Building emission processing and / or sequestration systems and methods

Abstract

To provide building emission processing and sequestration systems, which can address carbon dioxide generation from combustion of fossil fuels and proliferation thereof in metropolitan areas.SOLUTION: There are provided systems and / or methods for capture of carbon dioxide from flue gas generated within a building. The systems or methods can include: a step of providing air and fuel to a combustion burner; a step of combusting the air and fuel within the combustion burner; a step of monitoring the amount of free oxygen in the burner; and a step of controlling the amount of air and fuel provided to the burner to maintain a free oxygen amount of about 3%.SELECTED DRAWING: Figure 3C

Description

Technical Field

[0001] (Cross - Reference to Related Applications) This application claims priority and the benefit of U.S. Provisional Patent Application No. 62 / 840,206, filed on April 29, 2019, entitled "Building Carbon Dioxide Sequestration Systems and Metho ds (Construction of Carbon Dioxide Sequestration Systems and Methods)" and U.S. Provisional Patent Application No. 62 / 977,050, filed on February 14, 2020, entitled "Building Emission Processing and / or Sequestratio n Systems and Methods (Building Emission Processing and / or Sequestration Systems and Methods)", the entireties of each of which are hereby incorporated by reference into this specification.

[0002] The field of the present invention relates to the treatment of building emissions, which can include carbon dioxide management systems and methods, and more specifically, to large combustion energy sources for building systems, such as steam heating and hot water with by - product generation of emissions, utilized by a large number of floors and large - area buildings.

[0003]

Background Art

[0003] The generation of carbon dioxide within buildings, particularly in metropolitan areas, is an important contributor to overall carbon dioxide generation. Carbon dioxide is currently listed as a greenhouse gas, and its reduction is sought worldwide. The generation of carbon dioxide is an essential part of respiration and life, but it is important to limit its generation to address climate change. ​​​ is necessary. The present disclosure provides a building emissions treatment and isolation system that can address the combustion of fossil fuels in urban areas and the resulting carbon dioxide emissions from their rapid increase. SUMMARY OF THE INVENTION

[0004] A system or method for operating a combustion boiler within a building is provided. The system or method can include supplying air and fuel to a combustion burner, combusting the air and fuel within the combustion burner, monitoring the amount of free oxygen within the burner, and controlling the amount of air and fuel supplied to the burner to maintain an amount of free oxygen of about 3%. The system or method can include combusting air and fuel within the burner to generate flue gas having an oxygen concentration, and restricting air from the flue gas by substantially eliminating tramp air within a conduit operably positioned to convey the flue gas from the burner.

[0005] A system or method for cooling flue gas from a combustion boiler within a building is provided. The system or method can include supplying flue gas to at least one economizer having at least one set of cooling coils that convey boiler feed water, cooling the flue gas, and heating the boiler feed water.

[0006] A system or method for separating carbon dioxide from flue gas generated from a combustion boiler within a building is provided. The system or method can include supplying flue gas containing less than about 3% water, compressing the flue gas, cooling the compressor with a heat transfer fluid, and a chiller and ​The step of supplying a heat transfer fluid to and / or from a cooling tower can be included. The system or method can include the step of compressing flue gas and the step of drying the flue gas using nitrogen recovered during the separation of carbon dioxide recovered from the flue gas. The system or method can use a pressure swing adsorption assembly to remove at least a portion of nitrogen from the flue gas to produce greater than about 95% carbon dioxide, and before supplying the flue gas to the pressure swing adsorption assembly, use the nitrogen removed from the flue gas to remove water from the flue gas. The system or method can use a pressure swing adsorption assembly to remove at least a portion of nitrogen from the flue gas to produce greater than about 95% carbon dioxide, and supply at least a portion of the nitrogen removed from the flue gas to a gas expander / generator. The system or method can use a pressure swing adsorption assembly to remove at least a portion of nitrogen from the flue gas to produce greater than about 95% carbon dioxide, and supply at least a portion of the nitrogen removed from the flue gas to both a dryer and an expander / generator, or to a dryer and a control valve. The control valve may or may not be equipped with a silencer.

[0007] A system or method for cooling carbon dioxide separated from flue gas generated from a combustion boiler within a building is provided. The system or method can use a pressure swing adsorption assembly to separate nitrogen from the flue gas and a turbine expander in the presence of a heat exchanger. A step of expanding nitrogen to cool the fluid in the heat exchanger, and the cooled fluid is transferred to another heat exchanger operably aligned with the carbon dioxide product of the pressure swing adsorption assembly to cool the carbon dioxide product. A method including the steps of is provided.

[0008] A system or method for liquefying carbon dioxide separated from flue gas generated from a combustion boiler in a building is provided. The system or method can include the step of supplying gaseous carbon dioxide into liquid carbon dioxide in a storage container via a sparge assembly is provided. is provided. is provided.

[0009] A building is provided that utilizes a carbon fuel source and generates carbon emissions during combustion of the carbon fuel source. The emissions of the building can be operably coupled to a carbon capture system configured to separate and condense carbon dioxide from the carbon emissions. This system can be configured to process the carbon emissions and return heat to the building is provided. This system can be configured to process the carbon emissions and generate electricity is provided. This system can be configured to process the carbon emissions and store electrical energy is provided. This system can be configured to dynamically control the combustion system and the capture system to reduce carbon combustion and increase carbon capture is provided. is provided.

Brief Description of the Drawings

[0010] Embodiments of the present disclosure are described below with reference to the following accompanying drawings.

[0011]

Figure 1

Figure 2

Figure 3A

Figure 3B

Figure 3C

Figure 4A

Figure 4B

Figure 4C

Figure 5A

Figure 5B

Figure 6

Figure 7

Figure 8

Figure 9

Figure 10

Figure 11

Figure 12A

Figure 12B

DETAILED DESCRIPTION OF THE INVENTION

[0012] The present disclosure will be described with reference to FIGS. 1 to 12B. The systems and methods of the present disclosure can be operated unattended and / or continuously in a building for up to 10 years with only relatively periodic maintenance. Referring first to FIG. 1, a system 10 is provided that includes a flue gas source, such as a boiler, that burns air and fuel to produce flue gas. The flue gas 12 can include typical combustion products from a building's heating and / or cooling system. These buildings can be considered commercial, residential, and / or industrial buildings. System 10 may rely on the combustion of fossil fuels. These fossil fuels can include oil and / or natural gas. When the fuel burns, CO can be produced as part of the flue gas. In the case of natural gas combustion, system 10 can produce at least about 10% CO and about 18% water. The systems and / or methods of the present disclosure can include a section 14 for separation, a section 16 for liquefaction, a section 18 for storage, and a section 19 for the transfer of CO 2 The occurrence is possible. In the case of natural gas combustion, system 10 can produce at least about 10% CO 2 and about 18% water. The systems and / or methods of the present disclosure can include a section 14 for separation, a section 16 for liquefaction, a section 18 for storage, and a section 19 for the transfer of CO 2 can include.

