Systems and methods for CO2 capture using molten salts

Abstract

The present disclosure provides a system and method for capturing carbon dioxide using molten salt. A stream containing carbon dioxide from an industry can be contacted with molten borate to produce a carbon-rich stream. The carbon-rich stream can be directed to a desorber where the molten salt is regenerated and pure carbon dioxide is released for use elsewhere.

Description

[Technical Field]

[0001] CROSS-REFERENCE TO RELATED APPLICATIONS [1] This application claims the benefit of U.S. Provisional Patent Application No. 63 / 384,582, filed November 21, 2022, which is incorporated by reference herein in its entirety. [Background technology]

[0002] background [2] Industrial processes can generate carbon-containing products, such as CO2, a greenhouse gas that can affect changes in the Earth's temperature and contribute to global warming. Such industrial processes may include coal-, oil-, or fossil-fuel-fired power plants, manufacturing processes, oil refineries, or any other process that produces carbon-containing products either intentionally or as an unwanted by-product. Traditionally, CO2 is either released into the environment or treated using inefficient and resource-intensive scrubbers. Summary of the Invention [Means for solving the problem]

[0003] overview [3] Disclosed herein are systems and methods for capturing and releasing carbon dioxide using molten salt. Such processes can, for example, minimize carbon emissions from industrial processes. It is advantageous to utilize heat generated within the system to regenerate the molten salt and release the carbon dioxide. However, certain methods involve using steam as a sweep gas to regenerate the molten salt in a desorber. Practical challenges exist (e.g., requiring redesign of the steam turbine) related to passing large amounts of superheated steam through the desorber and other sections of the system to recover carbon dioxide from the steam. Other methods involve burning fuel in high-purity oxygen to achieve the temperatures and heat required by the desorber to regenerate the molten salt. Such methods are inefficient and costly. Furthermore, certain methods involve using electrolysis to regenerate the molten salt. However, such methods require large and prohibitive amounts of electrical energy. Accordingly, a need is recognized herein to address the above-mentioned problems. Provided herein are systems and methods that utilize heat generated within high temperature systems to absorb and desorb carbon dioxide into molten salts, thereby increasing efficiency while minimizing external energy or heat input, associated costs, and adverse climate and environmental impacts.

[0004] [4] In one aspect, described herein is a method for capturing carbon dioxide (CO) from an industrial process, the method comprising: (a) providing a gas stream comprising CO; (b) contacting the gas stream with a first stream comprising molten salt in an absorber, thereby absorbing CO from the gas stream into the first stream and producing a second stream comprising molten salt and absorbed CO; (c) directing the second stream to a desorber; and (d) desorbing the absorbed CO from the second stream using the desorber, thereby generating (i) a third stream comprising molten salt, and (ii) an output stream comprising CO desorbed from the second stream, wherein the third stream comprises less than 50 mol% steam.

[0005] [5] In some embodiments, at least a portion of the industrial process occurs in a kiln. In some embodiments, at least a portion of the industrial process occurs in a reactor. In some embodiments, at least a portion of the industrial process occurs in a furnace.

[0006] [6] In some embodiments, the temperature of at least a portion of the industrial process exceeds a temperature of 600°C. In some embodiments, the temperature of at least a portion of the industrial process exceeds a temperature of 1200°C. In some embodiments, the temperature of at least a portion of the industrial process exceeds a temperature of 2000°C.

[0007] [7] In some embodiments, at least a portion of the industrial process comprises a combustion process. In some embodiments, at least a portion of the industrial process comprises a gasification process. In some embodiments, at least a portion of the industrial process comprises a reforming process. In some embodiments, at least a portion of the industrial process comprises a calcination process. In some embodiments, at least a portion of the industrial process comprises a smelting process. In some embodiments, at least a portion of the industrial process comprises burning a solid fuel. In some embodiments, the solid fuel comprises coal, biomass, waste, or garbage, or any combination thereof. In some embodiments, at least a portion of the industrial process comprises burning a gaseous fuel. In some embodiments, the gaseous fuel comprises natural gas, methane, propane, or refinery gas, or any combination thereof.

[0008] [8] In some embodiments, at least a portion of the industrial process includes producing electricity, steam, heat, cement, steel, hydrogen, pulp, or paper, or any combination thereof.

[0009] [9] In some embodiments, at least a portion of the industrial process occurs in a boiler. In some embodiments, the boiler includes a radiant section and a convection section.

[0010]

[10] In some embodiments, the radiating section exceeds a temperature of 600°C. In some embodiments, the radiating section exceeds a temperature of 1200°C. In some embodiments, the radiating section exceeds a temperature of 2000°C.

[0011]

[11] In some embodiments, the convection zone exceeds a temperature of 200°C. In some embodiments, the convection zone exceeds a temperature of 400°C. In some embodiments, the convection zone exceeds a temperature of 600°C.

[0012]

[12] In some embodiments, the desorber is at a higher temperature than the absorber.

[0013]

[13] In some embodiments, the absorber is located in the convective section and the desorber is located in the radiative section.

[0014]

[14] In some embodiments, the absorber exceeds a temperature of 400°C. In some embodiments, the absorber exceeds a temperature of 500°C. In some embodiments, the absorber exceeds a temperature of 600°C. In some embodiments, the absorber exceeds a temperature of 700°C.

[0015]

[15] In some embodiments, the desorber exceeds a temperature of 700°C. In some embodiments, the desorber exceeds a temperature of 800°C. In some embodiments, the desorber exceeds a temperature of 900°C. In some embodiments, the desorber exceeds a temperature of 1000°C.

[0016]

[16] In some embodiments, the first stream comprises at least 0.01 moles of CO2 per kilogram of molten salt. In some embodiments, the first stream comprises at least 0.1 moles of CO2 per kilogram of molten salt. In some embodiments, the first stream comprises at least 1 mole of CO2 per kilogram of molten salt. In some embodiments, the second stream comprises at least 1 mole of CO2 per kilogram of molten salt. In some embodiments, the second stream comprises at least 10 moles of CO2 per kilogram of molten salt. In some embodiments, the second stream comprises at least 100 moles of CO2 per kilogram of molten salt.

[0017]

[17] In some embodiments, the export stream has a CO2 concentration of greater than 80%. In some embodiments, the export stream has a CO2 concentration of greater than 90%. In some embodiments, the export stream has a CO2 concentration of greater than 95%. In some embodiments, the export stream has a CO2 concentration of greater than 99%. In some embodiments, the export stream has a CO2 concentration of greater than 99.9%.

[0018]

[18] In some embodiments, the desorber comprises a packed bed, a tank, a heat exchanger, or a combination thereof.

[0019]

[19] In some embodiments, the desorber comprises a packing material. In some embodiments, the packing material comprises random packing. In some embodiments, the packing material comprises structured packing.

[0020]

[20] In some embodiments, the method further comprises, prior to (c), directing the second stream to a heat exchanger.

[0021]

[21] In some embodiments, the method further includes directing the third stream to a heat exchanger.

[0022]

[22] In some embodiments, the heat exchanger facilitates heat transfer from the third stream to the second stream.

[0023]

[23] In some embodiments, the heat exchanger comprises a shell-and-tube heat exchanger including a shell side and a tube side.

[0024]

[24] In some embodiments, the third stream is directed to a tube side of the heat exchanger and the second stream is directed to a shell side of the heat exchanger.

[0025]

[25] In some embodiments, the first stream and the third stream are the same.

[0026]

[26] In some embodiments, the first stream comprises at least a portion of the third stream.

[0027]

[27] In some embodiments, the heat exchanger is a salt-salt heat exchanger.

[0028]

[28] In some embodiments, the heat exchanger comprises a helical coil heat exchanger.

[0029]

[29] In some embodiments, the heat exchanger comprises a tube-in-tube heat exchanger.

[0030]

[30] In some embodiments, the tube-in-tube heat exchanger is a salt-salt heat exchanger.

[0031]

[31] In some embodiments, the second stream flows up the inner tube of the tube-in-tube heat exchanger and the third stream flows down the outer tube of the tube-in-tube heat exchanger.

[0032]

[32] In some embodiments, the heat exchanger comprises a printed circuit heat exchanger.

[0033]

[33] In some embodiments, the heat exchanger is located below the desorber.

[0034]

[34] In some embodiments, the heat exchanger is located at least 0.1 meters below the desorber. In some embodiments, the heat exchanger is located at least 1 meter below the desorber. In some embodiments, the heat exchanger is located at least 10 meters below the desorber.

[0035]

[35] In some embodiments, the method further includes directing the third stream through a transfer pump.

[0036]

[36] In some embodiments, the transfer pump operates with an outlet pressure of at least 1 bar absolute. In some embodiments, the transfer pump operates with an outlet pressure of at least 5 bar absolute. In some embodiments, the transfer pump operates with an outlet pressure of at least 10 bar absolute. In some embodiments, the transfer pump operates with an outlet pressure of at least 20 bar absolute. In some embodiments, the transfer pump operates with an outlet pressure of at least 100 bar absolute.

[0037]

[37] In some embodiments, the method further includes directing the third flow through one or more filters.

[0038]

[38] In some embodiments, the method further includes directing the second flow through one or more filters.

[0039]

[39] In some embodiments, the first stream, the second stream, or the third stream comprises a molten borate.

[0040]

[40] In some embodiments, the molten borate is A x B 1-x O 1.5-x wherein x is a number from 0 to 1, and A comprises an alkali metal. In some embodiments, x is a number from about 0.5 to about 0.95. In some embodiments, A is lithium (Li). In some embodiments, A is sodium (Na). In some embodiments, A is potassium (K). In some embodiments, A is rubidium (Rb). In some embodiments, A is cesium (Cs). In some embodiments, A is francium (Fr). In some embodiments, A comprises sodium and lithium.

[0041]

[41] In some embodiments, the desorber is connected to an industrial process.

[0042]

[42] In some embodiments, the carbon dioxide is generated as a by-product of at least part of an industrial process.

[0043]

[43] In some embodiments, the third stream comprises less than 20 mol% steam. In some embodiments, the third stream comprises less than 10 mol% steam. In some embodiments, the third stream comprises less than 5 mol% steam.

[0044]

[44] In some embodiments, the third stream has no detectable vapor.

[0045]

[45] In some embodiments, the gas stream comprising CO2 is generated from an industrial process.

[0046]

[46] In another aspect, described herein is a method for retrofitting an industrial process with a carbon capture system, the method including: (a) providing the industrial process; and (b) retrofitting the industrial process with a carbon capture system, the carbon capture system using molten salt to (i) capture carbon dioxide (CO2) and (ii) desorb the CO2, resulting in a stream comprising the desorbed CO2 and the molten salt, wherein the stream comprises less than 50 mol% steam.

[0047]

[47] In another aspect, described herein is a system for capturing carbon dioxide (CO) from an industrial process, the system comprising: (a) an absorber configured to contact a gas stream comprising CO with a first stream comprising molten salt, thereby absorbing CO from the gas stream into the first stream and producing a second stream comprising molten salt and absorbed CO; and (b) a desorber in fluid communication with the absorber, the desorber configured to receive the second stream, or a derivative thereof, from the absorber and desorb the absorbed CO from the second stream, thereby generating (i) a third stream comprising molten salt, and (ii) an output stream comprising CO desorbed from the second stream, wherein the third stream comprises less than 50 mol% steam.

[0048]

[48] ​​In some embodiments, the system further comprises a salt-salt heat exchanger.

[0049]

[49] In some embodiments, the salt-salt heat exchanger is a tube-in-tube salt-salt heat exchanger.

[0050]

[50] Additional aspects and advantages of the present disclosure will become readily apparent to those skilled in the art from the following detailed description. In the detailed description, only exemplary embodiments of the present disclosure are shown and described. As will be recognized, the present disclosure is capable of other and different embodiments, and its several details are capable of modifications in various obvious respects, all without departing from the present disclosure. Accordingly, the drawings and description are to be regarded as illustrative in nature, and not as restrictive.

[0051] Incorporation by Reference

[51] All publications, patents, and patent applications referred to in this specification are incorporated by reference herein to the same extent as if each individual publication, patent, or patent application was specifically and individually indicated to be incorporated by reference. To the extent that the publications, patents, or patent applications incorporated by reference conflict with the disclosure contained herein, the present specification is intended to supersede and / or take precedence over any such conflicting matter.

