Integrated energy systems for green industrial applications such as energy generation and nitric acid production.

Abstract

This specification describes techniques that can be implemented in an integrated energy system (IES) for producing nitric acid (HNO3) while minimizing the carbon footprint. When implemented by a resource production plant, such techniques may include receiving electricity and steam from a power plant and producing hydrogen (H2) gas from the steam in a hydrogen (H2) production subplant; receiving electricity from a power plant and air from the environment and producing nitrogen (N2) gas in a nitrogen (N2) production subplant; producing ammonia (NH3) from hydrogen (H2) gas and nitrogen (N2) gas in a nitrogen production subplant; and producing nitric acid (HNO3) from ammonia (NH3) in a nitric acid (HNO3) production subplant.

Description

Technical Field

[0001] Cross - reference to Related Applications This application claims the benefit of U.S. Patent Application No. 18 / 606,962, filed on March 15, 2024, and U.S. Provisional Patent Application No. 63 / 453,018, filed on March 17, 2023, entitled "SMALL MODULAR NUCLEAR REACTOR INTEGRATED ENERGY SYSTEMS FOR ENERGY PRODUCTION AND GREEN INDUSTRIAL APPLICATIONS, SUCH AS THE PRODUCTION OF NITRIC ACID", the entireties of which are incorporated herein by reference.

[0002] This technology is directed to integrated energy systems (IES) for nuclear reactors for energy generation and green industrial applications such as the production of green nitric acid, as well as related devices and methods.

Background Art

[0003] The landscape of energy generation has evolved rapidly in recent years, with increasing emphasis on decarbonization, sustainability, and resilience, driving the adoption of cleaner and more efficient forms of power generation. While fossil fuels continue to play a significant role in the world's energy supply, there is a clear trend towards an increasing introduction of renewable energy, in conjunction with progress in energy storage, grid modernization, and energy efficiency measures, to address the challenges of climate change and energy transition.

[0004] Cumulative carbon dioxide emissions are a major driver of climate change. The seven largest CO2-emitting industries in the world are: (1) power plants (coal, natural gas, oil combustion), (2) oil refining plants, (3) ammonia production plants, (4) chemical manufacturing and production plants, (5) cement production plants, (6) steel manufacturing plants, and (7) transportation. Many of these processes, as well as other processes in the petroleum, chemical, pharmaceutical, and materials manufacturing industries, require a combination of electricity, steam, heat, and hydrogen (H2) to operate and produce industrial products. For example, hydrogen (H2) is used in each of the above industries (2) to (7). Currently, most of the hydrogen (H2) produced in the United States comes from the steam-methane reforming process. In the United States, the steam-methane reforming process accounts for more than 95% of total hydrogen (H2) production, producing approximately 10 million metric tons (MT) of H2 annually. Nearly 70% of this hydrogen is used in the petroleum refining industry, and 20% is used in fertilizer production. The remaining 10% is used in chemical and materials manufacturing processes.

[0005] Energy systems incorporate various energy conversion technologies, including power plants, cogeneration (combination of heat and electricity) systems, and distributed power generation units (such as solar panels and wind turbines). These technologies convert primary energy sources into usable forms of energy, such as electricity, heat, and mechanical power, which can be used as secondary energy sources. Energy systems utilize a diverse range of energy resources, including renewable energy sources (such as solar, wind, and hydroelectric power), conventional fuels (such as natural gas and coal), and emerging technologies (such as hydrogen and biofuels). By combining multiple energy sources, these systems can enhance energy security and resilience. [Brief explanation of the drawing]

[0006] Detailed explanations are provided with reference to the attached figures. In each figure, the leftmost digit of the reference number identifies the figure in which the reference number first appears. The use of the same reference number in different figures indicates similar or identical items or features.

[0007] [Figure 1] This is a schematic diagram of an integrated energy system, including a power plant system, according to at least some embodiments. [Figure 2] A block diagram illustrating an example hydrogen production process for generating hydrogen gas, according to at least some embodiments, is depicted. [Figure 3] This is a schematic diagram of a typical HTSE electrolytic separator. [Figure 4] A block diagram illustrating the example ammonia production process, according to at least some embodiments, is depicted. [Figure 5] A block diagram illustrating the nitrate production process of an example nitrate production subplant for producing nitrate, according to at least some embodiments, is depicted. [Figure 6] This is a schematic diagram of an integrated energy system, including a power plant system, according to an additional embodiment of this technology. [Figure 7] This is a schematic diagram of a nuclear power plant system including multiple reactors according to an embodiment of this technology. [Figure 8] These are partial schematic and partial cross-sectional views of a reactor system configured according to an embodiment of this technology. [Figure 9] These are partial schematic and partial cross-sectional views of a reactor system configured according to an additional embodiment of this technology. [Figure 10] An example process for producing nitric acid according to an additional embodiment of this technology is shown. [Modes for carrying out the invention]

[0008] In embodiments, this disclosure covers techniques, as well as related devices and methods, that may be implemented in connection with integrated energy systems (IESs), such as for use in green industrial processes that produce little to no carbon emissions. An IES of this technology may comprise a power plant (e.g., a primary power plant) integrated with one or more resource generation plants. Resource generation according to embodiments of this technology may include industrial processes, applications, and operations such as chemical manufacturing and production, petroleum and oil refining, cement production, steel manufacturing, transportation, pharmaceutical production, and material manufacturing. Chemical manufacturing and production may include, for example, the production of hydrogen (H2), oxygen (O2), nitrogen (N2), ammonia (NH3), nitric acid (HNO3), and other chemicals that may be used in industrial applications. Such an IES may be capable of generating resources using excess electricity and steam from a power plant.

[0009] In some embodiments, the integrated energy system comprises a power plant system having multiple small modular reactors (SMRs) specifically configured to work together to support one or more industrial processes. SMRs are smaller in size (e.g., dimensions) and power compared to large conventional reactors. Furthermore, they are modular in that some or all of their systems and components can be assembled in a factory and transported as units to the installation site. In some aspects of the art, multiple SMRs in an integrated energy system can flexibly and dynamically provide electricity, steam, or a combination of both to industrial processes due to the modularity and flexibility of the SMRs. That is, the configuration of the SMRs can be switched during operation to provide various levels of steam and electricity output depending on the operating state and / or requirements of the industrial processes.

[0010] Driven by the push towards cleaner and more efficient forms of power generation, nuclear power will become increasingly important in the coming years. Nuclear power plants are attractive to countries seeking to reduce carbon emissions and enhance energy security, as they provide reliable baseload power and minimize greenhouse gas emissions during operation. For example, nuclear power plants generate electricity without emitting greenhouse gases such as carbon dioxide (CO2) during operation. During operation, a nuclear power plant uses nuclear fission to generate heat, which is then used to produce steam that rotates a turbine, generating electricity. This process can result in the production of both electricity and steam. The management and disposal of waste steam from nuclear power plants can be a challenge. Therefore, the challenges of climate change need to be addressed by reducing CO2 emissions in industrial processes, specifically in the production of H2. The advantages of nuclear energy for providing steam, electricity, and heat also necessitate the development of ways to use nuclear power in integrated energy systems.

[0011] In some embodiments, the power plant system is operably connected to a hydrogen (H2) and oxygen (O2) production plant configured to process water and / or steam for the production of hydrogen and oxygen. The hydrogen (H2) and oxygen (O2) production plant can utilize a high-temperature steam electrolysis (HTSE) process and / or a low-temperature steam electrolysis (LTSE) process. Thus, the power plant system can route high-temperature steam (e.g., via an auxiliary heater) and electricity to the hydrogen (H2) and oxygen (O2) production plant for use in the HTSE process, and (ii) route electricity to the hydrogen (H2) and oxygen (O2) production plant for use in the LTSE process. In some embodiments, the integrated energy system includes a water treatment plant and / or a desalination plant electrically connected to the power plant system and configured to provide high-quality water to the hydrogen (H2) and oxygen (O2) production plant for use in the LTSE process.

[0012] Therefore, the integrated energy system can produce both green hydrogen (H2) and green oxygen (O2). The integrated energy system may further comprise additional industrial process plants configured to utilize green hydrogen (H2) and / or green oxygen (O2) in further industrial processes, operably connected to the power plant system. For example, the integrated energy system may further comprise (i) an ammonia production plant configured to utilize green hydrogen (H2) and nitrogen (N2) from the environment (e.g., nitrogen (N2) drawn from air by a nitrogen (N2) generator, typically called a pressure swing adsorption (PSA) system) for producing green ammonia, and (ii) a nitrate production plant configured to utilize green ammonia for producing nitrate. The power plant system may further power some or all of these additional processes.

[0013] Nitrate (also known as HNO3, aquafortis, and nitrate extract) is an important industrial chemical for fertilizer production. The global nitrate market is projected to grow from $28.23 billion in 2021 to $34.76 billion by 2030, with over 75% of the market accounted for by fertilizer production. Nitrate is primarily used as an intermediate in the production of ammonium nitrate (NH4NO3), which is used as a high-nitrogen fertilizer in agriculture.

[0014] Pure nitrate compounds are colorless, but older or lower-quality samples may contain nitrogen oxides (NOx). X ) tends to have a yellowish hue due to impurities and water. Most commercially available nitric acid has a concentration of 68% (v / v) in water. When a solution contains more than 86% (v / v) nitric acid, it is called fuming nitric acid, which is further characterized as (i) white fuming nitric acid, or (2) red fuming nitric acid at concentrations greater than 95%, depending on the amount of nitrogen dioxide (NO2) present.

[0015] Today, nitric acid is produced almost entirely through the oxidation of ammonia and the absorption of the oxidation product in water. The chemistry of this process was experimentally demonstrated by Charles Frederic Kuhlmann in 1839. Around 1900, Wilhelm Ostwald developed and patented the Ostwald process by expanding on Kuhlmann's data and establishing the appropriate conditions required for the ammonia oxidation step.