[0013] According to an example, at least about 600 standard cubic feet per minute of the building's flue gas is CO in component 14 of system 10 ​2 is separated and purified from the flue gas process stream can be bypassed. This separation / purification component is under pressure swing (PSA), temperature swing (T SA), or electric swing (ESA), or any combination thereof, and can be an adsorption purification system operated under the conditions. According to an example, it is a layered solid phase adsorbent material that is combined and / or configured to function cooperatively to provide recovery of more than 85% of CO 2 A pressure swing adsorption system that includes a plurality of containers containing a layered solid phase adsorbent material. These multi-component adsorption systems can remove carbon dioxide from an essentially "dry" flue gas stream, typically to a purity of 95% or more, and in other cases at least 99%. Next, this purified carbon dioxide gas is liquefied in a continuous cooling and compression step to cause a phase change to form liquid carbon dioxide as liquefied component 16, and then the liquefied carbon dioxide is provided to storage component 18 and can be removed as needed in a planned manner . According to an example, this liquefied carbon dioxide can be transferred into transfer component 19 , and the transfer can be used, for example, in applications such as concrete hardening, wastewater treatment, other carbon dioxide sequestration methods, recycling for fire protection systems, industrial specialty gases, hybrid fuels and the production of organic intermediates chemicals, or carbonation of beverages, and can be provided to another source such as a storage facility where the carbon dioxide can be distributed for use. Next, referring to FIG. 2, a building system 30 having a system 32 therein is shown . Flue gas 12 is used to capture CO

[0014] from the flue gas generated by the building for 2 capture , a series of systems and / or methods 14, 16, 18, 19 and / or cooling tower 31 is provided to the part of.

[0015] Next, referring to FIGS. 3A - 3C, an example of a boiler configuration is shown as part of the system and / or method of the present disclosure.

[0016] First, referring to FIG. 3A, a boiler 40 that generates combustion 42 in the presence of a free oxygen sensor 43 is shown. The combustion 42 generates flue gas 44 that is supplied to the boiler exhaust 45. Referring to FIG. 3B, the boiler exhaust is operably coupled to a plenum 48. In the illustrated configuration, a plurality of boilers are shown, each having an exhaust 45 and 46. For example, each exhaust is operably coupled to the plenum 48. The combustion 42 generates flue gas 44 that is supplied to the boiler exhaust 45. Referring to FIG. 3B, the boiler exhaust is operably coupled to a plenum 48. In the illustrated configuration, a plurality of boilers are shown, each having an exhaust 45 and 46. For example, each exhaust is operably coupled to the plenum 48.

[0017] Next, referring to FIG. 3C, a boiler configured with the system and / or method of the present disclosure is shown. Thus, air 60 and fuel 62 can be provided to the combustion burner, and their mixture, and thus its combustion, is controlled by a combustion controller 66 operably connected to the free oxygen sensor 43. Thus, the boiler feed water 52 is received by the combustion boiler, heated to hot water or steam 50, which is used to heat building systems such as buildings and / or water heaters 58. The water heater system 58 can be configured to receive potable water for heating and / or industrial process water for heating. Thus, air 60 and fuel 62 can be provided to the combustion burner, and their mixture, and thus its combustion, is controlled by a combustion controller 66 operably connected to the free oxygen sensor 43. Thus, the boiler feed water 52 is received by the combustion boiler, heated to hot water or steam 50, which is used to heat building systems such as buildings and / or water heaters 58. The water heater system 58 can be configured to receive potable water for heating and / or industrial process water for heating. The water heater system 58 can be configured to receive potable water for heating and / or industrial process water for heating. can be configured to receive.

[0018] According to an exemplary embodiment, the control 66 can utilize the sensor 43 to monitor the amount of free oxygen in the combustion burner and maintain the amount of free oxygen at about 3%. About 3% free oxygen is the amount of free oxygen in the combustion burner and maintain the amount of free oxygen at about 3%. 、It may contain 3-7% free oxygen. According to the examples, combustion can produce flue gas 44. The composition of the flue gas 44 can be controlled to contain at least about 10% carbon dioxide. About 10% carbon dioxide may be 9-12% of the carbon dioxide in the flue gas from the combustion of natural gas. The system 10 can be utilized to burn fuels other than natural gas that may have other optimal CO flue gas concentrations. Therefore, the system 10 can be configured to utilize multiple fuels. 2 Determine the flue gas concentration The present disclosure's system and / or method can include the steps of separating carbon dioxide from the flue gas, liquefying the carbon dioxide after separating it from the flue gas, liquefying the separated carbon dioxide after separating it from the flue gas, storing the carbon dioxide after liquefying it, and / or transporting the carbon dioxide after storing it. Referring to both FIGS. 3B and 3C, a system and / or method for operating a combustion boiler within a building is provided, which includes burning air and fuel within a burner to produce flue gas 44 having an oxygen concentration, and restricting air from the flue gas by substantially eliminating tramp air within a conduit operably positioned to convey the flue gas from the burner. According to the examples, in the case of multiple boilers as shown in FIG. 3B, the exhausts 45 and 46 can be operably aligned with the plenum 48. Unused exhausts such as 46 are the tramp air to the plenum.

[0019] The system and / or method of the present disclosure can include the step of separating carbon dioxide from the flue gas, the step of liquefying the carbon dioxide after separating it from the flue gas, the step of liquefying the separated carbon dioxide after separating it from the flue gas, the step of storing the carbon dioxide after liquefying it, and / or the step of transporting the carbon dioxide after storing it. Referring to both FIGS. 3B and 3C, a system and / or method for operating a combustion boiler within a building is provided, which includes burning air and fuel within a burner to produce flue gas 44 having an oxygen concentration, and restricting air from the flue gas by substantially eliminating tramp air within a conduit operably positioned to convey the flue gas from the burner. According to the examples, in the case of multiple boilers as shown in FIG. 3B, the exhausts 45 and 46 can be operably aligned with the plenum 48. Unused exhausts such as 46 are the tramp air to the plenum. The system and / or method of the present disclosure can include the step of separating carbon dioxide from the flue gas, the step of liquefying the carbon dioxide after separating it from the flue gas, the step of liquefying the separated carbon dioxide after separating it from the flue gas, the step of storing the carbon dioxide after liquefying it, and / or the step of transporting the carbon dioxide after storing it. The system and / or method of the present disclosure can include the step of separating carbon dioxide from the flue gas, the step of liquefying the carbon dioxide after separating it from the flue gas, the step of liquefying the separated carbon dioxide after separating it from the flue gas, the step of storing the carbon dioxide after liquefying it, and / or the step of transporting the carbon dioxide after storing it. The system and / or method of the present disclosure can include the step of separating carbon dioxide from the flue gas, the step of liquefying the carbon dioxide after separating it from the flue gas, the step of liquefying the separated carbon dioxide after separating it from the flue gas, the step of storing the carbon dioxide after liquefying it, and / or the step of transporting the carbon dioxide after storing it.