[0052] BRIEF DESCRIPTION OF THE DRAWINGS

[52] The novel features of the systems and methods described herein are set forth with particularity in the appended claims. A better understanding of the features and advantages of the systems and methods described herein will be obtained by reference to the following detailed description setting forth illustrative embodiments and the accompanying drawings (also referred to herein as "Figure" and "FIG."). [Brief explanation of the drawings]

[0053] [Figure 1]

[53] Figure 1 shows a schematic of a method for capturing carbon dioxide (CO2) using molten salt and then desorbing the absorbed CO2 from the molten salt. [Figure 2]

[54] Figure 2 shows a schematic of a system for capturing CO2 from solid fuels in which an absorber is located in the convective section directly above a desorber in the radiative section. [Figure 3]

[55] Figure 3 shows a schematic of a system for capturing CO2 from solid fuels in which an absorber is placed in the convection section in parallel with a desorber in the radian section. [Figure 4]

[56] Figure 4 shows a schematic of a system for capturing CO2 from gaseous fuels in which an absorber is located in the convective section directly above a desorber in the radiative section. [Figure 5]

[57] Figure 5 shows a schematic of a system for capturing CO2 from gaseous fuels in which an absorber is placed in the convective section in parallel with a desorber in the radiative section. [Figure 6]

[58] Figure 6 shows a schematic of a system for capturing CO2 from a gas fuel in which an absorber, including a tube-in-tube heat exchanger, is placed in the convection section in parallel with a desorber in the radiant section. [Figure 7]

[59] Figure 7 illustrates a computer system programmed or otherwise configured to implement a method for capturing CO2 using molten salt. [Figure 8]

[60] Figure 8 shows a schematic of a system for capturing CO2 from a high temperature system using molten salt with an integrated heat recovery system utilizing steam pipes. [Figure 9]

[61] Figure 9 shows a schematic of a system for capturing CO2 from a high temperature system and an external flue of the high temperature system using molten salt. [Figure 10]

[62] Figure 10 shows a schematic of a system for capturing CO2 from a high temperature system using molten salt, transporting the captured CO2 for off-site use or storage, and directing the generated steam to a steam turbine to generate electricity. [Figure 11]

[63] Figure 11 shows a schematic of a system for capturing CO2 from a flue gas using molten salt and desorbing the captured CO2 using heat generated from the combustion of a fuel. [Figure 12]

[64] Figure 12 shows a schematic of a system for capturing CO2 from the flue using molten salt, spraying a CO2-rich molten salt stream into a combustion chamber, and using heat generated from the combustion of fuel to desorb the captured CO2. [Figure 13]

[65] Figure 13 shows a schematic of a system for capturing CO2 from a flue gas using molten salt and desorbing the captured CO2 using heat generated from electricity. DETAILED DESCRIPTION OF THE INVENTION

[0054] Detailed Description

[66] While various embodiments of the systems and methods described herein have been shown and described herein, it will be apparent to those skilled in the art that such embodiments are provided by way of example only. Numerous variations, changes, and substitutions will occur to those skilled in the art without departing from the systems and methods described herein. It is understood that various alternatives to the embodiments described herein may be employed. Unless the context requires otherwise, throughout this specification and the appended claims, the word "comprise" and variations thereof, such as "comprises" and "comprising," are to be construed in an open, inclusive sense, i.e., "including, but not limited to."

[0055]

[67] Whenever the terms "at least," "greater than," or "greater than or equal to" precede the first number in a series of two or more numbers, the term "at least," "greater than," or "greater than or equal to" applies to each and every number in the series. For example, greater than or equal to 1, 2, or 3 is equivalent to 1 or more, 2 or more, or 3 or more.

[0056]

[68] Whenever the term "no more than," "less than," or "less than or equal to" precedes the first number in a series of two or more numbers, the term "no more than," "less than," or "less than or equal to" applies to each and every number in the series. For example, less than or equal to 3, 2, or 1 is equivalent to 3 or less, 2 or less, or 1 or less.

[0057]

[69] The term "about," when used herein in reference to a number or numerical range, means that the stated number or numerical range is approximate within experimental variability (or within statistical experimental error). The number or numerical range may vary by 1% to 15% of the stated number or numerical range.

[0058]

[70] As used in this specification and the appended claims, the singular forms "a," "an," and "the" include plural referents unless the content clearly dictates otherwise. Please also note that the term "or" is generally used in its sense including "and / or" unless the content clearly dictates otherwise.

[0059]

[71] As used herein, the term "high purity" generally refers to a composition having a low level of impurities. In some cases, high purity refers to a mixture having a concentration of a component from about 80% to about 99.99%. In some cases, high purity refers to a mixture having a concentration of a component from about 80% to about 85%, about 80% to about 90%, about 80% to about 95%, about 80% to about 97%, about 80% to about 99%, about 80% to about 99.9%, about 80% to about 99.99%, about 85% to about 90%, about 85% to about 95%, about 85% to about 97%, about 85% to about 99%, about 85% to about 99.9%, about 85% to about 99.99%, about 90% to about 95%, about 90% to about 97%, High purity refers to a mixture having a concentration of a component of about 90% to about 99%, about 90% to about 99.9%, about 90% to about 99.99%, about 95% to about 97%, about 95% to about 99%, about 95% to about 99.9%, about 95% to about 99.99%, about 97% to about 99%, about 97% to about 99.9%, about 97% to about 99.99%, about 99% to about 99.99%, or about 99.9% to about 99.99%. In some cases, high purity refers to a mixture having a concentration of a component of about 80%, about 85%, about 90%, about 95%, about 97%, about 99%, about 99.9%, or about 99.99%. In some cases, high purity refers to a mixture having a concentration of a component of at least about 80%, about 85%, about 90%, about 95%, about 97%, about 99%, or about 99.9%.

[0060]

[72] The term "in proximity to," as used herein, generally refers to a distance of at most 20 meters between A and B. For example, when an absorber is said to be located in proximity to a boiler, it is understood to mean that the boundary of the absorber is at most 20 meters from the boundary of the boiler. In some embodiments, the distance may be at most 20 meters (m), 15 m, 10 m, 9 m, 8 m, 7 m, 6 m, 5 m, 4 m, 3 m, 2 m, 1 m, or less.

[0061]

[73] The term "industrial process," as used herein, generally refers to a process that extracts, transports, or treats raw materials to produce an end product using physical, mechanical, and / or chemical processes. An industrial process may generate electricity, steam, water, heat, cement, steel, hydrogen, pulp, paper, carbon dioxide, or a combination thereof. In some examples, an industrial process may refer to any process that generates a valuable product. In some embodiments, an industrial process may generate carbon dioxide as a by-product (e.g., a by-product of combustion). In some embodiments, an industrial process may generate heat (e.g., thermal energy). Examples of industrial processes include coal-fired power plants, oil-fired power plants, gas-fired power plants, or any other fossil fuel-fired power plants. Fossil fuels may include coal, petroleum, hashish, oil shale, bitumen, tar sands, and heavy oil.

[0062]

[74] The term "high temperature system," as used herein, generally refers to an entire system or portion of a system that can reach high temperatures (e.g., greater than 300°C). An industrial process may include one or more high temperature systems. Carbon dioxide capture and release using molten salts, as described herein, may occur in or near a high temperature system (e.g., a portion of a system that reaches a temperature of at least 300°C). A high temperature system may include a boiler.

[0063]

[75] The term "carbon capture system," as used herein, generally refers to a system that includes at least an absorber and a desorber for capturing and releasing carbon dioxide. The carbon capture system can be a closed-loop system through which a stream containing molten salt moves (e.g., from the absorber to the desorber and back to the absorber). The carbon capture system can be separate from the high-temperature system or the system in which the industrial process occurs. The carbon capture system can be integrated directly into the high-temperature system (e.g., a boiler). The carbon capture system can be located near (e.g., adjacent to) the high-temperature system. The carbon capture system can be retrofitted into an existing high-temperature system.

[0064] Systems and methods for CO2 capture

[76] Provided herein are systems and methods that can be used to capture carbon dioxide using molten salts.

[0065]

[77] In one aspect, the disclosure provides a method for capturing carbon dioxide (CO) from an industrial process, the method comprising: (a) providing a gas stream comprising CO generated from the industrial process; (b) contacting the gas stream with a first stream comprising molten salt in an absorber, thereby absorbing CO from the gas stream into the first stream and producing a second stream comprising molten salt and absorbed CO; (c) directing the second stream to a desorber; and (d) desorbing the absorbed CO from the second stream using the desorber, thereby generating (i) a third stream comprising molten salt, and (ii) an output stream comprising CO desorbed from the second stream, wherein the third stream comprises less than 50 mol% steam.

[0066]

[78] In some embodiments, the method may further include, prior to (c), directing the second stream to a heat exchanger. In some embodiments, the method may further include directing the third stream to a heat exchanger. In some embodiments, the heat exchanger may facilitate heat transfer from the third stream to the second salt stream. In some embodiments, the heat exchanger may be a salt-salt heat exchanger.

[0067]

[79] In one example, Figure 1 illustrates a process for CO2 capture. As shown in Figure 1, first, a gas stream containing carbon dioxide may be provided. Next, the gas stream containing carbon dioxide may be contacted with a stream containing molten salt, thereby absorbing the carbon dioxide into the molten salt and generating a carbon-rich stream. The carbon-rich stream may then be directed to a desorber. In the desorber, the carbon dioxide is desorbed from the carbon-rich stream, thereby generating a carbon-lean stream and an export stream containing carbon dioxide.

[0068]

[80] In another aspect, the disclosure provides a system for capturing carbon dioxide from an industrial process, the system comprising: (a) an absorber configured to contact a gas stream comprising carbon dioxide with a first stream comprising molten salt, thereby absorbing carbon dioxide from the gas stream into the first stream and producing a second stream comprising molten salt and absorbed carbon dioxide; and (b) a desorber in fluid communication with the absorber, the desorber configured to receive the second stream from the absorber or a derivative thereof and desorb the absorbed carbon dioxide from the second stream, thereby generating (i) a third stream comprising molten salt, and (ii) an export stream comprising carbon dioxide desorbed from the second stream, wherein the third stream comprises less than 50 mol% steam.

[0069]

[81] In some embodiments, heat generated within an industrial process system can be used to regenerate molten salt and release carbon-containing materials (e.g., carbon dioxide). To reduce the cost and energy requirements associated with regeneration compared to other methods, it can be advantageous to utilize heat generated within the system to regenerate molten salt and release carbon dioxide. For example, other methods use steam as a sweep gas to regenerate molten salt in a desorber, which can require large amounts of steam (e.g., greater than 75 mol% steam with respect to the molten salt stream). Steam can be generated in industrial processes through heating boiler feedwater, boiling boiler feedwater, or superheating steam. Practical challenges exist related to passing large amounts of superheated steam through the desorber and other sections of the system to recover carbon dioxide from the steam. For example, these challenges can include redesigning or significantly modifying the steam turbine to separate the steam and carbon dioxide mixture so that the steam can condense and the carbon dioxide can remain gaseous. Additionally, using a steam sweep can require a large desorber to accommodate large steam flows. Because a steam sweep may require maintaining the steam at high pressure, considerations regarding the materials used for the high temperature system and the durability of the high temperature system to withstand the high pressures required for the steam sweep may be challenging. Furthermore, regeneration methods using a steam sweep may only be applicable in facilities where superheated steam is already generated (e.g., large power plants) and may not be feasible in systems where steam is not generated (e.g., cement kilns, steel blast furnaces).

[0070] High Temperature Systems

[82] In some embodiments, at least a portion of the industrial process occurs in a high temperature system as described herein. The high temperature system may include a boiler, a furnace, a kiln, a reactor, or any combination thereof. In some embodiments, the high temperature system may include a system capable of generating carbon dioxide at a temperature of at least 400°C. In some embodiments, the industrial process occurs in a boiler. For example, fuel and air may enter the boiler, where heat from the boiler may combust the fuel to produce carbon dioxide, among other products (e.g., carbon monoxide, water, nitrogen oxides, sulfur dioxide, ash). In some embodiments, the industrial process occurs in a kiln. In some embodiments, the industrial process occurs in a reactor. In some embodiments, the industrial process occurs in a furnace. In some embodiments, the high temperature system is top-fired. In some embodiments, the high temperature system is bottom-fired.

[0071]

[83] In some cases, the high temperature system operates at a temperature between about 400°C and about 2,500°C. In some cases, the high temperature system operates at a temperature between about 400°C and about 500°C, between about 400°C and about 750°C, between about 400°C and about 1,000°C, between about 400°C and about 1,500°C, between about 400°C and about 2,000°C, between about 400°C and about 2,500°C, between about 500°C and about 750°C, between about 500°C and about 1,000°C, between about 500°C and about 1,500°C, between about 500°C and about 2,000°C, or between about 500°C and about 2,500°C. , about 750°C to about 1,000°C, about 750°C to about 1,500°C, about 750°C to about 2,000°C, about 750°C to about 2,500°C, about 1,000°C to about 1,500°C, about 1,000°C to about 2,000°C, about 1,000°C to about 2,500°C, about 1,500°C to about 2,000°C, about 1,500°C to about 2,500°C, or about 2,000°C to about 2,500°C. In some cases, the high temperature system operates at a temperature of about 400°C, about 500°C, about 750°C, about 1,000°C, about 1,500°C, about 2,000°C, or about 2,500°C. In some cases, the high temperature system operates at a temperature of at least about 400°C, about 500°C, about 750°C, about 1,000°C, about 1,500°C, or about 2,000°C. In some cases, the high temperature system operates at a temperature of at most about 500°C, about 750°C, about 1,000°C, about 1,500°C, about 2,000°C, or about 2,500°C. In some embodiments, the temperature of at least a portion of the industrial process may exceed a temperature of about 1200°C. In some embodiments, the temperature of at least a portion of the industrial process may exceed a temperature of about 2000°C.

[0072]

[84] In some embodiments, the reaction process performed as part of the industrial process may include combustion, gasification, reforming, calcination, smelting, or any other high temperature reaction. In some embodiments, the reaction process performed as part of the industrial process may include a combination of combustion, gasification, reforming, calcination, smelting, or any other high temperature reaction. In some embodiments, the industrial process may include a combustion process. In some embodiments, the industrial process may include a gasification process. In some embodiments, the industrial process may include a reforming process. In some embodiments, the industrial process may include a calcination process. In some embodiments, the industrial process may include a smelting process. In some embodiments, the industrial process may include combusting a solid fuel. In some embodiments, the industrial process may include combusting a gaseous fuel.