[0016] Oxidation is the process by which a chemical substance is altered by the addition of oxygen (O2). Air, or more precisely, oxygen in the air, is commonly used in the oxidation of ammonia (NH3) in the production of nitric acid because air is inexpensive and readily available. Air contains approximately 21% oxygen, 78% nitrogen, and approximately 1% argon and carbon dioxide. However, using air as an oxidizing agent instead of pure oxygen is less efficient and results in more undesirable reaction byproducts, impurities, and contamination. As described in EP0808797A2, the addition of pure oxygen to a standard nitric acid production process using air as the primary oxidizing agent results in NO X It is possible to control the reaction, increase acid strength, reduce impurities, and promote the production of nitric acid. Further advantages of using pure oxygen in the oxidation of ammonia include higher yield reaction, contamination control, and NO X This includes reducing emissions. However, the high cost of pure oxygen and the energy requirements for its production make oxygen injection practically unfeasible.

[0017] Today, in practice, most of the production of oxygen gas uses fossil fuels to meet the energy requirements of the process, resulting in greenhouse gas emissions and a non-carbon-neutral process. Industrial oxygen plants typically use air as a feedstock and separate it from other components of air by using various techniques such as pressure swing adsorption or membrane separation techniques. However, these techniques have relatively differences in oxygen purity and concentration, which are 93 - 95% for adsorption systems and 30 - 45% for membrane plants. Currently, these methods have limited capacity and high power consumption. These techniques also require a large input of natural gas.

[0018] The production of ammonia is also very energy-intensive and contributes a significant amount of CO2 due to the production of hydrogen (H2) via steam-methane reforming. When combined with the energy required to produce hydrogen (H2) and purified atmospheric nitrogen (N2), the production of ammonia (NH3) accounts for 1% - 2% of the world's energy consumption, 3% of the world's carbon emissions, and 3% - 5% of the natural gas consumption. The hydrogen (H2) required for ammonia (NH3) synthesis is mostly produced through the gasification of carbon-containing materials, mainly natural gas, but other potential carbon sources include coal, oil, peat, biomass, or agricultural waste. As of 2012, the world production of ammonia (NH3) generated from natural gas using the steam reforming process was 72%.

[0019] To address the challenges of climate change, reduce CO2 emissions, and reduce pollution and industrial by-products in high-yield chemicals such as nitric acid (HNO3), there is a need to develop systems and methods for producing green hydrogen (H2), oxygen (O2), ammonia (NH3), nitrogen (N2), and nitric acid (HNO3) that produce little or no carbon emissions.

[0020] Certain details are set forth in the following description and FIGS. 1-10 in order to provide a complete understanding of various embodiments of the present technology. In other instances, well-known structures, materials, operations, and / or systems associated with, for example, nuclear reactors, power generation plant systems, integrated energy systems, chemical production plants, industrial process plants, electrolysis systems, hydrogen and oxygen production plants, direct air capture (DAC) plants, oil refining, and the like are not set forth in detail in the following disclosure or described in order to avoid unnecessarily obscuring the description of various embodiments of the present technology. However, those skilled in the art will recognize that the present technology can be practiced without one or more of the details set forth herein and / or with other structures, methods, components, and the like. The terms used herein are to be interpreted in the broadest and most reasonable manner even though they are being used in conjunction with a detailed description of a particular example of an embodiment of the present technology.

[0021] The accompanying drawings depict embodiments of the present technology and are not intended to limit its scope unless otherwise explicitly indicated. The sizes of the various elements depicted are not necessarily drawn to scale, and these various elements may be enlarged for readability. Details of components may be abstracted in the figures to exclude details such as the arrangement of components and certain exact connections between such components when such details are not necessary to fully understand how to make and use the present technology. Many of the details, dimensions, angles, and other features shown in the figures are merely illustrative of particular embodiments of the present disclosure. Accordingly, other embodiments can have other details, dimensions, angles, and features without departing from the present technology. In addition, those skilled in the art will understand that further embodiments of the present technology can be practiced without some of the details described below.

[0022] Where any material incorporated herein by reference conflicts with the present disclosure, the present disclosure controls. The headings provided herein are for convenience only and are not to be construed as limiting the disclosed subject matter.

[0023] Figure 1 is a schematic diagram of an integrated energy system (IES) 100 comprising a power plant 102, according to at least some embodiments. For example, the power plant 102 may comprise the power plant system 750 of Figure 7, according to an additional embodiment of the present technology. In the exemplary embodiments, the power plant 102 is configured for use in one or more industrial processes / operations, and more specifically for use in resource generation / recovery operations. The power plant 102 may be located at or near the location of a resource generation plant 104. The resource generation plant 104 may include one or more chemical generation processes and industrial processes / operations that generate resources. For example, the power plant 102 may be a permanent or temporary installation built at or near the location of the resource generation plant 104 (e.g., approximately 1 km away), or it may be a mobile or partially mobile system that is moved to and assembled at or near the location of the resource generation plant 104. More generally, the power plant 102 may be local to the industrial process / operation it supports (e.g., located there or near there). For example, the power plant 102 may be located within 0.4 km (0.25 miles), 0.8 km (0.5 miles), 3.22 km (2 miles), 4.82 km (3 miles), or 8.1 km (5 miles) of the industrial process / operation it supports. In some embodiments, the power plant 102 may have 4, 6, 12, or a different number of reactors and have a power output of 308 to 924 megawatts (MWe). In some embodiments, the power plant 102 may have an output of approximately 308 to 924 MWe and approximately 1000 to 3000 megawatts (MWt) of heat.

[0024] In the exemplary embodiment, the power plant 102 is operably connected to a water source. The water source may include water from a storage tank, reservoir, river, lake, sea, groundwater, well, or similar. Water from the water source may be of high quality in that such water is relatively free of impurities. Water from the water source may be supplied to a water treatment plant to produce high-quality water. The water treatment plant may be a water treatment plant, desalination plant, and / or similar, and may be configured to produce high-quality water that can be supplied to the power plant 102 for use in power generation / cooling. For example, the water treatment plant may operate to desalinate the water source and / or otherwise remove contaminants and / or unwanted materials from the water source. Water treatment may include at least one purification method such as reverse osmosis, electrodialysis, distillation, desalination, deionization, filtration, ultrafiltration, or nanofiltration. Generally, water treatment plants may require a considerable amount of energy to operate. In some aspects of this technology, the power plant 102 can be electrically connected to a water treatment plant and configured to flexibly and reliably deliver electricity to the water treatment plant.

[0025] The water treatment plant can route the high-quality water produced to the power plant 102, which can use the water to generate electricity along with a high-quality steam byproduct. In contrast to the limitations of conventional technology, including the lack of any available solutions for efficiently treating the source water (e.g., brine), the power plant 102 can utilize an SMR to generate clean, high-quality water efficiently and without emissions (e.g., carbon emissions). The clean water produced may be suitable for various downstream operations. For example, the power plant 102 can utilize an SMR to generate clean water, which can be used for electrolysis, for example, as will be discussed in more detail below. In alternative or additional examples, the water produced can be used as a secondary coolant in one or more steam generators of the reactor. In some embodiments, the water treatment plant can be omitted, and the power plant 102 can utilize water from other sources to generate steam.

[0026] In one embodiment, the power plant 102 can be electrically connected to a water treatment plant, a resource generation plant 104, and a power grid to selectively supply electricity (e.g., power) thereto (e.g., via one or more of the electrical output paths from the power transmission system of the power plant system). Similarly, individual steam output paths from the power plant 102 can be fluidly connected to the resource generation plant 104 to selectively supply steam thereto. In another embodiment, the power plant 102 can be operably connected to additional or fewer outputs, and / or various outputs can receive electricity and / or steam from other sources (e.g., conventional steam generators, conventional power sources, etc.).

[0027] In embodiments where the power plant 102 supplies steam and electricity to the resource generation plant 104, the resource generation plant 104 may use a combination of steam and electricity to produce specific resources. These resources may include chemical substances such as hydrogen, oxygen, nitrogen, ammonia, and nitric acid (HNO3). For example, the power plant 102 and the resource generation plant 104 may act as a closed-loop system to generate resources. In such cases, the amount of steam and electricity supplied to the resource generation plant 104 may be sufficient to achieve a specified level of production for the resource. For example, the amount of electricity and steam directed to the resource generation plant 104 may be the amount necessary to produce a given amount of resource, which can then be stored. In some cases, the steam supplied by the power plant 102 is condensed into liquid water during the resource generation process and then returned to the power plant 102 (in some cases, via a water treatment plant).

[0028] The resource generation plant 104 may include a hydrogen generation subplant 106 that generates hydrogen from steam. In an embodiment, the steam may be supplied by a power plant 102. The hydrogen generation subplant 106 may carry out the hydrogen generation process 200 shown in Figure 2, which is described in detail below, according to an additional embodiment of the present technology.

[0029] The resource generation plant 104 may include an ammonia generation subplant 110 that generates ammonia by combining hydrogen from the hydrogen generation subplant 106 with nitrogen drawn from the ambient air. The ammonia generation subplant 110 may include the ammonia generation process 400 shown in Figure 4, which is described in detail below, according to an additional embodiment of the present technology.

[0030] The resource generation plant 104 may include a nitrogen generator 108 configured to extract nitrogen from the ambient air. The nitrogen generator 108 may include a nitrogen generator 402, as shown in detail below in Figure 4, according to an additional embodiment of the present technology.

[0031] The resource generation plant 104 may include a nitric acid (HNO3) generation subplant 112 that produces nitric acid (HNO3) from ammonia. The nitric acid (HNO3) generation subplant 112 may include a nitric acid (HNO3) generation process 500, as shown in detail below in Figure 5, according to an additional embodiment of the present technology.

[0032] For clarity, a certain number of components are shown in Figure 1. However, it is understood that embodiments of the present disclosure may include two or more of each component. In addition, some embodiments of the present disclosure may include fewer or more components than all of the components shown in Figure 1. Furthermore, the components in Figure 1 may communicate over any suitable communication medium (including the Internet) using any suitable communication protocol.

[0033] In various embodiments, the power plant 102 and the resource generation plant 104 (e.g., the hydrogen generation subplant 106, the nitrogen generator 108, the ammonia generation subplant 110, the nitric acid (HNO3) generation subplant 112, and / or one or more other parts of the IES 100) can operate in one or more of various modes (e.g., various states such as one or more control states). In some examples, the power plant 102 and the resource generation plant 104 (e.g., the hydrogen generation subplant 106, the nitrogen generator 108, the ammonia generation subplant 110, the nitric acid (HNO3) generation subplant 112, and / or one or more other parts of the IES 100) can operate in a first mode in which nitric acid (HNO3) is not produced. In those or other examples, the power plant 102 and the resource generation plant 104 (e.g., the hydrogen generation subplant 106, the nitrogen generator 108, the ammonia generation subplant 110, the nitric acid (HNO3) generation subplant 112, and / or one or more other parts of IES 100) can operate in a second mode in which nitric acid (HNO3) is being produced. For example, in the second mode, nitric acid can be produced using the nitric acid (HNO3) generation process 500.