[0020] Referring to both FIGS. 3B and 3C, a system and / or method for operating a combustion boiler within a building is provided, which includes burning air and fuel within a burner to produce flue gas 44 having an oxygen concentration, and restricting air from the flue gas by substantially eliminating tramp air within a conduit operably positioned to convey the flue gas from the burner. According to the examples, in the case of multiple boilers as shown in FIG. 3B, the exhausts 45 and 46 can be operably aligned with the plenum 48. Unused exhausts such as 46 are the tramp air to the plenum. Referring to both FIGS. 3B and 3C, a system and / or method for operating a combustion boiler within a building is provided, which includes burning air and fuel within a burner to produce flue gas 44 having an oxygen concentration, and restricting air from the flue gas by substantially eliminating tramp air within a conduit operably positioned to convey the flue gas from the burner. According to the examples, in the case of multiple boilers as shown in FIG. 3B, the exhausts 45 and 46 can be operably aligned with the plenum 48. Unused exhausts such as 46 are the tramp air to the plenum. Referring to both FIGS. 3B and 3C, a system and / or method for operating a combustion boiler within a building is provided, which includes burning air and fuel within a burner to produce flue gas 44 having an oxygen concentration, and restricting air from the flue gas by substantially eliminating tramp air within a conduit operably positioned to convey the flue gas from the burner. According to the examples, in the case of multiple boilers as shown in FIG. 3B, the exhausts 45 and 46 can be operably aligned with the plenum 48. Unused exhausts such as 46 are the tramp air to the plenum. Referring to both FIGS. 3B and 3C, a system and / or method for operating a combustion boiler within a building is provided, which includes burning air and fuel within a burner to produce flue gas 44 having an oxygen concentration, and restricting air from the flue gas by substantially eliminating tramp air within a conduit operably positioned to convey the flue gas from the burner. According to the examples, in the case of multiple boilers as shown in FIG. 3B, the exhausts 45 and 46 can be operably aligned with the plenum 48. Unused exhausts such as 46 are the tramp air to the plenum. Referring to both FIGS. 3B and 3C, a system and / or method for operating a combustion boiler within a building is provided, which includes burning air and fuel within a burner to produce flue gas 44 having an oxygen concentration, and restricting air from the flue gas by substantially eliminating tramp air within a conduit operably positioned to convey the flue gas from the burner. According to the examples, in the case of multiple boilers as shown in FIG. 3B, the exhausts 45 and 46 can be operably aligned with the plenum 48. Unused exhausts such as 46 are the tramp air to the plenum. Referring to both FIGS. 3B and 3C, a system and / or method for operating a combustion boiler within a building is provided, which includes burning air and fuel within a burner to produce flue gas 44 having an oxygen concentration, and restricting air from the flue gas by substantially eliminating tramp air within a conduit operably positioned to convey the flue gas from the burner. According to the examples, in the case of multiple boilers as shown in FIG. 3B, the exhausts 45 and 46 can be operably aligned with the plenum 48. Unused exhausts such as 46 are the tramp air to the plenum. Referring to both FIGS. 3B and 3C, a system and / or method for operating a combustion boiler within a building is provided, which includes burning air and fuel within a burner to produce flue gas 44 having an oxygen concentration, and restricting air from the flue gas by substantially eliminating tramp air within a conduit operably positioned to convey the flue gas from the burner. According to the examples, in the case of multiple boilers as shown in FIG. 3B, the exhausts 45 and 46 can be operably aligned with the plenum 48. Unused exhausts such as 46 are the tramp air to the plenum. It may be a source of supply. According to an exemplary embodiment, the system and / or The method provides fluid communication between the burner and the plenum during operation of one boiler, while at the same time Restrict fluid communication between the plenum and the burner during idle of the other operating boiler Steps can be included. In at least one configuration, a door or partition 47 is provided It can be made operable to exclude draft air from the exhaust of the burner during idle. possible.

[0021] According to at least one aspect of the present disclosure, real-time control of a combustion source or boiler is For example, higher efficiency can be achieved to reduce natural gas or fuel consumption while increasing the concentration of carbon dioxide in the flue gas. This may seem counterintuitive to increase the concentration of carbon dioxide in the flue gas when the system and / or The method of the present disclosure is being used to reduce carbon emissions from a building. However, increasing the concentration of carbon dioxide Can provide the benefit of reducing fuel consumption by reducing heat loss due to exhaust. Controlling free oxygen to 3% by adjusting combustion Can provide higher combustion efficiency. According to an example, when burning natural gas through combustion control, it approaches the 12% concentration value of CO And it is desirable to achieve a carbon dioxide concentration of at least about 10% in the flue gas. This is at least one feature of the disclosed building emissions treatment system And / or method, and can be used as one of the first steps in carbon capture. 2 And achieve a carbon dioxide concentration of at least about 10% in the flue gas. This is at least one feature of the disclosed building emissions treatment system And / or method, and can be used as one of the first steps in carbon capture. It can be used as.

[0022] Inside the building, the combustion burner is set to various predetermined combustion rates, 1) off state, 2) slow combustion rate, and / or 3) By controlling to a fast combustion rate, it can respond to the need for hot water or steam By doing so, the operation of the boiler can be instructed. These speeds may have been established in older boilers, for example, via a calibrated mechanical linkage. Recognizing that the operation of a periodic boiler varies greatly from hour to hour, day to day, and season to season, it is desirable to establish automatic control of the flame speed continuously across the entire boiler load range while controlling free oxygen as described above. The system and / or method of the present disclosure can be configured to reduce the on-off cycle by extending the operating time of the boiler at a reduced flame speed, extending the life of the boiler, and providing a more continuous flow of flue gas to a separation, liquefaction, storage, and / or transportation system and / or the method of the present disclosure.

[0023] Therefore, the boiler and system control (e.g., FIG. 11) can achieve higher building thermal efficiency while generating optimal conditions for the supply of flue gas to the system and method of the present disclosure.

[0024] Next, referring to FIGS. 4A-4C, a plurality of parts of a system and method for separating water from flue gas and cooling the flue gas are shown. First, referring to FIGS. 4A-4C, three different configurations of a system and / or method for cooling flue gas from a combustion boiler in a building are shown. First, referring to FIG. 4A, the flue gas 44 can proceed to a combination of a non-condensing and a condensing economizer 60a. The flue gas 44 is first supplied with boiler feed water 52 through a conduit, a set of conduits, and / or a coil, and the flue ​​​​​​​​​​​​​​The flue gas is cooled and proceeds to a non-condensing configuration where the boiler feed water is heated. Thus, the fuel A method for cooling flue gas from a combustion boiler in a building is provided. When the boiler feed water is heated, it can be supplied to the boiler, thus reducing the energy required to heat the feed water to hot water and / or steam.

