Patent Publication Number: US-2023147875-A1

Title: Integrated green energy and selective molecular separation system, and process of generating electricity and selectively separating and capturing predetermined molecules present in surrounding environment (green energy blue)

Description:
CROSS REFERNCE TO RELATED APPLICATIONS 
     This application is a non-provisional application that claims priority to U.S. Provisional Application No. 63/278,316, filed on Nov. 11, 2021 and U.S. Provisional Application No. 63/284,354, filed on Nov. 30, 2021. The disclosures of the prior applications are hereby incorporated by reference herein in their entireties. 
    
    
     TECHNICAL FIELD 
     The present disclosure relates to green energy generation processes and systems, such as thermal, solar, wind, and kinetic energy processes and systems, which generate electricity. The present disclosure also relates to selective molecular separation (e.g., greenhouse gas capturing) processes and systems that separate and capture predetermined molecules, such as greenhouse gas (carbon dioxide (CO 2 )), carbon monoxide (CO), and nitrogen oxides (NO X ), from the surrounding environment. In particular, the present disclosure relates to a green energy generating system that is integrated with a selective molecular separation (e.g., greenhouse gas capturing) system such that the output of each system is utilized by the other to form a unitary system that produces green energy (i.e., electricity) while also separating and capturing predetermined molecules (e.g., greenhouse gases) from the surrounding environment. The present disclosure further relates to processes of integrating green energy generation with selectively separating and capturing predetermined molecules present in a surrounding environment. 
     BACKGROUND 
     Known green energy systems include thermal (e.g., geothermal) energy systems, solar energy systems, and wind energy systems (such as wind farms), that utilize a naturally occurring energy source to generate electricity. Geothermal energy systems extract heat from an underground geologic formation, such as a hot rock reservoir. In a typical geothermal energy system, a fluid is pumped down into an underground rock formation to transfer thermal energy of the rock formation to the surface. At the surface, the heated fluid is utilized in a process that drives a turbine and an electrical generator to produce electrical power, and then the fluid is pumped back into the underground formation to repeat the cycle. Solar energy systems convert sunlight energy into electrical energy either through photovoltaic (PV) panels or through lenses or mirrors that concentrate solar radiation. When the sun shines onto a solar panel, energy from the sunlight is absorbed by the PV cells in the panel. This energy creates electrical charges that move in response to an internal electrical field in the cell, causing electricity to flow. Lenses or mirrors concentrate solar radiation so that photons in the concentrated radiation raise the temperature of a primary fluid (e.g., molten salt), which is used in a process that eventually heats a secondary fluid to drive a turbine and an electrical generator to produce electrical power. In wind energy systems, wind turns the propeller-like blades of a turbine around a rotor, which spins the shaft of an electrical generator to produce electricity. 
     Greenhouse gas capturing systems may include devices/equipment and chemical materials for removing greenhouse gases (carbon dioxide (CO 2 )), as well as carbon monoxide (CO), and nitrogen oxides (NO X ), or other harmful gases from the environment such as the air in the atmosphere that we breathe. Some systems involve chemical and/or physical mechanisms for removing some molecules (e.g. greenhouse gas) from the environment. 
     SUMMARY 
     While green energy systems and greenhouse gas capturing systems have been used to positively impact the Earth&#39;s environment by reducing pollution, the two systems have always been two independent and discrete systems or processes. Green energy systems and greenhouse gas capturing systems have not been considered in combination, i.e., as one integrated system or process. 
     The present disclosure describes different types of energy systems, such as thermal, solar, wind, combustion, and kinetic energy systems, that can be integrated with a selective molecular separation (e.g., greenhouse gas capturing) system. The energy system and the selective molecular separation system are integrated with each other because the output of each system is utilized by the other to form a unitary system that produces green energy (i.e., electricity) while also separating and capturing predetermined molecules (e.g., greenhouse gas) from the surrounding environment. The present disclosure further describes different green energy processes, such as thermal, solar, wind, and kinetic energy systems, that can be integrated with a selective molecular separation (e.g., greenhouse gas capturing) process to form one unitary process that produces green energy (i.e., electricity) while separating and capturing predetermined molecules (e.g., greenhouse gases) from the surrounding environment. In some embodiments, a kinetic energy fluid turns a blade that rotates a shaft connected to an electrical generator. The rotating shaft produces electromagnetic induction in the electrical generator to produce electricity. The kinetic energy fluid can be subsequently directed to and integrated with a regeneration/desorption process in the selective molecular separation unit where thermal energy of the kinetic energy fluid is exchanged to break hands between separated predetermined molecules and a sorbent and/or molecular sieve membrane in order to be captured and stored. In other embodiments, heat from arm electrical heater associated with the selective molecular separation unit and powered by the electricity from the electrical generator is used to break the bonds between separated predetermined molecules and the sorbent and/or molecular sieve membrane. The present disclosure thus provides an integrated green energy and selective molecular separation system and process (“Green Energy Blue”) that is an improvement over known systems and processes for generating green energy, and over known systems and processes for capturing greenhouse gases. 
     In an embodiment, a process of generating electricity and selectively separating and capturing predetermined molecules present in a surrounding environment comprises: providing kinetic energy fluid derived from an energy source; driving a turbine by rotating a shaft of the turbine via the kinetic energy fluid; driving a generator via rotation of the shaft of the turbine to generate electricity by electromagnetic induction; supplying at least one of (i) the kinetic energy fluid exiting the turbine and (ii) electricity generated by the generator to a selective molecular separation unit; intaking the predetermined molecules into the selective molecular separation unit and selectively separating at least one predetermined molecule from other molecules of the surrounding environment; and capturing the at least one predetermined molecule via a desorption process of the at least one predetermined molecule in the selective molecular separation unit using heat from thermal energy of at least one of (i) the kinetic energy fluid and (ii) an electrical heater powered by the electricity generated by the generator. 
     In an embodiment, the at least one predetermined molecule is selectively separated via at least one of a sorption process and a molecular sieve membrane in the selective molecular separation unit. 
     In an embodiment, the desorption process regenerates at least one of a sorbent material used in the sorption process and the molecular sieve membrane. 
     In an embodiment, the thermal energy is sufficient to break a bond between the separated predetermined molecule and at least one of the sorbent material and the molecular sieve membrane to regenerate the at least one of the sorbent material and the molecular sieve membrane for a next cycle of selective separation of another predetermined molecule of the surrounding environment. 
     In an embodiment, the sorption process utilizes at least one of an absorption process and adsorption process. 
     In an embodiment, the sorbent material is impregnated or grafted in the molecular sieve membrane. 
     In an embodiment, the process further comprising storing the at least one predetermined molecule in a storage unit after the capturing. 
     In an embodiment, the turbine is a windmill. 
     In an embodiment, the energy source is at least one of: a combustion process which produces the kinetic energy fluid; a burning process which produces the kinetic energy fluid; and the surrounding environment including wind which produces the kinetic energy fluid. 
     In an embodiment, the combustion process occurs in one of an engine and a gas turbine. 