[0073]

[85] A solid fuel as described herein may include coal, biomass (e.g., plants and crops), waste, tar, garbage, or any carbon-containing solid. A gaseous fuel as described herein may include natural gas, petroleum, refinery gas, C1-C8 alkanes (e.g., methane, propane, butane, pentane, hexane, heptane, octane), or any other carbon-containing gas. A carbon-containing gas as described herein may be any substance in a gaseous state containing one or more carbon atoms. In some embodiments, the carbon-containing gas may include a fossil fuel (e.g., natural gas). In some embodiments, the carbon-containing gas may include biogas. In some embodiments, the carbon-containing gas may include carbon dioxide or carbon monoxide. In some embodiments, the fuel may be a liquid fuel. In some embodiments, the liquid fuel may include petroleum, bio-oil, or any other combustible liquid.

[0074]

[86] In some embodiments, an industrial process may generate electricity, steam, water, heat, cement, steel, hydrogen, pulp, paper, or a combination thereof. In some embodiments, an industrial process may include generating any product of value. In some embodiments, an industrial process may generate carbon dioxide as a by-product. In some embodiments, an industrial process may generate heat (e.g., thermal energy).

[0075]

[87] In some embodiments, the industrial process includes one or more unit operations including a baghouse, air heater, boiler, absorber, desorber, heat exchanger, transfer pump, filter, packing material, low-pressure steam turbine, high-pressure turbine, condenser, bunker, fan, superheater, air heater, compression unit, tank, storage unit, or combinations thereof. The industrial process may include a high-temperature system. The industrial process may include a high-temperature system and a carbon capture system. The high-temperature system may include a boiler. The carbon capture system may include an absorber, desorber, one or more streams, packing material, transfer pump, heat exchanger, and filter. In some embodiments, the carbon capture process may occur at least partially within a boiler in the high-temperature system. In some embodiments, carbon capture and desorption may occur within or near the high-temperature system. In some embodiments, carbon capture and desorption may occur adjacent to the high-temperature system. In some embodiments, carbon capture and desorption may occur within 20 meters of the high-temperature system. In some embodiments, carbon capture and desorption can occur within 10 meters of the high temperature system. In some embodiments, carbon capture and desorption can occur within 1 meter of the high temperature system.

[0076]

[88] In some embodiments, the high-temperature system includes a boiler. The boiler may include a radiant section and a convection section. The radiant section of the boiler may include an absorber or desorber as part of a carbon capture system. The convection section of the boiler may include an absorber or desorber as part of a carbon capture system. In some embodiments, the radiant section may include a desorber, and the convection section may include an absorber as part of a carbon capture system. In one embodiment, the convection section may be positioned parallel (e.g., side-by-side) with the radiant section within the boiler. In another embodiment, the convection section may be positioned above (e.g., higher than) the radiant section within the boiler. In some examples, the convection section may be positioned directly above the radiant section. Positioning the convection section parallel to the radiant section may be advantageous to allow sufficient space for flue gases exiting the radiant section to cool before entering the convection section. Positioning the convection section parallel to the radiant section may be advantageous to reduce the overall height of the system (e.g., plant). In some embodiments, an industrial process (e.g., a reaction process) may occur at least in part within the boiler.In some embodiments, an industrial process (e.g., a reaction process) may occur at least in part within the boiler.

[0077]

[89] In some embodiments, the emissive section may exceed a temperature of at least about 400°C, 500°C, 600°C, 700°C, 800°C, 900°C, 1000°C, 1200°C, 1400°C, 1600°C, 1800°C, 2000°C, 2500°C, or more. In some embodiments, the emissive section may exceed a temperature of at least about 600°C. In some embodiments, the emissive section may exceed a temperature of at least about 1200°C. In some embodiments, the emissive section may exceed a temperature of at least about 2000°C. In some embodiments, the convection zone may exceed a temperature of at least about 100°C, 200°C, 300°C, 400°C, 500°C, 600°C, 700°C, 800°C, 900°C, 1000°C, 1200°C, 1400°C, 1600°C, 1800°C, 2000°C, 2500°C, or more. In some embodiments, the convection zone may exceed a temperature of at least about 200°C. In some embodiments, the convection zone may exceed a temperature of at least about 400°C. In some embodiments, the convection zone may exceed a temperature of at least about 600°C.

[0078]

[90] In some embodiments, the temperature of the radiant section may be higher than the temperature of the convective section. In some embodiments, the temperature of the radiant section may be at least about 100°C higher than the temperature of the convective section. In some embodiments, the temperature of the radiant section may be at least about 200°C higher than the temperature of the convective section. In some embodiments, the temperature of the radiant section may be at least about 300°C higher than the temperature of the convective section. In some embodiments, the temperature of the radiant section may be at least about 400°C higher than the temperature of the convective section. In some embodiments, the temperature of the radiant section may be at least about 500°C higher than the temperature of the convective section.

[0079]

[91] The temperature of the radiant section can be controlled or influenced by the relative flow rates of flue gas, fuel, air, steam, or any other heat transfer medium into the radiant section of a high temperature system. The temperature of the convection section can be controlled or influenced by the relative flow rates of fuel, air, steam, or any other heat transfer medium into the convection section of a high temperature system. In some embodiments, the flue gas can include a mixture of air and fuel. In some embodiments, the heat transfer medium can include steam. The ratio between the flow rates of the heat transfer medium (e.g., steam) and the flue gas can be about 0.01, about 0.1, about 0.5, about 1.0, about 1.5, about 2.0, about 10, about 20, about 30, about 40, about 50, about 60, about 70, about 80, about 90, about 100, or more. In some embodiments, the ratio between the flow rates of the heat transfer medium (e.g., steam) and the flue gas can be about 0.1 to about 10. In some embodiments, the ratio between the flow rates of the heat transfer medium (e.g., steam) and the flue gas may be about 1. For example, a lower air or fuel flow rate may reduce the rate at which carbon dioxide is generated in the boiler, which may then reduce the carbon dioxide that is captured and releases heat in the convection section, thereby reducing the temperature of the convection section.

[0080] Carbon Capture System

[92] The carbon capture system can be a component of a high-temperature system used in an industrial process. In some embodiments, the high-temperature system can be constructed or built along with the carbon capture system components. In some embodiments, a carbon capture system for carbon dioxide absorption and desorption as described herein can be retroactively incorporated into a system used in an industrial process, particularly a high-temperature system component. For example, a desorber of the carbon capture system can be integrated into the high-temperature system. In some embodiments, the desorber can be integrated into a boiler. In some embodiments, the desorber can be integrated into the high-temperature system in the form of a tube. The tube can be a heat exchanger tube. In some embodiments, the heat exchanger tube can be a tube-in-tube salt-salt heat exchanger tube. In some embodiments, a desorber integrated with a high-temperature system using a tube can further include a tank to allow space for carbon-containing material to desorb from the molten borate.

[0081]

[93] In some examples, the carbon capture system is configured such that heat generated in a high temperature system (e.g., a boiler) is transferred to a desorber in the carbon capture system. In some embodiments, heat of reaction is generated in a convective section of the carbon capture system upon absorption of carbon-containing material into a stream containing molten salt. In some embodiments, the generated heat can be passed to the desorber to regenerate the molten salt and carbon-containing material. In some embodiments, the desorbed carbon-containing material can be a high-purity carbon-containing material (e.g., high-purity carbon dioxide).

[0082]

[94] In some embodiments, the tube-in-tube heat exchanger may be positioned within a high temperature system (e.g., within a boiler) to facilitate the transfer of molten salt and heat. In some embodiments, the tube-in-tube heat exchanger may be positioned within a radiant section. In some embodiments, the tube-in-tube heat exchanger may be in the shape of a coil or a spiral. In some embodiments, the tube-in-tube heat exchanger may include multiple straight sections. In some embodiments, the tube-in-tube heat exchanger may include two or more straight sections, each straight section positioned at an angle between 0 and 180 degrees relative to an adjacent straight section. In some embodiments, the angle may be between 30 and 120 degrees. In some embodiments, the angle may be approximately 90 degrees.

[0083]

[95] In some embodiments, a tube-in-tube heat exchanger can include a first tube (e.g., an outer tube) that can surround a second tube (e.g., an inner tube). In some embodiments, the molten salt can travel upward within the outer tube and downward within the inner tube. In other embodiments, the molten salt can travel upward within the inner tube and downward within the outer tube. The molten salt can travel downward via gravity from the top of the tube to the bottom. In some embodiments, the molten salt and heat can be transferred to the desorber through multiple tube-in-tube heat exchangers (e.g., 2 to about 100 tube-in-tube heat exchangers). In some embodiments, the molten salt and heat can be transferred to the desorber through one or more tubes. In some embodiments, the molten salt and heat can be transferred to the desorber through a single tube. In some embodiments, the molten salt and heat can be transferred to the desorber through multiple tubes (e.g., 2 to about 100 tubes).

[0084]

[96] The carbon capture system may include an absorber. The absorber may be located within a high-temperature system of an industrial process. The absorber may be located adjacent to a high-temperature system of an industrial process. The absorber may be located within a boiler of the system. In some embodiments, the absorber may be located adjacent to a boiler of the system. In some embodiments, the absorber may be located near a boiler of the system. In some embodiments, the absorber may be located within the convection section of the boiler. The absorber may include one or more types of molten salts, which are used to sequester (e.g., absorb carbon dioxide). The absorber may operate at temperatures of at least 200°C, 300°C, 400°C, 500°C, 600°C, 700°C, 800°C, 900°C, 1000°C, 1200°C, or any other temperature within the aforementioned range. In some embodiments, the absorber temperature may exceed about 400°C. In some embodiments, the absorber temperature may exceed about 500°C. In some embodiments, the absorber temperature may be greater than about 600°C. In some embodiments, the absorber temperature may be greater than about 700°C. In some embodiments, the absorber temperature may be between about 300°C and about 800°C. In some embodiments, the absorber temperature may be between about 400°C and about 700°C. In some embodiments, the absorber temperature may be between about 400°C and about 600°C.

[0085]

[97] The molten salt in the absorber may capture at least about 40%, 50%, 60%, 70%, 80%, 90%, 95%, 99%, or 100% of the carbon-containing material (e.g., carbon dioxide) it contacts. In some embodiments, the absorber may capture at least about 40%, 50%, 60%, 70%, 80%, 90%, 95%, 99%, or 100% of the carbon-containing material (e.g., carbon dioxide) it contacts. The absorber may capture at least about 50% of the carbon-containing material it contacts, about 75% of the carbon-containing material it contacts, about 80% of the carbon-containing material it contacts, about 85% of the carbon-containing material it contacts, about 90% of the carbon-containing material it contacts, or about 95% of the carbon-containing material it contacts.

[0086]

[98] The carbon capture system may include a desorber. The desorber may be located within the high temperature system. In some embodiments, the desorber may be located adjacent to the high temperature system. In some embodiments, the desorber may be located near the high temperature system. The desorber may be located within a boiler of the system. In some embodiments, the desorber may be located adjacent to a boiler of the system. In some embodiments, the desorber may be located near a boiler of the system. In some embodiments, the desorber may be located within a radiant section of a boiler. The desorber may be used to release or desorb carbon dioxide from the molten salt. The desorber may have a temperature of at least 200°C, 300°C, 400°C, 500°C, 600°C, 700°C, 800°C, 900°C, 1000°C, 1200°C, 1400°C, 1600°C, 2000°C, or any other temperature within the aforementioned ranges. In some embodiments, the desorber temperature may be greater than about 700°C. In some embodiments, the absorber temperature may be greater than about 800°C. In some embodiments, the absorber temperature may be greater than about 900°C. In some embodiments, the absorber temperature may be greater than about 1000°C. In some embodiments, the absorber temperature may be between about 600°C and about 1200°C. In some embodiments, the absorber temperature may be between about 700°C and about 1000°C. In some embodiments, the absorber temperature may be between about 700°C and about 900°C.

[0087]

[99] The desorber may release about 10% of the carbon-containing material absorbed in the stream containing molten salt, about 20% of the carbon-containing material absorbed in the stream containing molten salt, about 30% of the carbon-containing material absorbed in the stream containing molten salt, about 40% of the carbon-containing material absorbed in the stream containing molten salt, about 50% of the carbon-containing material absorbed in the stream containing molten salt, about 60% of the carbon-containing material absorbed in the stream containing molten salt, about 70% of the carbon-containing material absorbed in the stream containing molten salt, about 80% of the carbon-containing material absorbed in the stream containing molten salt, about 85% of the carbon-containing material absorbed in the stream containing molten salt, about 90% of the carbon-containing material absorbed in the stream containing molten salt, about 95% of the carbon-containing material absorbed in the stream containing molten salt, or about 99% of the carbon-containing material absorbed in the stream containing molten salt, or about 100% of the carbon-containing material absorbed in the stream containing molten salt. In some embodiments, the desorber may release between about 10% and about 100% of the carbon-containing material absorbed in the stream containing molten salt. In some embodiments, the desorber may release between about 40% and about 100% of the carbon-containing material absorbed in the stream containing molten salt. For example, a carbon-rich stream containing molten salt may contain about 50% carbon dioxide, and after desorbing the carbon dioxide, the carbon-lean stream containing molten salt may contain about 30% carbon dioxide, thereby effectively releasing about 40% of the carbon dioxide absorbed in the stream containing molten salt.