[0025] Furthermore, the economizer can be configured for condensation. Thus, a conduit, a set of conduits, or the coil 54 can be configured to carry, for example, potable or industrial process water received from a utility. This water is typically carried through underground pipes and may have a temperature close to that of the groundwater. Thus, the water will have a substantially different temperature from the flue gas even after being partially cooled in the non-condensing economizer. By supplying the flue gas to these conduits, water can be removed from the flue gas, thus producing a condensate effluent 53. This water proceeding through the conduit is heated and provided to the hot water system 58 (FIG. 3C) as the intake 54 of the water heating system, where it is heated and can be received through the outlet 56. Thus, the amount of energy required to heat the water in the hot water system 58 is at least less than if the water received for heating had to be heated from a temperature typically associated with typical tap water, rather it is preheated and thus less for that reason. According to an alternative configuration, referring to FIG. 4B, one set of coils 52 can be associated with one economizer 60b and another set of coils 54 can be associated with another economizer 65a. In this configuration, the economizer 60b can be a non-condensing economizer and the economizer 65a can be configured as a condensing economizer. ​​​​​​​ According to another embodiment of the present disclosure, the diverter 64 can be operably coupled to the economizer as shown in FIGS. 4A - 4C. According to an example, the cooled flue gas can be supplied from the diverter 64 using a blower. The system and / or method can control the amount of flue gas processed using the diverter. According to an example, the current system according to FIG. 4C is expected to receive 450 - 500 standard cubic feet per minute (SCFM) of wet flue gas 44. This diverter can be controlled by an overall master system (FIG. 11) that can control the electric butterfly valve within the diverter. The master system can collect data on the temperature and flow rate of the gas and operate the blower as shown in FIG. 6. Therefore, if the economizer is downstream of the process stream from the diverter, the blower may precede the economizer. According to an example, the flue gas is at least about 10% carbon dioxide and / or at least about 3% free oxygen before entering the first economizer. The systems and / or methods of the present disclosure can utilize an economizer configured as shown in FIGS. 5A and 5B, for example, and the method can include additional separation as well as liquefaction, storage, and transportation. The moisture content of the flue gas from the boiler is about 18% and the temperature is determined to be in the range up to 350°F.

[0026]

[0027]

[0027] This water can be substantially removed from the flue gas before separating the CO₂. 2 This can be done by lowering the temperature of the flue gas below the dew point and condensing the water as a liquid. As the moisture content of the flue gas decreases, the dew point also decreases, and the requires additional cooling, which can result in flue gas condensation. .

[0028] Flue gas condensate tends to be slightly acidic (pH<=5), which is why Unsuitable construction materials (such as carbon steel) can cause damage to the plenums of some buildings. In such cases, the gas is removed from the plenum and the gas is removed from the exhaust pipes of acid-resistant stainless steel construction. The condenser must be condensed in an external heat exchanger with a component element. This can result in some small particles remaining in the gas stream. These small particles are This disclosure may be referred to as an acid aerosol, which may be present at ppm levels. These systems and / or methods are directed to removing azoles, e.g., wet It includes a wall heat exchanger, an impinger with inert reticulated carbon foam, and a precipitator.

[0029] In accordance with the above, a non-condensing economizer can operate above the dew point temperature and can Without condensation, the economizer would be able to reduce most of the preheating. May be compatible with Nam building materials.

[0030] As mentioned above, a condensing economizer extracts flue gas from the plenum and condenses it into a A diverter (Figure 4C) can be provided downstream of the condensing economizer. These condensates can be chemically neutralized before proceeding to the building drain.

[0031] Referring now to FIG. 6, drying the flue gas increases the pressure of the flue gas from the diverter. It can be continued using blower 68 to effect this. This blower 68 can support the flow through heat exchanger / condenser 70 and can be operably coupled to the quench assembly 74 and can include a water outlet 71. The heat exchanger 70 can be configured to cool the gas below the dew point to condense most of the water, leaving less than about 3% water or about as little as 0.2% water. The heat exchanger 70 can be configured to cool the gas below the dew point to condense most of the water, leaving less than about 3% water or about as little as 0.2% water. The heat exchanger 70 can be cooled by, for example, an external water / glycol loop provided from a chiller and / or water from, for example, a building's cooling tower and can be of a tube and shell configuration. As shown, the water removed from the system in the heat exchanger 70 may be slightly acidic and the water can be expected to be neutralized before proceeding to a public treatment works (POTW) or sewer system. In addition, some water remains in the process stream as small micro-droplets, mist, or acidic aerosol, which can be minimized or removed by special heat exchanger designs, impingement devices, or in some cases settlers. After most of the water has been removed and the acidic aerosol reduced, the cooled flue gas 72 can proceed to a compressor to increase the pressure of the flue gas to an optimum level of about 100 psi g or less as directed by the PSA system specifications.

[0032] Referring now to FIG. 7, compressor 74 can receive flue gas 72. Compressor 74 can be an "oil-free" compressor to eliminate downstream product contamination and the compressor can be configured with a variable frequency drive (VFD) to respond to variable gas flow rates. The heat exchanger 70 can be cooled by, for example, an external water / glycol loop provided from a chiller and / or water from, for example, a building's cooling tower and can be of a tube and shell configuration. As shown, the water removed from the system in the heat exchanger 70 may be slightly acidic and the water can be expected to be neutralized before proceeding to a public treatment works (POTW) or sewer system. In addition, some water remains in the process stream as small micro-droplets, mist, or acidic aerosol, which can be minimized or removed by special heat exchanger designs, impingement devices, or in some cases settlers. After most of the water has been removed and the acidic aerosol reduced, the cooled flue gas 72 can proceed to a compressor to increase the pressure of the flue gas to an optimum level of about 100 psi g or less as directed by the PSA system specifications. Referring now to FIG. 7, compressor 74 can receive flue gas 72. Compressor 74 can be an "oil-free" compressor to eliminate downstream product contamination and the compressor can be configured with a variable frequency drive (VFD) to respond to variable gas flow rates. The heat exchanger 70 can be cooled by, for example, an external water / glycol loop provided from a chiller and / or water from, for example, a building's cooling tower and can be of a tube and shell configuration.

[0033] After most of the water has been removed and the acidic aerosol reduced, the cooled flue gas 72 can proceed to a compressor to increase the pressure of the flue gas to an optimum level of about 100 psi g or less as directed by the PSA system specifications. Referring now to FIG. 7, compressor 74 can receive flue gas 72. Compressor 74 can be an "oil-free" compressor to eliminate downstream product contamination and the compressor can be configured with a variable frequency drive (VFD) to respond to variable gas flow rates. The heat exchanger 70 can be cooled by, for example, an external water / glycol loop provided from a chiller and / or water from, for example, a building's cooling tower and can be of a tube and shell configuration.

[0034] Referring now to FIG. 7, compressor 74 can receive flue gas 72. Compressor 74 can be an "oil-free" compressor to eliminate downstream product contamination and the compressor can be configured with a variable frequency drive (VFD) to respond to variable gas flow rates. Compressor 74 can be an "oil-free" compressor to eliminate downstream product contamination and the compressor can be configured with a variable frequency drive (VFD) to respond to variable gas flow rates. The heat exchanger 70 can be cooled by, for example, an external water / glycol loop provided from a chiller and / or water from, for example, a building's cooling tower and can be of a tube and shell configuration. Since the contraction can increase the temperature of the flue gas, the second heat exchanger 76 can be utilized to lower the temperature of the flue gas to less than 40°C. At this stage, the gas may contain less than about 3% water that may be present as steam, the gas may be at a temperature less than 40°C, and the pressure may be about 100 psig.

