Using carbon dioxide from direct air capture system as low global warming car and industrial refrigerant

Abstract

To provide use of carbon dioxide from a direct air capture system as a low global warming car and industrial refrigerant.SOLUTION: An apparatus 800 includes a captured carbon dioxide input 23. The captured carbon dioxide input is coupled to receive captured carbon dioxide from a direct air capture system. The apparatus uses the captured carbon dioxide as a low global warming refrigerant to provide cooling functionality in automotive, commercial and industrial applications, or other operations involving low global warming refrigerants. In various embodiments, the apparatus is a refrigeration apparatus or a heat pump apparatus 800. The low global warming carbon dioxide refrigerant is natural, non-toxic, non-flammable and abundant when obtained from a direct air capture system. Moreover, the carbon dioxide refrigerant has a high heat transfer coefficient and has a global warming potential (GWP) of one.SELECTED DRAWING: Figure 8

Description

[Technical field]

[0001] CROSS-REFERENCE TO RELATED APPLICATIONS

[0001] This application is a continuation of U.S. Nonprovisional Patent Application No. 18 / 101,068, entitled "Using Carbon Dioxide From A Direct Air Capture System As A Low Global Warming Car And Industrial Refrigerant," filed on January 24, 2023, and claims the benefit of the same under 35 U.S.C. § 120. U.S. Nonprovisional Patent Application No. 18 / 101,068 is a continuation-in-part of U.S. Nonprovisional Patent Application No. 18 / 091,315, entitled "Efficient And Fully Automated Catalytic Direct Carbon Dioxide Capture From Air System," filed on December 29, 2022, and claims the benefit of the same under 35 U.S.C. § 120. U.S. Nonprovisional Patent Application No. 18 / 091,315 is a continuation-in-part of U.S. Nonprovisional Patent Application No. 17 / 948,492, entitled “Fully Automated Direct Air Capture Carbon Dioxide Processing System,” filed on September 20, 2022, which claims the benefit under 35 U.S.C. § 120. U.S. Nonprovisional Patent Application No. 18 / 101,068 is also a continuation-in-part of U.S. Nonprovisional Patent Application No. 17 / 948,492, entitled “Fully Automated Direct Air Capture Carbon Dioxide Processing System,” filed on September 20, 2022, which claims the benefit under 35 U.S.C. § 120. Additionally, U.S. Non-provisional Patent Application No. 18 / 091,315 and U.S. Non-provisional Patent Application No. 17 / 948,492 claim the benefit under 35 U.S.C. § 119 of U.S. Provisional Patent Application No. 63 / 295,942, entitled "Fully Automated Direct Air Capture Carbon Dioxide Processing System," filed on January 2, 2022. The subject matter of each of the above U.S. non-provisional patent applications and U.S. provisional patent applications is incorporated herein by reference.

[0002] Technical Field This invention relates to scalable, large-scale industrial applications of carbon dioxide via direct air capture as a low global warming potential fluid in mobile or stationary cooling or heat pump applications. [Background technology]

[0003] Background information

[0003] HFO-1234yf, or CF3CF=CH2, a low global warming potential automotive refrigerant, is an excellent drop-in refrigerant in the automotive industry. However, the entire supply chain associated with the production of molecules like HFO-1234yf (CF3CF=CH2) tells a completely different story. There is a significant carbon footprint and a lot of energy required associated with the conversion from hydrocarbons to chlorinated hydrocarbons, then to fluorinated hydrocarbons, and finally to hydrofluoroolefins like HFO-1234yf. Furthermore, toxic and life-threatening working environments are inevitable surrounding every step of the process. Ultimately, the low global warming potential of HFO-1234yf is hardly expected at the point of supply, since a lot of carbon dioxide has already been released into the atmosphere during its production process. The definition of the global warming potential of a molecule over a 100-year period is the ratio of the global warming potential of a particular molecule to the global warming potential of carbon dioxide over a 100-year period. Since the global warming potential of carbon dioxide for 100 years is 1, there is no refrigerant that can reduce the global warming potential more than carbon dioxide itself as a refrigerant. Although supercritical and subcritical carbon dioxide show good cooling efficiency, sourcing carbon dioxide can worsen the carbon footprint as badly as the currently used HFO-1234yf. Therefore, the inventors aim to improve the above by using carbon dioxide from our direct air capture as a truly low global warming potential automotive and industrial refrigerant.

[0004]

[0004] In chemical manufacturing plants and downstream refining processes, acid gases including H2S and carbon dioxide are very often removed from tail gas mixtures at concentrations between 15-50 wt% using aqueous amine or amino alcohol solutions or metal carbonates such as those used in natural gas sweetening processes. The amine or carbonate reacts with carbon dioxide gas to form salts which can be reversibly decomposed at mildly elevated temperatures into the starting amine or carbonate and acid gases. However, the same process that works with tail gases having any carbon dioxide concentration in the range of 5-50 wt% does not work with direct air recovery, which uses air as a feedstock, where the carbon dioxide concentration is often only in the range of 400-700 ppm. Summary of the Invention [Means for solving the problem]

[0005] overview

[0005] An apparatus includes a captured carbon dioxide inlet. The captured carbon dioxide inlet is coupled to receive captured carbon dioxide obtained from a direct air capture system. The apparatus uses the captured carbon dioxide as a low global warming potential refrigerant to provide heating or cooling functions in automotive, commercial, and industrial applications, or other operations involving refrigerants. In various embodiments, the apparatus is a cooling device or a heat pump device.

[0006]

[0006] Carbon dioxide refrigerant has a low global warming potential when obtained from a direct air capture system, is natural, non-toxic, non-flammable, and abundant. Additionally, carbon dioxide refrigerant has a high heat transfer coefficient and a global warming potential (GWP) of 1. Carbon dioxide refrigerant is a more sustainable and efficient cooling agent choice than common refrigerants such as R22, R404a, R152, or even R1234yf refrigerants.

[0007]

[0007] The direct air recovery system comprises a continuous flow reactor operable in a first stage and a second stage. In the first stage, air reacts with a basic solution in the presence of a packing material and a gas-liquid distributor to produce a basic solution with carbon dioxide and an exhaust gas that is discharged from the reactor. The packing material is designed to maximize contact between the air and the basic solution. The exhaust gas is "clean air" with less carbon dioxide than the air received in the continuous flow reactor. In the second stage, the basic solution with carbon dioxide is heated to produce carbon dioxide in the presence of a catalyst and a basic solution without carbon dioxide. The basic solution is recycled into the first stage, thereby providing a continuous carbon treatment function. The carbon dioxide is further processed for injection into the device and can be used as a low global warming potential refrigerant.

[0008]

[0008] Further details and embodiments and methods are described in the following detailed description. The above summary is not intended to define the invention. The invention is defined by the claims.