[0088]

[0100] In some embodiments, the desorber may have a higher temperature than the absorber. For example, if the absorber has a temperature of about 600°C, then the desorber may have a temperature of at least 900°C. In another example, if the absorber has a temperature of about 700°C, then the desorber may have a temperature of at least 1000°C. The temperature difference between the absorber and desorber may be at least about 100°C, 200°C, 300°C, 400°C, 500°C, 600°C, or more. In some embodiments, the temperature difference between the absorber and desorber may be at least about 100°C. In some embodiments, the temperature difference between the absorber and desorber may be at least about 200°C. In some embodiments, the temperature difference between the absorber and desorber may be at least about 300°C. In some embodiments, the desorber may consume heat in the radiant section of the high temperature system, which may prevent extremely high temperatures (e.g., at least 1000°C) in the desorber. In such embodiments, the extremely high temperature in the desorber may be at least 1000°C, at least 1200°C, at least 2000°C, or higher. The desorber may reduce heat flux through vane walls located in the radiant section of the high temperature system. In some embodiments, the higher temperature of the desorber (relative to the absorber) may facilitate desorption of carbon dioxide from the molten salt.

[0089]

[0101] The high-temperature system may include one or more vane walls. The vane walls may be positioned within the radiant section of the high-temperature system to reduce heat flux. Such vane walls may prevent the radiant section from reaching extremely high temperatures and causing damage to the radiant section due to high temperatures. In some examples, the extremely high temperatures within the radiant section may be at least 1000°C, at least 1200°C, at least 2000°C, or even higher. The vane walls may include one or more pipes positioned near or in contact with the wall of the radiant section. In some embodiments, the one or more pipes in the vane walls may be positioned at most about 5 meters from the wall of the radiant section, at most about 2 meters from the wall of the radiant section, at most about 1 meter from the wall of the radiant section, or less. In some embodiments, the one or more pipes in the vane walls may be positioned in contact with the wall of the radiant section. In some embodiments, the pipes in the vane walls may contain feedwater from a boiler and generate steam through contact with hot flue gases. In some embodiments, the pipes in the vane walls may contain feedwater from a boiler and generate steam through contact with heat in the desorber. In some embodiments, steam may be generated in a steam drum (e.g., a steam tank).

[0090]

[0102] In some embodiments, the carbon capture system may include a packed bed, a tank, a heat exchanger, or a combination thereof. In some embodiments, the carbon capture system may include a packed bed and a heat exchanger. In some embodiments, the carbon capture system may include a tank and a heat exchanger. In some embodiments, the desorber may include a packing material. In some embodiments, the desorber may not include a packing material. The packing material may be part of the packed bed. The packing material may include random packing, structured packing, or a combination thereof. The packed bed may increase the duration of residence of the carbon-rich stream in the desorber to provide more opportunities for carbon-containing materials to desorb from the carbon-rich stream. In some embodiments, the absorber may include a packing material. The packing material may be part of the packed bed. The packing material may include random packing, structured packing, or a combination thereof. In some embodiments, the packing material may provide a high surface area for the molten salt stream to interact with. In some embodiments, the packing material may reduce the pressure drop when the stream containing molten salt passes through the packed bed. In some embodiments, the packing material may include a low-cost material. The filler material may include a conductive material, hi some embodiments, the filler material may include a metal, a metal alloy, a ceramic material, or a combination thereof.

[0091]

[0103] In some embodiments, the carbon capture system may include a tank. The tank may include a space that allows residence of the carbon-containing material released from the carbon-rich stream (e.g., a CO2 drum or a molten salt drum). In some embodiments, the tank is a flash tank. In some embodiments, the tank is a drum. In some embodiments, the tank may contain a mixture of liquid molten salt (e.g., carbon-lean molten salt and carbon-rich molten salt) and gaseous carbon-containing material. In some embodiments, at any given time during the desorption process, the tank may be at least 10% liquid-filled, at least 20% liquid-filled, at least 50% liquid-filled, at least 80% liquid-filled, or more. In some embodiments, the tank may include a riser. In some embodiments, the tank may include a downcomer. In some embodiments, the tank may include a cyclone. In some embodiments, the tank may include baffles. A larger tank may increase the residence time of the molten salt in the tank, thereby achieving a greater degree of desorption. A large tank can reduce the velocity of the molten salt flow and prevent entrainment of the molten salt flow into the carbon-containing material gas stream. A small tank can reduce the residence time of the molten salt in the tank. A small tank can increase heat transfer from the radiant section. A small tank can reduce the total amount of molten salt required in the system. In some embodiments, the residence time of the molten salt in the tank can be at least 30 seconds, at least 1 minute, at least 2 minutes, at least 5 minutes, at least 10 minutes, or at least 20 minutes. The molten salt flow in the large tank can have a residence time of at least 5 minutes, at least 10 minutes, at least 20 minutes, or more. The molten salt flow in the small tank can have a residence time of at most about 10 minutes, about 5 minutes, about 2 minutes, about 1 minute, about 30 seconds, or less. In some embodiments, the tank can be exposed to hot flue gas. In some embodiments, the pressure of the desorbed carbon-containing gas in the tank can be controlled by a downstream fan. In some embodiments, the fan can rotate when contacted with the carbon dioxide flow.

[0092]

[0104] In some embodiments, the carbon capture system may include a heat exchanger. In some embodiments, the heat exchanger may include a helical coil heat exchanger, a tube-in-tube heat exchanger, a printed circuit heat exchanger, a salt-salt heat exchanger, or a combination thereof. In some embodiments, the heat exchanger includes a salt-salt heat exchanger. In some embodiments, the heat exchanger may include a conventional shell-and-tube heat exchanger including a shell side and a tube side.

[0093]

[0105] Relative to the desorber, the heat exchanger may be positioned within the carbon capture system at an altitude below (e.g., lower than) the altitude of the desorber. For example, the heat exchanger may be positioned below the desorber within the carbon capture system. Although measures may be taken to suppress desorption of carbon-containing materials within the heat exchanger, some carbon-containing materials may be desorbed within the heat exchanger. Positioning the heat exchanger at a lower altitude than the desorber may facilitate the ascent of desorbed carbon-containing materials into the desorber. In some embodiments, the heat exchanger may be positioned at an altitude that is at least 0.01 meters (m), 0.1 m, 0.5 m, 1 m, 2 m, 3 m, 4 m, 5 m, 6 m, 7 m, 8 m, 9 m, 10 m, 12 m, or more lower than the altitude of the desorber. In some embodiments, the heat exchanger may be positioned at an altitude that is at least 0.1 m lower than the altitude of the desorber. In some embodiments, the heat exchanger may be located at an elevation at least 1 meter lower than the elevation of the desorber. In some embodiments, the heat exchanger may be located at an elevation at least 10 meters lower than the elevation of the desorber.

[0094]

[0106] In some embodiments, a transfer pump may be used to facilitate transport of streams within the carbon capture system. In some embodiments, a transfer pump may be used to transport a first stream. In some embodiments, a transfer pump may be used to transport a second stream. In some embodiments, a transfer pump may be used to transport a third stream. In some embodiments, a first stream may be directed through a transfer pump. In some embodiments, a second stream may be directed through a transfer pump. In some embodiments, a third stream may be directed through a transfer pump. In some embodiments, a transfer pump may be used to transport any stream to a location within the carbon capture system.

[0095]

[0107] In some embodiments, the transfer pump may operate with an outlet absolute pressure of at least 0.5 bar, 1 bar, 2 bar, 3 bar, 4 bar, 5 bar, 6 bar, 7 bar, 8 bar, 9 bar, 10 bar, 15 bar, 20 bar, 30 bar, 40 bar, 50 bar, 60 bar, 70 bar, 80 bar, 90 bar, 100 bar, 120 bar, 150 bar, 200 bar, or more. In some embodiments, the transfer pump may operate with an outlet absolute pressure of at least 1 bar. In some embodiments, the transfer pump may operate with an outlet absolute pressure of at least 5 bar. In some embodiments, the transfer pump may operate with an outlet absolute pressure of at least 10 bar. In some embodiments, the transfer pump may operate with an outlet absolute pressure of at least 20 bar. In some embodiments, the transfer pump may operate with an outlet absolute pressure of at least 100 bar.

[0096]

[0108] In some embodiments, the transfer pump may operate at a temperature of at least about 300°C, 400°C, 500°C, 600°C, 700°C, 800°C, 900°C, 1000°C, 1200°C, 1400°C, 1600°C, 2000°C, or higher. In some embodiments, the transfer pump may operate at a temperature of at least about 400°C. In some embodiments, the transfer pump may operate at a temperature of at least about 600°C. In some embodiments, the transfer pump may operate at a temperature of at least about 800°C.

[0097]

[0109] A heat exchanger positioned in the path between the absorber and the desorber can be used to increase or decrease the temperature of the stream. The heat exchanger can be a salt-salt heat exchanger. The salt-salt heat exchanger can utilize a molten salt stream as the heat exchange fluid. In some embodiments, the salt-salt heat exchanger can increase the temperature of the carbon-rich stream and decrease the temperature of the carbon-lean stream. For example, the salt-salt heat exchanger can increase the temperature of the carbon-rich stream to a temperature sufficient to desorb carbon dioxide from the molten salt and decrease the temperature of the carbon-lean molten salt before transporting it back to the absorber for a subsequent cycle of carbon capture. For example, the salt-salt heat exchanger can increase the temperature of the second stream from about 600°C to about 900°C and decrease the temperature of the third stream from about 900°C to about 600°C. For example, the salt-salt heat exchanger may increase the temperature of the second stream from about 600°C to about 900°C and decrease the temperature of the third stream from about 900°C to about 700°C.

[0098]

[0110] In some embodiments, the salt-salt heat exchanger may increase the temperature of the carbon-rich stream (e.g., the second stream) by at least about 50°C, 100°C, 150°C, 200°C, 300°C, 350°C, 400°C, or more. In some embodiments, the salt-salt heat exchanger may utilize heat flux from the radiant section and heat from the returning carbon-lean stream (e.g., the third stream) to increase the temperature of the carbon-rich salt stream (e.g., the second stream). In some embodiments, the salt-salt heat exchanger may increase the temperature of the carbon-rich salt stream to approximately the temperature of the desorber. In some embodiments, the salt-salt heat exchanger may increase the temperature of the carbon-rich salt stream to approximately a temperature that is about 20°C, 50°C, 80°C, 100°C, 150°C, 200°C, 250°C, 300°C, or more lower than that of the desorber.

[0099]

[0111] In some embodiments, the salt-salt heat exchanger may reduce the temperature of the carbon-lean stream (e.g., the third stream) by at least about 50°C, 100°C, 150°C, 200°C, 300°C, 350°C, 400°C, or more before transporting the carbon-lean stream to the absorber for a subsequent cycle of carbon capture. In some embodiments, heat associated with the third stream may be transferred to the carbon-rich stream in the salt-salt heat exchanger to increase its temperature. In some embodiments, heat associated with the third stream may be transferred as thermal energy for use elsewhere in the industrial process or system. In some embodiments, heat associated with the third stream may be transferred to water to generate steam for use elsewhere in the industrial process or system (e.g., temperature control). Reducing the temperature of the carbon-lean stream (e.g., the third stream) may also prevent damage to the storage tank or transfer pump if the storage tank or transfer pump is not constructed of materials that can withstand the high temperatures the streams may reach.

[0100]

[0112] In some embodiments, the salt-salt heat exchanger may be positioned within the carbon capture system such that the carbon-lean stream (e.g., the third stream) exiting the desorber can flow into the salt-salt heat exchanger without the need for a transfer pump (e.g., via gravity). However, a transfer pump for the carbon-lean stream may be located at the outlet of the salt-salt exchanger. In some embodiments, the salt-salt heat exchanger may be located within the high-temperature system or external to the high-temperature system. In some embodiments, the salt-salt heat exchanger may be located within the high-temperature system. In some embodiments, the salt-salt heat exchanger may have a height of at least 1 m, at least 2 m, at least 5 m, at least 10 m, or at least 20 m. In some embodiments, the salt-salt heat exchanger may have a width of at least 0.5 m, at least 1 m, at least 2 m, at least 5 m, or at least 10 m. In some embodiments, the salt-salt heat exchanger may have a depth of at least 0.5 m, at least 1 m, at least 2 m, at least 5 m, or at least 10 m.

[0101]

[0113] In some embodiments, the carbon capture system may include a transfer pump for the carbon-rich stream. In such embodiments, the transfer pump may operate at a high pressure to increase the partial pressure of the carbon-containing material through the salt-salt heat exchanger to suppress desorption of the carbon-containing material in the second stream before entering the desorber. In some embodiments, the transfer pump may operate at a pressure of at least about 0.1 bar, 1 bar, 2 bar, 3 bar, 4 bar, 5 bar, 6 bar, 7 bar, 8 bar, 9 bar, 10 bar, 20 bar, 30 bar, 40 bar, 50 bar, or more. In some embodiments, the transfer pump may operate at a pressure of from about 1 bar to about 10 bar. In some embodiments, the carbon-rich stream may be located on the shell side of the salt-salt heat exchanger so that desorption of the carbon-containing material does not block the downward flow. In some embodiments, the third stream may be directed to the tube side of the heat exchanger, and the second stream may be directed to the shell side of the heat exchanger.

[0102]

[0114] In some embodiments, one or more filters may be positioned in the flow path (e.g., between the absorber and desorber, between the desorber and absorber, adjacent to a heat exchanger). In some embodiments, one or more filters may be positioned on a bypass line. In some embodiments, one or more filters may be positioned on a downstream line. In some embodiments, one or more filters may be positioned on the main line between the transfer pump and the absorber. In some embodiments, one or more filters may be positioned on the main line between the transfer pump and the desorber. In some embodiments, a filter may be positioned downstream of the carbon-lean molten salt transfer pump. The filter may be used to remove solids that may accumulate in the flow. In some embodiments, the filter may retain at least 50%, 60%, 70%, 80%, 90%, or 100% of the solids on the first side of the filter. In some embodiments, the first flow may be directed through one or more filters. In some embodiments, the second flow may be directed through one or more filters. In some embodiments, the third flow may be directed through one or more filters.