[0035] Referring to FIG. 7, a system and / or method for separating carbon dioxide from flue gas generated from a combustion boiler within a building includes supplying flue gas 72 containing less than about 3% water, compressing the flue gas, and cooling the compressor 74 with a heat transfer fluid 90 and providing the heat transfer fluid between the chiller and / or cooling tower. An example of the compressor is shown in FIG. 8. The heat transfer fluid can be, for example, water, and the water of the chiller can be cooled within the cooling tower of the building before returning the used heat transfer fluid to the chiller. Thus, the system and / or method of the present disclosure can include additional separation, liquefaction, storage, and / or transportation. This is only an example of the heat generating components of a system that can be cooled with the heat transfer fluid of the chiller and / or cooling tower. More than 70% of the cooling requirements of the system and / or method of the present disclosure can result from the heat generated by the compressor and / or pump, and from the heat exchangers on the liquefaction skid. Each of these components can be equipped with a water cooling circuit directly supplied from a local chiller or from a central chiller. The local chiller can be water cooled with a water loop provided by the cooling water from the central chiller or the cooling tower of the building. The central chiller can be designed, for example, to prioritize heat transfer in the following order: a) domestic hot water make-up, b) cooling tower, c) exchange with the outside air. ​​​​​​​​​​​​​​​​

[0036] Referring again to FIG. 7, after compression, the flue gas can be supplied to a dryer 78, such as a desiccant dryer. The dryer 78 can be operably engaged with a sweep feed nitrogen feed configured to regenerate the spent desiccant. Typically, the dryer is a two-chamber cycling device where one chamber dries and the other chamber is regenerated for drying, and these cycles continue. Nitrogen can be supplied to the spent desiccant in one chamber while at the same time the other chamber is drying the flue gas. Thus, a system and / or method is provided for separating carbon dioxide from flue gas generated from a combustion boiler in a building, which can include drying the flue gas using the recovered nitrogen during separation of the recovered carbon dioxide from the flue gas. This recovered nitrogen is conveyed from the pressure swing adsorption assembly 80 to the dryer 78 via conduit 92 and can then be exhausted through stack 86. According to an embodiment, the dried flue gas can be supplied for further separation, liquefaction, storage, and / or transportation. From the dryer, the flue gas 79 containing less than 10 ppm of water can proceed to a pressure swing adsorption (PSA) assembly 80. This pressure swing adsorption assembly can provide CO recovery of greater than 85% with a purity of greater than 95%, 1 psig, and 100 °C. The maximum CO output flow at this point can be about 40 SCFM.

[0037] The remaining portion of the flue gas, mainly nitrogen, may continue under pressure and / or be split by some returning to the dryer 78. Another portion of the nitrogen can proceed to the turbine expander 82 / generator 93. 2 2 At this point, the maximum CO 2 ​ can, and the turbine expander 82 / generator 93 can provide electrical energy 94 and a low-temperature output gas at approximately ambient pressure. Additionally, a control valve 84 equipped with a silencer can be positioned operably in parallel with the expander 82 / generator 93.

[0038] Accordingly, a method for separating carbon dioxide from flue gas generated from a combustion boiler in a building is provided that can include the step of using a pressure swing adsorption assembly 80 to remove at least a portion of nitrogen from the flue gas to produce carbon dioxide 78 in excess of about 95%. The nitrogen removed from the flue gas can be used, for example, in a dryer 78 to remove water from the flue gas prior to supplying the flue gas to the pressure swing adsorption assembly. Alternatively, or additionally, at least a portion of the nitrogen removed from the flue gas can be supplied to a gas expander / generator. Alternatively, or additionally, a portion of the nitrogen from the PSA can be provided to a control valve equipped with a silencer and another portion to the expander / generator. According to an exemplary embodiment, the system and / or method of the present disclosure can include the steps of separating nitrogen into portions, supplying one portion to a dryer, and supplying another portion to the expander / generator. In one example, one portion is about one-third of the nitrogen from the pressure swing adsorption assembly. adsorption assembly. One example is about one-third of the nitrogen from the pressure swing adsorption assembly.

[0039] A system and / or method for cooling carbon dioxide separated from flue gas generated from a combustion boiler in a building using the nitrogen exhaust of the PSA is also provided. The system and / or method uses a pressure swing adsorption assembly 80 to remove nitrogen from the flue gas and The step of separating, and expanding nitrogen by a turbine in the presence of a heat exchanger 92 to heat the step of cooling the fluid in the exchanger 92, and transferring the cooled fluid to another heat exchanger 100 operably aligned with the carbon dioxide product of the pressure swing adsorption assembly to cool the carbon dioxide product 78. The turbine can be, for example, part of a generator 93 or provided to cool the exchanger 92. The nitrogen gas exiting the PSA typically has a flow rate exceeding 65% of the rated system flow rate and can be at least 85 psig. According to an embodiment, nitrogen can be processed and stored as a marketable product. For power generation, grid-compatible power conversion is required. The output of the turbine generator is at 500 Hz and is not compatible with a 60 Hz grid. Thus, appropriate power conversion is assumed to be specified. This can be rectification followed by a DC-AC multiphase inverter with appropriate safety features in the event of a building power outage.

[0040] After being used in the heat exchanger with the turbine generator and CO the nitrogen waste gas can return to the exhaust stack or plenum. Referring now to FIG. 9, in another series of components of the present disclosure, CO with a purity greater than 95% can be cooled and compressed in a continuous step as shown in heat exchanger 110 with compressors 106 and 108 and a heat exchanger with a compressor operably engaged with a cooling transfer fluid 90 to approach a phase change state for liquefaction. According to an embodiment, CO with a purity greater than 95% has a temperature resulting from the PSA that can reach 100 °C. The nitrogen waste gas can return to the exhaust stack or plenum after being used in the heat exchanger with the turbine generator and CO The nitrogen waste gas can return to the exhaust stack or plenum after being used in the heat exchanger with the turbine generator and CO 2 After being used in the heat exchanger with the turbine generator and CO the nitrogen waste gas can return to the exhaust stack or plenum.

