctuation on electrolytic water hydrogen production, its yield will change. When the power generation is sufficient, the electrolytic tank can run at full load, producing more hydrogen; when the power generation is insufficient, the hydrogen production will decrease accordingly. At this time, the organic liquid hydrogen storage part plays a role in regulating the balance of hydrogen supply and demand. When the hydrogen production is greater than the amount of hydrogen required for the synthesis of ammonia, the excess hydrogen can be stored in the organic liquid, i.e. increase ; when the hydrogen production is less than the amount of hydrogen required for the synthesis of ammonia, the hydrogen in the organic liquid can be released, i.e. increase , to meet the needs of the synthesis of ammonia reaction. In this way, the system can maintain the balance of hydrogen under different production conditions, ensuring the stable progress of the synthesis of ammonia reaction.

[0158] In some embodiments, steam balance reasonably allocates and adjusts the use of steam according to the real-time demand of the system, ensuring efficient use of heat in the system. The working principle of the system is based on the heat recovery of the heat generated by the synthesis of ammonia reaction and the heating demand in the process of organic liquid hydrogen storage. Through accurate calculation and control, the balance between steam production, steam extraction and condensation is achieved.

[0159] First, the calculation of steam production is the basis of the steam balance system. In the green ammonia synthesis part, the waste heat recovery device at the outlet of the reactor can recover a large amount of heat generated by the synthesis of ammonia reaction and convert it into high-quality steam. Let the theoretical heat of each ton of synthesis of ammonia reaction be , the available steam production heat corresponding to each ton of ammonia production be , and the coefficient between them be , i.e.:

[0160]

[0161] The steam production at this moment can be calculated by the ammonia production at each moment , and the calculation formula is as follows:

[0162]

[0163] is the waste heat recovery efficiency coefficient (0 < 1); is the unit synthesis ammonia reaction theoretical heat release (kJ / t); is the available steam heat per ton of synthesis ammonia (unit: MJ / t); is the ammonia production at t moment (unit: t / h); is the initial enthalpy value of the steam by-product of the synthesis ammonia reaction (unit: MJ / t); is the enthalpy value of the extraction steam (unit: MJ / t); is the specific enthalpy of the waste heat boiler feed water (unit: MJ / t).

[0164] Next is the calculation of the extraction steam quantity. The determination of the extraction steam quantity mainly depends on the heating requirement of the organic liquid hydrogen storage part dehydrogenation reactor. If the organic liquid hydrogen storage is in the state of releasing hydrogen at t moment, the heat required for each hydrogen gas is , the hydrogen content is , and the total heating heat required at this time is:

[0165]

[0166] The extracted steam temperature is , the pressure is , and the enthalpy value is calculated as . The heating requirement of the organic liquid hydrogen storage is:

[0167]

[0168] is the heat required for each cubic meter of hydrogen gas to be released (unit: ); is the hydrogen release quantity at t moment (unit: ); is the total heating heat requirement at t moment (unit: MJ / h); is the maximum extraction heat of the turbine (unit: kWh / h); is the maximum extraction quantity of the turbine (kg / s); is the extraction enthalpy value.

[0169] ​​​In actual operation, the steam balance system needs to monitor and adjust these parameters in real time to ensure the stable operation of the system. Various sensors are installed in the system to monitor the temperature, pressure, flow rate of steam, and hydrogen content of organic liquid hydrogen storage, etc. in real time. The control system adjusts the steam extraction valve of the turbine and the power of the electric heating system according to these monitoring data to achieve dynamic balance of steam production, steam extraction and condensing gas.

[0170] For example, when the ammonia production increases, the steam production also increases accordingly. At this time, the control system will appropriately increase the steam extraction amount to meet the heating demand of the dehydrogenation reactor according to the heating demand of the organic liquid hydrogen storage. If there is still surplus steam after increasing the steam extraction amount, the condensing gas amount will be increased to make the surplus steam continue to generate electricity in the turbine condensing section. Conversely, when the ammonia production decreases, the steam production decreases, and the control system will accordingly reduce the steam extraction amount and the condensing gas amount to avoid waste of energy.