[0103]

[0115] In another aspect, the present disclosure provides a method for retrofitting an industrial process with a carbon capture system, the method comprising: (a) providing an industrial process; and (b) retrofitting the industrial process with said carbon capture system, wherein the carbon capture system uses molten salt to (i) capture carbon dioxide and (ii) desorb the carbon dioxide, resulting in a stream comprising the desorbed CO2 and molten salt, wherein the stream comprises less than 50 mol% steam.

[0104] Molten salt flow molten borate

[0116] The carbon capture system may use molten salt. The molten salt may include molten borate. The borate is A x B 1-x O 1.5-x In such formulas, "A" refers to an alkali metal, "B" refers to boron, "O" refers to oxygen, and "x" is a value between 0 and 1.

[0105]

[0117] In some embodiments, "x" is a number between 0 and 1. In some embodiments, "x" is about 0.4, 0.45, 0.5, 0.55, 0.6, 0.65, 0.7, 0.75, 0.8, 0.85, 0.9, 0.91, 0.92, 0.93, 0.94, 0.95, 0.96, 0.97, 0.98, or 0.99. In some embodiments, "x" is a number between about 0.25 and about 0.98. In some embodiments, "x" is a number between about 0.3 and about 0.95. In some embodiments, "x" is a number between about 0.5 and about 0.95. In some embodiments, "x" is a number between about 0.6 and about 0.9. In some embodiments, "x" is about 0.75.

[0106]

[0118] In some embodiments, "A" comprises an alkali metal. The alkali metal may be lithium (Li), sodium (Na), potassium (K), rubidium (Rb), cesium (Cs), or francium (Fr). In some embodiments, "A" is lithium. In some embodiments, "A" is sodium. In some embodiments, "A" is potassium. In some embodiments, "A" is rubidium. In some embodiments, "A" is cesium. In some embodiments, "A" is francium. In some embodiments, "A" may comprise an alkaline earth metal. The alkaline earth metal may be beryllium (Be), strontium (Sr), calcium (Ca), magnesium (Mg), barium (Ba), or radium (Ra). In some embodiments, "A" may be any cation containing a +1 positive charge. In some embodiments, "A" may comprise a transition metal having a +1 charge (e.g., copper, silver, or any other transition metal). In some embodiments, "A" may comprise a transition metal. The transition metals are scandium (Sc), yttrium (Y), lanthanum (La), actinium (Ac), titanium (Ti), zirconium (Zr), hafnium (Hf), rutherfordium (Rf), vanadium (V), niobium (Nb), tantalum (Ta), dubnium (Db), chromium (Cr), molybdenum (Mo), tungsten (W), seaborgium (Sg), manganese (Mn), technetium (Tc), rhenium (Re), and boron. The metal can be sodium (Bh), iron (Fe), ruthenium (Ru), osmium (Os), hassium (Hs), cobalt (Co), rhodium (Rh), iridium (Ir), meitnerium (Mt), nickel (Ni), palladium (Pd), platinum (Pt), darmstadtium (Ds), copper (Cu), silver (Ag), gold (Au), roentgenium (Rg), zinc (Zn), cadmium (Cd), mercury (Hg), or copernicium (Cn). In some embodiments, the borate salt can include a mixture of metals. A can include an alkali metal, an alkaline earth metal, a transition metal, or a mixture of any combination thereof. For example, the formula for a borate salt is (A 1 y A 2 1-y ) xB 1-x O 1.5-x where A 1 and A 2 are each a separate "A" as described herein, "y" is a number from 0 to 1, and "x" is a number from 0 to 1. In some embodiments, the borate salt may include a mixture of lithium and sodium. In some embodiments, A 1 is lithium and A 2 is sodium. In some embodiments, A 1 is lithium and A 2 is sodium, y is 0.4, and x is 0.75. 1 is lithium and A 2 is sodium, y is 0.5, and x is 0.75. 1 is lithium and A 2 is sodium, y is 0.33, and x is 0.75. In some embodiments, the borate is Na 0.75 B 0.25 O 0.75 , (Li 0.5 Na 0.5 ) 0.75 B 0.25 O 0.75 , (Li 0.4 Na 0.6 ) 0.75 B 0.25 O 0.75 , (Li 0.3 Na 0.7 ) 0.75 B 0.25 O 0.75、 (Li 0.2 Na 0.8 ) 0.75 B 0.25 O 0.75 , (Li 0.1 Na 0.9 ) 0.75 B 0.25 O 0.75 , (Li 0.33 Na 0.33 K 0.33 ) 0.75 B 0.25 O 0.75 , (Li 0.4 Na 0.5 K0.1 ) 0.75 B 0.25 O 0.75 , (Li 0.7 Na 0.3 ) 0.5 B 0.5 O 1.0 , (Li 0.5 Na 0.5 ) 0.83 B 0.17 O 0.67 , (Li 0.7 Na 0.3 ) 0.83 B 0.17 O 0.67 , or (Li 0.3 Na 0.7 ) 0.83 B 0.17 O 0.67 The composition may include:

[0107]

[0119] In some embodiments, the borate salt may include impurities or contaminants, such as iron (Fe), chromium (Cr), nickel (Ni), manganese (Mn), molybdenum (Mo), cobalt (Co), vanadium (V), copper (Cu), zinc (Zn), aluminum (Al), titanium (Ti), cadmium (Cd), mercury (Hg), potassium (K), magnesium (Mg), silicon (Si), phosphorus (P), and sulfur (S), or any other contaminant. The amount of impurities in the borate salt can be at most about 30 weight percent (wt%), 20 wt%, 10 wt%, 5 wt%, 2 wt%, 1 wt%, 0.5 wt%, 0.1 wt%, 0.08 wt%, 0.05 wt%, 0.01 wt%, 0.005 wt%, 0.001 wt%, or less.

[0108]

[0120] In some embodiments, Formula A 0.75 B 0.25 O 0.75 In some embodiments, the borate salt comprising the formula A may be represented as ABO. 0.5 B 0.5 O 1.0 In some embodiments, the borate salt comprising the formula A 0.83 B 0.17 O 0.67Borates containing the compound may be represented as A5BO4.

[0109] Molten salt flow

[0121] The carbon capture system may include one or more streams comprising molten salt. In some embodiments, each stream of the one or more streams may comprise molten borate. In some embodiments, the system or process may include multiple streams, wherein at least one of the multiple streams has a different composition.

[0110]

[0122] The first stream may refer to a stream of molten salt fed to the absorber. The second stream may refer to a stream generated from contacting gaseous carbon-containing material with molten salt (e.g., the first stream) in the absorber. The third stream may refer to a stream after desorption of the carbon-containing material. The third stream and the first stream may be carbon-lean streams. The second stream may be a carbon-rich stream. In some embodiments, the concentrations of carbon in each stream are related. For example, the carbon-lean stream (e.g., the first or third stream) may contain a small amount of carbon-containing material, but the concentration of carbon-containing material in the first or third stream is lower than the concentration of carbon-containing material in the second stream (e.g., the carbon-rich stream). The first stream may at least partially comprise regenerated molten salt from the third stream. For example, the first stream may comprise at least a portion of the third stream. The first stream may be a regenerated stream (e.g., the third stream). The first stream may include the regenerated stream in addition to new molten salt. The new molten salt may be combined with the third stream to form the first stream. The concentrations of carbon-containing materials in the first and third streams can be the same or different.

[0111]

[0123] In some embodiments, the first stream may contain a carbonaceous material (e.g., carbon dioxide, carbon monoxide) concentration per kilogram of molten salt of at least about 0.01 moles (mol / kg), 0.05 mol / kg, 0.1 mol / kg, 0.5 mol / kg, 1.0 mol / kg, 1.5 mol / kg, 2 mol / kg, 3 mol / kg, 4 mol / kg, 5 mol / kg, or 6 mol / kg. In some embodiments, the first stream may contain a carbonaceous material concentration of at least about 0.01 mol / kg to about 4 mol / kg. In some embodiments, the first stream may contain a carbonaceous material concentration of at least about 2 mol / kg to about 4 mol / kg. In some embodiments, the first stream is free of carbonaceous material. In some embodiments, the first stream may contain a carbonaceous material concentration of at least 0.01 mol / kg of molten salt. In some embodiments, the first stream may contain a carbonaceous material concentration of at least 3 mol / kg of molten salt. In some embodiments, the first stream may include a carbon-containing material concentration of at least 4 mol / kg of molten salt.

[0112]

[0124] In some embodiments, the second stream can include a concentration of carbonaceous material (e.g., carbon dioxide, carbon monoxide) per kilogram of molten salt of at least about 0.1 moles per kilogram (mol / kg), 1 mol / kg, 5 mol / kg, 6 mol / kg, 7 mol / kg, 8 mol / kg, 9 mol / kg, 10 mol / kg, 20 mol / kg, or more. In some embodiments, the second stream can include a concentration of carbonaceous material of at least 5 mol / kg of molten salt. In some embodiments, the second stream can include a concentration of carbonaceous material of at least 10 mol / kg of molten salt. The concentration of carbonaceous material in the second stream can always be greater than the concentration of carbonaceous material in the first stream.

[0113]

[0125] In some embodiments, the third stream may contain a carbonaceous material (e.g., carbon dioxide, carbon monoxide) concentration per kilogram of molten salt of at least about 0.01 moles (mol / kg), 0.05 mol / kg, 0.1 mol / kg, 0.5 mol / kg, 1.0 mol / kg, 1.5 mol / kg, 2 mol / kg, 3 mol / kg, 4 mol / kg, 5 mol / kg, or 6 mol / kg. In some embodiments, the first stream may contain a carbonaceous material concentration of at least about 0.01 mol / kg to about 4 mol / kg. In some embodiments, the first stream may contain a carbonaceous material concentration of at least about 2 mol / kg to about 4 mol / kg. In some embodiments, the third stream is free of carbonaceous material. In some embodiments, the third stream may contain a carbonaceous material concentration of at least 0.01 mol / kg of molten salt. In some embodiments, the third stream may contain a carbonaceous material concentration of at least 3 mol / kg of molten salt. In some embodiments, the third stream can include a carbonaceous material concentration of at least 4 mol / kg of molten salt. The concentration of the carbonaceous material in the second stream can always be greater than the concentration of the carbonaceous material in the third stream.

[0114] In some embodiments, the first and third streams may be referred to herein as carbon-lean molten salt streams. In some embodiments, the second stream may be referred to herein as a carbon-rich stream. The carbon-lean stream may contain at least some amount of carbon-containing material. In some embodiments, the carbon-lean stream may be free of carbon-containing material. As described herein, the carbon-lean stream contains a lower concentration of carbon-containing material when compared to the concentration of carbon-containing material in the carbon-rich stream.

[0115] Carbon Capture and Molten Salt Regeneration

[0126] Described herein is a process for absorbing carbon dioxide into molten salt and regenerating the molten salt and carbon dioxide in a desorber. An absorber may be used to contact gaseous carbon-containing materials (e.g., carbon dioxide, carbon monoxide) with molten salt, as described elsewhere herein, thereby transferring the gaseous carbon-containing materials to a liquid stream of molten salt. The stream containing the absorbed carbon-containing materials may be referred to herein as a carbon-rich stream or a rich stream. The rich stream may be directed to a desorber, where the molten salt may be regenerated, and the stream containing the desorbed carbon-containing materials may be further cooled, compressed, and / or prepared for export elsewhere in the system or external to the system. For example, the desorbed carbon-containing materials may be exported for injection into the formation or converted into products such as fuels or other chemicals. The regenerated molten salt may also be referred to herein as carbon-lean molten salt or a lean molten salt. The lean molten salt may be transferred again to the absorber for another cycle of carbon capture.

[0116]

[0127] The absorber can be located in the convection section of the high-temperature system, whereby flue gas (e.g., exhaust gas) can flow upward toward the absorber and molten salt (e.g., the first or third stream) can flow downward toward the absorber. When flue gas containing carbonaceous material is contacted with a stream containing molten salt (e.g., the first stream), an exothermic reaction can occur as the carbonaceous material reacts and is absorbed into borate salt. Heat generated from the exothermic reaction can be captured in situ and used to heat a process fluid in tubes embedded throughout the packing material in the packed bed of the convection section, thereby recovering energy. In some embodiments, the process fluid is water for generating steam. In some embodiments, the process fluid is steam for generating superheated steam. In some embodiments, the process fluid is air for generating hot air or preheater air. In some embodiments, the process fluid can include a combination of water, steam, and air. The flow of a heat transfer medium (e.g., steam) through the tubes can control the temperature of the absorber. In some embodiments, the absorber packing material is integrated with an exchanger (e.g., a salt-salt heat exchanger). In such embodiments, the heat exchanger may include a steam bundle for generating steam. The steam bundle may include one or more pipes disposed inside a boiler containing water. The steam bundle may be referred to herein as a water tube or vane wall.