[0009] BRIEF DESCRIPTION OF THE DRAWINGS

[0009] In the accompanying drawings, embodiments of the present invention are illustrated, in which like numerals indicate similar components. [Brief description of the drawings]

[0010] [Figure 1] 1 is a diagram of a carbon processing system. [Diagram 2]

[0011] FIG. 1 is a functional diagram of the first stage (absorption stage) of the carbon treatment system. [Diagram 3]

[0012] FIG. 2 is a functional diagram of the second stage (desorption stage) of the carbon treatment system. [Figure 4]

[0013] 1 is a detailed embodiment of a carbon processing system. [Diagram 5]

[0014] 1 is a flow chart of a method for processing carbon dioxide according to one embodiment of a carbon processing system. [Figure 6]

[0015] 1 illustrates an embodiment of a cooling device configured to utilize carbon dioxide produced by an embodiment of a carbon processing system. [Figure 7]

[0016] 1 illustrates an embodiment of a cooling device configured to utilize carbon dioxide produced by an embodiment of a carbon processing system. [Figure 8]

[0017] 1 illustrates an embodiment of a heat pump apparatus configured to utilize carbon dioxide produced by an embodiment of a carbon processing system. [Figure 9]

[0018] 1 is a flow chart of a method of providing heating and cooling utilizing carbon dioxide produced by an embodiment of a carbon processing system. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0011] Detailed Description

[0019] Reference will now be made in detail to certain embodiments of the invention, examples of which are illustrated in the accompanying drawings.

[0012]

[0020] 1 is a diagram of a carbon processing system 10. The carbon processing system 10 includes an air mover 27 and a multi-stage reactor having a first stage 11 and a second stage 19. The first stage 11 includes a distributor 12, a packing material 13, a collection reservoir 15, and a pump 17. The second stage 19 includes a reservoir 21 and a refill system 22. The system 10 also includes a controller 26 that receives inputs from various sensors and provides outputs to valves and other control mechanisms to control the operation and processing of the first stage 11 and the second stage 19.

[0013]

[0021] In one embodiment, carbon processing system 10 employs direct air capture techniques (and is therefore also referred to herein as a "direct air capture system"). For example, carbon processing system 10 uses an air mover 27 to provide air 14 to system 10 for processing. Air mover 27 comprises at least one of a compressor, a blower, a fan, a turbofan, a pump, a diaphragm pump, an air octator, a falling film evaporator, or an absorber. A multi-stage reactor includes a single vessel or two or more vessels that provide multi-stage functions. In various embodiments, air mover 27 can be used to input air into the system and remove or process air from the system, such as exhaust air.

[0014]

[0022] The multi-stage direct air recovery reactor includes a basic medium 25. The basic medium is + X - The symbol Q in this general chemical formula is a quaternary ammonium salt, and X is a hydroxide and a weak base, M2. 2+ CO3 2- The symbol M in this general chemical formula is K, Na, Li, NH4, or a quaternary ammonium selected from the group consisting of N(CH3)4, N(ethylmethyl)4, N(butyl)4, or mixtures thereof.

[0015]

[0023] In another embodiment, the basic medium 25 contains a catalyst or accelerator. Sodium, potassium, ammonium, or quaternary ammonium salts of amino acids such as glycine, proline, arginine, cysteine, asparagine, and guanidine are used as accelerators to double or even triple the rate of the carbon dioxide absorption reaction in the basic medium. A weight concentration of 0.1 to 5% by weight of these accelerators is sufficient. However, a 30 to 60% aqueous solution of these is used as a carbonate-free base.

[0016]

[0024] In operation, the air mover 27 moves air 14 having less than 800 PPM carbon dioxide across the packing material 13. The pump 17 pumps the basic medium 25 from the collection reservoir 15 to the distributor 12, which distributes the basic medium 25 evenly over the packing material 13. Any excess basic medium 25 above the packing material 13 flows back to the collection reservoir 15. In this manner, the pump 17 continuously circulates the basic medium 25 from the collection reservoir 15 to the distributor 12 and back over the packing material 13.

[0017]

[0025] As the basic medium 25 is distributed over the packing material 13, carbon dioxide is removed from the air stream 14 by the air stream 14 flowing over the packing material 13. As a result, the carbon dioxide is captured in the basic medium 25. The carbon dioxide concentration of the basic medium 25 in the collection reservoir 15 begins to increase and the carbon dioxide concentration of the exhaust air 18 decreases.

[0018]

[0026] In one embodiment, the carbon dioxide detector 16 detects the carbon dioxide concentration in the basic medium 25. When the carbon dioxide concentration reaches a threshold level, the basic medium 25 in the trapping reservoir 15 is moved to the reservoir 21 of the second stage 19. In one embodiment, additional basic medium is then added to the trapping reservoir 15.

[0019]

[0027] In the second stage 19, heat 24 is applied to the carbon dioxide-rich basic medium 20 to extract carbon dioxide 23. A catalyst is used to facilitate the desorption process. The output of the reservoir 21 flows through a replenishment system 22 which regenerates the carbon dioxide-free basic medium 25, which flows back to the capture reservoir 15. The carbon dioxide-free basic medium 25 can be reused in treating new air. The extracted carbon dioxide 23 is then output from the second stage 19. The absorption reaction in the first stage 11 and the desorption reaction in the second stage 19 are reversible reactions, so that the basic medium is regenerated to the form it was in before contacting the air.

[0020]

[0028] The carbon processing system 10 is highly scalable and consumes less processing power than is required by many conventional carbon processing techniques.

[0021]

[0029] 2 is a functional diagram of the first stage 11 (absorption stage) of the carbon processing system 10. During operation, air 14 contacts the basic medium, which extracts carbon dioxide to form a basic medium 20 having a high concentration of carbon dioxide. Exhaust air 18 with reduced levels of carbon dioxide is discharged. The basic medium 20 having a high concentration of carbon dioxide is transferred to the second stage 19 of the reactor.

[0022]

[0030] 3 is a functional diagram of the second stage 19 (desorption stage) of the carbon processing system 10. During operation, heat 24 is applied to a basic medium 20 having a high concentration of carbon dioxide to extract carbon dioxide 23. The basic medium is returned to its original carbon dioxide-free state 25 and returned to the first stage 11.

[0023]

[0031] FIG 4 is a detailed embodiment of the carbon processing system 10. FIG 4 shows the first stage reactor 11 and the second stage reactor 19 of the carbon processing system 10. The first stage reactor 11 includes a fan 27, a distributor 12, a packing material 13, a condenser 402, a mist eliminator 404, a collection reservoir 15, and a pump 17. The second stage reactor 19 includes a reservoir 21 and a refill system 22.

[0024]

[0032] In various embodiments, the filler 13 comprises a film fill designed to expose as much of the basic medium's surface area as possible to as much air as possible for as long as possible to eliminate diffusion limitations and provide maximum reaction contact time. The film fill allows the basic medium to form a thin, flowing sheet exposing as much of the basic medium's surface area as possible to the interacting air stream. A variety of commercially available film fill products are suitable for use in embodiments of the carbon treatment system 10.

[0025]

[0033] In various embodiments, the basic medium is formed in one or more different configurations and includes one or more catalysts to facilitate absorption of carbon dioxide. Controller 26 operates to output control signals used to control various operations of first stage 11 and second stage 19. Controller 26 also receives sensor inputs from various sensors (e.g., carbon dioxide sensors, temperature sensors, etc.) and detectors used to monitor the operation of first stage 11 and second stage 19.

[0026]

[0034] In operation, the pump 17 draws basic medium 25 with low carbon dioxide concentration from the collection reservoir 15 and supplies the basic medium 25 to the distributor 12, which distributes the basic medium 25 evenly over the packing material 13. The fan 27 moves air across the packing material 13 so that carbon dioxide in the air is picked up by the basic medium 25 flowing over the packing material 13. As the airflow leaves the packing material 13, it passes through a condenser 402 which condenses any medium in the air and returns it to the collection reservoir 15. A mist eliminator 404 removes any mist of basic medium that may still be present in the airflow. Exhaust air 18 is released with low or no carbon dioxide.