[0041] Referring now to FIG. 9, in another series of components of the present disclosure, CO with a purity greater than 95% 2 78 can be cooled and compressed in a continuous step as shown in heat exchanger 110 with compressors 106 and 108 and a heat exchanger with a compressor operably engaged with a cooling transfer fluid 90 to approach a phase change state for liquefaction. According to an embodiment, pure CO with a purity greater than 95% 78 can be cooled and compressed in a continuous step as shown in heat exchanger 110 with compressors 106 and 108 and a heat exchanger with a compressor operably engaged with a cooling transfer fluid 90 to approach a phase change state for liquefaction. According to an embodiment, pure CO with a purity greater than 95% 2 is provided at a temperature resulting from the PSA that can reach 100 °C. It is possible. As described, a heat exchanger is provided to lower the temperature of the gas to a sufficient temperature, and then the gas can be compressed to a higher pressure. According to the embodiment, this CO 2 stream - The heat removed from the m can be transferred via an external water / glycol cooling loop back to a heat management system that supports preheating of the make-up water as shown in FIG. 9A. It can also be provided to raise the temperature of the nitrogen gas exiting the PSA before it expands through the turbine. This allows the nitrogen flow to be maximized before exceeding the low temperature output limit, thereby improving the turbine efficiency. This is just one of several examples for obtaining a more efficient overall system by utilizing heat from system components elsewhere in the system. According to FIG. 9, there is a continuous stepwise cooling and / or compression of the CO gas, driving towards a final state of 311 psig and 0°F, at which point a phase change occurs and the C 2 O becomes liquid. O 2 becomes liquid.

[0042] Next, referring to FIG. 10, a CO 2 liquefaction and storage system and / or method is shown, wherein the CO 2 gas 112 is dispersed inside a container 113 such as a heat-insulated container. Examples of heat-insulated containers include, but are not limited to, liquid storage tanks with vacuum jackets. Inside this container the gas 112 can be converted to a liquid 114. According to the embodiment, the gas 112 can be provided to a sparge assembly 118, where the gas 112 is provided as a sparge gas 120 that liquefies when dispersed into the liquid 114.

[0043] The vapor 116 at the top of the container 113 is by a refrigeration system 122 that cools the vapor 116 managed, and the vapor 116 condenses back into the liquid 114, and the liquid 114 returns into the container 113 . According to an exemplary configuration, the system 122 can be configured as a loop in fluid communication with the container 113 and the vapor CO 2 116 enters the system 122 and returns to the container 113 as the liquid CO 2 114 . In at least one configuration, the system 122 is configured as a low-temperature condenser with an evaporator.

[0044] In the event of a power loss in the building, for example, due to the excellent insulation of the vacuum jacketed tank , the liquid CO 2 can be maintained for at least 30 days. According to an embodiment, the building itself , for example, a fire related to electronic components that require a CO 2 extinguishing method, such as a fire, may be discharged into the container 113 to supply CO for extinguishing the fire. 2

[0045] Referring to FIGS. 1, 11, 12A, and 12B, according to another embodiment, a CO 2 offtake management can be included that uses one or more vehicles provided in conjunction with the need for delivery as provided by CO removal and / or system control, and a CO 2 removal and / or delivery system is provided. For example, the liquid CO attached to the truck 200 from the container 11 2 3 is directly transferred to the CO 2 tank on the truck 200, and a removal and / or delivery truck 200 can be provided. The system can be based on the capacity of the container 113, the CO of the stem 10 2 ​​Generate a legal date / time pick-up window and / or is CO 2 Based on a number of parameters such as the need for CO delivery 2 Generate pick-up times It can be configured to do so. CO 2 Regarding the need for delivery, such high-purity CO 2 is It is contemplated that it can be stored in a warehouse or directly delivered to the user without the need for additional purification. An example of direct delivery can be delivery to a wastewater treatment plant.

[0046] Next, referring to FIG. 11, the components of the control system at the plant, process, and field levels are shown. According to an embodiment, a combustion emissions and control, master PLC (MASTER PLC) controller, diverter, compressor, dryer, separator, cooling and compression, refrigeration / storage, and food-grade CO 2 An exemplary overall control system showing the provision of is provided. These systems are also coupled to electrical, natural gas, and water utility systems These control systems illustrate a basic network architecture diagram. The MASTER PLC controls the entire plant using Ethernet loop connections and Internet IP protocol communication to local packet controllers, as well as direct connection and control to digital and analog I / O field instrumentation levels. The HMI server collects data from the MASTER PLC, manages the real-time display of the plant, runs logging, data management applications, and communicates with external users through a secure firewall. Also, defined in the MASTER PLC controls the entire plant. The HMI server collects data from the MASTER PLC, manages the real-time display of the plant, runs logging, data management applications, and communicates with external users through a secure firewall. Also, defined in the MASTER PLC alarm time display, executes logging, data management applications, and communicates with external users through a secure firewall. Also, defined in the MASTER PLC communicates with external users through a secure firewall. Also, defined in the MASTER PLC Engineering to maintain all operating software and updates that are periodically downloaded This includes development workstations.

[0047] Referring to FIGS. 12A and 12B, sequences of different components and processes described herein, and systems and / or methods embodiments are disclosed that detail additional heat management components associated with a building. As seen throughout the figures and accompanying descriptions, there are multiple locations where heat is transferred from different components of the disclosed system to an existing building system. For example, as shown, a chiller can be located both within a building and within an existing cooling tower. These in-operation cooling components can be operably coupled to the heat removed from process components via individual cooling loops. According to an embodiment, heat, also referred to as waste heat, can be transferred to a building system that can operate more efficiently using the excess heat. Thus, with respect to waste heat from the disclosed system, design choices are to transfer the waste heat first to the building's steam and hot water make-up system, then to the building's cooling tower, and finally to an appropriate chiller that includes heat exchange with air. As shown in FIGS. 11 and 12A and 12B, a heat management system (see, e.g., reference to a MASTER PLC, a controller, etc.) can optimize combustion using a combustion controller to conserve the use of fuels such as natural gas in a boiler, control the removal of moisture from flue gas with a front-end controller, perform additional separation with a dryer, perform PSA with a separation controller, liquefy and store CO with a liquefaction / storage controller, and take-off control ler, and take-off control ler to transfer waste heat to an appropriate chiller that includes heat exchange with air.

[0048] As shown in FIGS. 11 and 12A and 12B, a heat management system (e.g., refer to a MASTER PLC, a controller, etc.) can optimize combustion using a combustion controller to conserve the use of fuels such as natural gas in a boiler, control the removal of moisture from flue gas with a front-end controller, perform additional separation with a dryer, perform PSA with a separation controller, liquefy and store CO by optimizing combustion using a combustion controller, thereby saving the use of fuels such as natural gas in a boiler, controlling the removal of moisture from flue gas with a front-end controller, performing additional separation with a dryer, performing PSA with a separation controller, liquefying and storing CO in a liquefaction / storage controller, and taking off control with an off-take controller. 2 liquefy and store it, and off-take control It can be instructed by a trolley to pick up and / or off-take to a delivery truck. These and additional controllers can function to control boiler feed water, drinking and / or industrial service water, chiller water, and / or cooling tower water, and nitrogen expansion cooling to reduce and / or eliminate the heat load within the system. Accordingly, the flue gas can be cooled for water knockout, and the heat-generating electrical components such as compressors, blowers, pumps, fans, etc. can also be cooled.

[0049] According to an embodiment, the system and / or method of the present disclosure can include an energy storage system configured to include power conversion components and / or a battery or battery bank component. As an example, energy can be generated through nitrogen turbine expansion, and this energy can be converted and stored within the building. The energy can be converted and provided directly to system components such as compressors, and / or provided to system components after storage, thereby reducing the building's energy demand. Further, the energy can be provided to the power grid associated with the building itself.