[0117]

[0128] Absorption of carbon-containing substances alters the structure of the initial borate. For example, carbon dioxide can react with borate to form carbonate and altered borate as shown below: A3BO3+CO2--> ABO2+A2CO3, (Li 0.5 Na 0.5 )3BO3+CO2--> (Li 0.5 Na 0.5 )BO2+(Li 0.5 Na 0.5 )2CO3, A 0.75 B 0.25 O 0.75 +CO2 → A 0.5 B 0.5 O 1.0 +A2CO3, 1 / (x - 0.5)A x B 1-x O 1.5-x + CO2 → (1 - x) / (x - 0.5)ABO2 + A2CO3, where 0.5 < x < 1.0, or A x B 1-x O 1.5-x + CO2 → A y B 1-y O 1.5-y + A z CO3, where 0.0 < x < 1.0, 0.0 < y < 1.0, 0.0 < z < 2.0. The reaction between the borate and carbon dioxide may be reversible. In some embodiments, the resulting carbonate (A2CO3) is a liquid. In some embodiments, other components of the flue gas (e.g., components not absorbed by the borate) may exit the system through an exhaust stack.

[0118]

[0129] The methods and systems described herein may include a small amount of vapor in the process of removing carbon-containing substances from a melt salt-containing stream. In some embodiments, the vapor may occupy the headspace near the carbon-rich stream during desorption. In some embodiments, for at least a portion of the time during which desorption is performed, the headspace may contain vapor in an amount of at most 70 weight percent (wt%), 60 wt%, 50 wt%, 40 wt%, 30 wt%, 20 wt%, 10 wt%, 5 wt%, 1 wt%, or less. In some embodiments, for at least a portion of the time during which desorption is performed, the headspace may contain approximately 0 wt % vapor. In some embodiments, for at least a portion of the time during which desorption is performed, the headspace may not contain a detectable amount of vapor. The remaining volume within the headspace may contain carbon-containing gas.

[0119]

[0130] In some embodiments, the molar ratio of steam in the gas phase to carbon-containing material absorbed in the carbon-rich stream (e.g., the second stream) in the desorber during desorption can be at most 1, at most 0.9, 0.8, 0.7, 0.6, 0.5, 0.4, 0.3, 0.2, 0.1, 0.05, or less, at least over the portion of time during which desorption is occurring. In some embodiments, the molar ratio of steam in the gas phase to carbon-containing material absorbed in the carbon-rich stream can be 0.

[0120]

[0131] In some embodiments, the molar ratio of steam in the gas to molten salt in the desorber can be at most 0.1, 0.05, 0.01, or less. In some embodiments, the molar ratio of steam in the gas to molten salt in the desorber can be 0.

[0121]

[0132] In some embodiments, the second stream delivered to the desorber contains at most 70 mol%, 60 mol%, 50 mol%, 40 mol%, 30 mol%, 20 mol%, 10 mol%, 5 mol%, 2 mol%, 1 mol%, 0.5 mol%, or less steam. In some embodiments, the second stream may contain about 0 mol% steam. In some embodiments, the second stream may be free of steam. In some embodiments, the second stream may have no detectable steam.

[0122]

[0133] In some embodiments, the stream containing the regenerated molten salt (the third stream) may contain less than 50 mole percent (mol%) steam, 40 mol% steam, 30 mol% steam, 20 mol% steam, 10 mol% steam, 5 mol% steam, 2 mol% steam, 1 mol% steam, 0.5 mol% steam, or less. In some embodiments, the third stream may contain less than 20 mol% steam. In some embodiments, the third stream may contain less than 10 mol% steam. In some embodiments, the third stream may contain less than 5 mol% steam. The methods and systems described herein may not use steam in the process of desorbing carbon-containing materials from the molten salt stream during the regeneration process. In some embodiments, the third stream may contain approximately 0 mol% steam. In some embodiments, the third stream may be free of steam. In some embodiments, the third stream may have no detectable steam.

[0123]

[0134] The desorbed carbonaceous material may be prepared for export from the desorber. In some embodiments, the desorbed carbonaceous material may be stored on-site. In some embodiments, the desorbed carbonaceous material may be provided as an export stream. In some embodiments, the export stream may include a carbonaceous material (e.g., carbon dioxide) concentration of at least about 50%, 60%, 70%, 80%, 90%, 95%, 99%, 99.9%, or more. In some embodiments, the export stream may include a carbonaceous material concentration of at least about 80%. In some embodiments, the export stream may include a carbonaceous material concentration of at least about 90%. In some embodiments, the export stream may include a carbonaceous material concentration of at least about 95%. In some embodiments, the export stream may include a carbonaceous material concentration of at least about 99%. In some embodiments, the export stream may include a carbonaceous material concentration of at least about 99.9%.

[0124]

[0135] In some embodiments, the export stream may be passed through a convection section of the high temperature system. Passing the export stream through the convection section cools the stream and may recover heat through the generation of steam or the transfer of heat to another process fluid.

[0125] Computer Systems

[0136] In one aspect, the present disclosure provides a computer system programmed or otherwise configured to implement the methods of the present disclosure, e.g., any of the subject methods for capturing carbon dioxide using molten salt. Figure 7 shows a computer system 701 programmed or otherwise configured to implement a method for capturing carbon dioxide using molten salt. The computer system 701 can be configured, for example, to control the flow of carbon dioxide into the system or to monitor energy output as described elsewhere herein. The computer system 701 can be a user's electronic device or a computer system located remotely relative to the electronic device. The electronic device can be a mobile electronic device.

[0126]

[0137] The computer system 701 may include a central processing unit (CPU; herein also referred to as "processor" and "computer processor") 705, which can be a single-core or multi-core processor, or multiple processors for parallel processing. The computer system 701 also includes memory or memory locations 710 (e.g., random access memory, read-only memory, flash memory), electronic storage 715 (e.g., hard disk), a communication interface 720 (e.g., network adapter) for communicating with one or more other systems, and peripheral devices 725, such as cache, other memory, data storage, and / or an electronic display adapter. The memory 710, storage 715, interface 720, and peripheral devices 725 communicate with the CPU 705 through a communication bus (solid lines), such as a motherboard. The storage 715 can be a data storage device (or data repository) for storing data. The computer system 701 may be operably coupled to a computer network ("network") 730 with the aid of the communication interface 720. Network 730 can be the Internet, an Internet and / or extranet, or an intranet and / or extranet in communication with the Internet. Network 730 is, in some cases, a telecommunications and / or data network. Network 730 can include one or more computer servers, which can enable distributed computing, such as cloud computing. Network 730 can, in some cases, implement a peer-to-peer network, which can enable devices coupled to computer system 701 to act as clients or servers, with the aid of computer system 701.

[0127]

[0138] The CPU 705 can execute a series of machine-readable instructions, which may be embodied in the form of a program or software. The instructions may be stored in a memory location, such as the memory 710. The instructions may be directed to the CPU 705, which can then program or otherwise configure the CPU 705 to implement the methods of the present disclosure. Examples of operations performed by the CPU 705 may include fetch, decode, execute, and writeback.

[0128]

[0139] The CPU 705 can be part of a circuit, such as an integrated circuit. One or more other components of the system 701 can also be included in the circuit. In some cases, the circuit is an application specific integrated circuit (ASIC).

[0129]

[0140] Storage device 715 can store files such as drivers, libraries, and saved programs. Storage device 715 can store user data, such as user preferences and user programs. Computer system 701 may optionally include one or more additional data storage devices located outside of computer system 701 (e.g., on a remote server in communication with computer system 701 over an intranet or the Internet).

[0130]

[0141] Computer system 701 can communicate with one or more remote computer systems over network 730. For example, computer system 701 can communicate with a remote computer system of a user (e.g., an operator overseeing or monitoring carbon dioxide capture, energy output, etc.). Examples of remote computer systems include a personal computer (e.g., a portable PC), a slate or tablet PC (e.g., an Apple® iPad, a Samsung® Galaxy Tab), a telephone, a smartphone (e.g., an Apple® iPhone, an Android-enabled device, a Blackberry®), or a personal digital assistant. A user can access computer system 701 over network 730.

[0131]

[0142] Methods as described herein may be implemented through machine (e.g., computer processor) executable code stored on electronic storage locations of computer system 701, such as, for example, on memory 710 or electronic storage 715. The machine-executable or machine-readable code may be provided in the form of software. During use, the code may be executed by processor 705. In some cases, the code may be retrieved from storage 715 and stored on memory 710 for immediate access by processor 705. In some circumstances, electronic storage 715 may be omitted, and machine-executable instructions stored on memory 710.

[0132]

[0143] The code may be precompiled and configured for use by a machine having a processor adapted to execute the code, or may be compiled during run time. The code may be supplied in a programming language selected to allow the code to be executed in a precompiled or as-compiled manner.

[0133]

[0144] Aspects of the systems and methods provided herein, such as computer system 701, may be embodied in the form of programming. Various aspects of the technology may be considered a "product" or "article of manufacture," typically in the form of machine (or processor) executable code and / or associated data carried on or embodied within some type of machine-readable medium. The machine-executable code may be stored on electronic storage, such as memory (e.g., read-only memory, random-access memory, flash memory) or a hard disk. A "storage" type medium may include any or all of the tangible memory of a computer, processor, or the like, or their associated modules, such as various semiconductor memories, tape drives, disk drives, and the like, which may provide non-transitory storage for software programming from time to time. All or portions of the software may, from time to time, be communicated over the Internet or various other telecommunications networks. Such communication may enable, for example, loading of the software from one computer or processor into another, e.g., from a management server or host computer into the computer platform of an application server. Thus, other types of media that may carry software elements include, for example, light waves, radio waves, and electromagnetic waves used across physical interfaces between local devices, through wired and optical landline networks, and over various air links. Physical elements that carry such waves, such as wired or wireless links, optical links, or the like, may also be considered software-bearing media. As used herein, unless limited to non-transitory tangible "storage" media, terms such as computer or machine "readable medium" refer to any medium that participates in providing instructions to a processor for execution.

[0134]

[0145] Thus, machine-readable media, such as computer-executable code, may take many forms, including, but not limited to, tangible storage media, carrier wave media, or physical transmission media. For example, non-volatile storage media, including optical or magnetic disks, or any storage device within any computer(s) or the like, may be used to implement the databases, etc., shown in the figures. Volatile storage media include dynamic memory, such as the main memory of such a computer platform. Tangible transmission media include coaxial cables, copper wire, and fiber optics, including the wiring that comprises a bus within a computer system. Carrier-wave transmission media may take the form of electric or electromagnetic signals, or acoustic or light waves, such as those generated during radio frequency (RF) and infrared (IR) data communications. Thus, common forms of computer readable media include, for example, floppy disks, flexible disks, hard disks, magnetic tape, any other magnetic media, CD-ROMs, DVDs or DVD-ROMs, any other optical media, punched cards, paper tape, any other physical storage media with a pattern of holes, RAM, ROM, PROMs and EPROMs, Flash EPROMs, any other memory chips or cartridges, carrier waves that transport data or instructions, cables or links that transport such carrier waves, or any other medium from which a computer can read programming code and / or data. Many of these forms of computer readable media may be involved in carrying one or more sequences of one or more instructions to a processor for execution.

[0135]

[0146] The computer system 701 may include or communicate with an electronic display 735 that includes a user interface (UI) 740 to provide, for example, a portal for a user to monitor or track one or more processes for producing flexible film materials from waste cooking oil and compounds derived therefrom. The portal may be provided through an application programming interface (API). A user or entity may also interact with various elements within the portal through the UI. Examples of UIs include, but are not limited to, graphical user interfaces (GUIs) and web-based user interfaces.

[0136]

[0147] The methods and systems of the present disclosure may be implemented through one or more algorithms. The algorithms may be implemented through software when executed by the central processing unit 705. For example, the algorithms may be configured to adjust the operation of the system in response to energy demands (e.g., decreasing energy output or increasing energy output). [Example]

[0137] Example Example 1: CO2 capture via solid fuel, with the absorber placed directly above the desorber.

[0148] FIG. 2 illustrates a process for capturing carbon dioxide from solid fuel in which an absorber is located in the convection section directly above a desorber in the radiant section. Solid fuel (201) enters the high-temperature system through a bunker (205) and may be combusted when contacted with air (202) in a boiler (210). Carbon dioxide (not shown) produced as a by-product of combustion in the boiler (210) may be directed to an absorber (220). In some cases, molten borate enters the absorber from the top (CO2-lean stream), trickles down a packed bed where it contacts the carbon dioxide, and collects at the bottom of the absorber as a CO2-rich stream. The CO2-rich stream may be directed via gravity to a salt-salt heat exchanger (240) before entering the desorber (250). In the desorber (250), CO2 is desorbed from the molten salt and exits to be prepared for export elsewhere in the system. The CO2-lean molten salt is then directed to the salt pump (260) and again passed through the salt-salt heat exchanger (240). The CO2-lean stream is then directed again to the absorber (220) and passed through a filter (270) to separate any solids before being used for another cycle of CO2 capture. The absorber may have a temperature of about 600°C, while the desorber has a temperature of about 900°C.

[0138] Example 2: CO2 capture via solid fuel, with an absorber placed in parallel with a desorber.

[0149] Figure 3 shows a process for capturing carbon dioxide from solid fuel in which an absorber in the convection section is arranged in parallel with a desorber in the radiant section. Solid fuel (301) enters the high-temperature system through a bunker (305) and may be combusted in a boiler (310) where it is contacted with air (302). Carbon dioxide (not shown) produced as a by-product of combustion in the boiler (210) may be directed to an absorber (320). Molten borate enters the absorber from the top (CO2-lean stream) and trickles down the packed bed where it contacts the carbon dioxide, collecting at the bottom of the absorber as a CO2-rich stream. The CO2-rich stream may be directed to a transfer pump (330) before being directed through a salt-salt heat exchanger (340) and finally to a desorber (350). In the desorber (350), the CO2 is desorbed from the molten salt and exits to be prepared for export elsewhere in the system, while the CO2-lean stream is again directed through the salt-salt heat exchanger (340). The CO2-lean molten salt is then directed to a salt pump (360) and passed through a filter (370) to separate any solids before being directed back to the absorber (320) and used for another cycle of CO2 capture. The absorber may have a temperature of about 600°C, while the desorber has a temperature of about 900°C.