     In an embodiment, the burning process occurs in one of a flare, a water heater and a furnace. 
     In an embodiment, the heat is generated via at least one of: (i) one or more of a Rankine Cycle; a Carnot Cycle; a Brayton Cycle; a Diesel Engine Cycle, an Otto Cycle; an Ericsson Cycle; a Hygroscopic Cycle; a Scuderi Cycle; a Stirling Cycle; a Manson Cycle; a Stoddard Cycle; an Atkinson Cycle; a Humphrey Cycle; a Bell Coleman Cycle and a Lenoir Cycle; and (ii) the electrical heater powered by the generator in combination with the one or more Cycles in (i). 
     In an embodiment, the kinetic energy fluid is at least one of in a supercritical state; and has an increased flow rate when driving the turbine. 
     In another embodiment, an integrated green energy and selective molecular separation system comprises: an energy source that provides thermal energy to heat a working fluid to produce a heated working fluid; a turbine that is driven by the heated working fluid; a generator that is driven by the turbine to generate electricity by electromagnetic induction; and a selective molecular separation unit that intakes predetermined molecules present in a surrounding environment and receives at least one of (i) the heated working fluid exiting the turbine and (ii) electricity generated by the generator, wherein the selective molecular separation unit selectively separates at least one predetermined molecule from other molecules of the surrounding environment and captures the at least one predetermined molecule via a desorption process using heat from thermal energy of at least one of (i) the heated working fluid and (ii) an electrical heater that is associated with the selective molecular separation unit and that is powered by the electricity generated by the generator. 
     In an embodiment, the selective molecular separation unit comprises at least one of a sorbent material and a molecular sieve membrane that selectively separates the at least one predetermined molecule of the surrounding environment. 
     In an embodiment, heat transferred from the thermal energy regenerates at least one of the sorbent material and the molecular sieve membrane by breaking a bond between the separated at least one predetermined molecule and at least one of the sorbent material and the molecular sieve membrane for a next cycle of selective separation of another predetermined molecule of the surrounding environment. 
     In an embodiment, the sorbent material is at least one of an absorbent material and adsorbent material. 
     In an embodiment, the sorbent material is impregnated or grafted in the molecular sieve membrane. 
     In an embodiment, the system further comprises a storage unit that stores the at least one predetermined molecule after the at least one predetermined molecule is captured. 
     In an embodiment, the heat is generated via at least one of: (i) one or more of: a Rankine Cycle; a Carnot Cycle; an Ericsson Cycle; a Hygroscopic Cycle; a Scuderi Cycle; a Stirling Cycle; a Manson Cycle; and a Stoddard Cycle; and (ii) the electrical heater powered by the generator in combination with the one or more Cycles in (i). 
     In an embodiment, the selective molecular separation unit further comprising a condenser that extracts heat from the heated working fluid exiting the turbine to desorb the separated at least one predetermined molecule and regenerate at least one of the sorbent material and the molecular sieve membrane, and wherein the condenser reduces a temperature of the heated working fluid to produce a reduced-temperature working fluid. 
     In an embodiment, the system further comprises: a compressor that receives the reduced-temperature working fluid from the condenser and increases a pressure of the reduced-temperature working fluid to produce an increased-pressure, reduced-temperature working fluid, and conveys the increased-pressure, reduced-temperature working fluid to a heat exchanger that also receives the thermal energy from the energy source, wherein the heat exchanger transfers the thermal energy from the energy source to the increased-pressure, reduced-temperature working fluid to increase a temperature of the increased-pressure, reduced-temperature working fluid to produce the heated working fluid having increased pressure and increased temperature. 
     In an embodiment, the system further comprises: one of an expansion valve and a nozzle to increase a velocity of the heated working fluid before the heated working fluid enters the turbine. 
     In an embodiment, the energy source is one of: an underground geothermal energy source comprising a primary fluid that transfers heat to the heated working fluid to increase kinetic energy of the heated working fluid; a thermal energy source including one of a flare and an exhaust flue gas comprising a primary fluid that transfers heat to the heated working fluid to increase kinetic energy of the heated working fluid; and a solar energy source that raises the temperature of a primary fluid that transfers heat to the heated working fluid to increase kinetic energy of the heated working fluid. 
     In a further embodiment, an integrated green energy and selective molecular separation system comprises: an energy source that provides kinetic energy fluid; a turbine comprising a shaft that is driven by the kinetic energy fluid; a generator that is driven via rotation of the shaft of the turbine to generate electricity by electromagnetic induction; a selective molecular separation unit that intakes predetermined molecules present in a surrounding environment and receives at least one of (i) the kinetic energy fluid exiting the turbine and (ii) electricity generated by the generator, wherein the selective molecular separation unit selectively separates at least one predetermined molecule from other molecules of the surrounding environment and captures the at least one predetermined molecule via a desorption process using heat from thermal energy of at least one of (i) the kinetic energy fluid and (ii) an electrical heater that is associated with the selective molecular separation unit and that is powered by the electricity generated by the generator. 
     In an embodiment, the energy source is at least one of: a combustion process which produces the kinetic energy fluid; a burning process which produces the kinetic energy fluid; and the surrounding environment including wind which produces the kinetic energy fluid. 
     In an embodiment, the turbine is a windmill. 
     In an embodiment, the system further comprises at least one of: a compressor to increase a pressure of the kinetic energy fluid before the kinetic energy fluid enters the turbine; a combustor to increase a temperature of the kinetic energy fluid before the kinetic energy fluid enters the turbine; and a burner to increase a temperature of the kinetic energy fluid before the kinetic energy fluid enters the turbine. 
     In an embodiment, the selective molecular separation unit comprises at least one of a sorbent material and a molecular sieve membrane that selectively separates the at least one predetermined molecule of the surrounding environment. 
     In an embodiment, heat transferred from the thermal energy regenerates at least one of the sorbent material and the molecular sieve membrane by breaking a bond between the separated at least one predetermined molecule and at least gone of the sorbent material and the molecular sieve membrane for a next cycle of selective separation of another predetermined molecule of the surrounding environment. 
     In an embodiment, the system further comprises a heat exchanger to exchange the thermal energy from the kinetic energy fluid to at least one of the sorbent material and the molecular sieve membrane to regenerate and desorb the at least one predetermined molecule. 
     In an embodiment, the sorbent material is at least one of an absorbent material and adsorbent material. 
     In an embodiment, the sorbent material is impregnated or grafted in the molecular sieve membrane. 
     In an embodiment, the system further comprises a storage unit that stores the at least one predetermined molecule after the at least one predetermined molecule is captured. 
     In an embodiment, the heat is generated via at least one of: (i) one or more of: a Brayton Cycle; a Diesel Engine Cycle, a Otto Cycle; an Atkinson Cycle; a Humphrey Cycle; a Bell Coleman; and a Lenoir Cycle; and (ii) the electrical heater powered by the generator in combination with the one or more Cycles in (i). 
     In an embodiment, the turbine is a windmill. 
     In an embodiment, the energy source is at least one of: a combustor which produces the kinetic energy fluid; a burner which produces the kinetic energy fluid; and a windmill which produces the kinetic energy fluid. 
     In an embodiment, the combustor is one of an engine and a gas turbine. 
     In an embodiment, the burner is one of a flare, a water heater and a furnace. 
    