[0034] In various embodiments, individual SMRs can operate in various modes. For example, one SMR may operate in a steam generation mode used for nitric acid (HNO3) production, while another SMR operates in a power generation mode to power the system together with the nitric acid (HNO3) production-oriented SMR and / or power one or more other plants / systems / components. Additionally or alternatively, one of the SMRs may generate both power and steam. SMRs may be switched from one mode to another and / or used interchangeably and / or in conjunction with each other.

[0035] In some examples, one or more parts of the power plant 102 and / or resource generation plant 104 can be controlled based on one or more operating / control modes of various types used in the power plant 102 (e.g., in the SMR). The SMR can be controlled in modes to generate different types (e.g., levels) of power and / or steam. The types of power and / or steam can be used for different purposes and / or applications. For example, the types of power and / or steam can be used, based on their respective modes, to provide a specific amount of power to an electrolytic cell, to deliver a specific amount of steam to the resource generation plant 104, to provide a specific amount of power to one or more other plants / systems, to deliver a specific amount of steam to one or more other plants / systems, or any combination thereof.

[0036] In various embodiments, the power plant 102 and the resource generation plant 104 (e.g., a hydrogen generation subplant 106, a nitrogen generator 108, an ammonia generation subplant 110, a nitric acid (HNO3) generation subplant 112, and / or one or more other plants / systems of IES 100), and optionally one or more other plants / subplants / systems / subsystems configured to utilize nitric acid (HNO3), can be located on the same site. For example, any of the plants / subplants / systems / subsystems of the generation plant can be located in the same place (e.g., within a threshold distance of each other). Any of the plants / subplants / systems / subsystems of the generation plant can be fully integrated and / or interconnected with each other.

[0037] Production plants using the techniques discussed herein offer many advantages over plants / systems operating by conventional technologies. Conventional plants / systems utilizing nitric acid (HNO3) have relatively significant inefficiencies and operating costs due to the required safety measures and / or operational constraints / limitations. Plants / systems used for the production of electricity, steam, and / or nitric acid (HNO3) by conventional technologies must be physically separated from each other. Existing systems that produce nitric acid (HNO3) often require the transport of nitrogen from nitrogen production facilities / suppliers over long distances between different countries and / or regions of the world. Existing systems that produce nitric acid (HNO3) require natural gas to generate nitric acid (HNO3). Existing nitric acid (HNO3) production facilities do not have the capacity to produce hydrogen for the purpose of generating nitric acid (HNO3). Existing nitric acid (HNO3) production facilities also require the transport of oxygen.

[0038] In contrast to existing systems, the production plants using the techniques discussed herein do not require resources (such as nitrogen and oxygen) to be transported between plants. The production plants using the techniques discussed herein can be integrated and / or interconnected. The production plants, which can be field plants operating via on-grid or off-grid operation, can be self-sufficient and compact. The production plants may comprise a single hydrogen, oxygen, ammonia, and nitric acid (HNO3) production plant.

[0039] The production plant obtains resources such as hydrogen and oxygen from air and water, and can utilize these resources for nitric acid (HNO3) production. Nitric acid (HNO3) can be produced by the production plant without the need for natural gas input. The production plant can be customized to produce nitric acid (HNO3) at any specified concentration as desired. The integrated and / or combined plant / system of the production plant can be used to efficiently, cost-effectively, and safely produce electricity, steam, and / or nitric acid (HNO3) without carbon emissions. No carbon dioxide is emitted by the production plant. By avoiding the transport of various resources (nitrogen, oxygen, etc.), the production plant using the techniques discussed herein also eliminates pollution caused by vehicle emissions that would otherwise occur due to the operation of existing systems.

[0040] Figure 2 depicts a block diagram showing an example hydrogen production process 200 for generating hydrogen gas, according to at least some embodiments. In some cases, the hydrogen production process 200 may include the hydrogen production subplant 106 shown in Figure 1. In some cases, the hydrogen production process 200 generates hydrogen gas using steam and electricity generated by a power plant 102. For example, in an exemplary process for generating H2, the steam may be supplied at 30.33 bar (440 psia) and 280°C (537°F). In such a case, the power plant 102 may be located at some distance (e.g., 1 km) from the hydrogen production subplant 10. Thus, the steam may be supplied via at least one supply pipe that is insulated to maintain suitable steam conditions.

[0041] In the exemplary hydrogen production process 200, steam is received and initially supplied to the desuperheater component 202 in order to return the superheated steam to its saturated state. Specifically, the steam is first supplied to the high-pressure desuperheater component. The steam exiting the high-pressure desuperheater component is suppressed to 8.34 bar (121 psia). This steam enters a separator to collect and discharge any condensates. The condensates are discharged to a condensate collection tank 204 and supplied to be returned to the power plant 102 (e.g., via a water treatment plant). The suppressed steam then enters a low-pressure desuperheater. In the hydrogen production process 200, the steam exiting the low-pressure desuperheater will be close to its saturation temperature.

[0042] During the hydrogen production process 200, the condensate collection tank 204 should be started with enough water to support H2 production. The water level in the condensate collection tank 204 should be maintained at approximately 50% of its capacity. During operation, the tank is maintained at a specific pressure, e.g., 7 bar (101.5 psia), and a control valve is used to discharge the tank to maintain that level. If the tank level exceeds a high set value, two condensate transfer pumps may be used to assist in discharging the tank. One or more of these pumps may be automatically started when the water level in the condensate collection tank 204 exceeds a first threshold capacity. In such cases, the pumps may also be automatically stopped when the water level in the condensate collection tank 204 falls below a second threshold capacity.

[0043] The steam from the desuperheater component 202 enters the steam generator (boiler) 206. The steam generator 206 is configured to regulate the steam to provide steam to downstream process components at a specific pressure and / or temperature. For example, the steam generator 206 may provide steam at 5.17 bar (75 psia) and 228°C (442°F). The steam generator 206 supplies steam to the H2 mixing chamber 212.

[0044] In some embodiments, H2 gas is drawn from the condensate collection tank 204 by a fuel recycling compressor 208 and transferred to a fuel low-heat recuperator 210. The fuel recycling compressor 208 should be operational when the hydrogen production process 200 is initiated. During the hydrogen production process 200, the outlet valve can be adjusted to control the recycled fuel flow and maintain the H2 and vapor concentrations entering the downstream electrolytic separator 220 at a volume ratio of 50 / 50. The H2 gas transferred by the fuel recycling compressor 208 enters the fuel low-heat recuperator 210. The H2 gas may be heated (via heat exchange) by the "hot side" gas being transported to the condenser.

[0045] H2 gas exiting the fuel low-heat recuperator 210 enters the H2 mixing chamber 212. In the hydrogen production process 200, the mixture of steam and H2 is controlled to maintain a ratio of 50 vol% steam and 50 vol% H2. A steam flow control valve is used to allow steam from the steam generator 206 to be introduced in order to maintain this concentration. In local control, the steam flow setpoint can be calculated based on the amount of H2 flow entering the H2 mixing chamber 212 (for example, to maintain an H2 concentration of 50 vol%). The setpoint can also be used to maintain a minimum level of steam flow.

[0046] The steam bypass valve 214 is used to control the steam pressure in the H2 mixing chamber 212. During module startup, the steam generator 206 pressurizes the steam to 5.2 bar (75.5 psia), and the steam flow is bypassed to the condenser 216 using the bypass control valve 214. When the hydrogen production process 200 is running, the pressure setpoint for the bypass control valve 214 can then be increased to allow the bypass control valve 214 to close during this operation. This also allows the bypass control valve 214 to function as a pressure relief valve / steam overflow control.

[0047] A mixture of steam and H2 is supplied to the fuel high-temperature recuperator 218 by an H2 mixing chamber 212. In some embodiments, the steam and H2 mixture is heated (via heat exchange) by a "high-temperature side" gas leaving one or more electrolytic separators 220 which are being transported to a condenser 216. The steam and H2 mixture then enters an electric heater. The electric heater has a variable heat output and is used to control the temperature of the mixture to a specific temperature, for example, 750°C (1382°F). If the temperature of the mixture exceeds a high setpoint threshold, for example, 788°C (1450°F), the heater will be turned off. The electric heater of the fuel high-temperature recuperator 218 should only be operating if there is flow passing through it.

[0048] The mixture of vapor and H2 emanating from the electric heater of the fuel high-temperature recuperator 218 then enters one or more electrolytic separators 220. A processor for the electrolytic separators 220 can calculate the electrochemistry based on one or more detected conditions of the vapor and H2 mixture. As mentioned elsewhere, one or more detected conditions of the vapor and H2 mixture can be determined based on information obtained using sensors connected to various components. For example, such sensors can obtain information about temperature, pressure, and / or voltage related to the mixture.

[0049] The oxygen (e.g., O2) produced in this manner can be stored and / or used in downstream systems. In some cases, O2 is combined with another element to produce an oxide that can be used in fuel cells, such as solid oxide fuel cells (SOFCs). Such fuel cells can later be used to generate electricity through the oxidation of a fuel (e.g., H2 gas produced via process 200).

[0050] In the hydrogen production process 200, vapor (H2O) is dissociated into hydrogen and oxygen molecules. In some cases, this may involve the use of a high-temperature steam electrolysis (HTSE) process. HTSE cells are highly efficient when the input vapor temperature is maintained at 700–850°C. Figure 3 is a schematic diagram of a typical HTSE electrolytic separator where the inlet vapor temperature is maintained at 700–850°C. Referring to Figure 3, a typical HTSE cell is a solid-state construct (ceramic and metal) with a high operating temperature. The combination of these features leads to several unique and attractive attributes, including flexibility in cell and stacking designs, multiple manufacturing options, and the selection of multi-fuel capabilities. Hydrogen molecules remain on the fuel side of the electrolytic separator 220, while oxygen molecules are pulled through the cell ceramic. The mass flow exiting from the fuel side will be smaller than the mass flow entering. Additionally, the vapor and H2 mixture entering the electrolytic separator 220 has a 50 / 50 ratio, while the vapor and H2 mixture exiting the electrolytic separator 220 is 75% by volume of H2.