[0027]

[0035] When the carbon dioxide concentration of the basic medium 25 meets the threshold level, the carbon dioxide-rich basic medium 20 is transferred to the reservoir 21 of the second stage reactor 19. A catalyst is also added to the reservoir 21 to facilitate the absorption of carbon dioxide. Heat 24 is added to the reservoir 21 to extract the carbon dioxide-poor portion of the basic medium 25 and the carbon dioxide-rich basic medium 406. The replenishment system 22 separates the carbon dioxide 410 from the basic medium 25, which is returned to the first stage reactor 11. The replenishment system 22 also compensates for the loss of liquid volume by adding liquid medium to the carbon dioxide-poor basic medium 25. The carbon dioxide 410 extracted from the basic medium 25 is then compressed in stages to supercritical carbon dioxide or liquid carbon dioxide 23 in the compression system 450. The carbon dioxide 23 can be fed to a sequestration system, used as a low global warming potential refrigerant, or output for use in any suitable application.

[0028]

[0036] 5 is a flow chart of a method 500 for processing carbon dioxide according to one embodiment of a carbon processing system. Method 500 includes operations performed by a first stage (absorption) 11 and operations performed by a second stage (desorption) 19. In one embodiment, method 500 is performed by carbon processing system 10.

[0029]

[0037] At block 502, a basic medium is generated and placed in a collection reservoir of a first stage of a carbon processing system. For example, basic medium 25 is generated according to any of the embodiments disclosed herein and placed in collection reservoir 15 of first stage reactor 11.

[0030]

[0038] At block 504, a pump circulates the basic medium from the collection reservoir to a distributor that distributes the basic medium across the packing material. For example, pump 17 distributes basic medium 25 to distributor 12, which distributes basic medium 25 onto packing material 13.

[0031]

[0039] At block 506, an air mover is activated to move air over the packing material. For example, a fan moves air having a carbon dioxide concentration over the packing material 13 covered with the basic medium 25.

[0032]

[0040] In block 508, the air contacts the basic medium to produce a basic medium having a concentration of carbon dioxide and to produce exhaust air. For example, the air contacts the basic medium 25 on the packing 13, and carbon dioxide in the air is collected by the basic medium 25.

[0033]

[0041] In block 510, the exhaust air is condensed to recover the basic medium, for example, air coming from the packing 13 flows to the condenser 402, and the basic medium 20 received by the condenser 402 is returned to the collection reservoir 15.

[0034]

[0042] The exhaust air is defogged and released at block 512. For example, air coming from the condenser 402 is defogged by the defogger 404. The exhaust air 18, with no or reduced carbon dioxide concentration, is released.

[0035]

[0043] At block 514, a determination is made as to whether the carbon dioxide concentration of the basic medium meets a threshold level. For example, the controller 26 receives various sensor inputs and determines when the carbon dioxide concentration in the basic medium meets a threshold level. The threshold level can be set to any suitable level. For example, the controller 26 receives carbon dioxide detection levels in the collection reservoir 15, the input air flow, and the exhaust air flow 18. The controller 26 uses the detected carbon dioxide levels to determine whether the basic medium has a carbon dioxide concentration that meets a threshold level. The controller 26 also receives various sensor inputs, such as temperature sensor, liquid level sensor, and other sensor inputs, and uses these inputs to determine the operation of the system and when the basic medium meets a carbon dioxide concentration threshold level. If the carbon dioxide concentration of the basic medium does not exceed the threshold level, the method proceeds to block 504. If the carbon dioxide concentration of the basic medium exceeds the threshold level, the method proceeds to block 516.

[0036]

[0044] At block 516, the basic medium having a carbon dioxide concentration above a threshold level is heated with a catalyst to produce a carbon dioxide rich medium, e.g., by applying heat 24 to the reservoir 21 to extract the carbon dioxide lean portion 25 of the basic medium and the carbon dioxide rich basic medium 406.

[0037]

[0045] The carbon dioxide and basic media are separated from the carbon dioxide rich media at block 518. For example, the replenishment system 22 separates the carbon dioxide 23 and basic media 25 from the carbon dioxide rich media 406.

[0038]

[0046] In block 520, the recovered basic medium is returned to the first stage. For example, the carbon dioxide-poor basic medium 25 is returned to the first stage 11.

[0039]

[0047] At block 522, the carbon dioxide is captured and utilized for any suitable purpose, for example, carbon dioxide 23 is captured for further use.

[0040]

[0048] Thus, method 500 operates to provide a carbon dioxide treatment process to remove carbon dioxide from air. It should be noted that the operations of method 500 are exemplary, and that operations may be added, deleted, rearranged, or otherwise modified within the scope of the embodiments.

[0041]

[0049] 6 illustrates one embodiment of a cooling device 600 configured to utilize carbon dioxide produced by an embodiment of the carbon processing system 10 disclosed herein. For example, in one embodiment, the device 600 utilizes the carbon dioxide output from the compression system 450 as a low global warming potential refrigerant / coolant to provide cooling in automotive applications. Carbon dioxide used as a refrigerant is natural, non-toxic, non-flammable, abundant, has a high heat transfer coefficient, and has a global warming potential (GWP) of just 1. As such, carbon dioxide refrigerant is a more sustainable and efficient cooling agent option than common refrigerants such as R22, R152, R404a, and R1234yf refrigerants.

[0042]

[0050] In one embodiment, cooling system 600 is configured to utilize carbon dioxide as a coolant to economically and sustainably maintain a comfortable cabin temperature for use in automotive applications. By using carbon dioxide from direct air capture as provided by the embodiments of carbon processing system 10 disclosed herein, cooling system 600 provides automotive cooling using carbon dioxide as a sustainable and competitive coolant solution.

[0043]

[0051] In one embodiment, the cooling system 600 includes a low-side Schrader valve 602, a compressor 604, a condenser 606, a receiver / dryer 608, a high-side Schrader valve 610, a thermostatic expansion valve 612, and an evaporator 614.

[0044]

[0052] In one embodiment, carbon dioxide 23 produced by direct air capture performed by carbon processing system 10 is input to cooling device 600. For example, carbon dioxide 23 is output from compression system 450. The carbon dioxide 23 is received by low-side Schrader valve 602, which allows the carbon dioxide 23 to be charged to cooling device 600. Valve 602 also functions as a test port in conjunction with high-side Schrader valve 610 to ensure that the proper pressure differential is maintained within device 600.

[0045]

[0053] The carbon dioxide flows through valve 602 to compressor 604, which pressurizes and heats the carbon dioxide 23. The high pressure and temperature carbon dioxide flows to condenser 606, which cools and liquefies the carbon dioxide. A receiver / dryer 608 then removes water from the liquefied carbon dioxide.

[0046]

[0054] High-side Schrader valve 610 allows liquid carbon dioxide to flow to a thermostatic expansion valve 612. High-side Schrader valve 610 also serves as a test port in conjunction with low-side Schrader valve 602 to ensure that the proper pressure differential is maintained within device 600.

[0047]

[0055] The thermostatic expansion valve 612 expands the carbon dioxide, thereby reducing its pressure. The evaporator 614 changes the liquefied carbon dioxide back to a gaseous state. When a fan in the automobile cabin blows cabin air 616 across the evaporator 614, the carbon dioxide absorbs heat, thereby providing cooler, drier air. The carbon dioxide then flows back to the valve 602, completing the cycle.