[0171] In addition, the steam balance system also needs to consider other steam users that may appear in the future. Although it is not considered in detail in the current simplified process, in actual application, the system needs to have certain extensibility and flexibility to adjust the steam distribution according to new demands.

[0172] Through such a steam balance system, the green ammonia synthesis system can fully utilize the heat generated by the ammonia synthesis reaction to achieve efficient use of energy. At the same time, the system can reasonably distribute steam according to the heating demand of the organic liquid hydrogen storage to ensure the stable progress of the organic liquid hydrogen storage process. This precise steam balance control provides a strong guarantee for the stable and efficient operation of the entire green ammonia synthesis system.

[0173] The overall steam balance is:

[0174]

[0175] wherein, is the total steam production at time t (unit: t / h); is the ammonia production at time t (unit: t / h); is the steam amount in the turbine condensing section at time t (unit: t / h).

[0176] In some embodiments, the power balance is the basis for maintaining the normal operation of the system. The power sources of the system include external power supply and electricity generated by the ammonia turbine generator set. The external power supply can come from the power grid or renewable energy power generation such as solar energy, wind energy, etc. The power balance relationship can be represented as:

[0177]

[0178] wherein, is the external power supply power at time t (unit: MW); P t is the turbine power at time t (unit: MW); P e is the electrolysis power at time t (unit: MW); P a is the ammonia synthesis power at time t (unit: MW); P s is the auxiliary system power at time t (unit: MW); P h is the hydrogen storage system electric heating power at time t (unit: MW).

[0179] In the power balance, the power consumption of each part will change with the running state of the system. For example, the electrolysis power consumption (which is proportional to the hydrogen production, when the hydrogen production increases, the electrolysis cell needs to consume more power. The ammonia synthesis power consumption is mainly used for the operation of devices such as compressors, and its power consumption will also change with the change of ammonia synthesis load. The power consumption of organic liquid hydrogen storage is related to the hydrogen release amount, when hydrogen needs to be released, the dehydrogenation reactor may need to be electrically heated to meet the heating demand, but the steam heat is preferred to reduce the power consumption.

[0180] The power generated by the ammonia turbine generator set Depends on the amount of steam generated by the ammonia synthesis reaction and the quality of the steam. When the ammonia production increases, the steam production will also increase accordingly, and the power generation of the turbine generator set will also increase. If the power generated by the turbine generator set is greater than the power consumption of the system, the excess power can be fed back to the power grid; if the power generation is less than the power consumption, then the power needs to be obtained from the external power grid to maintain the normal operation of the system.

[0181] Hydrogen balance and power balance have a crucial impact on the stability of the system. Hydrogen balance ensures the stable supply of hydrogen raw materials required for ammonia synthesis reaction, avoiding reaction interruption or efficiency reduction due to hydrogen deficiency or excess. Power balance provides protection for the normal operation of each device in the system, avoiding device failure and production interruption due to power shortage or excess. Only by maintaining the balance of the two, can the green ammonia synthesis system run efficiently and stably.

[0182] In some embodiments, in a green ammonia synthesis system, the optimization goal is to achieve maximum ammonia production and minimum cost per ton of ammonia production, which are interrelated and need to be considered comprehensively to maximize the overall benefit of the system. Calculations and decisions for future time scales based on the power generation curve and the current system operation are the key to achieving this optimization goal. The production cost mainly includes power cost, equipment investment cost, raw material cost and other public engineering consumption cost, etc. In terms of power cost, since the power source of the system includes external power supply and power generated by the ammonia synthesis turbine generator set, it is necessary to reasonably arrange the use of power and preferentially use low-priced power for water electrolysis hydrogen production and other equipment operation. Equipment investment cost is one-time, but in long-term operation, the depreciation and maintenance cost of equipment need to be considered. Raw material cost mainly involves the production and supply of hydrogen and nitrogen, and the production and storage method of hydrogen needs to be optimized to reduce cost. Other public engineering consumption costs such as steam use, cooling water, etc. also need to be reasonably controlled.