[0051] The steam and H2 mixture exits the electrolytic separator 220 and enters the "high-temperature side" of the fuel high-temperature recuperator 218. As described above, heat is exchanged between this steam and H2 mixture (i.e., the 75% H2 mixture) and the steam and H2 mixture exiting the H2 mixing chamber 212 (i.e., the 50 / 50 mixture). Thus, the 75% H2 mixture is cooled and then enters the "high-temperature side" of the fuel low-temperature recuperator 210. As described above, heat is then exchanged between this steam and H2 mixture and the H2 gas exiting the fuel low-temperature recuperator 210, further cooling the steam and H2 mixture. The steam and H2 mixture is then supplied to the condenser 216.

[0052] The condenser 216 condenses the water in the vapor and H2 mixture into a liquid form, which is then discharged into the condensate collection tank 204. Once the vapor in the mixture has condensed into water, the remaining volume of gas will be approximately 100% H2. The H2 gas exiting the condenser 216 can be pumped to the hydrogen storage tank 222. The H2 gas stored in the hydrogen storage tank 222 can then be consumed by another entity (for example, by the ammonia production subplant 110 for the production of ammonia).

[0053] In one embodiment, the H2 gas stored in the hydrogen storage tank 222 is stored at 689+ bar (10,000+ psia). When consumed during the ammonia production process, the hydrogen may be allowed to be introduced through an expansion tank to reduce its pressure to a usable level (e.g., expand), for example, 60-180 bar. In such an embodiment, a flow control valve is used to control the flow from the outlet of the H2 expander to the inlet of the fuel low-heat recuperator 210.

[0054] The inter-stage control valve of the H2 expander can be used to control the downstream hydrogen storage tank to store H2 gas at 6.9 bar (100 psia). Each stage of the expansion tank has an inlet valve and a bypass valve. As the pressure in the hydrogen storage tank decreases, the compressor's inlet stage descends in stages. The upstream stage inlet valve closes, and the new inlet stage bypass opens.

[0055] In this embodiment, each of the numerous stages in the expansion tank has an electric heater to maintain the temperature between the stages. As the H2 pressure continues to decrease (e.g., due to expansion), there is a significant temperature drop. Therefore, the heater maintains the temperature between the stages at 40°C (104°F).

[0056] Figure 4 depicts a block diagram showing an example ammonia production process 400 according to at least some embodiments. In some cases, the ammonia production process 400 may include the ammonia production subplant 110 shown in Figure 1. According to embodiments of the art, the ammonia production process 400 can produce ammonia by a chemical principle that achieves the function of combining hydrogen with nitrogen drawn from the ambient air to form ammonia. For example, the ammonia production process 400 may include a Haber-Bosch process.

[0057] The ammonia generation process 400 may include a nitrogen generator 402 that extracts nitrogen gas (N2) from ambient air. The nitrogen generator 402 may include nitrogen generator 108 in Figure 1 and nitrogen generator 608 in Figure 6. In embodiments, the nitrogen generator 402 is configured to receive air from the environment. The nitrogen generator 402 may include a duct configured to receive air. The nitrogen generator 402 may further include a fan, compressor, pump, vacuum, or other method of creating a pressure difference to move ambient air through the duct to the nitrogen generator 402 for processing. The nitrogen generator 402 may include a pressure swing adsorption (PSA) system, a membrane system, and / or a cryogenic system for generating nitrogen. In this disclosure, the terms “extract,” “generate,” “capture,” “separate,” and their equivalents may be used interchangeably to describe processes for generating N2 from air, which are described in more detail below.

[0058] A PSA system can consist of multiple columns filled with carbon molecular sieves (CMS). Compressed air enters the bottom of the column and flows upward through the CMS. Oxygen and other trace gases are preferentially adsorbed by the CMS, allowing nitrogen to pass through. After a preset time, the column automatically switches to regeneration mode, allowing contaminants to be released from the CMS. The CMS differs from ordinary activated carbon because it has a much narrower range of pore openings. This allows small molecules such as oxygen to penetrate the pores and separate from nitrogen molecules that are too large to enter the CMS. Larger nitrogen molecules bypass the CMS and emerge as nitrogen gas.

[0059] Membrane systems are constructed to separate compressed air through a hollow fiber membrane. Such membrane systems work by forcing compressed air into a container that selectively allows oxygen, water vapor, and other impurities to pass through its sidewalls. Nitrogen flows through the center and emerges as a gas. Membrane systems may be easier to operate and have lower operating costs than PSA and cryogenic systems.

[0060] The cryogenic system begins by drawing atmospheric air into an air separation unit. The air is compressed in a compressor, and its components are separated by fractional distillation. The air is then moved through a cleanup system where impurities such as hydrocarbons, moisture, and carbon dioxide are removed. Next, the air is directed to a heat exchanger and liquefied at cryogenic temperatures. At this stage, the air enters a high-pressure distillation column, where nitrogen is physically separated from oxygen and other gases. The nitrogen thus formed is recovered and placed in a low-pressure distillation column, where it is distilled until it meets commercial specifications.

[0061] In general, the nitrogen generator 402 may require a considerable amount of energy to operate. In embodiments, the nitrogen generator 402 may be configured to receive electricity from a power plant system, such as the power plant 102 in Figure 1 or the power plant system 750 in Figure 7. In some aspects of the art, the power plant system can flexibly and reliably deliver carbon-free electricity to the nitrogen generator 402. The generated nitrogen gas may be supplied to a storage unit, such as a tank, cylinder, pressurized vessel, or similar. The generated nitrogen gas may be supplied directly to a downstream process or from a storage unit to a downstream process. In embodiments, the nitrogen gas generated by the nitrogen generator 402 is supplied to an ammonia production subplant 110.

[0062] In one embodiment, the ammonia production subplant 110 receives nitrogen and hydrogen to produce ammonia (NH3). For example, the ammonia production process 400 uses a Haber-Bosch process to convert hydrogen and nitrogen into ammonia. Nitrogen and hydrogen may be supplied separately to the ammonia production subplant, or the two gases may be combined in a mixed supply flow. The supply flows of nitrogen and hydrogen may be mixed before or after entering the ammonia production subplant 110. The nitrogen gas and hydrogen may be configured to be the same or nearly the same pressure for combining in the supply flow. Hydrogen may be received from a hydrogen production process such as the hydrogen production subplant 106, and nitrogen may be received from a nitrogen production process such as the nitrogen generator 402. In one embodiment, the ammonia production subplant 110 receives nitrogen from the nitrogen generator 402.

[0063] The ammonia production process 400 includes an ammonia synthesis reactor 404 capable of converting hydrogen and nitrogen into ammonia. The primary reaction carried out by the ammonia synthesis reactor 404 is represented by Equation 1 shown below.

number

[0064] The ammonia synthesis reactor 404 operates at high temperature and high pressure. The operating temperature can be in the range of 300 to 500°C (572 to 932°F), and the operating pressure can be in the range of 60 to 180 bar. The nitrogen and hydrogen gas supply flows can be pressurized to the operating pressure before entering the ammonia synthesis reactor 404 by, for example, one or more compressors 406. The compressors 406 may be configured to operate in a steady state and may include dynamic compressors such as turbo compressors, axial flow compressors, centrifugal compressors, or mixing compressors. The nitrogen and hydrogen gas supply flows can be heated to the operating temperature before entering the ammonia synthesis reactor 404 by, for example, one or more preheating heaters 408. The preheating heaters 408 may be configured to operate in a steady state. The preheating heaters 408 may be configured to transfer heat from one or more high-temperature sources to the nitrogen and hydrogen gas supply flows. The high-temperature supply source may include steam such as steam from the power plant 102, high-temperature process flows within the ammonia production process 400 such as reactor product flow leaving the ammonia synthesis reactor 404, or high-temperature process flows from other processes, such as other processes within the resource production plant 104. The preheating heater 408 may also be configured to heat the nitrogen and hydrogen gas supply flows using an electric heater. The power plant 102 may be configured to supply electricity to the electric heater.

[0065] The ammonia synthesis reactor 404 may include at least one catalyst. The catalyst may include any compound or material suitable for synthesizing ammonia, such as iron (Fe), ruthenium (Ru), and osmium (Os). For example, the catalyst may include at least one iron catalyst. The iron (Fe) catalyst may include pulverized iron bound to an iron oxide support such as magnetite, and may include one or more co-catalysts, including potassium oxide (K2O), calcium oxide (CaO), silicon dioxide (SiO2), aluminum oxide (Al2O3), potassium hydroxide (KOH), molybdenum (Mo), and magnesium oxide (MgO).

[0066] The product flow leaving the ammonia synthesis reactor 404 contains the ammonia produced in the reactor 404, and may also contain some unreacted nitrogen and hydrogen gas. The resulting ammonia can be separated from the residual hydrogen and nitrogen gas to produce pure ammonia products. Since the boiling point of ammonia gas is significantly higher than that of hydrogen and nitrogen gas, ammonia can be separated from nitrogen and hydrogen by lowering the temperature of the reactor product flow to below the boiling point of ammonia, resulting in the condensation of ammonia gas into the liquid phase. The reactor product flow leaves the ammonia synthesis reactor 404 at operating temperature and pressure. The reactor product flow may pass through one or more heat exchangers 410 to reduce the temperature of the reactor product flow and recover heat from the product flow. One or more heat exchangers 410 may include preheating heaters 408. The reactor product flow can be fed from one or more heat exchangers 410 to a condenser 412 to separate the ammonia products from residual hydrogen and nitrogen. The condenser 412 may operate at the same or approximately the same pressure as the ammonia synthesis reactor 404, and at that pressure may cool the reactor product flow below the boiling point of ammonia, condense the ammonia, and separate it from the hydrogen and nitrogen gases. In other embodiments, the separation of ammonia may include an absorption-enhanced Haber-Bosch process, which may include an absorption, such as a metal halide or zeolite. The separated ammonia product may be supplied to a storage unit such as a tank, cylinder, pressurized vessel, or similar. In some cases, the separated ammonia may be supplied directly to a downstream process or from a storage unit to a downstream process. In embodiments, the ammonia produced by the ammonia production process 400 is supplied to a nitric acid (HNO3) subplant 112.