[0048]

[0056] 7 illustrates one embodiment of a cooling device 700 configured to utilize carbon dioxide produced by an embodiment of the carbon processing system 10 disclosed herein. For example, in one embodiment, the device 700 utilizes the carbon dioxide output from the compression system 450 as a low global warming potential refrigerant / coolant to provide cooling in industrial applications. For example, supermarkets and other suppliers can use the device 700 to cheaply and sustainably keep fresh produce at the right temperature.

[0049]

[0057] In one embodiment, the cooling apparatus 700 includes a first compressor 702, a condenser 704, a control valve 706, a receiver / dryer 708, a bypass valve 710, a first expansion valve 712, a first evaporator 714, a second expansion valve 716, a second evaporator 718, and a second compressor 720. The apparatus 700 also includes a controller 722 that operates to control the operation of the components of the apparatus 700 that provides cooling using carbon dioxide as a refrigerant as described herein.

[0050]

[0058] In one embodiment, carbon dioxide 23 produced by the direct air capture performed by carbon processing system 10 is input to cooling device 700. For example, carbon dioxide 23 is output from compression system 450 and pumped into device 700. Carbon dioxide 23 is received by a first compressor 702, which compresses the carbon dioxide and sends it to a gas cooler / condenser 704. Condenser 704 cools the gaseous carbon dioxide (e.g., supercritical and unable to change phase) and sends the cooled carbon dioxide gas to a control valve 706.

[0051]

[0059] The control valve 706 adjusts the pressure of the carbon dioxide gas refrigerant and outputs the pressure-regulated gas to the receiver / dryer 708. The receiver / dryer 708 receives the pressure-regulated carbon dioxide gas and separates the carbon dioxide according to phase (gas or liquid). The carbon dioxide gas flows from the receiver / dryer 708 to a bypass valve 710. The carbon dioxide liquid flows along line A to a first expansion valve 712 and along line B to a second expansion valve 716.

[0052]

[0060] In one embodiment, a bypass valve 710 supplies gaseous carbon dioxide to the input line of the first compressor 702. A first expansion valve 712 allows the liquid carbon dioxide to expand before entering a first evaporator 714, which removes unwanted heat and redirects the carbon dioxide back to the first compressor 702.

[0053]

[0061] A second expansion valve 716 allows the liquid carbon dioxide to expand before entering a second evaporator 718, which removes unwanted heat and redirects the carbon dioxide to a second compressor 720. The second compressor 720 further increases the pressure of the carbon dioxide before input to the first compressor 702.

[0054]

[0062] In various exemplary embodiments, more efficient versions of the apparatus 700 may be implemented. In one embodiment, the control valve 706 is replaced with a compound multi-ejector and an additional compressor is added in parallel to the first compressor 702. These modifications serve to increase overall efficiency by reducing the workload of the individual compressors, especially the first compressor 702 which does a lot of work, especially in high temperature environments.

[0055]

[0063] In apparatus 700, line A is a medium temperature line (e.g., for use in a refrigerator) and line B is a low temperature line (e.g., for use in a freezer). Therefore, the carbon dioxide from line B must undergo further compression. In a real world application, there may be more lines, each with specific temperature requirements, and further compressors would be provided as necessary.

[0056]

[0064] 8 illustrates one embodiment of a heat pump device 800 configured to utilize carbon dioxide produced by an embodiment of the carbon processing system 10 disclosed herein. For example, in one embodiment, device 800 utilizes carbon dioxide output from compression system 450 as a low global warming potential refrigerant / coolant to provide heat pump operations (e.g., heating and cooling) in industrial applications.

[0057]

[0065] In one embodiment, heat pump apparatus 800 includes a first expansion valve 802, a first check valve 804, an outdoor heat exchanger 806, a reversing valve 808, a compressor 810, an indoor heat exchanger 812, a second expansion valve 814, a second check valve 816, a two-way filter / dryer 818, and an access window 820. Apparatus 800 also includes a controller 822 operative to control the operation of components of apparatus 800 that provides heating and cooling using carbon dioxide as a low global warming potential refrigerant as described herein.

[0058]

[0066] In one embodiment, carbon dioxide 23 produced by direct air capture performed by carbon processing system 10 is input to heat pump apparatus 800. For example, carbon dioxide 23 is output from compression system 450 and pumped into apparatus 800.

[0059]

[0067] The apparatus 800 operates in a cooling mode in which carbon dioxide flows generally clockwise around the apparatus 800, as indicated by cooling flow direction arrow 826. The apparatus 800 operates in a heating mode in which carbon dioxide flows generally counterclockwise around the apparatus 800, as indicated by heating flow direction arrow 824.

[0060]

[0068] During operation, carbon dioxide 23 is received by a first expansion valve 802, which allows the pressure and temperature of the carbon dioxide to be reduced during a cooling mode. A first check valve 804 allows the carbon dioxide to flow during a heating mode. An inspection window 820 allows visual inspection. A two-way filter / dryer 818 removes water and other particulates from the carbon dioxide stream. A second expansion valve 814 allows the pressure and temperature of the carbon dioxide to be reduced during a heating mode. A second check valve 816 allows the carbon dioxide to flow during a cooling mode.

[0061]

[0069] An indoor heat exchanger 812 transfers heat between the carbon dioxide and the indoor air. A reversing valve 808 controls the direction of the carbon dioxide flow as it alternates between heating and cooling. A compressor 810 compresses the carbon dioxide as needed. An outdoor heat exchanger transfers heat between the carbon dioxide and the outdoor air.

[0062]

[0070] The controller 822 obtains data from sensors in the system to monitor and control the designated heating or cooling mode.

[0063]

[0071] FIG. 9 is a flow chart of a method 900 for utilizing carbon dioxide produced by the carbon processing system 10 to provide heating and cooling in automotive, commercial, and industrial applications.

[0064]

[0072] At block 902, the carbon processing system is operated to capture carbon dioxide directly from air. For example, the carbon processing system 10 is operated with a basic medium as disclosed in any of the embodiments to capture carbon dioxide directly from air.

[0065]

[0073] At block 904, the captured carbon dioxide is output from the carbon processing system. For example, the captured carbon dioxide is output from the compression system 450 of the carbon processing system 10.

[0066]

[0074] The captured carbon dioxide is injected into a chiller or heat pump system at block 906. For example, the captured carbon dioxide 23 is injected into chiller 600, chiller 700, or heat pump system 800.

[0067]

[0075] At block 908, a device that receives the directly captured carbon dioxide is operated to provide heating or cooling in an automotive, commercial, or industrial application.

[0068]

[0076] In this manner, method 900 operates to provide heating and cooling in automotive, commercial, and industrial applications utilizing carbon dioxide produced by carbon processing system 10. It should be noted that the operations of method 900 are exemplary and not limiting, and that additions, deletions, rearrangements, or other modifications may be made within the scope of the embodiments.

[0069]

[0077] Various embodiments for generating the basic medium and catalyst used by the novel carbon processing system are discussed below. It should be understood that there may be slight variations or adjustments within the scope of the embodiments regarding the chemicals used in the direct air capture device.