    
     
       BRIEF DESCRIPTION OF THE FIGURES 
       The summary above, as well as the following detailed description of illustrative embodiments, is better understood when read in conjunction with the appended drawings. For the purpose of illustrating the present disclosure, exemplary constructions of the disclosure are shown in the drawings. However, the disclosure is not limited to specific methods and instrumentalities disclosed herein. 
         FIG.  1 A  is a schematic illustration of an integrated green energy and selective molecular separation system that uses thermal energy as the source of green energy, according to an embodiment. 
         FIG.  1 B  is a schematic illustration of another embodiment of an integrated green energy and selective molecular separation system that uses thermal energy as the source of green energy. 
         FIG.  1 C  is a schematic illustration of an integrated green energy and selective molecular separation system that uses solar energy as the source of green energy, according to another embodiment. 
         FIG.  1 D  is a schematic illustration of an integrated green energy and selective molecular separation system that uses wind energy as the source of green energy, according to an embodiment. 
         FIG.  1 E  is a schematic illustration of another integrated green energy and selective molecular separation system that uses wind energy as the source of green energy, according to an embodiment. 
         FIG.  2 A  is an illustration of a Rankine Cycle that is implemented by an integrated green energy and selective molecular separation system, according to an embodiment. 
         FIG.  2 B  is another illustration of a Rankine Cycle that is implemented by an integrated green energy and selective molecular separation system, according to an embodiment. 
         FIG.  2 C  illustrates a graph of a Rankine Cycle using water as a working fluid according to an embodiment. 
         FIG.  2 D  illustrates a specific example of a Rankine Cycle that is implemented by an integrated green energy and selective molecular separation system, according to an embodiment. 
         FIG.  2 E  is an illustration of a Carnot Cycle that can be implemented by an integrated green energy and selective molecular separation system, according to an embodiment. 
         FIG.  2 F  is another illustration of Carnot Cycle that can be implemented by an integrated green energy and selective molecular separation system, according to an embodiment. 
         FIG.  3 A  is a schematic illustration of another type integrated green energy and selective molecular separation system, according to an embodiment. 
         FIG.  3 B  is a schematic illustration of a first variation of the integrated green energy and selective molecular separation system of  FIG.  3 A , according to an embodiment. 
         FIG.  3 C  is a schematic illustration of an integrated green energy and selective molecular separation system according to another embodiment. 
         FIG.  3 D  is a schematic illustration of a second variation of the integrated green energy and selective molecular separation system of  FIG.  3 A , according to an embodiment. 
         FIG.  3 E  is a schematic illustration of a third variation of the integrated green energy and selective molecular separation system of  FIG.  3 A , according to an embodiment. 
         FIG.  3 F  is a schematic illustration of a fourth variation of the integrated green energy and selective molecular separation system of  FIG.  3 A , according to an embodiment. 
         FIG.  3 G  is a schematic illustration of a fifth variation of the integrated green energy and selective molecular separation system of  FIG.  3 A , according to an embodiment. 
         FIG.  3 H  is a schematic illustration of a first variation of the integrated green energy and selective molecular separation system of  FIG.  3 C , according to an embodiment. 
         FIG.  3 I  is a schematic illustration of a second variation of the integrated green energy and selective molecular separation system of  FIG.  3 C , according to an embodiment. 
         FIG.  3 J  illustrates a combustion process (i.e., Brayton Cycle) that may occur in an integrated green energy and selective molecular separation system, according to an embodiment, and illustrates corresponding graphs. 
         FIG.  3 K  is an exemplary implementation of an integrated green energy and selective molecular separation system of  FIG.  3 C  in a jet engine (i.e., Brayton Cycle), according to an embodiment. 
         FIG.  4    is a schematic illustration of an absorption and a desorption process that may occur in an integrated green energy and selective molecular separation system, according to an embodiment. 
         FIG.  5 A  shows several types of solid adsorbent materials that may be used in an adsorption process of an integrated green energy and selective molecular separation system, according to an embodiment. 
         FIG.  5 B  illustrates one example of an adsorption process using an adsorbent material that may occur in an integrated green energy and selective molecular separation system, according to an embodiment. 
         FIG.  5 C  illustrates another example of an adsorption process that may occur in an integrated green energy and selective molecular separation system, according to an embodiment. 
         FIG.  5 D  illustrates different types of molecular bonding in a desorption process that may occur in an integrated green energy and selective molecular separation system, according to an embodiment. 
         FIG.  6    illustrates an adsorption process using an adsorbent material/membrane and a desorption process of the adsorbent material/membrane that may occur in an integrated green energy and selective molecular separation system, according to an embodiment. 
         FIG.  7    illustrates an example of a sorption process in which one or more liquid absorbents are passed through one or more solid adsorbent materials that may occur in an integrated green energy and selective molecular separation system, according to an embodiment. 
         FIG.  8    illustrates examples of a separation process using a molecular sieve membrane that may occur in an integrated green energy and selective molecular separation system, according to an embodiment. 
         FIG.  9 A  illustrates an example of generating carbon dioxide molecule (CO 2 ) by mixing a water (H 2 O) molecule with a carbon monoxide (CO) molecule in an integrated green energy and selective molecular separation system, according to an embodiment. 
         FIG.  9 B  illustrates an example of a catalytic converting unit to convert a carbon monoxide molecule (CO) to a carbon dioxide molecule (CO 2 ) that may be implemented in an integrated green energy and selective molecular separation system, according to an embodiment. 
     
    
    