[0067] The residual hydrogen and nitrogen gas separated from the ammonia products in the condenser 412 can be recycled by being supplied back to the ammonia synthesis reactor 404. The recycled hydrogen and nitrogen flow can be compressed to operating pressure, for example, by a compressor 414. The recycled flow can then be mixed with the hydrogen and nitrogen supply flow at operating pressure before entering the preheating heater 408. Alternatively, the recycled flow can be supplied to the ammonia synthesis reactor 404 separately from the supply flow after passing through one or more compressors 414 and / or preheating heaters to reach operating temperature and pressure.

[0068] The ammonia production process 400 should not be limited to the embodiment shown in Figure 4 or the embodiments described above. Determining the preferred reaction conditions for the ammonia synthesis reactor 404, as well as the process configuration of the heat exchanger, compressor, and process flow, is within the capabilities of those skilled in the art, based on the needs of those skilled in the art. Unless otherwise claimed, it should be understood that variations of the described process that achieve the same final result should be considered equivalent to process 400. For example, as discussed throughout this disclosure, various pressures / temperatures may be used for various operations, but are not limited thereto. In some cases, other pressures / temperatures suitable for each operation may be used in a similar manner for the purpose of performing the techniques discussed herein.

[0069] Figure 5 is an exemplary schematic diagram showing an example of a nitric acid (HNO3) production process 500 configured to produce nitric acid (HNO3). The nitric acid (HNO3) production process 500 may include a nitric acid (HNO3) production subplant 112. According to embodiments of the present technology, the nitric acid (HNO3) production process 500 can produce nitric acid (HNO3) by a chemical principle that achieves the function of converting ammonia to nitric acid (HNO3). For example, the nitric acid (HNO3) production process 500 may include the Ostwald process. The overall reaction for the production of nitric acid (HNO3) by the Ostwald process can be represented by Equation 2 shown below.

number

[0070] The first step of the Ostwald process involves the oxidation of ammonia to nitric oxide (NO). The nitric acid (HNO3) production process may include a primary oxidation chamber 502 for the oxidation of ammonia to nitric oxide. The primary oxidation reaction takes place in the presence of catalyst 504 and can be represented by equation 3 shown below.

number

[0071] Ammonia can be oxidized by heating with oxygen in the presence of one or more catalysts 504 that support the conversion of ammonia to nitric oxide. Catalysts 504 may include, for example, at least one of platinum gauze catalysts such as rhodium-platinum (Pt-Rh) gauze, copper catalysts, or nickel catalysts. The oxidation of ammonia is a reversible and exothermic reaction. Therefore, according to Le Chatelier's principle, a decrease in temperature favors a forward reaction, so that the exothermic reaction continues as long as both ammonia gas and oxygen are supplied to the reaction chamber. Operating conditions for the primary oxidation chamber 502 include a pressure of 4–10 standard atmospheres (405–1,013 kPa; 59–147 psi) and a temperature of about 870–1,073 K (600–800 °C; 1,110–1,500 °F). These conditions can contribute to an overall yield of about 98%.

[0072] In some embodiments, ammonia, such as that produced by the ammonia production process 400, is supplied to the primary oxidation chamber 502 at the operating temperature and pressure of the primary oxidation chamber 502. An oxidizing agent, which may contain a portion of oxygen, is also supplied to the primary oxidation chamber 502. The oxidizing agent may include, for example, pure oxygen gas, such as oxygen separated from hydrogen in the electrolytic separator 220 of the hydrogen production process 200. In some cases, the oxidizing agent includes air, or a combination of air and pure oxygen. In some embodiments, 1 volume of ammonia and 8 volumes of oxygen are introduced into the primary oxidation chamber. The ammonia and oxidizing agent may be combined in a single supply flow before entering the primary oxidation chamber 502. In some cases, the ammonia and oxidizing agent may be supplied to the primary oxidation chamber 502 separately. The supply flow of ammonia and oxidizing agent may be heated to the operating temperature by one or more preheating heaters before entering the primary oxidation chamber 502. The preheating heaters may be configured to operate in a steady state. The preheating heaters may be configured to transfer heat from one or more high-temperature sources to the ammonia and oxidizing agent supply flow. The high-temperature supply source may include steam such as steam from the power plant 102, high-temperature process flows within the nitric acid (HNO3) production process 500 such as primary chamber product flow leaving the primary oxidation chamber 502, or high-temperature process flows from other processes, such as other processes within the resource production plant 104. The preheating heater may also be configured to heat the ammonia and oxidizer supply flows using an electric heater. The power plant 102 may be configured to supply electricity to the electric heater.

[0073] The supply flow of ammonia and oxidizer can be pressurized to the operating pressure by one or more compressors before entering the primary oxidation chamber 502. The compressors may be configured to operate in a steady state and may include dynamic compressors such as turbo compressors, axial flow compressors, centrifugal compressors, or mixing compressors. In the primary oxidation chamber 502, ammonia is oxidized in the presence of catalyst 504 to produce nitric oxide (NO). For example, at an operating temperature of about 600°C and in the presence of a platinum gauze catalyst, 95% of the ammonia can be converted to nitric oxide (NO) in the primary oxidation chamber 502.

[0074] The primary chamber product flow exits the primary oxidation chamber 502 and is cooled to approximately 150°C. The primary chamber product flow may enter a cooling chamber 506. The cooling chamber 506 may be equipped with one or more heat exchangers and may be configured to recover heat from the primary chamber product flow, for example, by exchanging heat with the ammonia and oxidant feed flow. The primary chamber product flow contains unreacted ammonia and oxidant, oxygen (O2), and the generated nitric oxide (NO) and vapor (H2O).

[0075] Upon cooling, the primary chamber product flow may be supplied to the secondary oxidation chamber 508, where NO in the primary chamber product flow may be oxidized to nitrogen dioxide (NO2) by oxygen (O2). The oxidizing agent is pure oxygen gas, such as oxygen separated from hydrogen in the electrolytic separator 220 of the hydrogen production process 200. In some cases, the oxidizing agent can be air, or a combination of air and pure oxygen. Nitric oxide is oxidized to NO2 in the secondary oxidation chamber 508 at approximately 50°C and by the reaction represented by Equation 4 shown below.

number

[0076] The secondary chamber product stream exits from the secondary oxidation chamber 508. The secondary chamber product stream contains nitrogen dioxide (NO2) produced in the secondary oxidation chamber 508, as well as unreacted nitric oxide (NO) and oxygen (O2). The secondary chamber product stream may also contain unreacted products from the primary chamber product stream, such as H2O, and reaction byproducts.

[0077] The secondary chamber product stream can be introduced into absorption column 510, where nitrogen dioxide produced in secondary oxidation chamber 508 is converted to nitric acid (HNO3). Nitric acid (HNO3) is obtained from the absorption of NO2 gas in H2O by the reaction represented by equation 5 shown below.

number

[0078] The absorption column 510 may comprise one or more packed column or plate column absorption towers. The tower may comprise a non-reactive quartz bed 516. In the absorption column 510, NO2 gas is bubbling through the quartz bed 516 and water 512. Water 512 may be sprayed onto the quartz bed 516 and the rising NO2 gas by a water dispersion device 514. The gas is removed from the absorption column 510 in one or more streams. One or more gas streams include unreacted NO2 gas, nitric oxide (NO) formed in the absorption reaction of NO2 and H2O, unreacted components supplied to the absorption column 510 from the secondary oxidation chamber 508, and reaction byproducts. At least one gas stream exiting the absorption column 510 may be recycled by being returned to the absorption column 510 to improve NO2 absorption. At least one gas stream exiting the absorption column 510 may be considered waste and sent for waste gas treatment.

[0079] The nitric acid (HNO3) produced by absorption in the absorption column 510 can be highly diluted in water. HNO3 can be produced using water 512 at any specified concentration. For example, the nitric acid (HNO3) production process 500 can be controlled to output HNO3 at one concentration, then at another concentration, and so on. The aqueous HNO3 solution can be removed from the absorption column 510 and concentrated by distillation, for example, by extractive distillation. Distillation of the aqueous HNO3 solution can produce HNO3 concentrated to a maximum of approximately 68% by mass.

[0080] Further concentration of an aqueous HNO3 solution can be achieved by dehydration with concentrated sulfuric acid (H2SO4). Concentrated sulfuric acid (H2SO4) is a dehydrating agent and can therefore absorb water from the aqueous HNO3 solution. To increase the concentration of HNO3, HNO3 vapor can be passed over concentrated H2SO4, and concentrated HNO3 up to 98% can be obtained. The generated nitric acid (HNO3) can be supplied to a storage unit such as a tank, cylinder, pressurized vessel, or similar. The generated nitrogen gas (N2) can be supplied directly to a downstream process for further use, or supplied from the storage unit to a downstream process. For example, the generated nitric acid (HNO3) can be converted to ammonium nitrate (NH4NO3), which can then be used in agriculture as a high-nitrogen fertilizer.

[0081] The nitric acid (HNO3) production process 500 should not be limited to the embodiment shown in Figure 5 or the embodiments described above. Determining suitable reaction conditions and catalysts for the conversion of ammonia (NH3) to nitric acid (HNO3), and determining the precise configuration of the reactor, heat exchanger, compressor, and process flow, is within the capabilities of those skilled in the art, based on the needs of those skilled in the art. Unless otherwise claimed, it should be understood that variations of the described process that achieve the same final result should be considered equivalent to process 400.

[0082] Figure 6 is a schematic diagram of an integrated energy system 600, including the power plant system 750 of Figure 7, according to an additional embodiment of the present technology. In the exemplary embodiment, the integrated energy system 600 is configured to produce "green" hydrogen (H2), oxygen (O2), nitrogen (N2), and ammonia (NH3) for use in producing "green" nitric acid (HNO3). Specifically, the power plant system 750 generates electricity and routes it to one or more water generating plants 602, one or more auxiliary heaters 604, one or more hydrogen (H2) and oxygen (O2) generating plants 606, one or more nitrogen (N2) generators 608, one or more ammonia (NH3) generating plants 610, and one or more nitric acid (HNO3) generating plants 612. In some embodiments, the power plant system 750 can further route the electricity (e.g., excess electricity) to a power grid 680. The power plant system 750 further generates steam and routes the steam to an auxiliary heater 604.