[0050] According to an embodiment, using a MASTER PLC, the energy generated in the system can be utilized during "peak demand" times (e.g., when electricity rates are high) and / or when the building is using a "peak" amount of power. During these times, the MASTER PLC monitors the building's demand and then changes system parameters to efficiently use energy storage and / or change carbon dioxide separation, liquefaction, storage, and / or transportation. Reduce energy consumption during "peak demand", thereby saving energy costs. Provide.

[0051] Examples of the systems and / or methods of the present disclosure can not only reduce carbon emissions in a carbon capture system, but also improve the overall energy efficiency (both thermal and electrical) of a building while reducing CO 2 emissions. Examples can include steps to reduce carbon fuel consumption through optimization of boiler combustion, steps to provide warmer boiler feedwater, thereby reducing the energy required to heat the boiler feedwater, steps to warm drinking water or process water and thereby reduce the energy required to heat the drinking water or process water further, steps to generate electrical energy and use the same to power system components, and / or steps to use the building's cooling tower to reduce the building's heat load, etc., which can individually and / or collectively be part of a system that dramatically improves the efficiency of the building. Reduce carbon fuel consumption by optimizing boiler combustion, Provide warmer boiler feedwater, thereby reducing the energy required to heat the boiler feedwater, Warm drinking water or process water and thereby reduce the energy required to heat the drinking water or process water further, Generate electrical energy and use the same to power system components, and / or Use the building's cooling tower to reduce the building's heat load, etc., which can individually and / or collectively be part of a system that dramatically improves the efficiency of the building. Examples can include steps to reduce carbon fuel consumption through optimization of boiler combustion, steps to provide warmer boiler feedwater, thereby reducing the energy required to heat the boiler feedwater, steps to warm drinking water or process water and thereby reduce the energy required to heat the drinking water or process water further, steps to generate electrical energy and use the same to power system components, and / or steps to use the building's cooling tower to reduce the building's heat load, etc., which can individually and / or collectively be part of a system that dramatically improves the efficiency of the building. Examples can include steps to reduce carbon fuel consumption through optimization of boiler combustion, steps to provide warmer boiler feedwater, thereby reducing the energy required to heat the boiler feedwater, steps to warm drinking water or process water and thereby reduce the energy required to heat the drinking water or process water further, steps to generate electrical energy and use the same to power system components, and / or steps to use the building's cooling tower to reduce the building's heat load, etc., which can individually and / or collectively be part of a system that dramatically improves the efficiency of the building.

Claims

1. 1. A method for operating a combustion boiler in a building, comprising: supplying air and fuel to a combustion burner; combusting air and fuel in the combustion burner; monitoring the amount of free oxygen in the burner; The amount of air and fuel supplied to the burner is controlled to maintain a free oxygen content of approximately 3%. and The method includes:

2. The combustion produces a flue gas, and the method comprises: The method of claim 1 further comprising producing carbon.

3. The method of claim 1 further comprising separating the carbon dioxide from the flue gas.

4. The method further includes the step of liquefying the carbon dioxide after separating the carbon dioxide from the flue gas. The method of claim 3 .

5. The method further includes storing the carbon dioxide after separating the carbon dioxide from the flue gas. The method of claim 3 .

6. 6. The method of claim 5, further comprising the step of transporting the carbon dioxide after storing the carbon dioxide. Method of posting.

7. 1. A method for operating a combustion boiler in a building, comprising: A stove is a device in which air and fuel are combusted in a burner to produce a flue gas having a free oxygen concentration. Tep and a trough in a conduit operatively positioned to convey the flue gas from the burner; restricting air from said flue gases by substantially excluding lamp air. and

8. There are at least two boilers operably coupled to a shared plenum, and the method includes: providing fluid communication between the operating burners of one of the boilers and the plenum, and Steps for restricting fluid communication between the lenum and the idle burners of the other operating boiler The method of claim 7, further comprising:

9. 8. The method of claim 7, further comprising separating carbon dioxide from the flue gas. 。

10. The method further includes the step of liquefying the carbon dioxide after separating the carbon dioxide from the flue gas. The method of claim 9 .

11. Combusting the air and fuel to produce a flue gas having at least about 10% carbon dioxide. The method of claim 7 further comprising generating the gas.

12. Combusting the air and fuel to produce a flue gas having about 3% free oxygen. The method of claim 7 further comprising the steps of:

13. A method for cooling flue gas from a combustion boiler in a building, comprising: The flue gas is circulated through at least one economizer having at least one set of cooling coils. providing a cooling gas to the flue gas; and heating the boiler feedwater.

14. 2. The method of claim 1 , further comprising the step of: supplying the heated boiler feedwater to the combustion boiler.

14. The method according to claim 13.

15. The flue gas is fed to the set of coils and then transported to a station for transporting drinking or industrial process water. supplying the flue gas to another set of coils, the supplying step being performed to reduce the amount of flue gas in the flue gas. further cooling the flue gas; and heating said potable or industrial process water. The method of claim 13 , further comprising:

16. supplying the heated potable or industrial process water to a hot water system. The method of claim 15, comprising:

17. The method of claim 1, further comprising the step of heating the hot water system with steam from the combustion boiler. Item 17. The method according to item 16.

18. One set of cooling coils is a component of an economizer, and the other set of cooling coils is The method of claim 15 , wherein the is another economizer component.

19. One economizer is a non-condensing economizer and the other is a condensing economizer. The method of claim 18,

20. The flue gas is supplied to one of the economizers, and then the cooled flue gas is passed through a die. a second economizer for supplying at least a portion of the cooled flue gas to the second economizer through a second inverter; 20. The method of claim 18, further comprising the step of bypassing the mixer.

21. The cooled flue gas is blown from the diverter to the other economizer using a blower.

21. The method of claim 20, further comprising the step of providing a

22. Prior to entering one of the economizers, the flue gas is enriched in at least about 10% carbon dioxide. The method of claim 13, wherein

23. 2. The method of claim 1, wherein the flue gas is about 3% free oxygen prior to entering the one economizer.

14. The method according to claim 13.

24. 13. The method of claim 1, further comprising the step of liquefying carbon dioxide after cooling the flue gas.

3. The method according to claim 3.

25. 1. A method for separating carbon dioxide from flue gas generated by a combustion boiler in a building, comprising: providing a flue gas containing less than about 3% water; compressing the flue gas; Cool the compressor with a heat transfer fluid and supply the heat transfer fluid between the compressor and the chiller and / or cooling tower. and

26. The cooling tower of the building is used to cool the chiller before returning the spent heat transfer fluid to the chiller. The method of claim 25 further comprising cooling the heat transfer fluid.

27. Recovering water from the heat exchanger and treating the recovered water prior to discharging the recovered water.

26. The method of claim 25, further comprising the step of: processing.

28. Separating carbon dioxide from the flue gas and then liquefying the carbon dioxide from within the flue gas.

26. The method of claim 25, further comprising the steps of:

29. 1. A method for separating carbon dioxide from flue gas generated by a combustion boiler in a building, comprising: compressing the flue gas; Nitrogen recovered during the separation of carbon dioxide from the flue gas is used to and drying the gas.