     DETAILED DESCRIPTION 
     While processes, systems and devices are described herein by way of examples and embodiments, those skilled in the art recognize the processes, systems and devices are not limited to the embodiments or drawings described. It should be understood that the drawings and description are not intended to be limited to the particular form disclosed. Rather, the intention is to cover all modifications, equivalents and alternatives falling within the spirit and scope of the appended claims and description. Any headings used herein are for organization purposes only and are not meant to limit the scope of the description of the claims. As used herein, the word “may” is used in a permissive sense (i.e., meaning having the potential to) rather than the mandatory sense (i.e., meaning must). Similarly, the words “include,” “including,” and “includes” mean including, but not limited to. The present disclosure describes particular embodiments and with reference to certain drawings, but the subject matter is not limited thereto. 
     The present disclosure will provide description to the accompanying drawings, in which some, but not all embodiments of the subject matter of the disclosure are shown. Indeed, the subject matter may be embodied in many different forms and should not be construed as limited to the embodiments set forth herein, rather, these embodiments are provided so that this disclosure satisfies all the legal requirements. The disclosure herein is illustrative and explanatory of one or more embodiments and variations thereof, and it will be appreciated that various changes in the design, organization, means of operation, structures and location, methodology, and use of mechanical equivalents may be made without departing from the spirit of the invention. Because many varying and different embodiments may be made within the scope of the concept(s) herein taught, and because many modifications may be made in the embodiments described herein, it is to be understood that the details herein are to be interpreted as illustrative and non-limiting. 
     Certain terminology is used in the following description for convenience only and is not limiting. Certain words used herein designate directions in the drawings to which reference is made. Unless specifically set forth herein, the terms “a,” “an” and “the” are not limited to one element, but instead should be read consistent with the meaning of “one or more,” “at least one,” and “one or more than one.” As used herein “another” means at least a second or more. The terminology includes the words noted above, derivatives thereof and words of similar import. 
     Use of the term “about”, when used with a numerical value, is intended to include +/−10%. For example, if a number of amino acids is identified as about 200, this would include 180 to 220 (plus or minus 10%). Similarly, use of the term “approximately”, when used with a numerical value, is intended to include +/−10%. For example, if a number of amino acids is identified as approximately 200, this would include 180 to 220 (plus or minus 10%). 
     Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art. 
       FIG.  1 A  illustrates one embodiment of an integrated green energy and selective molecular separation system (“Green Energy Blue”) that uses thermal energy as the source  1 A of green energy. In the green energy portion of this system, at least some portion of thermal energy from the source  1 A is transferred as heat to a working fluid  3  by heat exchange. That is, the working fluid  3  absorbs heat from the thermal energy of the source  1 A. In the present disclosure, a thermal energy source can be any source of enemy that transfers thermal energy (i.e., heat) to raise the thermal energy and/or temperature of the working fluid  3 . The transferred heat from the thermal source can subsequently elevate the kinetic energy of the working fluid  3 . The heated working fluid  3  may have a relatively high temperature and pressure. The thermal energy may be derived from the motion and vibration of molecules of the energy source  1 A. Thermal energy sources may include, but are not limited to: geothermal energy sources, such as wells and reservoirs in underground geologic formations; solar energy sources, such as radiation from the sun; burners, such as gas flares resulting from the burning process of natural gas associated with oil extraction; exhaust emitted from an engine; heat conducted from oil and gas pipelines; combustion occurring in an engine or a gas turbine; and commercial and residential heaters, such as water heaters, furnaces, ovens and stoves (i.e., “burners” that derive heat from a flame). The burning processes herein may also produce a kinetic energy fluid. 
     The green energy portion of the integrated system shown in  FIG.  1 A  includes a heat exchanger  2  in which the thermal energy of the energy source  1 A is transferred to the working fluid  3 . In the present disclosure, a heat exchanger can be any mechanical device that exchanges heat between a higher thermal energy source and a lower thermal energy working fluid. In  FIG.  1 A , the thermal energy (heat) is transferred to the working fluid  3  in the heat exchanger  2 . The energy source  1 A in the embodiment of  FIG.  1 A  may be one or more of: gas flares resulting from the burning process of natural gas associated with oil extraction; exhaust emitted from an engine; heat conducting from oil and gas pipelines; combustion occurring in an engine or a gas turbine; and commercial and residential heaters, such us water heaters, furnaces, ovens and stoves (i.e., “burners” that derive heat from a flame). However, other thermal energy sources, such as the geothermal and solar energy sources discussed above, could also be used in the  FIG.  1 A  embodiment. Upon absorbing the thermal energy (heat) in the heat exchanger  2 , the working fluid  3  may increase its temperature, volume and pressure, and thus its enthalpy, and may change its phase state from a liquid to a gas/vapor. The structure of the heat exchanger  2  is not limited in the present disclosure to any particular design or configuration, so long as the heat exchanger  2  is operable to transfer heat from the thermal energy source to the working fluid. As examples, the heat exchanger  2  may be a finned tube heat exchanger, a shell and tube heat exchanger, or a plate heat exchanger. Other types of heat exchangers not listed here that may be used to transfer heat to the working fluid  3  are within the scope of this invention. The heated working fluid  3  is then directed from the heat exchanger  2  towards a turbine  5 . In some instances, the heated working fluid  3  may be considered as a kinetic energy fluid by virtue of its molecular movement to drive the turbine  5 . 
     In the embodiment shown in  FIG.  1 A , a nozzle  4  is provided between the heat exchanger  2  and the turbine  5 , so that the high pressure and temperature working fluid  3  passes through the nozzle  4  before entering the turbine  5 . In other embodiments, the nozzle  4  may not be required, and may be omitted from the green energy portion of the integrated system. In such a case, a high pressure and temperature working fluid  3  flows directly from the heat exchanger  2  into the turbine  5 . In the integrated system of  FIG.  1 A , the nozzle  4  provides a restriction in the path of the heated working fluid  3  in order to transfer some of the pressure of the heated working fluid  3  to velocity, and thus expand the volume of the heated working fluid  3 . The nozzle  4  may be a fixed restriction in the path of the heated working fluid  3 , or may be an adjustable expansion valve that can be controlled, e.g., electronically or manually, to adjust the size of the restriction based on system conditions, a desired temperature and/or pressure of the heated working fluid  3 , or other considerations. As the heated working fluid  3 , preferably in the supercritical gas state/phase, enters the turbine  5 , its kinetic energy will move a series of blades mounted on a shaft of the turbine  5 . The force turns the blades, which rotates the shaft to drive the turbine  5 . In the present disclosure, a turbine is any mechanical device that performs work by using kinetic energy of a working fluid. Two main factors for having a significant amount of kinetic energy entering the turbine  5  can be a supercriticality state of the working fluid  3 , as well as the flow rate of the working fluid  3 . The working fluid  3  with high supercriticality will have higher kinetic energy, and thus and create more work. A higher flowrate of the working fluid  3  will also create more work due to its higher magnitude coming out of the nozzle  4 . More work has the potential to eventually generate more electricity, and capture more predetermined molecules in a selective separation unit  9 ,  15 ,  16  oldie integrated system. 
     The turbine  5 , in turn, drives an electricity generator  6  to generate electricity  7  via electromagnetic induction. In the present disclosure, electricity generator  6  is any mechanical/electrical device that changes kinetic energy to electrical energy. In one embodiment, the electricity generator  6  includes a rotor that is connected to shaft of the turbine  5  so as to rotate with rotation of the shaft. The rotor of the electricity generator  6  may include a coil of copper wire (armature) that rotates in response to rotation of the shaft of the turbine  5 . Two polar field magnets on either side of the armature create a magnetic field inside the in the electricity generator  6 . As the rotor, shaft, and armature rotate, they move within the electric field created by the magnets. As the turbine  5  rotates the armature through the magnetic field, an electrical current is created within the copper coil of the armature. This process of generating electrical current is known as electromagnetic induction. The electricity  7  produced can be extracted from the electricity generator  6 , and may be sent to an electrical grid for commercial distribution and use. In this regard, the frequency of the electricity  7  from the electricity generator  6  can be adjusted to the grid-line frequency of the grid to synchronize the transmission. The electricity  7  produced by the electricity generator  6  can also be directly fed to a desorption unit  16  in the selective molecular separation unit  9 ,  15 ,  16  of the integrated system as discussed in further detail below. Further, the heated working fluid  8  exiting the turbine  5  after driving the turbine  5  (which is a low pressure, high temperature working fluid  8 ) is conveyed to a condenser/heat exchanger  9  in the selective molecular separation unit  9 ,  15 ,  16  of the integrated system as discussed in detail below. 
     As shown in  FIG.  1 A , the selective molecular separation unit  9 ,  15 ,  16  of the integrated system receives an inlet fluid  13  from the surrounding environment. The surrounding environment may be the atmosphere of the earth, such that the inlet fluid  13  is air. The air may be polluted with greenhouse gas (carbon dioxide (CO 2 )), carbon monoxide (CO), and nitrogen oxides (NO X ). Other harmful gases not listed here may also be present in the air. The inlet fluid  13  may be received in the selective molecular separation unit  9 ,  15 ,  16  via an opening, a fan  18  (see  FIG.  1 B ), a vacuum, a pressure difference, or other similar device or process for intaking the inlet fluid  13  and moving the inlet fluid  13  through the selective molecular separation unit  9 ,  15 ,  16 . The selective molecular separation unit  9 ,  15 ,  16  includes a separation portion  15  in which one or more predetermined molecules of the greenhouse gases in the inlet fluid  13  are selectively separated from other molecules of the surrounding environment. The separation may be carried out in the separation portion  15  via a sorption process and/or a molecular sieve membrane. The sorption process utilizes an absorption process and/or an adsorption process. In the absorption process, one or more vessels may contain a liquid absorbent material such as, for example, ethanol amine, mono ethanol amine (MEA), Di ethanol amine (DEA), Methyl Di ethanol amine (MDEA) and tetra ethylene pent-amine (TEPA). Other liquid absorbent materials not listed here are encompassed within the scope of the present disclosure. The inlet fluid  13  containing the greenhouse gases is passed through the liquid absorbent in the vessels (see  FIG.  4   ) at which the predetermined molecules, such as carbon dioxide (CO 2 ), are absorbed by the liquid absorbent in a chemical process. Absorption of the predetermined molecules, such as carbon dioxide (CO 2 ), carbon monoxide (CO), and nitrogen oxides (NO X ) by the liquid absorbent separates the predetermined molecules from other molecules of the inlet fluid  13 . The other molecules, such as oxygen (O 2 ) and nitrogen (N 2 ), which have been separated from the predetermined molecules in the inlet fluid  13  and which do not constituted greenhouse gases may exit the vessels in the separation portion  15  and flow through the condenser/heat exchanger  9  of the selective molecular separation unit  9 ,  15 ,  16  to be released as outlet fluid  14  into the surrounding environment. Meanwhile, the liquid absorbent material containing the predetermined molecules, such as carbon dioxide (CO 2 ), carbon monoxide (CO), and nitrogen oxides (NO X ), subsequently undergoes a desorption process, discussed below, in the same or another vessel as shown in  FIG.  4    via heat from the green energy portion of the integrated system. 
     The adsorption process utilizes solid adsorbent material to adsorb the predetermined molecules (e.g., carbon dioxide (CO 2 ), carbon monoxide (CO), and nitrogen oxides (NO X )) of the inlet fluid  13  to a surface of the absorbent material via molecular bonding. The solid adsorbent material may be one or more of: Zeolite, Layered double hydroxide (LDH), Silica, Metal organic framework (MOF), Activated carbon, Activated carbon fibers (ACF), DOF, Alkali-metal-based materials, ordered porous carbon, Graphene, Carbon molecular sieves (CMS), and combinations thereof (see  FIG.  5 A ). Other solid adsorbent materials not listed here are encompassed within the scope of the present disclosure. Adsorption of the predetermined molecules, such as carbon dioxide (CO 2 ), carbon monoxide (CO), and nitrogen oxides (NO X ) by the solid adsorbent separates the predetermined molecules from other molecules of the inlet fluid  13  which are not adsorbed by the solid adsorbent. The other molecules, such as oxygen (O 2 ) and nitrogen (N 2 ), which have been separated from the predetermined molecules in the inlet fluid  13  and which do not constituted greenhouse gases may exit the separation portion  15  and flow through the condenser/heat exchanger  9  of the selective molecular separation unit  9 ,  15 ,  16  and be released as outlet fluid  14  back into the surrounding environment. In order to enhance the sorption process, the solid adsorbent material may be impregnated with one or more liquid absorbent materials. The porous nature of Zeolite beneficially increases the surface area of this adsorbent material, providing more area to adsorb the predetermined molecules. Results of a study in the following table show that each cubic centimeter of Zeolite has enough pores to adsorb approximately 0.31 grams of carbon dioxide (CO 2 ). 
     