[0139] Example 3: CO2 capture via gas fuel with an absorber placed in the convective section directly above the desorber in the radiative section.

[0150] FIG. 4 illustrates a process for capturing carbon dioxide from a gaseous fuel in which an absorber is located in the convection section directly above a desorber in the radiant section. The gaseous fuel (401) may enter a high-temperature system including a boiler (410) where it is combusted in contact with air (402). Within the boiler (410), carbon dioxide (not shown) produced as a by-product of combustion may be directed to an absorber (420). Molten borate enters the absorber at the top (CO2-lean stream), trickles down a packed bed where it contacts the carbon dioxide, and collects at the bottom of the absorber as a CO2-rich stream. The CO2-rich stream may be directed and passed through a rich salt pump (430) before being directed to a salt-salt heat exchanger (440) before finally entering the desorber (450). Within the desorber (450), the CO2 is desorbed from the molten salt and exits to be prepared for export elsewhere in the system. The CO2-lean molten salt is again directed to the salt-salt heat exchanger (440) and then to the salt pump (460). The CO2-lean molten salt is then again directed to the absorber (420) and passed through a filter (470) to separate any solids before being used for another cycle of CO2 capture. The absorber may have a temperature of about 600°C, while the desorber has a temperature of about 900°C.

[0140] Example 4: CO2 capture via gas fuel with absorber in parallel with desorber

[0151] FIG. 5 illustrates a process for capturing carbon dioxide from a gaseous fuel in which an absorber in the convective section is arranged in parallel with a desorber in the radiant section. The gaseous fuel (501) may enter a high-temperature system including a boiler (510) where it is combusted in contact with air (502). Within the boiler (510), carbon dioxide (not shown) produced as a by-product of combustion may be directed to an absorber (520). Molten borate enters the absorber at the top (CO2-lean stream), trickles down a packed bed where it contacts the carbon dioxide, and collects at the bottom of the absorber as a CO2-rich stream. The CO2-rich stream may be directed and passed through a rich salt pump (530) before being directed to a salt-salt heat exchanger (540) before finally entering the desorber (550). Within the desorber (450), the CO2 is desorbed from the molten salt and exits to be prepared for export elsewhere in the system. The CO2-lean molten salt is again directed to the salt-salt heat exchanger (540) and then to the salt pump (560). The CO2-lean molten salt is then again directed to the absorber (520) and passed through a filter (570) to separate any solids before being used for another cycle of CO2 capture. The absorber may have a temperature of about 600°C, while the desorber has a temperature of about 900°C.

[0141] Example 5: CO2 capture via gas fuel where an absorber is placed in parallel above a desorber with a tube-in-tube heat exchanger.

[0152] Figure 6 illustrates a process for capturing carbon dioxide from a gaseous fuel in which an absorber in the convection section, which also includes a storage compartment, is arranged in parallel with a desorber in the radiant section. The gaseous fuel (601) may enter a high-temperature system including a boiler (610) where it is combusted against air (602), thereby producing flue gas. Within the boiler (610), the carbon dioxide in the flue gas may be directed to an absorber (620), while the remaining flue gas is directed out of the system. Molten borate enters the absorber from the top (carbon-lean molten stream), trickles down a packed bed where it contacts the carbon dioxide, and collects in a storage compartment (635) at the bottom of the absorber as a carbon-rich stream. The carbon-rich molten salt may be transferred via a pump (630) to a tube-in-tube heat exchanger (640). The desorber (650) includes a tube-in-tube heat exchanger (640), where the carbon-rich molten salt travels up the outer tube (not shown) of the tube-in-tube heat exchanger (640), where carbon dioxide is released. The carbon-lean molten salt may travel back down the inner tube (not shown) of the tube-in-tube heat exchanger (640) and enter a storage compartment (680). The carbon-lean molten salt in the storage compartment (680) may be directed through a pump (685) and passed through a filter (670) before re-entering the absorber (620). The released carbon dioxide may reside in a carbon dioxide drum (655) before being directed through a cooler (656) and fan (658) for export elsewhere in the system. Separately, steam may be generated in a steam drum (698), where boiler feedwater from a tank (690) is contacted with heat from the boiler (610). Boiler feedwater may be used to regulate the temperature in the convection section of the high temperature system, while excess steam may be carried away from the steam drum (698).

[0142] Example 6: CO2 capture and heat recovery

[0153] FIG. 8 illustrates a process for capturing carbon dioxide (CO2) from an industrial process. The industrial process may include fuel combustion in a high-temperature system (810). The high-temperature system may be a boiler chamber (i.e., firebox) where fuel is burned. Fuel (801) enters the high-temperature system and is brought into contact with air (802), where it may be combusted, thereby producing CO2. Heat generated in the high-temperature system may be transferred to a pipe or piping system containing liquid water and used to heat the liquid water to gaseous steam in a steam line (ST-1). Alternatively, another high-temperature fluid may be used. The CO2 produced as a by-product of combustion may be directed to an absorber (820). The CO2 may exit the high-temperature system near the top and be pumped to the bottom of the absorber (820) via line (825). In some cases, molten borate enters the absorber from the top and trickles down the packed bed where it contacts and captures at least a portion of the CO2, thereby obtaining a CO2-rich molten salt stream. The CO2-rich molten salt stream may collect at the bottom of the absorber. Heat generated in the absorber may be transferred to a piping system containing liquid water and used to heat the liquid water to gaseous steam in a steam line (ST-2). The CO2-rich molten salt stream may be stored for a period of time in a rich storage tank (830). The CO2-rich molten salt stream may be directed to a salt-salt heat exchanger (840) using one or more pumps. After exiting the salt-salt heat exchanger (840), the CO2-rich molten salt stream may be directed to a desorber (850). The desorber (850) may be located in whole or in part within the high-temperature system (810). Heat generated from the high-temperature system (i.e., a boiler) may facilitate desorption of CO2 from the molten salt. The desorber (850) may be a series of pipes or tubes disposed within the high temperature system (810). The desorber (850) may be in a coiled configuration. In the desorber (850), CO2 may be desorbed from the molten salt, resulting in a CO2-lean molten salt stream and a CO2 stream. A CO2 drum (855) may be used to separate the CO2 stream and the CO2-lean molten salt stream. The CO2 may be cooled using a CO2 cooler (860).The CO2 chiller (860) may contain a liquid water stream used to cool the CO2. In the CO2 chiller, the CO2 may heat the water. The liquid water may be heated so that it exits the CO2 chiller as a gaseous vapor in the vapor line (ST-3). After exiting the CO2 chiller (860), the CO2 may be processed for export. The CO2 may enter a multi-stage compression system with intercooling. The CO2 may be transported and used off-site or stored (see Figure 10). In some cases, the captured CO2 is stored underground.

[0143]

[0154] The CO2-lean molten salt stream exits the CO2 drum (855) and may be directed to a salt-salt heat exchanger (840). The salt-salt heat exchanger (840) may facilitate heat transfer from the CO2-lean molten salt stream to the CO2-rich molten salt stream, thereby heating the CO2-rich molten salt stream before entering the desorber (850). After exiting the salt-salt heat exchanger (840), the CO2-lean molten salt stream may be stored for a period of time in a lean storage tank (863). The CO2-lean molten salt stream may be directed to a salt cooler (865). The salt cooler (865) may be used to transfer heat from the CO2-lean molten salt stream to another fluid. In some cases, the heat transferred from the CO2-lean molten salt stream in the salt cooler (865) may be recovered. In some cases, the heat transferred from the CO2-lean molten salt stream in the salt cooler (865) may be used to preheat air. In some cases, heat transferred from the CO2-lean molten salt stream in the salt cooler (865) can be used to heat water. The liquid water can be heated, causing it to exit the salt cooler as a gaseous vapor in the steam line (ST-4). The CO2-lean molten salt stream can then exit the salt cooler (865) and enter the absorber (820) to capture additional CO2. Steam generated at any point in the system can exit the system as export steam. Steam from steam lines ST-1, ST-2, ST-3, and ST-4 can be combined and exit the system through a single export stream (870). Before exiting the system, the steam can pass through a steam drum (875). The export stream (870) can be fed to a steam turbine (see FIG. 10), which can be used to convert the thermal energy in the steam into electricity. Steam lines ST-1, ST-2, ST-3, and ST-4 can be fluidly connected to a single water source or multiple water sources. Water may be pumped from a single source (i.e., a water tank) and partially diverted at various points in the system. A first portion of the water may be diverted to the CO2 cooler (860), where it is heated to steam, which flows through steam line ST-3. A second portion of the water may be diverted to recover heat from the high temperature system, where it is heated to steam, which flows through steam line ST-1.A third portion of the water may be diverted to the salt cooler (865) where it is heated to steam, which flows through steam line ST-3. A fourth portion of the water may be diverted to recover heat from the absorber, where it is heated to steam, which flows through steam line ST-2.

[0144] Example 7: CO2 capture from multiple CO2 sources

[0155] In some cases, CO2 may be captured from one or more additional flue sources (in addition to the CO2 captured from the high-temperature system located in or near the desorber). For example, FIG. 9 shows the system of FIG. 8 with an additional CO2 source (880). The additional CO2 source can be an existing flue. CO2 from the additional CO2 source (880) can be fed into the absorber (820). The CO2 from the additional CO2 source (880) can be combined with CO2 from the high-temperature system in the absorber (820). The additional CO2 source (880) can be an existing system. The system shown in FIG. 8 can be retrofitted to an existing system to capture CO2 and mitigate the CO2 emissions of the existing system, thereby achieving the design shown in FIG. 9.

[0145] Example 8: CO2 capture from a flue source external to a high temperature system

[0156] FIG. 11 illustrates a process for capturing carbon dioxide from a flue (880). The flue source (880) may contain carbon dioxide (CO2) as a by-product of an industrial process. The CO2-containing flue may be directed to an absorber (820). Optionally, molten borate enters the absorber from the top and trickles down a packed bed where it contacts and captures at least a portion of the CO2, thereby obtaining a CO2-rich molten salt stream. The CO2-rich molten salt stream may collect at the bottom of the absorber. Heat generated in the absorber may be transferred to a piping or tubing system containing liquid water and used to heat the liquid water in a steam line (ST-2) to a gaseous vapor. The CO2-rich molten salt stream may be stored for a period of time in a rich storage tank (830). The CO2-rich molten salt stream may be directed to a salt-salt heat exchanger (840) using one or more pumps. After exiting the salt-salt heat exchanger (840), the CO2-rich molten salt stream can be directed to a desorber (850). The desorber (850) can be located entirely or partially within the high-temperature system (810). The high-temperature system (810) can be a boiler chamber (i.e., firebox) in which fuel is burned. When fuel (801) enters the high-temperature system and is contacted with oxygen (803), it can be combusted, thereby producing CO2 and water vapor. The oxygen source can be at least 90%, 95%, 96%, 97%, 98%, 99%, or 99.5% oxygen. The CO2 produced in the high-temperature system can be cooled, pressurized, and exported. Heat generated in the high-temperature system can be transferred to a piping or tubing system containing liquid water and used to heat the liquid water in the steam line (ST-1) to gaseous steam. Alternatively, another high-temperature fluid can be used. Heat generated from the high temperature system (i.e., boiler) can facilitate the desorption of CO from the molten salt. The desorber (850) can be a series of pipes or tubes disposed within the high temperature system (810). The desorber (850) can be in a coil configuration. Alternatively, the desorber could be in a tube-in-tube or packed bed configuration. Within the desorber (850), CO can be desorbed from the molten salt, thereby producing a CO lean molten salt stream and a CO stream. A CO drum (855) can be used to separate the CO and CO lean molten salt streams.The CO2 can be cooled using a CO2 chiller (860). The CO2 chiller (860) can contain a liquid water stream used to cool the CO2. In the CO2 chiller, the CO2 can heat the water. The liquid water can be heated so that it exits the CO2 chiller as a gaseous vapor in a vapor line (ST-3). After exiting the CO2 chiller (860), the CO2 can be processed for export. The CO2 can enter a multi-stage compression system with intercooling. The CO2 can be transported and used off-site or stored (see Figure 10). In some cases, the captured CO2 is stored underground.