[0083] The power plant system 750 may be a permanent or temporary installation constructed at or near the location of the water generation plant 602, the auxiliary heater 604, the hydrogen (H2) and oxygen (O2) generation plants 606, the nitrogen (N2) generator 608, the ammonia (NH3) generation plant 610, and / or the nitric acid (HNO3) generation plant, or it may be a mobile or partially mobile system that is moved and assembled at or near the location of the various components. More generally, the power plant system 750 may be local to the industrial process / operation it supports (e.g., located there or near there). For example, the power plant system 750 may be located within 0.4 km (0.25 miles), 0.8 km (0.5 miles), 3.22 km (2 miles), 4.82 km (3 miles), or 8.1 km (5 miles) of the industrial process / operation it supports. In some embodiments, the power plant system 750 comprises four, six, twelve, or a different number of reactors 700 (Figure 7) and has a power output of 308 to 924 megawatts (MWe). In some embodiments, the power plant system 750 can output approximately 308 to 924 MWe and approximately 1000 to 3000 megawatts (MWt) of heat.

[0084] The water generation plant 602 is configured to produce high-quality water and route the produced high-quality water to the integrated energy system 600. The high-quality water can be routed, for example, to the hydrogen (H2) and oxygen (O2) generation plant 606, the power generation plant system 750, and / or the nitrate (HNO3) generation plant 612.

[0085] In some embodiments, the hydrogen and oxygen production plant 606 can (i) produce hydrogen (H2) and oxygen (O2) using a high-temperature steam electrolysis (HTSE) process utilizing high-quality, high-temperature steam generated by an auxiliary heater 604, and / or (ii) produce hydrogen (H2) and oxygen (O2) using a low-temperature steam electrolysis (LTSE) process utilizing high-quality water generated by a water production plant 602. In embodiments, the hydrogen (H2) and oxygen (O2) production plant 606 may include a hydrogen (H2) production subplant 106 and a hydrogen production process 200.

[0086] In some cases, the power plant system 750 can use high-quality water to produce high-quality steam. For example, the produced water can be used as a secondary coolant in one or more steam generators of the reactor 700. In certain embodiments, the nitric acid (HNO3) production plant 612 can use high-quality water as a reagent in the production of nitric acid (HNO3).

[0087] The water generation plant 602 may be a water treatment plant, a desalination plant, and / or similar, and may be configured to produce high-quality water. For example, the water generation plant 602 may operate to desalinate a water source and / or remove contaminants and / or unwanted materials from the water source. The water generation plant 602 may include, for example, reverse osmosis, electrodialysis, distillation, desalination, deionization, filtration, ultrafiltration, and / or nanofiltration. In general, the water purification plant 602 may require a considerable amount of energy to operate. In some embodiments of this technology, the power generation plant system 750 can flexibly and reliably deliver carbon-free electricity to the water generation plant 602.

[0088] The nitrogen (N2) generator 608 can receive air and use electricity from the power plant system 750 to separate / capture nitrogen (N2) from the air. For example, the nitrogen generator 608 may be equipped with a pressure swing adsorption (PSA) system, a membrane system, and / or a cryogenic system for generating nitrogen (N2). In general, the nitrogen (N2) generator 608 may require a considerable amount of energy to operate. In some aspects of this technology, the power plant system 750 can flexibly and reliably deliver carbon-free electricity to the nitrogen generator 608. The nitrogen (N2) generator 608 may include, for example, a nitrogen (N2) generator 108 and a nitrogen (N2) generator 402.

[0089] The ammonia (NH3) production plant 610 can receive hydrogen (H2) from the hydrogen (H2) and oxygen (O2) production plant 606 and nitrogen (N2) from the nitrogen (N2) generator 608, and use the hydrogen (H2) and nitrogen (N2) to produce ammonia (NH3). For example, the ammonia (NH3) production plant 610 can perform a Haber-Bosch process to convert hydrogen (H2) and nitrogen (N2) into ammonia (NH3). The ammonia (NH3) production plant 610 may include, for example, an ammonia (NH3) production subplant 110.

[0090] The nitric acid (HNO3) production plant 612 can generate nitric acid (HNO3) using the Ostwald process, for example, as described above and shown in Figure 5, by (i) receiving hydrogen (H2) and oxygen (O2) from the hydrogen (H2) and oxygen (O2) production plant 606, (ii) receiving ammonia (NH3) from the ammonia (NH3) production plant 610, (iii) receiving water from the water production plant 602, and (iv) receiving electricity from the power plant system 750.

[0091] In some aspects of this technology, the integrated energy system 600 can produce nitric acid (HNO3) in a highly efficient manner while producing little to no carbon emissions. In particular, each stage of hydrogen (H2), nitrogen (N2), oxygen (O2), ammonia (NH3), and water (H2O) production can be powered using electricity and / or steam from a carbon-free nuclear energy power plant system 750. In contrast, conventional systems for producing hydrogen (H2) for nitric acid (HNO3) production typically rely on steam-methane reforming processes that produce significant carbon emissions. Similarly, processes for producing nitrogen (N2) for ammonia (NH3) production are energy-intensive and typically rely on energy from the combustion of fossil fuels, which produces even more significant carbon emissions. Therefore, this technology makes it possible to produce "green" nitric acid (HNO3) by using sustainable nuclear energy sources and green production means. Furthermore, the power plant system 750 can be controlled to selectively supply electricity and / or steam to various components of the integrated energy system 600 based on their requirements, operating conditions, and / or similar, as described in detail in this application and as shown in Figure 7 below.

[0092] In some embodiments, the integrated energy system 600 may include several features that are at least generally similar in structure and function to, or identical in structure and function to, the corresponding features of the integrated energy system described in detail in U.S. Patent Application No. 18 / 116,819, filed March 2, 2023, titled "SMALL MODULAR NUCLEAR REACTOR INTEGRATED ENERGY SYSTEMS FOR ENERGY PRODUCTION AND GREEN INDUSTRIAL APPLICATIONS," which are incorporated herein by reference in their entirety as Appendix A.

[0093] Figure 7 is a schematic diagram of a nuclear power plant system 750 ("power plant system 750") comprising a plurality of reactors 700 (each individually identified as the 1st to 12th reactors 700a to l) according to an embodiment of the present technology. Each of the reactors 700 may be similar to or identical to the reactor systems 800 and / or reactor systems 900, which are described in detail below with reference to Figures 8 and 9. The power plant system 750 may be "modular" in that each of the reactors 700 may operate independently to provide output such as electricity or steam. In embodiments, the power plant system may comprise small modular reactors (SMRs). The power plant system 750 may comprise fewer than 12 reactors 700 (e.g., 2, 3, 4, 5, 6, 7, 8, 9, 10, or 11 reactors 700) or more than 12 reactors 700. The power plant system 750 may be a permanent installation or it may be mobile (e.g., mounted on a truck, tractor, mobile platform, and / or similar). In the exemplary embodiment, each of the reactors 700 may be located in a common housing 751, such as a reactor plant building, and may be controlled and / or monitored via a control room 752.

[0094] Each of the reactors 700 can be connected to a corresponding power conversion system 740 (each individually identified as the 1st to 12th power conversion systems 740a to l). The power conversion system 740 may include one or more devices that generate electricity or any other form of usable electricity from the steam generated by the reactor 700. For example, the power conversion system 740 may include features similar to or identical to the power conversion system 840 described in detail below with reference to Figure 8. In some embodiments, multiple reactors 700 can be connected to the same power conversion system 740, and / or one or more reactors 700 can be connected to multiple power conversion systems 740 such that there is no one-to-one correspondence between the reactors 700 and the power conversion systems 740.

[0095] The power conversion system 740 may be further connected to a power transmission system 754, for example, via a power bus 753. The power transmission system 754 and / or power bus 753 may include one or more transmission lines, transformers, and / or similar for regulating the current, voltage, and / or other characteristics of the electricity generated by the power conversion system 740. The power transmission system 754 may route the electricity to one or more end uses, such as different electrical loads of an integrated energy system, via multiple electrical output paths 755 (individually identified as electrical output paths 755a to n), as described in more detail below.

[0096] The power plant system 750 can be configured to supply electricity to the water generation plant 602 in a first operating state (for example, via one or more of the electrical output paths 755 from the power transmission system 754). The water generation plant 602 can route the high-quality water it produces to the power plant system 750, which can use the water to generate high-quality steam. For example, the produced water can be used as a secondary coolant in one or more steam generators of the reactor 700. In some embodiments, the water generation plant 602 can be omitted, and the power plant system 750 can utilize water from other sources to generate steam.

[0097] Each of the reactors 700 can be further connected to a steam transfer system 756, for example, via a steam bus 757. The steam bus 757 can route steam generated from the reactors 700 to the steam transfer system 756, which can then route the steam to one or more end uses, such as different steam inputs in an integrated energy system, via a plurality of steam output routes 758 (individually identified as steam output routes 758a to n), as described in more detail below.

[0098] In some embodiments, the reactor 700 can be individually controlled (e.g., via a control room 752) to supply steam to a steam transmission system 756 and / or to a corresponding one of the power conversion systems 740 to supply electricity to a power transmission system 754. In some embodiments, the reactor 700 is configured to supply steam to either a steam bus 757 or a corresponding one of the power conversion systems 740, and can switch quickly and efficiently between supplying steam to either. Thus, in some aspects of the art, the reactor 700 can be controlled modularly and flexibly so that the power plant system 750 can supply electricity through a power transmission system 754 and / or steam through a steam transmission system 756 at different levels / amounts. For example, if the power plant system 750 is used to supply electricity and steam to one or more industrial processes, such as various components of an integrated energy system described in detail below, the reactor 700 can be controlled to meet the different electrical and steam requirements of the industrial processes.