       
         
           
               
             
               
                 TABLE 1 
               
             
            
               
                   
               
               
                 Capacity of 1 cm 3  Zeolite to Adsorb carbon dioxide (CO 2 ) 
               
            
           
           
               
               
               
               
            
               
                 Inlet Fluid Flow 
                 Approximate Amount of 
                 Potential Amount of 
                 Potential Annual CO 2   
               
               
                 Rate in Gallons per 
                 Zeolite that is Fully 
                 CO 2  Captured 
                 Captured 
               
               
                 Minute (GPM) 
                 Regenerated (m 3 ) 
                 (kg) 
                 (Tons) 
               
               
                   
               
            
           
           
               
               
               
               
            
               
                 5 
                 0.172824 
                 53.575 
                 28.159 
               
               
                 10 
                 0.345648 
                 107.151 
                 56,318.565 
               
               
                 50 
                 1.72824 
                 535.754 
                 281,502.303 
               
               
                 100 
                 3.45648 
                 1,071.51 
                 563,185.656 
               
               
                 200 
                 6.91296 
                 2,143.017 
                 1,173,301.808 
               
               
                   
               
            
           
         
       
     
     In an embodiment in which a molecular sieve membrane is used in the sorption process, the inlet fluid  13  may pass through a membrane or a set of membranes that act as filters to physically separate larger molecules from smaller molecules in the inlet fluid  13 . For example, the sieve membrane(s) may physically separate larger oxygen (O 2 ) and nitrogen (N 2 ) molecules from a smaller carbon dioxide (CO 2 ) molecule. That is, the molecular sieve membrane or a set of molecular sieve membranes may have microscopic apertures that are sized to allow only the smaller carbon dioxide (CO 2 ) molecule to pass through, while the larger oxygen (O 2 ) and nitrogen (N 2 ) molecules are deflected and subsequently be directed to an outlet of the selective molecular separation unit  9 ,  15 ,  16  as outlet fluid  14 , and released back into the atmosphere (surrounding environment). The smaller carbon dioxide (CO 2 ) molecule may then pass through one or more additional molecular sieve membranes or sorption processes in the separation portion  15  for further separation. In order to enhance the separation (filtration) process, one of the sorbent materials discussed above impregnated or grafted in the molecular sieve membrane(s). In such a case, the impregnated or grafted in the molecular sieve membrane(s) can be subjected to the desorption process discussed below. 
     After the predetermined molecules of the greenhouse gases in the inlet fluid  13  are selectively separated according to any of the sorption and/or (impregnated/grafted in) molecular sieve membrane embodiments discussed above, the separated predetermined molecules are captured from the sorbent material and/or impregnated/grafted in molecular sieve membrane(s) via a desorption/regeneration process in a desorption unit  16  of the selective molecular separation unit  9 ,  15 ,  16 . The desorption process uses thermal energy to break a bond between the separated predetermined molecule (e.g., carbon dioxide (CO 2 ), carbon monoxide (CO), and nitrogen oxides (NO X )) and the sorbent material (e.g., absorbent, adsorbent material) and/or the impregnated molecular sieve membrane(s). For instance, a solid adsorbent material (e.g., Zeolite) and a liquid absorbent material (e.g., MEA) may require a temperature of, e.g., 80-110 degrees Celsius to release carbon dioxide (CO 2 ) as a gas from the material. In the embodiment illustrated in  FIG.  1 A , the thermal energy used in the desorption process comes from the green energy portion of the integrated system via either thermal energy of the working fluid  8  or/and generated electricity  7  by electrical generator  6 .  FIG.  4    shows an embodiment in which heat from the green energy portion of the integrated system is used to capture the predetermined molecules, such as carbon dioxide (CO 2 ), carbon monoxide (CO), and nitrogen oxides (NO X ) contained in the liquid absorbent material. The liquid absorbent material may be desorbed in the same vessel used in the absorption process, or may be transferred to another vessel for the desorption process as shown in  FIG.  4   . 
     As discussed above, the selective molecular separation unit  9 ,  15 ,  16  receives one or both of: the heated working fluid  8  exiting the turbine  5  and the electricity  7  produced by the electricity generator  6 . The heated working fluid  8  exiting the turbine  5  may be in a superheated gas/vapor state. In this state, the fluid may have a decreased pressure, but a still relatively high temperature. This low pressure, high temperature working fluid  8  is received at the condenser/heat exchanger  9  which exchanges the heat of the high temperature gas/vapor working fluid  8  with the ambient temperature of the air in the desorption unit  16 . This exchange causes the superheated gas/vapor working fluid  8  to cool while the heat is conveyed to one or more vessels, adsorbent materials, or molecular sieve membrane(s) depending on which of these processes is being used in the desorption unit  16  of the selective molecular separation unit  9 ,  15 ,  16  for selectively separating the predetermined molecules. The heat breaks the bond(s) between the separated predetermined molecule(s) (e.g., carbon dioxide (CO 2 ), carbon monoxide (CO), and nitrogen oxides (NO X )) and the sorbent material (e.g., absorbent, adsorbent material) and/or the molecular sieve membrane(s) so that the separated predetermined molecule(s) are released from the sorbent material and/or the molecular sieve membrane(s). The released predetermined molecule(s) (e.g., carbon dioxide (CO 2 ), carbon monoxide (CO), and nitrogen oxides (NO X )) may subsequently be captured, stored and/or sequestered. The carbon dioxide (CO 2 ) molecules may be conveyed from the desorption unit  16  for storage  17  in a storage tank (not shown), or may be transported for later processing and/or use in the fields of, e.g., refrigerants, fire extinguishers, inflatable devices, blasting coal, foaming rubber and plastics, growth of plants in greenhouses, and carbonated beverages. Releasing the separated predetermined molecule(s) from the sorbent material and/or the molecular sieve membrane(s) in the desorption process regenerates the sorbent material and/or the molecular sieve membrane(s) so that the sorbent material and/or the molecular sieve membrane(s) are free of the separated predetermined molecule(s), and able to be reused in a next cycle of selective separation of additional predetermined molecules coming into the separation portion  15  as new inlet fluid  13  from the surrounding environment. In this way, the green energy portion of the system may continuously regenerate and recycle the materials used for desorption, thus improving the efficiency and life of the separation portion  15  and desorption unit  16 . 
     In addition or in the alternative to the heated working fluid  8  used in the desorption process, the desorption unit  16  may include an electrical heater that is powered by the electricity  7  generated by the electricity generator  6 . Thermal energy from the electrical heater in the desorption unit  16  may provide the heat required to break the bond(s) between the separated predetermined molecule(s) (e.g., carbon dioxide (CO 2 ), carbon monoxide (CO), and nitrogen oxides (NO X )) and the sorbent material (e.g., absorbent, adsorbent material) and/or the molecular sieve membrane(s) so that the separated predetermined molecule(s) are released from the sorbent material and/or the molecular sieve membrane(s), as discussed above. That is, the desorption unit  16  may use heat from one or both of: the heated working fluid  8  exiting the turbine  5 ; and the electrical heater powered by the electricity  7  from the electricity generator  6 , in the desorption process discussed above. 
     In the above embodiments, the separation portion  15  and the desorption unit  16  may include one or more vessels for the sorption and desorption processes, respectively. The number of vessels is not limited in the present disclosure. When only one vessel is used, the sorption and desorption processes are implemented in an alternating sequential intervals. That is, the one vessel accommodates the sorption process in one time interval without heat in the desorption process, and in the next time interval is heated in the desorption process without accommodating the sorption process. The time intervals then repeat. Alternatively, the one vessel may undergo both the sorption and desorption process at the same time. In yet another embodiment, the separation portion  15  and the desorption unit  16  may include two or more vessels or a set of several vessels which alternate undergoing the sorption and desorption process. That is, one vessel may accommodate the sorption process while the other vessel undergoes the desorption process simultaneously. After a predetermined amount of time, the one vessel undergoes the desorption process while the other vessel accommodates the sorption process at the same time. In this manner, a continuous sorption and desorption process occurs in the separation portion  15  and the desorption unit  16 . These processes of sorption and desorption can be done as a batch or continuous systems. 