[0146]

[0157] The CO2-lean molten salt stream exits the CO2 drum (855) and may be directed to a salt-salt heat exchanger (840). The salt-salt heat exchanger (840) may facilitate heat transfer from the CO2-lean molten salt stream to the CO2-rich molten salt stream, thereby heating the CO2-rich molten salt stream before entering the desorber (850). After exiting the salt-salt heat exchanger (840), the CO2-lean molten salt stream may be stored for a period of time in a lean storage tank (863). The CO2-lean molten salt stream may be directed to a salt cooler (865). The salt cooler (865) may be used to transfer heat from the CO2-lean molten salt stream to another fluid. In some cases, the heat transferred from the CO2-lean molten salt stream in the salt cooler (865) may be recovered. In some cases, the heat transferred from the CO2-lean molten salt stream in the salt cooler (865) may be used to preheat air. In some cases, heat transferred from the CO2-lean molten salt stream in the salt cooler (865) can be used to heat water. The liquid water can be heated, causing it to exit the salt cooler as a gaseous vapor in the steam line (ST-4). The CO2-lean molten salt stream can then exit the salt cooler (865) and enter the absorber (820) to capture additional CO2. Steam generated at any point in the system can exit the system as export steam. Steam from steam lines ST-1, ST-2, ST-3, and ST-4 can be combined and exit the system through a single export stream (870). Before exiting the system, the steam can pass through a steam drum (875). The export stream (870) can be fed to a steam turbine (see FIG. 10), which can be used to convert the thermal energy in the steam into electricity. Steam lines ST-1, ST-2, ST-3, and ST-4 can be fluidly connected to a single water source or multiple water sources. Water may be pumped from a single source (i.e., a water tank) and partially diverted at various points in the system. A first portion of the water may be diverted to the CO2 cooler (860), where it is heated to steam, which flows through steam line ST-3. A second portion of the water may be diverted to recover heat from the high temperature system, where it is heated to steam, which flows through steam line ST-1.A third portion of the water may be diverted to the salt cooler (865) where it is heated to steam, which flows through steam line ST-3. A fourth portion of the water may be diverted to recover heat from the absorber, where it is heated to steam, which flows through steam line ST-2.

[0147] Example 9: Desorption via direct spraying of CO2-rich molten salt

[0158] In some cases, the system shown in FIG. 11 can be modified so that the CO2-rich molten salt stream is sprayed directly into the high-temperature system (810) in the desorber (850). This configuration is shown in FIG. 12. CO2 can be desorbed from the molten salt, resulting in a desorbed CO2 and CO2-lean molten salt stream. The CO2-lean molten salt stream can exit the desorber (850) and be directed to a salt-salt heat exchanger (840). Thus, the desorbed CO2 and CO2 generated in the high-temperature system via combustion of fuel and oxygen can be combined. The combined CO2 can be cooled, pressurized, and exported.

[0148] Example 10: Electrical heating of the desorber

[0159] In some cases, the systems described herein can be modified so that the desorber is heated electrically. Electrical heating can provide additional heating to facilitate desorption of CO from the molten salt in the desorber. In some cases, electrical heating can completely replace the need for a high temperature system, as shown in Figure 13. Figure 13 shows the system of Figure 12 modified so that the desorber is heated entirely electrically.

[0149]

[0160] While specific embodiments of the present systems and methods have been shown and described herein, it will be apparent to those skilled in the art that such embodiments are provided by way of example only. The systems and methods described herein are not intended to be limited by the specific examples provided herein. The descriptions and illustrations of the embodiments herein are not intended to be construed in a limiting sense. Those skilled in the art will now envision numerous variations, changes, and substitutions without departing from the systems and methods described herein. Furthermore, it should be understood that all aspects of the systems and methods described herein are not limited to the specific depictions, configurations, or relative proportions set forth herein, which depend upon a variety of conditions and variables. It should be understood that various alternatives to the embodiments described herein may be employed. Accordingly, it is intended that the systems and methods described herein encompass any such alternatives, modifications, variations, or equivalents. The appended claims define the scope of the systems and methods described herein, and it is intended that methods and structures within the scope of these claims and their equivalents be covered thereby.

Claims

1. Carbon dioxide (CO) from industrial processes ２ ) ... (a) CO ２ providing a gas stream comprising: (b) contacting the gas stream with a first stream comprising a molten salt in an absorber, thereby removing CO from the gas stream; ２ into the first stream, and ２ generating a second stream comprising: (c) directing the second stream to a desorber; (d) using the desorber to remove the absorbed CO ２ from the second stream, thereby producing (i) a third stream comprising the molten salt, and (ii) the CO desorbed from the second stream. ２ wherein the third stream comprises less than 50 mol% steam; A method comprising:

2. The method of claim 1 , wherein at least a portion of the industrial process occurs in a kiln.

3. The method of claim 1 , wherein at least a portion of the industrial process occurs in a boiler.

4. The method of claim 1 , wherein at least a portion of the industrial process occurs in a combustion chamber.

5. The method of claim 1 , wherein at least a portion of the industrial process is carried out in a reactor.

6. The method of claim 1 , wherein at least a portion of the industrial process is carried out in a furnace.

7. 10. The method of claim 1, wherein the temperature of at least a portion of the industrial process exceeds a temperature of 600°C.

8. 10. The method of claim 1, wherein the temperature of at least a portion of the industrial process exceeds a temperature of 1200°C.

9. 10. The method of claim 1, wherein the temperature of at least a portion of the industrial process exceeds a temperature of 2000°C.

10. The method of claim 1 , wherein at least a portion of the industrial process comprises a combustion process.

11. The method of claim 1 , wherein at least a portion of the industrial process comprises a gasification process.

12. The method of claim 1 , wherein at least a portion of the industrial process comprises a reforming process.

13. The method of claim 1 , wherein at least a portion of the industrial process comprises a calcination process.

14. The method of claim 1 , wherein at least a portion of the industrial process comprises a smelting process.

15. The method of claim 1 , wherein at least a portion of the industrial process comprises burning a solid fuel.

16. The method of claim 15 , wherein the solid fuel comprises coal, biomass, waste, or garbage, or any combination thereof.

17. The method of claim 1 , wherein at least a portion of the industrial process comprises burning a gaseous fuel.

18. The method of claim 17 , wherein the gas fuel comprises natural gas, methane, propane, or refinery gas, or any combination thereof.

19. The method of claim 1 , wherein at least a portion of the industrial process includes producing electricity, steam, heat, cement, steel, hydrogen, pulp, or paper, or any combination thereof.

20. The method of claim 1 , wherein at least a portion of the industrial process occurs in a boiler.

21. 21. The method of claim 20, wherein the boiler comprises a radiant section and a convection section.

22. 22. The method of claim 21, wherein the radiating section exceeds a temperature of 600°C.

23. 22. The method of claim 21, wherein the radiating section exceeds a temperature of 1200°C.

24. 22. The method of claim 21, wherein the radiating section exceeds a temperature of 2000°C.

25. 22. The method of claim 21, wherein the convection section exceeds a temperature of 200°C.

26. 22. The method of claim 21, wherein the convection section exceeds a temperature of 400°C.

27. 22. The method of claim 21, wherein the convection section exceeds a temperature of 600°C.

28. The method of claim 1 wherein the desorber is at a higher temperature than the absorber.

29. 22. The method of claim 21, wherein the absorber is located in the convective section and the desorber is located in the radiative section.

30. 10. The method of claim 1, wherein the absorber exceeds a temperature of 400°C.

31. The method of claim 1 wherein the absorber exceeds a temperature of 500°C.

32. The method of claim 1 wherein the absorber exceeds a temperature of 600°C.

33. The method of claim 1 wherein the absorber exceeds a temperature of 700°C.

34. The method of claim 1 wherein the desorber exceeds a temperature of 700°C.

35. The method of claim 1 wherein the desorber exceeds a temperature of 800°C.

36. The method of claim 1 wherein the desorber exceeds a temperature of 900°C.

37. The method of claim 1 wherein the desorber exceeds a temperature of 1000°C.

38. the first stream having at least 0.01 moles of CO per kilogram of molten salt; ２ The method of claim 1 , comprising:

39. the first stream containing at least 0.1 moles of CO per kilogram of molten salt; ２ The method of claim 1 , comprising:

40. the first stream containing at least 1 mole of CO per kilogram of molten salt; ２ The method of claim 1 , comprising:

41. the second stream containing at least 0.1 moles of CO per kilogram of molten salt; ２ The method of claim 1 , comprising:

42. the second stream containing at least 1 mole of CO per kilogram of molten salt; ２ The method of claim 1 , comprising:

43. the second stream containing at least 10 moles of CO per kilogram of molten salt; ２ The method of claim 1 , comprising:

44. The output stream is greater than 80% CO ２ The method of claim 1 having a concentration.

45. The output stream is greater than 90% CO ２ The method of claim 1 having a concentration.

46. the output stream being greater than 95% CO ２ The method of claim 1 having a concentration.

47. the output stream being greater than 99% CO ２ The method of claim 1 having a concentration.

48. the output stream being greater than 99.9% CO ２ The method of claim 1 having a concentration.

49. The method of claim 1 , wherein the desorber comprises a packed bed, a tank, a heat exchanger, a knockout drum, or an orifice plate, or a combination thereof.

50. The method of claim 1 , wherein the desorber comprises a packing material.

51. 51. The method of claim 50, wherein the packing material comprises random packing.

52. 51. The method of claim 50, wherein the packing material comprises structured packing.

53. The method of claim 1 , further comprising, prior to (c), directing the second stream to a heat exchanger.

54. 54. The method of claim 53, further comprising, after (d), directing the third stream to the heat exchanger.

55. 55. The method of claim 54, wherein the heat exchanger facilitates heat transfer from the third stream to the second stream.

56. 56. The method of claim 55, wherein the heat exchanger comprises a shell-and-tube heat exchanger including a shell side and a tube side.

57. 57. The method of claim 56, wherein the third stream is directed to the tube side of the heat exchanger and the second stream is directed to the shell side of the heat exchanger.

58. The method of claim 1 , wherein the first flow and the third flow are the same.

59. The method of claim 1 , wherein the first stream comprises at least a portion of the third stream.

60. 55. The method of claim 54, wherein the heat exchanger is a salt-salt heat exchanger.

61. 54. The method of claim 53, wherein the heat exchanger comprises a helical coil heat exchanger.

62. 55. The method of claim 54, wherein the heat exchanger comprises a tube-in-tube heat exchanger.

63. 63. The method of claim 62, wherein the tube-in-tube heat exchanger is a salt-to-salt heat exchanger.

64. 64. The method of claim 63, wherein the second stream flows up an inner tube of the tube-in-tube heat exchanger and the third stream flows down an outer tube of the tube-in-tube heat exchanger.

65. 54. The method of claim 53, wherein the heat exchanger is a printed circuit heat exchanger.

66. 54. The method of claim 53, wherein the heat exchanger is located below the desorber.

67. 67. The method of claim 66, wherein the heat exchanger is located at least 0.1 meters below the desorber.

68. 67. The method of claim 66, wherein the heat exchanger is located at least one meter below the desorber.

69. 67. The method of claim 66, wherein the heat exchanger is located at least 10 meters below the desorber.

70. The method of claim 1 , further comprising directing the third stream through a transfer pump.

71. 71. The method of claim 70, wherein the transfer pump operates with an outlet pressure of at least 1 bar absolute.

72. 71. The method of claim 70, wherein the transfer pump operates with an outlet pressure of at least 5 bar absolute.

73. 71. The method of claim 70, wherein the transfer pump operates with an outlet pressure of at least 10 bar absolute.

74. 71. The method of claim 70, wherein the transfer pump operates with an outlet pressure of at least 20 bar absolute.

75. 71. The method of claim 70, wherein the transfer pump operates with an outlet pressure of at least 100 bar absolute.

76. The method of claim 1 , further comprising directing the third flow through one or more filters.

77. The method of claim 1 , further comprising directing the second flow through one or more filters.

78. The method of claim 1 , wherein the first stream, second stream, or third stream comprises a molten borate salt.

79. The molten borate is A ｘ B １－ｘ O １．５－ｘ 79. The method of claim 78, wherein x is a number from 0 to 1 and A comprises an alkali metal.

80. 80. The method of claim 79, wherein x is a number from about 0.5 to about 0.

95.

81. 80. The method of claim 79, wherein A is lithium (Li).

82. 80. The method of claim 79, wherein A is sodium (Na).

83. 80. The method of claim 79, wherein A is potassium (K).

84. 80. The method of claim 79, wherein A is rubidium (Rb).

85. 80. The method of claim 79, wherein A is cesium (Cs).

86. 80. The method of claim 79, wherein A is francium (Fr).

87. 80. The method of claim 79, wherein A comprises sodium, potassium, and lithium.

88. The method of claim 1 , wherein the desorber is connected to the industrial process.

89. 20. The method of claim 19, wherein carbon dioxide is generated as a by-product of at least part of the industrial process.

90. The method of claim 1 , wherein the third stream comprises less than 20 mol % steam.

91. The method of claim 1 , wherein the third stream comprises less than 10 mol % steam.

92. The method of claim 1 , wherein the third stream comprises less than 5 mol % steam.

93. The method of claim 1 , wherein the third stream has no detectable vapor.

94. CO ２ The method of claim 1 , wherein the gas stream comprising:

95. 1. A method for retrofitting an industrial process with a carbon capture system, comprising: (a) providing said industrial process; (b) retrofitting the carbon capture system into the industrial process, wherein the carbon capture system uses molten salt to produce (i) carbon dioxide (CO ２ (ii) capturing the CO ２ and the desorbed CO ２ and providing a stream comprising the molten salt, the stream comprising less than 50 mol% steam; A method comprising:

96. Carbon dioxide (CO) from industrial processes ２ 1. A system for capturing (a) CO ２ contacting a gas stream comprising the CO with a first stream comprising molten salt, thereby removing the CO from the gas stream ２ into the first stream, and ２ an absorber configured to produce a second stream comprising: (b) a desorber in fluid communication with the absorber, the desorber receiving the second stream or a derivative thereof from the absorber, and ２ thereby producing (i) a third stream comprising the molten salt, and (ii) the CO desorbed from the second stream. ２ wherein the third stream comprises less than 50 mol % steam; and A system comprising:

97. 97. The system of claim 96, further comprising a salt-to-salt heat exchanger.

98. 98. The system of claim 97, wherein the salt-to-salt heat exchanger is a tube-in-tube salt-to-salt heat exchanger.

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