[0099] As an example, during a first operating state of an integrated energy system using a power plant system 750, a first subset of reactors 700 (e.g., reactors 1 to 6, 700a to f) may be configured to supply steam to a steam transmission system 756 for use in the first operating state of the integrated energy system, while a second subset of reactors 700 (e.g., reactors 7 to 12, 700g to l) may be configured to supply steam to a corresponding power conversion system 740 (e.g., power conversion systems 7 to 12, 740g to l) to generate electricity for the first operating state of the integrated energy system. Subsequently, during a second operating state of the integrated energy system where different (e.g., more or less) amounts of steam and / or electricity are required, some or all of the first subset of the reactor 700 can be switched to supply steam to the corresponding power conversion systems 740 (e.g., the 7th to 12th power conversion systems 740g to l) and / or some or all of the second subset of the reactor 700 can be switched to supply steam to the steam transmission system 756, in order to vary the amount of steam and electricity generated to match the requirements / demands of the second operating state. Other variations in steam and electricity generation are possible based on the needs of the integrated energy system. That is, the reactor 700 can be dynamically / flexibly controlled during other operating states of the integrated energy system to meet the steam and electricity requirements of the operating state.

[0100] In contrast, some conventional nuclear power plant systems can typically generate either steam or electricity for output, and cannot be modularly controlled to provide varying levels of steam and electricity for output. Furthermore, switching between steam and electricity generation is typically difficult (e.g., expensive, time-consuming) in conventional nuclear power plant systems. Specifically, for example, in prototype large-scale nuclear power plant systems, switching between steam and electricity generation is typically extremely time-consuming.

[0101] The reactor 700 can be individually controlled via one or more operators and / or via a computer system. Therefore, many embodiments of the technology described herein may take the form of computer or machine or controller executable instructions, including routines executed by a programmable computer or controller. Those skilled in the art will understand that this technology can be implemented on computer / controller systems other than those shown and described herein. This technology can be embodied in a special-purpose computer, controller, or data processor that is specifically programmed, configured, or constructed to implement one or more of the computer executable instructions described below. Therefore, the terms “computer” and “controller” as used herein refer to any data processor and may include Internet appliances and handheld devices (including palmtop computers, wearable computers, cellular or mobile phones, multiprocessor systems, processor-based or programmable home electronic devices, network computers, minicomputers, and similar). Information handled by these computers may be presented on any suitable display medium, including liquid crystal displays (LCDs).

[0102] This technology can also be implemented in a distributed environment in which tasks or modules are performed by remote processing devices linked through a communication network. In a distributed computing environment, program modules or subroutines may reside in local and remote memory storage devices. Embodiments of the technology described herein may be stored or distributed on computer-readable media, including magnetically or optically readable or removable computer disks, and may be electronically distributed over a network. Specific data structures and data transmissions for embodiments of this technology are also included within the scope of the embodiments of the technology.

[0103] Figures 8 and 9 show typical reactors that may be included in embodiments of the present technology. Figure 8 is a partial schematic, partial cross-sectional view of a reactor system 800 configured according to embodiments of the present technology. System 800 may comprise a power module 802 having a core 804 in which controlled nuclear reactions take place. Thus, the core 804 may comprise one or more fuel assemblies 801. The fuel assemblies 801 may include fissile and / or other suitable materials. The heat from the reactions generates steam in a steam generator 830, where the steam is directed to a power conversion system 840. The power conversion system 840 generates power and / or provides other useful outputs such as superheated steam. A sensor system 850 is used to monitor the operation of the power module 802 and / or other system components. Data acquired from the sensor system 850 can be used to control the power module 802 in real time and / or to update the design of the power module 802 and / or other system components.

[0104] The power module 802 then comprises a containment vessel 810 (e.g., a radiation shielding vessel or radiation shielding container) that houses / encloses a reactor vessel 820 (e.g., a reactor pressure vessel or reactor pressure container) that houses the reactor core 804. The containment vessel 810 can be housed in a power module bay 856. The power module bay 856 may include a cooling pool 803 filled with water and / or another suitable cooling fluid. The majority of the power module 802 can be located below the surface 805 of the cooling pool 803. Thus, the cooling pool 803 can act as a heat sink, for example, in the event of a system malfunction.

[0105] The volume between the reactor vessel 820 and the containment vessel 810 can be partially or completely evacuated to reduce heat transfer from the reactor vessel 820 to the surrounding environment (e.g., the cooling pool 803). However, in other embodiments, the volume between the reactor vessel 820 and the containment vessel 810 can be at least partially filled with gases and / or liquids that increase heat transfer between the reactor vessel 820 and the containment vessel 810. For example, the volume between the reactor vessel 820 and the containment vessel 810 can be at least partially filled (e.g., filled with primary coolant 807) during emergency operations.

[0106] Within the reactor vessel 820, the primary coolant 807 carries heat from the core 804 to the steam generator 830. For example, as indicated by the arrows located within the reactor vessel 820, the primary coolant 807 is heated in the core 804 toward the bottom of the reactor vessel 820. The heated primary coolant 807 (e.g., water with or without additives) rises from the core 804 through the core shroud 806 to the riser tube 808. The hot, buoyant primary coolant 807 continues to rise through the riser tube 808 and then exits the riser tube 808 and passes downward through the steam generator 830. The steam generator 830 comprises a number of conduits 832 arranged circumferentially around the riser tube 808, for example in a helical pattern, as schematically shown in Figure 8. The descending primary coolant 807 transfers heat to the secondary coolant (e.g., water) in the conduit 832 and descends to the bottom of the reactor vessel 820, where the cycle is restarted. The cycle can be driven by the change in the buoyancy of the primary coolant 807, thus reducing or eliminating the need for pumps to move the primary coolant 807.

[0107] The steam generator 830 may include a feedwater header 831 into which incoming secondary coolant enters the steam generator conduit 832. The secondary coolant rises through the conduit 832, is converted into vapor (e.g., steam), and collected in the steam header 833. The steam exits the steam header 833 and is directed to the power conversion system 840.

[0108] The power conversion system 840 may include one or more steam valves 842 that regulate the passage of high-pressure, high-temperature steam from the steam generator 830 to the steam turbine 843. The steam turbine 843 converts the thermal energy of the steam into electricity via a generator 844. The low-pressure steam exiting the turbine 843 is condensed in a condenser 845 and then directed to one or more feedwater valves 841 (e.g., via a pump 846). The feedwater valves 841 control the rate at which the feedwater re-enters the steam generator 830 via a feedwater header 831. In other embodiments, the steam from the steam generator 830 can be routed for direct use in industrial processes such as hydrogen and oxygen production plants, chemical production plants, and / or similar, as described in detail in this application. Thus, the steam exiting the steam generator 830 can bypass the power conversion system 840.

[0109] The power module 802 comprises several control systems and associated sensors. For example, the power module 802 may include a hollow cylindrical reflector 809 that returns neutrons into the core 804 to further accelerate the nuclear reaction occurring therein. Control rods 813 are used to regulate the nuclear reaction and are driven via a fuel rod driver 815. The pressure inside the reactor vessel 820 can be controlled via a pressurizer plate 817 by controlling the pressure in a pressurized volume 819 located above the pressurizer plate 817 (this can also function to direct the primary coolant 807 downward through the steam generator 830).

[0110] The sensor system 850 may include, for example, one or more sensors 851 located at various positions within and / or elsewhere in the power module 802 to identify operating parameter values ​​and / or changes in parameter values. The data collected by the sensor system 850 can then be used to control the operation of system 800 and / or generate design changes for system 800. For sensors located within the containment 810, the sensor link 852 directs data from the sensor to the flange 853 (where the sensor link 852 exits the containment 810) and to the sensor junction box 854. From there, the sensor data can be routed via the data bus 855 to one or more controllers and / or other data systems.

[0111] Figure 9 is a partial schematic, partial cross-sectional view of a reactor system 900 ("System 900") configured according to an additional embodiment of the present technology. In some embodiments, System 900 may include several features that are at least generally similar in structure and function to, or identical in structure and function to, the corresponding features of System 800, which are described in detail above with reference to Figure 8, and may operate in a manner generally similar to or identical to System 800.

[0112] In the exemplary embodiments, the system 900 comprises a furnace vessel 920 and a containment vessel 910 surrounding / enclosing the furnace vessel 920. In some embodiments, the furnace vessel 920 and the containment vessel 910 may be approximately cylindrical or capsule-shaped. The system 900 further comprises a plurality of heat pipe layers 911 within the furnace vessel 920. In the exemplary embodiments, the heat pipe layers 911 are spaced apart from each other and stacked. In some embodiments, the heat pipe layers 911 can be mounted / secured to a common frame 912, a portion of the furnace vessel 920 (e.g., its walls), and / or other suitable structures within the furnace vessel 920. In other embodiments, the heat pipe layers 911 can be stacked directly on top of each other such that each heat pipe layer 911 supports and / or is supported by one or more of the other layers of heat pipe layers 911.

[0113] In the exemplary embodiments, the system 900 further includes a shielding or reflector region 914 that at least partially surrounds the core region 916. The heat pipe layer 911 may be circular, linear, polygonal, and / or have other shapes, and as a result, the core region 916 has a corresponding three-dimensional shape (e.g., cylindrical, spherical). In some embodiments, the core region 916 is separated from the reflector region 914 by a core partition 915, such as a metal wall. The core region 916 may include one or more fuel sources, such as fissile material, for heating the heat pipe layer 911. The reflector region 914 may include one or more materials configured to contain / reflect products generated by burning fuel within the core region 916 during the operation of the system 900. For example, the reflector region 914 may include a liquid or solid material configured to reflect neutrons and / or other fission products radially inward toward the core region 916. In some embodiments, the reflector region 914 can completely surround the core region 916. In other embodiments, the reflector region 914 can partially surround the core region 916. In some embodiments, the core region 916 can include control material 917 such as a moderator and / or coolant. The control material 917 can at least partially surround the heat pipe layer 911 within the core region 916 and transfer heat between them.

[0114] In the exemplary embodiments, the system 900 further comprises at least one heat exchanger 930 (e.g., a steam generator) arranged around the heat pipe layer 911. The heat pipe layer 911 may extend at least partially from the core region 916 into the reflector region 914 and be thermally coupled to the heat exchanger 930. In some embodiments, the heat exchanger 930 may be located outside the reflector region 914 or partially within the reflector region 914. The heat pipe layer 911 provides a heat transfer path from the core region 916 to the heat exchanger 930. For example, each heat pipe layer 911 may include an array of heat pipes that provide a heat transfer path from the core region 916 to the heat exchanger 930. When the system 900 is operating, fuel in the core region 916 can heat and vaporize fluids in the heat pipes within the heat pipe layer 911, and the fluids can carry heat to the heat exchanger 930. The heat pipes within the heat pipe layer 911 can then return the fluid toward the core region 916 by suction, gravity, and / or other means of reheating and vaporizing.