     Similarly, the separation portion  15  and the desorption unit  16  may include one or more sorbents for the sorption and desorption processes. The number of sorbents is not limited in the present disclosure. When only one sorbent is used, the sorption and desorption processes are implemented in an alternating sequential intervals. That is, the one sorbent accommodates the sorption process in one time interval without heat in the desorption process, and in the next time interval is heated in the desorption process without accommodating the sorption process. The time intervals then repeat. Alternatively, the one sorbent may undergo both the sorption and desorption process at the same time. To yet another embodiment, the separation portion  15  and the desorption unit  16  may include two or more sorbents or a set of several sorbents which alternate undergoing the sorption and desorption process. That is, one sorbent may accommodate the sorption process while the other sorbent undergoes the desorption process. After a predetermined amount of time, the one sorbent undergoes the desorption process while the other sorbent accommodates the sorption process. In this manner, a continuous sorption and desorption process occurs in the separation portion  15  and the desorption unit  16 . These processes of sorption and desorption can be done as a batch or continuous systems. 
     Furthermore, the separation portion  15  and the desorption unit  16  may include one or more molecular sieve membranes for the sorption and desorption processes. The number of molecular sieve membranes is not limited in the present disclosure. When only one molecular sieve membrane is used, the sorption and desorption processes are implemented in an alternating sequential intervals. That is, the one molecular sieve membrane accommodates the sorption process in one interval without heat in the desorption process, and in the next interval is heated in the desorption process without accommodating the sorption process. The intervals then repeat. Alternatively, the one molecular sieve membrane may undergo both the sorption and desorption process at the same time. In yet another embodiment, the separation portion  15  and the desorption unit  16  may include two or more molecular sieve membranes or a set of several molecular sieve membranes which alternate undergoing the sorption and desorption process. That is, one molecular sieve membrane may accommodate the sorption process while the other molecular sieve membrane undergoes the desorption process. After a predetermined amount of time, the one molecular sieve membrane undergoes the desorption process while the other molecular sieve membrane accommodates the sorption process. In this manner, a continuous sorption and desorption process occurs in the separation portion  15  and the desorption unit  16 . These processes of sorption and desorption can be done as a batch or continuous systems. 
     As discussed above, the high temperature gas/vapor working fluid  8  is cooled by the condenser/heat exchanger  9 . In the present disclosure, a condenser is any mechanical device that lowers temperature of a fluid. Thus, the low pressure, low temperature working fluid  10  exiting the condenser/heat exchanger  9  may have a decreased temperature along with the decreased pressure. The lower temperature of the working fluid  10  is beneficial in the green energy portion of the integrated system because a lower (cooler) temperature allows the heated working fluid  10  to absorb more heat from the thermal energy of the energy source  1 A and thus increases the efficiency in reusing the heated working fluid in a cyclic thermodynamic process. 
     As is apparent from the foregoing, the green energy portion and the selective molecular separation unit  9 ,  15 ,  16  in the integrated system of  FIG.  1 A  mutually benefit from each other by utilizing outputs from each other. The desorption unit  16  utilizes the heat provided by the green energy portion for the desorption process, while the heated working fluid  8  of the green energy portion is cooled by the condenser/heat exchanger  9  in the selective molecular separation unit  9 ,  15 ,  16  to maximize the heat absorption and efficiency of the heated working fluid  8  in the thermodynamic process. The green energy portion and the selective molecular separation unit  9 ,  15 ,  16  are thus integrated together in one unitary system. 
     The working fluid  10  exiting the condenser/heat exchanger  9  may have a decreased temperature and a decreased and may be in a gas and/or a liquid state, as discussed above. In this state the heated working fluid  10  may be conveyed back to the green energy portion of the integrated system to be first compressed and then reheated by the thermal energy of the energy source  1 A and used again in the green energy process. In order to maximize heat absorption from the energy source  1 A, the heated working fluid  10  conveyed from the condenser/heat exchanger  9  may pass through a compressor  11  to increase the pressure of the heated working fluid  10 . In the present disclosure, a compressor is any mechanical device that elevates pressure of a fluid. The increase in pressure may produce the heated working fluid  12  leaving the compressor  11  in a liquid state with high pressure and low temperature. The high pressure, low temperature heated working fluid  12  is then conveyed back to the heat exchanger  2  to reabsorb heat provided by the thermal energy from the energy source  1 A. The integrated green energy and selective molecular separation process described above may then be repeated in a repetitive, cyclic manner to both generate green energy (e.g., electricity) and selectively remove predetermined molecules (e.g., greenhouse gas (carbon dioxide (CO 2 )), carbon monoxide (CO), and nitrogen oxides (NO X )) from the surrounding environment (e.g., the atmosphere). 
       FIG.  1 B  illustrates another embodiment of an integrated green energy and selective molecular separation system that uses thermal energy as the source of green energy. The integrated system in  FIG.  1 B  is similar to the one described above with respect to  FIG.  1 A , and the component parts of the systems identified with the same reference numerals in both embodiments may be the same and operate in the same manner. The energy source  1 B in the  FIG.  1 B  embodiment may be a geothermal energy source, such as a well, or an underground reservoir in a geologic formation. In this case for instance, heat from the bottom of the well or the reservoir is transferred to the surface via, e.g., fluid such as water, oil, gas, alcohol, and combinations thereof, that absorbs heat from the well or reservoir. However, other thermal energy sources, such as a solar energy source; gas flares; exhaust; heat from oil and gas pipelines; and commercial and residential heaters, discussed above, could also be used in the  FIG.  1 B  embodiment. The green energy portion of the integrated system in  FIG.  1 B  may interact with the selective molecular separation unit  9 ,  15 ,  16  in the same manner as discussed above with respect to the integrated system in  FIG.  1 A . In the  FIG.  1 B  integrated system, the selective molecular separation unit  9 ,  15 ,  16  may include additional components, including one or more additional molecular sieve membranes  19 , a selective catalytic reducer (SCR)  20 , a catalytic converting unit (DOC)  21  and/or a carbon monoxide (CO) reduction unit  22 . The one or more additional molecular sieve membranes  19  may be similar to the molecular sieve membranes discussed above, and can be used to separate larger oxygen (O 2 ), nitrogen (N 2 ) and hydrogen sulfide (H 2 S) molecules from a smaller carbon dioxide (CO 2 ) molecule. That is, the one or more additional molecular sieve membranes  19  may have microscopic apertures that are sized to allow only the smaller carbon dioxide (CO 2 ) molecule to pass through, while the larger oxygen (O 2 ), nitrogen (N 2 ) and hydrogen sulfide (H 2 S) molecules are deflected and redirected (see  FIG.  7   ). The smaller carbon dioxide (CO 2 ) molecule may then continue passing through additional separating devices or processes in the molecular separation unit  9 ,  15 ,  16  such as those discussed above. 
     The selective catalytic reducer (SCR)  20  can lower the concentration of nitrogen oxide (NOx) molecules (e.g., both nitric oxide (NO) and nitrogen dioxide (NO 2 )) in the inlet fluid  13 . Within the selective catalytic reducer (SCR)  20 , the nitrogen oxide (NOx) molecules are reduced by ammonia in water (H 2 O) and nitrogen (N 2 ), which are both non-polluting. The water (H 2 O) and nitrogen (N 2 ) can be then released into the atmosphere or used in a further separation process in the selective molecular separation unit  9 ,  15 ,  16 . For instance, the water (H 2 O) can be fed into the carbon monoxide (CO) reduction unit  22  to react with additional carbon monoxide (CO) molecules in future separation cycles. Catalysts for the selective catalytic reducer (SCR)  20  may include vanadium, molybdenum, tungsten, zeolites, or precious metals. 
     The catalytic converting unit (DOC)  21  (see  FIG.  9 B ) may contain palladium and/or platinum supported on alumina. This unit converts particulate matter (PM), hydrocarbons (i.e., unburnt and partially burned fuel), and carbon monoxide (CO) to carbon dioxide (CO 2 ) and water (H 2 O). The catalytic converting unit (DOC)  21  can therefore be used to reduce hydrocarbon and carbon monoxide from the surrounding environment. The oxidation of carbon monoxide to carbon dioxide may occur as follows: 2 CO+O 2 →2 CO 2 . The oxidation of hydrocarbons to carbon dioxide and water may occur as follows: C x H 2x+2 +[(3x+1)/2] O 2 →x CO 2 +(x+1) H 2 O. 