[0070] EMBODIMENT #1

[0078] In a first embodiment, the basic medium is 1 kg mole of M2 mixed with water to make an aqueous solution having any concentration ranging from 1% to 100% by weight. 2+ CO3 2- (M is Na, K, Li, NH4, or a quaternary ammonium) and a base. More specifically, the concentration is 20-80 wt % or 20-40 wt %. 0.1-5 wt % of a catalyst is added to the solution, which includes an amino acid or more preferably an amino acid salt of arginine, asparagine, cysteine, glycine, proline, or guanidine.

[0071]

[0079] 1 kg mole of pure carbon dioxide (99.9% purity) is contacted with the aqueous solution in an autoclave under stirring at a temperature between 5°C and 110°C. More specifically, the temperature is between 10°C and 60°C or between 40°C and 70°C. When most of the carbon dioxide has been absorbed into the solution, the autoclave overhead pressure is released. 0.1-5 wt% of freshly prepared dimethylformamide (DMSO) of general formula MO-(OH) n where "M" is Cr, V, Ti, and / or Mo, and "n" is an integer from 1 to 6.

[0072]

[0080] The steam jacketed desorber is then heated to 50-150°C. More specifically, the desorber is heated to 60-130°C or 70-125°C to desorb carbon dioxide. The pure carbon dioxide from the top is bottled for injection. The conversion rate in the absorption step is 100%, and the selectivity is 100%, while the conversion rate in the desorption step is about 90-100%, and the selectivity is 99.99%, respectively.

[0073] EMBODIMENT #2

[0081] In a second embodiment, the basic medium is 2+ CO3 2- and M is Na, K, Li, NH4, or quaternary ammonium. The basic medium is mixed with water to make an aqueous solution having any concentration ranging from 1% to 100% by weight. More specifically, the concentration is 20-80% or 20-40% by weight. 0.1-5 wt% of a catalyst is added to the solution, including an amino acid of glycine, proline, arginine, cysteine, asparagine, guanidine, or a carboxylate thereof.

[0074]

[0082] One kg molar equivalent of carbon dioxide, derived from an air stream having a carbon dioxide concentration of 400 ppm, is contacted with an aqueous solution in a continuous flow reactor at a temperature between 5°C and 110°C for a period of time. More specifically, the temperature is between 10°C and 60°C or between 15 and 50°C. When most of the carbon dioxide has been absorbed into the solution, the overhead pressure is released. 0.1 to 5 wt% of freshly prepared dimethylaminopropane of the general formula MO-(OH) nwhere "M" is Cr, V, Ti, and / or Mo, and "n" is an integer from 1 to 6.

[0075]

[0083] The steam jacketed desorber is then heated to 50-150°C. More specifically, the desorber is heated to 60-130°C or 70-125°C to desorb carbon dioxide. The pure carbon dioxide from the top is bottled for injection. The conversion rate in the absorption step is 30-70%, and the selectivity is 99%, and the conversion rate in the desorption step is about 70-100%, and the selectivity is 99%, respectively.

[0076] EMBODIMENT #3

[0084] In a third embodiment, the basic medium contains 1 kg mole of M2 2+ CO3 2- where M is Na, K, Li, NH4, or quaternary ammonium. The basic medium is mixed with water to make an aqueous solution having any concentration ranging from 1% to 100% by weight. More specifically, the concentration is 20-80% or 20-40% by weight. 0.1-5 wt% of a catalyst is added to the solution, including amino acids of glycine, proline, cysteine, arginine, asparagine, guanidine, and melamine, or their sodium, potassium, or ammonium salts.

[0077]

[0085] 1.5 kg molar equivalents of carbon dioxide in a tail gas stream having a carbon dioxide concentration of 10-35 wt% is contacted with an aqueous solution over time in a continuous flow reactor at a temperature of 5°C to 110°C. More specifically, the temperature is 10°C to 60°C or 40-70°C. When most of the carbon dioxide has been absorbed into the solution, the overhead pressure is released. 0.1-5 wt% of freshly prepared dimethylformamide of the general formula MO-(OH) n where "M" is Cr, V, Ti, and / or Mo, and "n" is an integer from 1 to 6.

[0078]

[0086] The steam jacketed desorber is then heated to 50-150°C. More specifically, the desorber is heated to 60-130°C or 70-125°C to desorb carbon dioxide. The pure carbon dioxide from the top is bottled for injection. The conversion rate in the absorption step is 30-70%, and the selectivity is 99%, and the conversion rate in the desorption step is about 70-100%, and the selectivity is 99%, respectively.

[0079] EMBODIMENT #4

[0087] In a fourth embodiment, the setup is the same as embodiment #2, but instead of using an air-liquid contactor, a bubble column reactor is used to achieve 85-90% conversion and 99% selectivity.

[0080] EMBODIMENT #5

[0088] In a fifth embodiment, the setup is the same as in embodiment #2, except that a 50%-50% by weight mixture of water and glycol is used as the solvent instead of 100% water. The conversion and selectivity to carbon dioxide are similar to embodiment #2. However, the water loss is minimized to 1-3% instead of the usual 5-7%.

[0081] EMBODIMENT #6

[0089] In the sixth embodiment, the configuration is the same as in embodiment #2, except that a 50%-50% by weight mixture of water and alcohol is used as the solvent instead of 100% water. The conversion and selectivity to carbon dioxide are similar to embodiment #2.

[0082] Example #7

[0090] In the seventh embodiment, the setup is the same as in embodiment #2, except that a 50%-50% by weight mixture of water and PGMEA is used as the solvent instead of 100% water. The conversion and selectivity to carbon dioxide is similar to embodiment #2, but the water loss is limited to 3%.

[0083] EMBODIMENT #8

[0091] In an eighth embodiment, the basic medium has a Q of 1 kg mole + X- "Q" is tetramethyl quaternary ammonium, tetraethyl quaternary ammonium, ethyl trimethyl quaternary ammonium, tetrabutyl quaternary ammonium, methyl tributyl quaternary ammonium, or methyl ethyl dibutyl quaternary ammonium; and "X - " is OH - The basic medium is mixed with water to produce an aqueous solution having any concentration ranging from 1% to 100% by weight. More specifically, the concentration is 20-80% by weight or 20-40% by weight. 0.1-5 wt% of a catalyst including an amino acid salt such as glycine is added to the solution.

[0084]

[0092] One kg mole of carbon dioxide equivalent in a stream of air having a carbon dioxide concentration of 400 ppm is contacted over time with an aqueous solution in a continuous flow reactor at a temperature between 5°C and 110°C. More specifically, the temperature is between 10°C and 60°C or between 40°C and 50°C. When most of the carbon dioxide has been absorbed into the solution, the overhead pressure is released. 0.1-5 wt% of freshly prepared cations of the general formula MO-(OH) n where "M" is Cr, V, Ti, and / or Mo, and "n" is an integer from 1 to 6.

[0085]

[0093] The steam jacketed desorber is then heated to 50-150°C. More specifically, the desorber is heated to 60-130°C or 70-120°C to desorb carbon dioxide. The pure carbon dioxide from the top is bottled for injection. The conversion rate in the absorption step is 50-90%, and the selectivity is 99%, and the conversion rate in the desorption step is about 70-90%, and the selectivity is 99%, respectively.