[0183] In order to achieve the optimization goal, calculations and decisions for future time scales need to be made based on the power generation curve and the current system operation. The power generation curve reflects the fluctuation of power supply, and through the analysis of the power generation curve, the power supply situation in different time periods in the future can be predicted. For example, if it is predicted that the power supply is sufficient and the price is low in a certain period of time in the future, then the production of water electrolysis hydrogen can be increased in this period of time, and the excess hydrogen can be stored for subsequent ammonia synthesis. At the same time, the production load of ammonia synthesis can also be adjusted according to the power generation curve, and the ammonia production can be increased when the power is sufficient, so as to fully utilize the low-priced power.

[0184] In the calculation of future time scales, several factors need to be considered. First, hydrogen balance needs to be predicted based on the production of hydrogen from water electrolysis, the state of organic liquid hydrogen storage, and the amount of hydrogen required for ammonia synthesis. For example, if it is predicted that ammonia production will increase in the future, sufficient hydrogen supply needs to be ensured in advance, which can be achieved by increasing the production of hydrogen from water electrolysis or releasing hydrogen stored in organic liquid. Second, steam balance needs to be predicted based on the amount of steam generated by the ammonia synthesis reaction, the heating demand of organic liquid hydrogen storage, and the operation of the turbine generator set. For example, if it is predicted that the amount of hydrogen released from organic liquid hydrogen storage will increase in the future, sufficient steam needs to be arranged in advance for heating to ensure the smooth release of hydrogen. Finally, electricity balance needs to be predicted based on the electricity consumption of each device in the system, external power supply, and power generation of the ammonia synthesis turbine generator set. For example, if it is predicted that the external power supply price will rise in the future, the electricity consumption strategy of the system can be adjusted in advance to increase the power generation of the ammonia synthesis turbine generator set and reduce the use of external power supply.

[0185] In the decision-making process, the above factors need to be considered comprehensively and weighed according to the optimization goal. For example, if the hydrogen storage capacity is increased in a certain period of time, it can reduce the cost of hydrogen production in the future, but it will lead to a decrease in current ammonia production, and at this time the ammonia market price is high, so it needs to be weighed whether to prioritize hydrogen storage or ammonia production. Through continuous calculation and decision-making, the system's operating parameters such as the production of hydrogen from water electrolysis, the production load of ammonia synthesis, and the state of organic liquid hydrogen storage are adjusted to achieve the optimization goal of maximizing ammonia production and minimizing the cost of producing one ton of ammonia.

[0186] In practical applications, mathematical models and optimization algorithms can be used to assist in calculation and decision-making. By establishing a mathematical model of the system, factors such as hydrogen balance, steam balance, and electricity balance are included in the model, combined with power generation curves and market demand information, and the optimal operating strategy is solved using optimization algorithms. At the same time, real-time monitoring data can be used to modify and optimize the model to improve the accuracy and reliability of the decision-making.

[0187] By calculating and making decisions for future time scales based on power generation curves and current conditions, considering factors such as hydrogen balance, steam balance, and electricity balance, and continuously adjusting the system's operating parameters, the green ammonia synthesis system can achieve the optimization goal of maximizing ammonia production and minimizing the cost of producing one ton of ammonia, improving the overall efficiency and market competitiveness of the system.

[0188] The basic calculation formula is to minimize the cost of producing one ton of ammonia:

[0189]

[0190] The production cost model for one ton of ammonia is as follows:

[0191]

[0192] in, The electricity cost for time period t (unit: yuan / h) is calculated using the following formula: ;

[0193] The steam cost for time period t (unit: yuan / h) is calculated using the following formula: ; The hydrogen storage operation cost for time period t (unit: yuan / h) is calculated using the following formula: ; Fixed cost allocation (equipment depreciation, maintenance, etc., unit: yuan / h); These represent the external electricity price for time period t, the cost per unit of steam heat, and the operating cost per unit of hydrogen storage, respectively.

[0194] In the calculation, a rolling time-domain optimization method can be used to divide the future T hours into N time periods (e.g., each time period is 15 minutes). In each current time period t, based on the predicted power generation curve: Solve the optimization problem.