     The carbon monoxide (CO) reduction unit  22  may mix water (H 2 O) molecules with carbon monoxide (CO) molecules to produce hydrogen (H 2 ) molecules and change the carbon monoxide (CO) molecules to carbon dioxide (CO 2 ) molecules in a manner shown in  FIG.  9 A  and discussed in further detail below. 
       FIG.  1 C  illustrates a further embodiment of an integrated green energy and selective molecular separation system that uses solar energy as the source of green energy. The integrated system in  FIG.  1 C  is similar to the ones described above with respect to  FIGS.  1 A and  1 B , and the component parts of the systems identified with the same reference numerals in the embodiments may be the same and operate in the same manner. The difference between the integrated system in  FIG.  1 C  and those in  FIGS.  1 A and  1 B  is that the energy source  1 C in  FIG.  1 C  is a solar energy source. Solar energy is generated by the sun. The green energy portion of the integrated system in  FIG.  1 C  may interact with the selective molecular separation unit  9 ,  15 ,  16  in the same manner as discussed above with respect to the integrated systems in  FIGS.  1 A and  1 B . In  FIG.  1 C , thermal energy from the solar energy source  1 C may be applied to a primary fluid, such as molten salt, to raise the temperature of the primary fluid. That is, the primary fluid absorbs heat from the solar energy source and becomes a heated primary fluid. The solar energy may be harnessed by using concaved lenses or mirrors to concentrate photons from the sun&#39;s rays into the center of a lens or mirror to melt salt. The concentration of photons generates thermal energy that is applied to the primary fluid. The heated primary fluid transfers its thermal energy (heat) to the working fluid  12  in the heat exchanger  2 . In an alternative embodiment, the thermal energy from the solar energy source  1 C may be applied directly to the working fluid  12  (i.e., without the primary fluid). That is, the working fluid  12  can absorb the solar thermal energy directly from sun. 
       FIG.  1 D  illustrates a further embodiment of an integrated green energy and selective molecular separation system that uses wind energy as the source of green energy. The integrated system of  FIG.  1 D  includes sonic of the component parts of the systems discussed above with respect to  FIGS.  1 A to  1 C , and the component parts identified with the same reference numerals in  FIGS.  1 A to  1 D  may be the same and operate in the same manner. Instead of a thermal energy source as in  FIGS.  1 A to  1 C , the energy source in  FIG.  1 D  is kinetic energy of an inlet fluid  1 D, such as wind, from the surrounding environment. That is, the energy is generated by the wind. As discussed above, the surrounding environment may be the atmosphere of the earth, such that the inlet fluid  1 D is air. The inlet fluid  1 D may be polluted with greenhouse gas (carbon dioxide (CO 2 )), carbon monoxide (CO), nitrogen oxides (NO X ), hydrogen sulfide (H 2 S), and/or other gases as discussed above. The integrated system in  FIG.  1 D  includes a windmill  23  that is driven by the inlet fluid  1 D (e.g., wind). The windmill  23  may include blades that are turned by movement of the inlet fluid  1 D. The windmill  23  may be mechanically connected to the rotor of an electricity generator  6  so that rotation of the windmill  23  rotates the rotor of the electricity generator  6  to generate electricity  7  via electromagnetic induction as discussed above. The electricity  7  produced can be extracted from the electricity generator  6 , and may be sent to an electrical grid for commercial distribution and. use, as discussed above. 
     The inlet fluid  13  that turns the windmill  23  to drive the electricity generator  6  also enters the selective molecular separation unit  15 . The selective molecular separation unit  15  may be the same as the selective molecular separation unit  15  in the embodiments of  FIGS.  1 A to  1 C  except that the selective molecular separation unit  15  in  FIG.  1 D  may not include the condenser/heat exchanger  9 . In all other respects, the selective molecular separation unit  15  of  FIG.  1 D  may operate as the selective molecular separation unit  15  in the embodiments of  FIGS.  1 A to  1 C  unless indicated otherwise below. In the integrated system of  FIG.  1 D , the inlet fluid  13  may pass through the molecular sieve membrane(s)  19 , the selective catalytic reducer (SCR)  20 , the catalytic converting unit (DOC)  21 , and for the carbon monoxide (CO) reduction unit  22  for initial separation and capture of predetermined molecules (e.g., greenhouse gases), as discussed above, before entering the separation portion  15 . Movement of the inlet fluid  13  may be assisted via the fan  18 , a vacuum or other similar device through the separation portion  15 . The inlet fluid  13  containing any remaining greenhouse gas (e.g., carbon dioxide (CO 2 ), carbon monoxide (CO), nitrogen oxides (NO X )) may then enter the separation portion  15  and undergo further separation via the sorption process and/or the molecular sieve membrane(s) discussed above. The desorption process in the desorption unit  16  in the embodiment of  FIG.  1 D  uses heat from the electrical heater powered by the electricity  7  from the electricity generator  6  in the manner discussed above. 
       FIG.  1 E  is a schematic illustration of another integrated green energy and selective molecular separation system that uses wind energy as the source of green energy. The integrated system of  FIG.  1 E  may be the same as the system of  FIG.  1 D , but excludes the fan  18 . The remaining component parts identified with the same reference numerals in  FIGS.  1 D and  1 E  may be the same and operate in the same manner. 
       FIG.  2 A  is an illustration of a Rankine Cycle that is implemented by an integrated green energy and selective molecular separation system, according to an embodiment.  FIG.  2 A  illustrates the relationship between pressure and enthalpy a Rankine Cycle, and includes four points or “states” (“A” through “D”) along the cycle. State “A” corresponds to a beginning point in the cycle at which the working fluid has particular pressure, temperature, enthalpy, and may be in a liquid state. The cycle proceeds to state “B” by introducing the working fluid into the heat exchanger  2 , at which the temperature and enthalpy increase, and the heated working fluid may be changed from a liquid state to a gas/vapor state. The cycle next proceeds to state “C”, corresponding to the heated working fluid from the heat exchanger  2  driving the turbine  5  with the state “B” characteristics. At step “C”, after the heated working fluid exits the turbine  5 , the pressure, temperature and enthalpy of the working fluid may be decreased. The cycle then proceeds to state “D” corresponding to the working fluid passing through the condenser  9  of the selective molecular separation unit  9 ,  15 ,  16  with the state “C” characteristics. The condenser  9  may decrease the enthalpy of the working fluid, and change the state of the working fluid at least mostly back to a liquid state. The cycle finally returns to state “A”, corresponding to the working fluid passing through the compressor  11 , which elevates the pressure of the working fluid and may change to the state of the working fluid to a complete liquid state. In the Rankine Cycle, the ideal net energy equals zero according to the conservation of energy law. 
       FIG.  2 B  is another illustration of a Rankine Cycle that is implemented by an integrated green energy and selective molecular separation system, according to an embodiment.  FIG.  2 B  illustrates the relationship between pressure and entropy in a Rankine Cycle, and includes four points or “states” (“A” through “D”) along the cycle. State “A” corresponds to a beginning point in the cycle at which the working fluid has particular pressure, temperature, entropy, and may be in a liquid state. The cycle proceeds to state “B” by introducing the working fluid into the heat exchanger  2 , at which the temperature and entropy may increase, and the heated working fluid may be changed from a liquid state to a gas vapor state. The cycle next proceeds to state “C”, corresponding to the heated working fluid from the heat exchanger  2  driving the turbine  5  with the state “B” characteristics. At step “C”, after the heated working fluid exits the turbine  5 , the pressure, temperature of the working fluid may be decreased. The cycle then proceeds to state “D” corresponding to the working fluid passing through the condenser  9  of the selective molecular separation unit  9 ,  15 ,  16  with the state “C” characteristics. The condenser  9  may decrease the entropy of the working fluid, and change the state of the working fluid at least mostly back to a liquid state. The cycle finally returns to state “A”, corresponding to the working fluid passing through the compressor  11 , which elevates the pressure of the working fluid and may change to the state of the working fluid to a complete liquid state. 
       FIG.  2 C  illustrates a graph of a Rankine Cycle in which water is the working fluid according to an embodiment. In the embodiment, the steam has a temperature of 300 degrees Celsius, and the thermal energy source is a flame or flare having a temperature of about 700 to 1,400 degrees Celsius. The working fluid is heated by a flame or flare in a heat exchanger to have a temperature of 300 degrees Celsius. The following table illustrates the electrical energy that can be produced along with the number of people able to receive the electricity according to different flows rates of the working fluid, according to the inventor&#39;s calculation. 
     