[0086] EMBODIMENT #9

[0094] In a ninth embodiment, the basic medium has a Q of 1 kg mole + X -"Q" is tetramethyl quaternary ammonium, tetraethyl quaternary ammonium, ethyl trimethyl quaternary ammonium, tetrabutyl quaternary ammonium, methyl tributyl quaternary ammonium, or methyl ethyl dibutyl quaternary ammonium; and "X - " is OH - The basic medium is mixed with water and glycerol to make an aqueous solution having any concentration ranging from 1% to 100% by weight. More specifically, the concentration is 20-80% by weight or 20-40% by weight. 0.1-5 wt% of a catalyst including an amino acid salt such as glycine, proline, or guanidine is added to the solution.

[0087]

[0095] 1.1 kg moles of carbon dioxide equivalent in a tail gas stream having a carbon dioxide concentration of 5-35 wt% is contacted over time with an aqueous solution in a continuous flow reactor at a temperature of 5°C to 110°C. More specifically, the temperature is 10°C to 60°C or 50-75°C. When most of the carbon dioxide has been absorbed into the solution, the overhead pressure is released. 0.1-5 wt% of freshly prepared dimethylaminopropane of the general formula MO-(OH) n where "M" is Cr, V, Ti, and / or Mo, and "n" is an integer from 1 to 6.

[0088]

[0096] The steam jacketed desorber is then heated to 50-150°C. More specifically, the desorber is heated to 60-130°C or 70-130°C to desorb carbon dioxide. The pure carbon dioxide from the top is bottled for injection. The conversion rate in the absorption step is 80-100%, and the selectivity is 99%, while the conversion rate in the desorption step is about 90-100%, and the selectivity is 99.9%, respectively.

[0089] Embodiment #10

[0097] In a tenth embodiment, the configuration is the same as embodiment #8, but instead of an air-liquid contactor, a bubble column reactor is used to achieve 85-90% conversion and 99% selectivity.

[0090] Embodiment #11

[0098] In an eleventh embodiment, the setup is the same as in embodiment #8, except that a 50%-50% by weight mixture of water and glycol is used as the solvent instead of 100% water. The conversion and selectivity to carbon dioxide are similar to embodiment #8. However, the water loss is minimized to 1-3% instead of the usual 5-7%.

[0091] Example #12

[0099] In a twelfth embodiment, the configuration is the same as in embodiment #8, except that a 50%-50% by weight mixture of water and alcohol is used as the solvent instead of 100% water. The conversion and selectivity to carbon dioxide are similar to embodiment #8.

[0092] Embodiment #13

[0100] In a thirteenth embodiment, the composition is the same as in embodiment #8, except that a 50%-50% by weight mixture of water and PGMEA is used as the solvent instead of 100% water. The conversion and selectivity to carbon dioxide are similar to embodiment #8, but the water loss is limited to 3%.

[0093] Embodiment #14

[0101] In a fourteenth embodiment, the basic medium comprises 1 kg mole of M2 2+ CO3 2- where "M" is Na, K, Li, NH4, or quaternary ammonium. The basic medium is 0.1-1 wt% glycine and 0.1-1 wt% tetrabutylammonium hydroxide, mixed with a water-glycerol solvent mixture to make an aqueous solution having any concentration ranging from 1 wt% to 100 wt%. More specifically, the concentration is 20-80 wt% or 20-40 wt%.

[0094]

[0102] One kilomol of carbon dioxide in a stream of air having a carbon dioxide concentration of 400 ppm is contacted over time with an aqueous solution in a continuous flow reactor at a temperature between 5°C and 110°C. More specifically, the temperature is between 10°C and 75°C or between 50°C and 70°C. When most of the carbon dioxide has been absorbed into the solution, the overhead pressure is released. 0.1-5 wt% of freshly prepared dimethylaminopropane of the general formula MO-(OH) n where "M" is Cr, V, Ti, and / or Mo, and "n" is an integer from 1 to 6.

[0095]

[0103] The steam jacketed desorber is then heated to 50-150°C. More specifically, the desorber is heated to 60-130°C or 70-120°C to desorb carbon dioxide. The pure carbon dioxide from the top is bottled for injection. The conversion rate in the absorption step is 30-70%, and the selectivity is 99%, and the conversion rate in the desorption step is about 70-100%, and the selectivity is 99%, respectively.

[0096] Example #15

[0104] In a fifteenth embodiment, the basic medium has a Q of 1 kg mole + X - Including Q + is a tetramethyl quaternary ammonium cation, a tetraethyl quaternary ammonium cation, an ethyltrimethyl quaternary ammonium cation, a tetrabutyl quaternary ammonium cation, a methyltributyl quaternary ammonium cation, a methylethyldibutyl quaternary ammonium cation, or an ammonium cation; X - is the hydroxide anion. The basic medium is 0.1-1 wt% arginine and 0.1-1 wt% KOH, which is mixed with a water-glycerol solvent mixture to make an aqueous solution having any concentration ranging from 1 wt% to 100 wt%. More specifically, the concentration is 20-80 wt% or 20-40 wt%.

[0097]

[0105] One kilomol of carbon dioxide in a stream of air having a carbon dioxide concentration of 400 ppm is contacted over time with an aqueous solution in a continuous flow reactor at a temperature between 5 and 110°C. More specifically, the temperature is between 10 and 75°C or between 50 and 70°C. When most of the carbon dioxide has been absorbed into the solution, the overhead pressure is released. 0.1 to 2 wt% of freshly prepared dimethylaminopropane of the general formula MO-(OH) n where "M" is Cr, V, Ti, and / or Mo, and "n" is an integer from 1 to 6.

[0098]

[0106] The steam jacketed desorber is then heated to 50-150°C. More specifically, the desorber is heated to 60-130°C or 70-120°C to desorb carbon dioxide. The pure carbon dioxide from the top is bottled for injection. The conversion rate in the absorption step is 30-70%, and the selectivity is 99%, and the conversion rate in the desorption step is about 70-100%, and the selectivity is 99%, respectively.

[0099] Embodiment #16

[0107] In a sixteenth embodiment, the basic medium comprises 1 kg mole of sodium, potassium, and ammonium salts or free forms of glycine, proline, arginine, cysteine, asparagine, guanidine, or mixtures thereof, in water or a water-glycerol solvent mixture to produce an aqueous solution having any concentration ranging from 1% to 100% by weight, more specifically, from 20 to 80% by weight or from 20 to 40% by weight.

[0100]

[0108] One kg molar equivalent of carbon dioxide in a stream of air having a carbon dioxide concentration of 400 ppm is contacted with an aqueous solution over time in a continuous flow reactor at a temperature between 5 and 110°C. More specifically, the temperature is between 10 and 75°C or between 50 and 70°C. When most of the carbon dioxide has been absorbed into the solution, the overhead pressure is released. 0.1 to 2 wt% of freshly prepared dimethylaminopropane of the general formula MO-(OH) n where "M" is Cr, V, Ti, and / or Mo, and "n" is an integer from 1 to 6.

[0101]

[0109] The steam jacketed desorber is then heated to 50-150°C. More specifically, the desorber is heated to 60-150°C or 70-135°C to desorb carbon dioxide. The pure carbon dioxide from the top is bottled for injection. The conversion rate in the absorption step is 60-70%, and the selectivity is 99%, and the conversion rate in the desorption step is about 90-100%, and the selectivity is 99%, respectively.

[0102] Example #17

[0110] In a seventeenth embodiment, a solid material with a high surface area that is stable under high humidity conditions, such as zeolites, molecular sieves, and metal-organic frameworks (MOFs), is soaked in an aqueous basic solution containing any one of potassium or sodium carbonate, tetrabutylammonium hydroxide, or salts of amino acids such as glycine, proline, and guanidine, dried, and pretreated. The base-impregnated solid surface is exposed to air in a continuous flow reactor to capture carbon dioxide, which is adsorbed and then desorbed by a temperature swing process to obtain pure carbon dioxide gas as the product.