[0195] Only the decisions made in the first period (e.g.) are executed. ), and roll to the next time period to update the prediction. Finally, discretize the objective function to reflect the cardinality:

[0196]

[0197] In some embodiments, a molten salt thermal storage module plays a crucial role in the green ammonia synthesis system. It primarily consists of a molten salt storage unit, a heating unit, and a steam generation unit, working in conjunction with these units to achieve efficient heat storage and utilization. Firstly, the molten salt thermal storage module stores the heat generated during the ammonia synthesis reaction. In the green ammonia synthesis process, the reactor releases a significant amount of heat during the ammonia synthesis reaction. The molten salt thermal storage module transfers this heat to the low-temperature molten salt via a heat exchanger, raising the molten salt temperature and storing a large amount of thermal energy. Secondly, utilizing surplus electricity to generate steam is another important function of the molten salt thermal storage module. When the system has surplus electricity, the molten salt thermal storage module can use this surplus electricity to heat the molten salt via an electric heater. This converts electrical energy into thermal energy in the molten salt and stores it, avoiding the waste of surplus electricity. When steam is needed, the high-temperature molten salt enters the steam generator, where it exchanges heat with water to produce steam. This steam can be used to generate electricity, powering equipment such as compressors and electrolyzers within the system; it can also be used to heat the dehydrogenation reactor in the organic liquid hydrogen storage section, promoting hydrogen release.

[0198] In some embodiments, by integrating electrolytic water hydrogen production, organic liquid hydrogen storage and green ammonia synthesis, the synergistic energy management effectively solves the core problems of low energy utilization and dynamic balance adjustment difficulty in the prior art. The specific effects are reflected in the following aspects:

[0199] 1. Breakthrough of organic liquid hydrogen storage energy consumption bottleneck.

[0200] Traditional organic liquid hydrogen storage needs to rely on electric heating dehydrogenation reactor, and every release of 1 Hydrogen needs to consume 1 degree of electricity (4.8 ). And the invention replaces electric heating with turbine extraction steam heating, which significantly reduces energy consumption. Taking the production of 20 tons of ammonia at a certain time as an example, 2000 , of which 1 / 4 (5000 ) is provided by hydrogen storage, the traditional scheme needs to consume 5000kWh of electric heating energy. After using the invention, this part of heat is supplied by extraction steam (steam temperature = 280℃, pressure = 4.2MPa, enthalpy = 2950kJ / kg), and the extraction steam amount is calculated as:

[0201]

[0202] Among them, turbine extraction steam heating fully meets the demand, and the electric heating energy consumption is reduced to 0.

[0203] 2. Efficient use of ammonia synthesis waste heat.

[0204] Ammonia byproduct steam (400℃, 4.2MPa, H1=3396kJ / kg) is used to generate electricity through turbine, producing 0.97 tons of steam per ton of ammonia, and 19.4 tons of steam for 20 tons of ammonia. If all the electricity is generated, the turbine efficiency η=85%, and the power generation is:

[0205]

[0206] The remaining low-pressure steam in the traditional scheme needs to be condensed by cooling water (circulating water consumption 12.5m³ / t of steam), and the total water consumption is 242.5m³. The invention reduces the condensing amount to 19.4-92.3=-72.9 tons (negative value indicates the need to supplement steam) through extraction steam heating, and the actual circulating water consumption is reduced by 67% to 80m³.

[0207] 3. Comparison of comprehensive energy consumption.

[0208] The total energy consumption of the traditional split scheme = electrolytic hydrogen production electric consumption (20x2000x4.3kWh) + hydrogen storage electric consumption (5000kWh) = 172,000 + 5,000 = 177,000kWh.

[0209] The total energy consumption of the present application scheme = electrolytic hydrogen production electricity consumption (net electricity consumption of 153,300 kWh after deducting turbine power supply of 18.7 MWh) + circulating water energy consumption (converted electricity consumption of 800 kWh) = 154,100 kWh.

[0210] The energy saving rate = (177,000-154,100) / 177,000 = 12.9%, and 183,200 kWh of electricity can be saved in 8000 hours of annual operation.