[0115] In some embodiments, the heat exchanger 930 may be analogous to the steam generator 830 in Figure 8 and may comprise, for example, one or more helical coil tubes winding around a heat pipe layer 911. The tubes of the heat exchanger 930 contain or can contain a working fluid (a coolant such as water or another fluid) that carries heat from the heat pipe layer 911 out of the furnace vessel 920 and containment vessel 910 for use in generating electricity, steam, and / or the like. For example, in the embodiment shown, the heat exchanger 930 is operably connected to a turbine 943, a generator 944, a condenser 945, and a pump 946. As the temperature of the working fluid in the heat exchanger 930 rises, the working fluid may begin to boil and vaporize. The working fluid (e.g., steam) may be used to drive the turbine 943 and convert the thermal potential energy of the working fluid into electrical energy via the generator 944. The condenser 945 can condense the working fluid after it has passed through the turbine 943, and the pump 946 can direct the working fluid back to the heat exchanger 930, where the working fluid can initiate another thermal cycle. In other embodiments, the steam from the heat exchanger 930 can be routed for direct use in industrial processes such as resource generation plants, as described in detail above. Thus, the steam leaving the heat exchanger 930 can bypass the turbine 943, generator 944, condenser 945, pump 946, etc.

[0116] Figure 10 shows an example process 1000 for producing nitric acid. In various examples, the process can be carried out by an integrated energy system (IES). The IES may include power plants such as power plant 102 and power plant system 750. The IES may also include resource generation plants such as resource generation plant 104. In embodiments, the resource generation plant may include one or more chemical generation plants or subplants. The resource generation plant may include hydrogen generation processes such as a hydrogen (H2) generation subplant 106, a hydrogen generation process 200, and a hydrogen (H2) and oxygen (O2) generation plant 606; nitrogen (N2) generation systems such as a nitrogen (N2) generator 108, a nitrogen (N2) generator 402, and a nitrogen (N2) generator 608; ammonia (NH3) generation processes such as an ammonia (NH3) generation subplant 110, an ammonia (NH3) generation process 400, and an ammonia (NH3) generation plant 610; and nitrate generation processes such as a nitrate generation subplant 112, a nitrate (HNO3) generation process 500, and a nitrate (HNO3) generation plant 612. In embodiments, the hydrogen (H2) generation process, the ammonia (NH3) generation process, and the nitrate (HNO3) generation process are configured to receive electricity from a power plant.

[0117] In 1002, electricity and steam are received from power plants such as power plant 102 and power plant system 750. In embodiments, the power plants generate electricity and steam from nuclear energy. For example, the power plants may include SMRs as described elsewhere in this disclosure. In embodiments, the power plants may be local to resource generation plants. For example, the power plants may be located within 0.4 km (0.25 miles), 0.8 km (0.5 miles), 3.22 km (2 miles), 4.82 km (3 miles), or 8.1 km (5 miles) of the resource generation plants they support. In embodiments, the power plants are configured to supply a portion of the electricity to the power grid.

[0118] In 1004, hydrogen (H2) gas is produced from the steam received in 1002. In embodiments, hydrogen (H2) gas may be produced by hydrogen (H2) production processes such as a hydrogen (H2) production subplant 106, a hydrogen (H2) production process 200, and a hydrogen (H2) and oxygen (O2) production plant 606. In embodiments, the hydrogen (H2) production process may produce oxygen (O2) from the steam received by the power plant. In embodiments, the hydrogen (H2) production process includes electrolysis for separating hydrogen (H2) from oxygen (O2) in the steam.

[0119] In 1006, electricity is received from the power plant, and air is received from the environment. In 1008, nitrogen gas is generated. In the embodiment, electricity from the power plant is used to power nitrogen (N2) generators such as nitrogen generator 108, nitrogen (N2) generator 402, and nitrogen (N2) generator 608. In the embodiment, nitrogen (N2) is configured to receive air from the environment and to extract nitrogen (N2) from the ambient air.

[0120] In 1010, ammonia (NH3) is produced from nitrogen (N2) gas produced in 1008 and hydrogen (H2) gas produced in 1004. In the embodiment, ammonia (NH3) is produced in an ammonia (NH3) production process, such as an ammonia (NH3) production subplant 110, an ammonia (NH3) production process 400, and an ammonia (NH3) production plant 610. In the embodiment, ammonia (NH3) is produced by a Haber-Bosch process.

[0121] In 1012, nitric acid (HNO3) is produced from ammonia (NH3). In the embodiment, nitric acid (HNO3) is produced by nitric acid (HNO3) production processes such as the nitric acid (HNO3) production subplant 112, the nitric acid (HNO3) production process 500, and the nitric acid (HNO3) production plant 612. In the embodiment, nitric acid (HNO3) is produced from oxygen (O2) produced in 1004 and ammonia (NH3) produced in 1010. In the embodiment, nitric acid (HNO3) is produced by the Ostwald process. In the embodiment, process 1000 for producing nitric acid (HNO3) produces nitric acid (HNO3) using only electricity, steam, ambient air, and water.

[0122] conclusion While the above inventions are described in relation to specific embodiments, it should be understood that the scope of the invention is not limited to these specific embodiments. Other modifications and changes adapted to suit specific operating requirements and environments are obvious to those skilled in the art and are therefore not considered to be limited to the embodiments selected for disclosure purposes, but extend to all changes and modifications that do not depart from the true concept and scope of the invention.

[0123] This application describes embodiments having certain structural features and / or methodological actions, but it should be understood that the claims are not necessarily limited to the specific features or actions described. Rather, the specific features and actions are merely illustrative of some embodiments that fall within the scope of the claims.

Claims

1. An integrated energy system (IES), Power plants and From the steam generated by the aforementioned power plant, hydrogen (H ２ ) hydrogen (H ２ ) Production subplant and The hydrogen (H ２ ) is nitrogen (N) drawn from the surrounding air. ２ By combining it with ammonia (NH ３ Ammonia (NH) that produces ) ３ ) Production subplant and The ammonia (NH ３ ), nitric acid (HNO ３ ) is generated from nitric acid (HNO ３ ) generation sub-plant, and an integrated energy system (IES).

2. The integrated energy system (IES) according to claim 1, wherein the power plant generates electricity and steam from nuclear energy.

3. The integrated energy system (IES) according to claim 2, wherein the power plant comprises one or more small modular reactors.

4. The hydrogen (H ２ ) Production subplant, the ammonia (NH ３ ) Production subplant, and the nitric acid (HNO ３ The integrated energy system (IES) according to claim 2, wherein the generating subplant is configured to receive electricity from the power plant.

5. The hydrogen (H ２ The ) generation subplant generates oxygen (O) from the steam produced by the power plant. ２ The integrated energy system (IES) according to claim 1, further generating ).

6. The aforementioned nitric acid (HNO ３ ) The oxygen (O) generation subplant in the Ostwald process ２ ) and the ammonia (NH ３ ) from the nitric acid (HNO ３ The integrated energy system (IES) according to claim 5, which generates ).

7. The hydrogen (H ２ The ) generation subplant generates oxygen (O) in the steam. ２ ) from the hydrogen (H ２ The integrated energy system (IES) according to claim 1, which uses electrolysis to separate )

8. The ammonia (NH ３ The ammonia (NH) generation subplant is produced through the Haber-Bosch process. ３ The integrated energy system (IES) according to claim 1, which generates ).

9. The nitrogen (N) ２ ) is configured to draw nitrogen (N) from the surrounding air. ２ The integrated energy system (IES) according to claim 1, further comprising a generator.

10. Integrated Nitrate (HNO ３ ) A generation system, A power plant configured to receive at least one of electricity and steam from a power plant, and using only the electricity, steam, ambient air, and water to power nitric acid (HNO2). ３ A combined nitrate (HNO) comprising one or more chemical production subplants configured to produce ) ３ ) Generation system.

11. The one or more chemical production subplants described above Hydrogen (H ２ Hydrogen (H) configured to produce ) ２ ) Production subplant and Nitrogen (N ２ Nitrogen (N) configured to produce ) ２ ) Production subplant and The hydrogen (H ２ ) and the nitrogen (N ２ ) from ammonia (NH ３ Ammonia (NH) configured to produce ) ３ ) Production subplant and The ammonia (NH ３ ) from the nitric acid (HNO ３ Nitric acid (HNO) configured to produce ) ３ The integrated nitrate (HNO) according to claim 10, comprising a subplant for generating ) ３ ) Generation system.

12. The integrated nitrate (HNO) according to claim 10, wherein the power plant is configured to generate electricity and steam from nuclear energy. ３ ) Generation system.

13. The integrated nitrate (HNO) according to claim 12, wherein the power plant is local to the one or more chemical production subplants. ３ ) Generation system.

14. The integrated nitrate (HNO) according to claim 12, wherein the power plant is located within 0.4 km, 0.8 km, 3.22 km, 4.82 km, or 8.1 km of one or more chemical production subplants. ３ ) Generation system.

15. The integrated nitrate (HNO) according to claim 14, wherein the power plant comprises one or more small modular reactors. ３ ) Generation system.

16. The integrated nitrate production system according to claim 10, wherein the power plant is configured to supply a portion of the electricity to the power grid.

17. Nitric acid (HNO ３ A method for generating ) Electricity and steam are received from the power plant, and hydrogen (H) is obtained from the steam. ２ ) generating gas, The aforementioned power plant receives electricity, and receives air from the environment, and nitrogen (N) ２ ) generating gas, The hydrogen (H ２ ) gas and the nitrogen (N ２ ) Ammonia (NH ３ ) generates and the ammonia (NH ３ The process of producing nitric acid from ) and including nitric acid (HNO ３ A method for generating ).

18. The nitric acid (HNO) according to claim 17, wherein the power plant generates the electricity and steam from nuclear energy and comprises one or more small modular reactors. ３ A method for generating ).

19. From the electricity and steam from the power plant, oxygen (O ２ The nitric acid (HNO) according to claim 17, further comprising generating ) ３ A method for generating ).

20. The oxygen (O ２ ) and the ammonia (NH ３ ) from the nitric acid (HNO ３ A method for producing nitric acid according to claim 19, further comprising producing ).

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