[0103] Embodiment #18

[0111] In an eighteenth embodiment, the basic medium comprises a mixture of phase transfer agents including, but not limited to, 100 ppm to 100 wt % ethyl-methyl-dibutylammonium hydroxide, 10 to 80 wt % weak base such as K2CO3 or Na2CO3, 0.01 to 10 wt % potassium or sodium salts of amino acids such as glycine, asparagine, arginine, etc., mixed with water and a high boiling polyol to make an aqueous solution having any concentration ranging from 1 wt % to 100 wt %. More specifically, the concentration is 20 to 80 wt % or 20 to 40 wt %.

[0104]

[0112] The carbon treatment system 10 passes air over the solution to saturate the solution with carbon dioxide at 4° C. to 70° C. 0.1 to 5 wt % of freshly prepared carbon dioxide of the general formula MO-(OH) nis added to a carbon dioxide saturated solution, where "M" is Cr, V, Ti, and / or Mo, and "n" is an integer from 1 to 6.

[0105]

[0113] The steam jacketed desorber is then heated to 50°C to 150°C. More specifically, the desorber is heated to 60°C to 140°C or 70°C to 135°C to desorb carbon dioxide. The pure carbon dioxide at the top of the column is compressed and bottled. The conversion rate in the absorption step is 73%, and the selectivity is 98%, while the conversion rate in the desorption step is about 94% to 100%, and the selectivity is 99.99%, respectively.

[0106] Embodiment #19

[0114] In a nineteenth embodiment, the basic medium has a Q of 1 kg mole + X - wherein the cation Q is tetramethyl quaternary ammonium, tetraethyl quaternary ammonium, ethyl trimethyl quaternary ammonium, tetrabutyl quaternary ammonium, methyl tributyl quaternary ammonium, or methyl ethyl dibutyl quaternary ammonium, and the anion X is hydroxide. The basic medium is mixed with water to make an aqueous solution having any concentration in the range of 10% to 100% by weight. More specifically, the concentration is 20 to 80% by weight or 20 to 40% by weight. 0.1 to 5 wt% of a catalyst is added to the solution, the catalyst comprising one or more amino acid salts of any one or mixture of glycine, proline, arginine, cysteine, asparagine, and guanidine.

[0107]

[0115] The carbon treatment system 10 blows a stream of air having a carbon dioxide concentration of 400-700 ppm into contact with an aqueous solution over time in a continuous flow reactor at a temperature of 5-110°C. More specifically, the temperature is 10-60°C or 40-50°C. When most of the carbon dioxide has been absorbed into the solution, the carbon dioxide rich solution is pumped into a desorption reactor. 0.1-5 wt% freshly prepared cation exchange copolymer of the general formula MO-(OH) n where "M" is Cr, V, Ti, and / or Mo, and "n" is an integer from 1 to 6.

[0108]

[0116] The steam jacketed desorber is then heated to 50-150°C. More specifically, the desorber is heated to 60-150°C or 90-135°C to desorb carbon dioxide. The pure carbon dioxide from the top is bottled for injection. The conversion rate in the absorption step is 52-93%, and the selectivity is 99%, and the conversion rate in the desorption step is about 70-98%, and the selectivity is 99%, respectively.

[0109] Embodiment #20

[0117] In the twentieth embodiment, a basic medium containing a 10 to 60 wt % solution of an amino acid or a sodium salt or potassium salt thereof is added to the aqueous solution containing 100 to 500 ppm of Q + X - where "Q" is tetramethyl quaternary ammonium, tetraethyl quaternary ammonium, ethyl trimethyl quaternary ammonium, tetrabutyl quaternary ammonium, methyl tributyl quaternary ammonium, or methyl ethyl dibutyl quaternary ammonium, and "X" is a carbon dioxide absorption chemical with a phase transfer agent of - " is OH - A mixture of water and glycerol is used as a solvent to make an aqueous solution with any concentration ranging from 1% to 100% by weight. More specifically, the concentration is 20-80% by weight or 20-60% by weight. Next, 0.01-20 wt% of a catalyst containing free amino acids of sarcosine, glycine, proline, guanidine, cysteine, arginine, or asparagine or their sodium or potassium salts is added to the basic medium.

[0110]

[0118] After the carbon treatment system 10 completely absorbs the carbon dioxide in the chemical, the carbon dioxide-rich solution is pumped to a high-pressure desorber. n where "M" is Cr, V, Ti, and / or Mo, and "n" is an integer from 1 to 6.

[0111]

[0119] The steam jacketed desorber is then heated to 50-150°C. More specifically, the desorber is heated to 60-130°C or 70-130°C to desorb carbon dioxide. The pure carbon dioxide from the top is bottled for injection. The conversion rate in the absorption step is 55-85%, and the selectivity is 99%, while the conversion rate in the desorption step is about 95-100%, and the selectivity is 99.9%, respectively.

[0112] Embodiment #21

[0120] In a twenty-first embodiment, the same basic medium is used as in embodiment #20, but instead of using an air-liquid contactor, a bubble column reactor is used to achieve 85-90% conversion and 99% selectivity.

[0113] Embodiment #22

[0121] In a twenty-second embodiment, embodiment #20 is carried out with a 50%-50% by weight mixture of water and glycol as the solvent rather than 100% water. Conversion and selectivity to carbon dioxide are similar to embodiment #19, but water loss is minimized to 1-3% instead of the usual 5-7%.

[0114] Example #23

[0122] In a twenty-third embodiment, embodiment #20 is modified to run a 50%-50% by weight mixture of water and alcohol as the solvent instead of 100% water. The conversion and selectivity to carbon dioxide are similar to embodiment #19.

[0115] Embodiment #24

[0123] In a twenty-fourth embodiment, embodiment #20 is modified to run a 50%-50% by weight mixture of water and PGMEA as the solvent instead of 100% water. The conversion and selectivity to carbon dioxide is similar to embodiment #19, but the water loss is limited to 3%.

[0116] Example #25

[0124] In a twenty-fifth embodiment, a solid material with a high surface area that is stable under high humidity conditions, such as zeolites, molecular sieves, and MOFs, is soaked in an aqueous basic solution containing potassium or sodium carbonate, tetrabutylammonium hydroxide, or one of the salts of amino acids such as glycine, proline, guanidine, cysteine, arginine, and asparagine, dried, and pretreated. The base-impregnated solid surface on the filter paper is exposed to air in a continuous flow reactor to capture carbon dioxide, which is adsorbed and then desorbed by a temperature swing process with or without vacuum to obtain pure carbon dioxide gas as the product.