[0211] In some embodiments, referring to Figure 4 As shown, the green synthetic ammonia system includes a hydrogen production module 1, a hydrogen storage module 2, a synthetic ammonia module 3, a waste heat recovery module 4, and a turbine generator set module 5. The hydrogen production module 1 receives external power supply, carries out water electrolysis reaction to generate hydrogen, and outputs part of the hydrogen to the hydrogen storage module 2 for chemical storage. The synthetic ammonia module 3 receives hydrogen released from the hydrogen production module 1 and the hydrogen storage module 2, reacts with nitrogen to generate synthesis gas, and then further completes the condensation and liquefaction of ammonia in the waste heat recovery module 4 to output liquid ammonia products. A large amount of reaction heat released during the synthetic ammonia reaction is converted into byproduct steam by the waste heat recovery module 4, and the steam is supplied to the turbine generator set module 5 to drive the generator to generate electricity. The expanded steam is condensed and recovered to form medium-pressure steam returning to the hydrogen storage module 2 as a dehydrogenation heating heat source, realizing the cascade recovery and efficient utilization of system thermal energy. The above-mentioned modules are coupled through material and energy flow to realize the coordinated operation of hydrogen production, storage, synthesis, power generation and other links, and improve the overall energy efficiency of the system.

[0212] In some embodiments, as Figure 5 As shown, the steam balance process in the green synthetic ammonia system can be visually represented by the dynamic relationship between steam production, steam extraction and condensation. Wherein, the horizontal axis represents time t, and the vertical axis represents steam flow mSt. Curve A (red area) represents the byproduct steam flow mSt1 generated by the synthetic ammonia module, curve B (gray area) represents the steam extraction amount mSt2 required to supply the heat for the dehydrogenation reaction of the hydrogen storage module, and curve C (blue area) represents the remaining steam flow mCod entering the condensing section of the turbine generator set module. From Figure 5 It can be seen that the heat released during the synthetic ammonia reaction at different stages fluctuates significantly, and the corresponding steam production mSt1 presents periodic changes; to adapt to the heat load demand of the organic liquid hydrogen storage module, the system realizes the allocation of steam energy by adjusting the steam extraction amount mSt2, and the remaining part enters the condensing section as mCod to recover residual energy and generate electricity. Through this steam dynamic balance control strategy, the cascade utilization of synthesis heat energy and the efficient distribution of heat energy in the whole system are realized.

[0213] In some embodiments, this example focuses on a 567MW wind farm in Northwest China, with an annual power generation of 2.1 billion kWh. A green ammonia synthesis system driven by fluctuating renewable energy is constructed by combining supporting water electrolysis for hydrogen production, organic liquid hydrogen storage, and a green ammonia synthesis unit. The system as a whole exhibits good energy conversion efficiency and operational stability. The core parameters are as follows:

[0214] The wind power system has an installed capacity of 567MW and an annual power generation of approximately 2.1 billion kWh, with a curtailment rate controlled within 1%. The supporting energy storage system has a capacity of 157MW·h to mitigate power fluctuations. The electrolysis water hydrogen production system has a designed capacity of 83,000 Nm³ / h. The organic liquid hydrogen storage system has a total hydrogen storage capacity of 361,500 Nm³, with a hydrogen storage and release efficiency of no less than 98%, enabling efficient hydrogen storage and release cycles. The synthetic ammonia unit has a designed annual capacity of 284,000 tons, and under fluctuating power conditions, the actual annual output reaches 178,200 tons, demonstrating good load adaptability and operational stability. See Table 1 for details.

[0215] Table 1

[0216]

[0217] Based on the above embodiments, this specification aims to construct a multi-process thermodynamic deep coupling mechanism. By building a steam graded utilization network and a real-time dynamic balance control system, it achieves the efficient conversion of the exothermic reaction of ammonia synthesis into high-grade steam, prioritizing turbine power generation to meet the power demands of chemical plants such as water electrolysis for hydrogen production and ammonia synthesis, while also ensuring grid stability. The system utilizes turbine steam extraction to meet the medium-pressure steam load required for organic liquid hydrogen storage and dehydrogenation, replacing traditional electric heating methods to improve energy efficiency. To address fluctuations in renewable energy output, this specification further develops a minute-scale steam-hydrogen-electricity three-flow coupling control algorithm and constructs a multi-objective optimization decision model with economic efficiency as the goal. Under the premise of ensuring safe system operation, it coordinates the dynamic balance between hydrogen storage peak-shaving benefits and ammonia synthesis production benefits, thereby achieving efficient, stable, and economical operation of the green ammonia synthesis system.