30. 30. The method of claim 29, wherein the flue gas before compression is less than about 3% water.

31. and supplying the nitrogen to an exhaust stack after using the nitrogen in the dryer. The method of claim 29, further comprising:

32. 3. The method of claim 2, further comprising the step of supplying said nitrogen from a pressure swing adsorption assembly.

9. The method according to claim 9.

33. After the flue gas is fed to the dryer, the flue gas having less than about 10 ppm water is 33. The method of claim 32, further comprising the step of supplying said pressure swing adsorption assembly. Law.

34. A switch that supplies the nitrogen from the pressure swing adsorption assembly to both the dryer and a control valve.

33. The method of claim 32, further comprising the step of:

35. 1. A method for separating carbon dioxide from flue gas generated by a combustion boiler in a building, comprising: Removing at least a portion of the nitrogen from the flue gas using a pressure swing adsorption assembly. to produce greater than about 95% carbon dioxide; a pressure swing adsorption assembly that includes a pressure swing adsorption assembly having a pressure swing adsorption assembly that includes ... and using the removed nitrogen to remove water from the flue gas.

36. less than 10 ppm before the flue gas is supplied to the pressure swing adsorption assembly. The method of claim 35, wherein the water is

37. and feeding the nitrogen into the exhaust stack of the building after drying the flue gas. The method of claim 35, further comprising:

38. 1. A method for separating carbon dioxide from flue gas generated by a combustion boiler in a building, comprising: Removing at least a portion of the nitrogen from the flue gas using a pressure swing adsorption assembly. to produce greater than about 95% carbon dioxide; supplying at least a portion of said nitrogen removed from said flue gas to a gas expander / generator. and

39. providing electricity from the expander / generator to a building and / or a grid.

40. The method of claim 38, comprising:

40. 40. The method of claim 38, further comprising the step of supplying the nitrogen to an exhaust stack of the building. Method of posting.

41. separating the nitrogen from the pressure swing adsorption assembly; and a control valve and another portion to the expander / generator; 40. The method of claim 38, further comprising:

42. 39. The method of claim 38, wherein the control valve and the expander / generator are aligned in parallel. method.

43. 1. A method for separating carbon dioxide from flue gas generated by a combustion boiler in a building, comprising: Removing at least a portion of the nitrogen from the flue gas using a pressure swing adsorption assembly. to produce greater than 95% carbon dioxide; At least a portion of the nitrogen removed from the flue gas is fed to a dryer and a gas expander / exhaust gas and supplying both the live organ and the tissue to said device.

44. Prior to supplying the nitrogen to the pressure swing adsorption assembly, the nitrogen is used to 44. The method of claim 43, further comprising drying the gas to less than 10 ppm water.

45. The nitrogen is used to dry the flue gas, and then the nitrogen is pumped into the exhaust stack of the building.

45. The method of claim 44, further comprising the step of providing:

46. separating the nitrogen into portions, feeding one portion to the dryer and another portion to the expander; 44. The method of claim 43, further comprising the step of:

47. said portion being about one-third of said nitrogen from said pressure swing adsorption assembly; The method of claim 46.

48. 44. The method of claim 43, further comprising generating electricity using the expander / generator. Method of posting.

49. After the nitrogen is used in the expander / generator, the nitrogen is pumped into the exhaust stack of the building.

49. The method of claim 48, further comprising the step of providing.

50. A method for cooling carbon dioxide separated from flue gas generated by a combustion boiler in a building. There was, separating nitrogen from the flue gas using a pressure swing adsorption assembly; Expanding the nitrogen in the presence of a heat exchanger to cool the fluid in the heat exchanger. and, The cooled fluid is operably coupled to the carbon dioxide product of the pressure swing adsorption assembly. and transferring the carbon dioxide product to another heat exchanger aligned with the cooling facility to cool the carbon dioxide product. , a method comprising:

51. the flue gas received by the pressure swing adsorption assembly is less than 10 ppm; 51. The method of claim 50, wherein the water is

52. using an expander / generator to expand the nitrogen in the presence of a heat exchanger.

51. The method of claim 50, further comprising:

53. providing electricity from the expander / generator to the building grid. The method of claim 52.

54. 4. The method of claim 3 further comprising the step of: supplying the expanded nitrogen to an exhaust stack of the building.

52. The method according to claim 52.

55. The carbon dioxide product is greater than about 95% carbon dioxide and is at least about 100° C.

51. The method of claim 50.

56. 56. The method of claim 55, further comprising the step of reducing the temperature of the carbon dioxide product to less than about 100° C. The method described above.

57. A method for liquefying carbon dioxide separated from flue gas generated by a combustion boiler in a building The gaseous carbon dioxide is supplied through a sparge assembly to form a carbon dioxide gas in a vessel. A method comprising the step of sparging carbon into liquid carbon dioxide.

58. 58. The method of claim 57, wherein the gaseous carbon dioxide is at least 95% carbon dioxide. 。

59. further comprising bubbling the gaseous dioxide from the sparge assembly.

58. The method of claim 57.

60. 58. The method of claim 57, further comprising establishing a carbon dioxide liquid / vapor barrier within the tank. The method described above.

61. 7. The process of claim 6, further comprising cooling the vapor carbon dioxide to produce liquid carbon dioxide. The method according to claim 0.

62. A refrigeration unit is connected to the turbine to receive the vaporized carbon dioxide and liquefy the carbon dioxide.

62. The method of claim 61, further comprising the step of operably engaging the ink.

63. 63. The method of claim 62, further comprising returning the liquefied carbon dioxide to the tank. Law.

64. A building emission is operably coupled to a carbon capture system, the system capturing the carbon emission. and a carbon fuel source configured to separate and condense carbon dioxide from said carbon fuel. Buildings that produce carbon emissions when burning primary fuel sources.

65. The building emissions are operably coupled to a carbon capture system, the system converting the carbon emissions into a carbon-fuel source configured to be combusted and to return heat to the building; Buildings that sometimes produce carbon emissions.

66. The building emissions are operably coupled to a carbon capture system, the system converting the carbon emissions into Utilizing a carbonaceous fuel source and combusting the carbonaceous fuel source to process and generate electricity. Buildings that sometimes produce carbon emissions.

67. The building emissions are operably coupled to a carbon capture system, the system converting the carbon emissions into and storing electricity by utilizing a carbonaceous fuel source and burning said carbonaceous fuel source. Buildings that sometimes produce carbon emissions.

68. The building emissions are operably coupled to a carbon capture system, the system and configured to dynamically control the capture system to reduce carbon burning and increase carbon capture.

1. A building that utilizes a carbonaceous fuel source and produces carbon emissions upon combustion of said carbonaceous fuel source.

69. A system for generating carbon-based fuels that utilizes carbon fuel sources that are operably coupled to a carbon capture and removal system. a building using a carbon-based fuel source that produces carbon emissions upon combustion of said carbon fuel source.

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