[0117]

[0125] Although certain specific embodiments have been described for purposes of illustration, the teachings herein have general applicability and are not limited to the specific embodiments described above. Thus, various modifications, adaptations, and combinations of the various features of the described embodiments may be made without departing from the scope of the invention as set forth in the claims. [Explanation of symbols]

[0118] 10 Direct Air Recovery System 11 First stage reactor 12 Distributor 13 Filling material 14. Air 15 Collection reservoir 16 Carbon Dioxide Detector 17 Pump 18 Exhaust Air 19 Second stage reactor 20, 25, 406 Basic medium 21 Reservoir 22 Refill System 23, 410 Carbon dioxide 24 fever 26,822 Controller 27 Air Mover 402, 606, 704 Condenser 404 Mist Eliminator 450 Compression System 500, 900 methods 502, 504, 506, 508, 510, 512, 514, 516, 518, 520, 522, 902, 904, 906, 908 blocks 600, 700 cooling device 602 Low pressure side Schrader valve 604, 702, 720, 810 Compressors 608, 708 Receiver / Dryer 610 High pressure side Schrader valve 612 Thermostatic expansion valve 614, 714, 718 Evaporator 616 Cabin Air 706 Control valve 710 Bypass valve 712, 716, 802, 814 Expansion valve 800 Heat pump equipment 804, 816 Check valve 806 outdoor heat exchanger 808 Reversing valve 812 Indoor Heat Exchanger 818 Two-way filter / dryer 820 Inspection window 824, 826 Arrows

Claims

1. 1. An apparatus comprising: a captured carbon dioxide inlet coupled to receive captured carbon dioxide obtained from a direct air capture system, the direct air capture system capturing carbon dioxide from gas-liquid contact, the apparatus using the captured carbon dioxide as a low global warming potential refrigerant to provide cooling and heating; An apparatus comprising:

2. The apparatus of claim 1 , wherein the apparatus is a mobile and industrial cooling apparatus.

3. 1. An apparatus comprising: a captured carbon dioxide inlet coupled to receive captured carbon dioxide obtained from a direct air capture system, the apparatus providing cooling and heating using the captured carbon dioxide as a low global warming potential refrigerant, the apparatus being a heat pump apparatus; An apparatus comprising:

4. Sensors and readout devices for monitoring the operation and safety of said equipment The apparatus of claim 1 further comprising:

5. 2. The apparatus of claim 1, wherein the recovered carbon dioxide has a purity of between 91% and 100%.

6. a basic medium for the direct air capture system comprising: A phase transfer catalyst or mixture thereof, the phase transfer catalyst having a radical cation and a radical anion, the radical cation being a quaternary ammonium cation (NR ４ ＋ ), and the radical anion is a hydroxide anion (OH － ), fluoride anion (F － ), iodide anion (I － ), carbonate anion (CO ３ ２－ ) or bicarbonate anion (HCO ３ － a phase transfer catalyst or mixture thereof comprising at least one of a free amino acid or a sodium salt, a potassium salt, an ammonium salt, or a quaternary ammonium salt of an amino acid, or a mixture thereof; B ＋ Y － A base or a mixture thereof having the common structure of ＋ is a potassium, ammonium, sodium, calcium, vanadium, titanium, lithium, boron, or quaternary ammonium cation; Y － are hydroxide, carbonate, bicarbonate, borate, and titanate anions; B ＋ Y － or a mixture thereof, any primary, secondary, and quaternary amine in free form or salt form or mixtures thereof; A solvent system comprising water or a mixture of water / glycerol, water / glycol, water / polyol, water / alcohol, which recovers carbon dioxide from air at a purity of 71% to 100%. The apparatus of claim 1 , comprising:

7. 1. An apparatus comprising: a captured carbon dioxide inlet coupled to receive captured carbon dioxide obtained from a direct air capture system, the apparatus using the captured carbon dioxide as a low global warming potential refrigerant to provide cooling and heating, the carbon dioxide being compressed in multiple stages to accommodate variable temperature requirements throughout mobile and commercial low global warming potential refrigerant applications, and the captured carbon dioxide having a purity of 97% to 100%. An apparatus comprising:

8. 1. An apparatus comprising: a captured carbon dioxide inlet coupled to receive captured carbon dioxide obtained from a direct air capture system, the apparatus providing cooling and heating using the captured carbon dioxide as a low global warming potential refrigerant, and an additional multi-ejector system design employed to control refrigerant flow, optimize efficiency, and mitigate compressor load to enable operation in extreme weather conditions; An apparatus comprising:

9. An apparatus comprising: a captured carbon dioxide inlet coupled to receive captured carbon dioxide obtained from a direct air capture system, the apparatus using the captured carbon dioxide as a low global warming potential refrigerant to provide cooling and heating, the direct air capture system compressing the captured carbon dioxide by the apparatus to a supercritical or subcritical state for use as a low global warming potential refrigerant; An apparatus comprising:

10. injecting captured and compressed carbon dioxide obtained from a direct air capture system into an apparatus, the direct air capture system capturing carbon dioxide via gas-liquid contact, the apparatus using the captured carbon dioxide as a low global warming potential refrigerant to provide heating or cooling. A method comprising:

11. Monitoring the operation and safety of said equipment via sensors or readout devices The method of claim 10 further comprising:

12. Injecting captured and compressed carbon dioxide obtained from a direct air capture system into an apparatus, the apparatus using the captured carbon dioxide as a low global warming potential refrigerant to provide heating or cooling, the apparatus being a cooling apparatus, the captured carbon dioxide obtained from the direct air capture system being compressed to supercritical carbon dioxide or liquid carbon dioxide and injected into the cooling apparatus as a low global warming potential refrigerant. A method comprising:

13. injecting the captured and compressed carbon dioxide obtained from a direct air capture system into an apparatus, the apparatus using the captured carbon dioxide as a low global warming potential refrigerant to provide heating or cooling, the apparatus being a heat pump apparatus, the captured carbon dioxide obtained from the direct air capture system being injected into the heat pump apparatus as a low global warming potential refrigerant, and the purity of the captured carbon dioxide is between 91% and 100%. A method comprising:

14. Injecting captured and compressed carbon dioxide obtained from a direct air capture system into an apparatus that uses the captured carbon dioxide as a low global warming potential refrigerant to provide heating or cooling, where the carbon dioxide is compressed in multiple stages to accommodate variable temperature requirements throughout mobile and commercial low global warming potential refrigerant applications. A method comprising:

15. Injecting captured and compressed carbon dioxide obtained from a direct air capture system into an apparatus that uses the captured carbon dioxide as a low global warming potential refrigerant to provide heating or cooling, and an additional multi-ejector system design is employed to control refrigerant flow, optimize efficiency, and mitigate compressor load to enable operation in extreme weather conditions. A method comprising:

16. injecting the captured and compressed carbon dioxide obtained from the direct air capture system into an apparatus that uses the captured carbon dioxide as a low global warming potential refrigerant to provide heating or cooling, the direct air capture system compressing the captured carbon dioxide to a supercritical or subcritical state that can be used by the apparatus as a low global warming potential refrigerant; A method comprising:

17. a captured carbon dioxide inlet coupled to receive captured carbon dioxide obtained from a direct air capture system, the direct air capture system capturing carbon dioxide through gas-liquid contact; means for using the captured carbon dioxide as a low global warming potential refrigerant to provide heating or cooling. A system comprising:

18. 20. The system of claim 17, wherein the means is a cooling device.

19. A direct air recovery system; a multi-stage compression system that converts the carbon dioxide gas into subcritical and supercritical carbon dioxide fluid; A mobile or stationary cooling system that uses carbon dioxide via direct air capture as a low global warming potential refrigerant. A system comprising:

20. 20. The system of claim 19, wherein the resulting low global warming potential fluid carbon dioxide having a purity of 91-100% is of interest for applications in PC / MAC, cold chain / food retail / blast chillers, heat pumps, data centres and also for implementation as a transcritical booster, part of a cascade system or as a secondary coolant.

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