[0218] Although the present specification provides method operational steps in the order in which the steps are performed, the order of the steps can be changed based on the underlying logic of the method. The steps of the embodiments recited in the claims can be executed in any order that is practicable and / or desirable. The order of the steps can be varied in actual implementation of the method. The steps recited in the embodiments or the accompanying drawings can be executed in parallel or in series (for example, in a parallel processor or multi-threaded processing environment, or even in a distributed data processing environment). The terms "comprises", "comprising", or any other variations thereof are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but can include other elements not expressly listed or inherent to such process, method, article, or apparatus. An element proceeded by "comprises... a" does not, without more constraints, exclude the existence of additional identical or similar elements in the process, method, article, or apparatus that comprises the element. The terms "first", "second", and the like, do not denote any order, quantity, or importance, but rather are used to identify one element from another.

[0219] Those skilled in the art will also appreciate that, in addition to being embodied in a purely computer readable program code manner, the controller can be implemented in the form of logic gates, switches, application specific integrated circuits, programmable logic controllers, and embedded microcontrollers, etc. by logically programming the method steps to perform the same functions. Therefore, such a controller can be considered as a hardware component, and the means included therein for performing various functions can also be considered as structures within the hardware component. Alternatively, the means for performing various functions can be considered as both a software module implementing the method and a structure within the hardware component.

[0220] From the above description of the embodiments, those skilled in the art can clearly understand that the present specification can be implemented by means of software in conjunction with a necessary general hardware platform. Based on such an understanding, the technical solutions of the present specification can essentially be embodied in the form of a software product. The computer software product can be stored in a storage medium, such as a ROM / RAM, a magnetic disk, an optical disk, etc., and includes a number of instructions for causing a computer device (which can be a personal computer, a mobile terminal, a server, or a network device, etc.) to execute the methods described in the various embodiments or some parts of the embodiments.

[0221] Although the present specification is described by way of embodiments, those skilled in the art will appreciate that there are many variations and modifications of the present specification without departing from the spirit of the present specification, and it is intended that the appended claims encompass such variations and modifications without departing from the spirit of the present specification.

Claims

1. An energy management method for a synthetic ammonia production system, characterized in that, An application is made in a synthetic ammonia production system, the synthetic ammonia production system comprising at least: a hydrogen production module, a hydrogen storage module, a synthetic ammonia module, a waste heat recovery module, and a turbine generator set module; one end of the hydrogen production module is connected to the hydrogen storage module, and the other end is connected to the synthetic ammonia module; the synthetic ammonia module is connected to the waste heat recovery module; the waste heat recovery module is connected to the turbine generator set module; the turbine generator set module is connected to the hydrogen storage module; the method includes: In the process of producing liquid ammonia using a synthetic ammonia production system, according to preset control rules, the waste heat recovery module recovers the first steam generated by the synthetic ammonia module during the heat release process of producing liquid ammonia. According to the preset control rules, the turbine generator module generates electricity based on the expansion of the first steam to power the hydrogen production module, the hydrogen storage module and the ammonia synthesis module, and provides the first hydrogen to the ammonia synthesis module through the hydrogen production module; During the first steam expansion power generation process of the turbine generator module, according to the preset control rules and the amount of hydrogen in the first hydrogen, the corresponding second steam is recovered through the turbine extraction port. The dehydrogenation reactor in the hydrogen storage module releases and supplies the second hydrogen required for the operation of the ammonia synthesis module based on the second steam.

2. The method according to claim 1, characterized in that, The synthetic ammonia production system also includes a molten salt energy storage module and a power supply module. The molten salt energy storage module is used to store the heat released during the production of liquid ammonia by the synthetic ammonia module. The power supply module is used to provide green electricity or grid electricity to the synthetic ammonia production system, and together with the turbine generator module, it meets the system's power demand.

3. The method according to claim 2, characterized in that, The preset control rules are control rules constructed based on the power balance relationship, steam balance relationship, and hydrogen balance relationship, used to dynamically control the recovery amount of the first steam and the second steam.

4. The method according to claim 3, characterized in that, The method further includes: Based on the preset control rules, a first constraint condition based on the power balance relationship, a second constraint condition based on the steam balance relationship, and a third constraint condition based on the hydrogen balance relationship are constructed. Construct the target cost function based on the preset control rules; Based on the first, second, and third constraints, the corresponding amounts of first and second steam recovered are determined by optimizing the objective cost function.

5. The method according to claim 4, characterized in that, The method further includes: Obtain the operating characteristic parameters of the ammonia synthesis production system; wherein the operating characteristic parameters include at least one of the following: ammonia synthesis output, theoretical heat release per unit of ammonia synthesis reaction, and waste heat recovery efficiency coefficient; The recovery rate of the first steam is determined based on the aforementioned operating characteristic parameters.

6. The method according to claim 4, characterized in that, The method further includes: Obtain the operating characteristic parameters of the ammonia synthesis production system; wherein the operating characteristic parameters include at least one of the following: the amount of hydrogen required by the ammonia synthesis module, and the amount of hydrogen provided by the hydrogen production module for the first hydrogen; Based on the aforementioned operating characteristic parameters, determine the required extraction steam flow rate for the turbine generator set; The amount of second steam recovered from the turbine generator module is determined based on the extraction steam flow rate. The amount of hydrogen gas released by the dehydrogenation reactor in the hydrogen storage module is determined based on the amount of the second steam recovered.

7. The method according to claim 4, characterized in that, The method further includes: Obtain the operating characteristic parameters of the ammonia synthesis production system; wherein the operating characteristic parameters include at least one of the following: power generation of the turbine generator module, power consumption of the hydrogen production module, power consumption of the hydrogen storage module, and power consumption of the ammonia synthesis module; Based on the aforementioned operating characteristic parameters, the required external power supply for the ammonia synthesis production system is determined.

8. An energy management device for a synthetic ammonia production system, characterized in that, This device is applied to an ammonia synthesis production system, which at least includes: a hydrogen production module, a hydrogen storage module, an ammonia synthesis module, a waste heat recovery module, and a turbine generator set module; one end of the hydrogen production module is connected to the hydrogen storage module, and the other end is connected to the ammonia synthesis module; the ammonia synthesis module is connected to the waste heat recovery module; the waste heat recovery module is connected to the turbine generator set module; and the turbine generator set module is connected to the hydrogen storage module; the device includes: The first steam determination module is used to recover the first steam generated by the ammonia synthesis module during the production of liquid ammonia products using the ammonia synthesis production system, according to preset control rules, through the waste heat recovery module. The first hydrogen determination module is used to generate electricity based on the expansion of the first steam using the turbine generator set module according to the preset control rules, to supply power to the hydrogen production module, the hydrogen storage module and the ammonia synthesis module, and to supply the first hydrogen to the ammonia synthesis module through the hydrogen production module; The second steam determination module is used to recover the corresponding second steam through the turbine extraction port according to the preset control rules and the amount of hydrogen in the first hydrogen during the first steam expansion power generation process of the turbine generator module. The second hydrogen determination module is used to release and supply the second hydrogen required for the operation of the ammonia synthesis module based on the second steam from the dehydrogenation reactor in the hydrogen storage module.

9. An electronic device, characterized in that, The system includes a processor and a memory for storing processor-executable instructions, wherein the processor, when executing the instructions, implements the steps of the energy management method for a synthetic ammonia production system according to any one of claims 1 to 7.

10. A computer-readable storage medium, characterized in that, It stores computer instructions that, when executed by a processor, implement the steps of the energy management method for a synthetic ammonia production system according to any one of claims 1 to 7.

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