       
         
           
               
             
               
                 TABLE 2 
               
             
            
               
                   
               
               
                 Electrical Output Based on Working Fluid Flow Rate 
               
            
           
           
               
               
               
            
               
                   
                 Electrical Energy 
                 Number of Persons 
               
               
                 Working Fluid Flow Rate 
                 (Mega Watt 
                 Receiving Electricity 
               
               
                 (Gallons per Minute-GPM) 
                 Hour-MWH) 
                 in the U.S.A. 
               
               
                   
               
            
           
           
               
               
               
            
               
                 5 
                 0.118 
                 88 
               
               
                 10 
                 0.236 
                 175 
               
               
                 50 
                 1.181 
                 874 
               
               
                 100 
                 2.362 
                 1747 
               
               
                 200 
                 4.706 
                 3481 
               
               
                   
               
            
           
         
       
     
       FIG.  2 D  is illustrates a specific example of a Rankine Cycle that is implemented by an integrated green energy and selective molecular separation system, according to an embodiment. In the embodiment, water is used as the working fluid. At state “A” the heated working fluid is under a pressure (P) of 150 psi, has a (T) temperature of 25 degrees Celsius, has an enthalpy (H) of 105.88 kj/kg, has an entropy of 0.3669 kj/kgK, and is in a 100 percent liquid state. In the heat exchanger  2 , the temperature is raised to 300 degrees Celsius, the enthalpy (H) is raised to 3,048 kj/kg, the entropy is raised to 7.0612 kj/kgK, and the state of the heated working fluid is changed to gas/vapor state (e.g., 100 percent steam). The heated working fluid enters a turbine  5  in this state (state “B”) to drive the turbine  5  and perform work at 372.4 kj/kg. The work drives an electricity generator  6  to generate electricity via electromagnetic induction to produce electricity in the amount of 0.1034 kwh/kg, i.e., 0.906 mw/kg per year. After passing through the turbine  5 , the pressure of the working fluid is decreased to 14.7 psi, the temperature is decreased to 100 degrees Celsius, the enthalpy is decreased to 2,675.6 kj/kg, the entropy is raised to 7.3544 kj/kgK, and the working fluid is maintained in the gas/vapor state (e.g., 100 percent steam) as indicated in “C”. The working fluid may then pass through the condenser  9  of the selective molecular separation unit  9 ,  15   16 . The condenser  9  decreases the temperature of the working fluid to 25 degrees Celsius, the enthalpy of the working fluid to 104.92 kj/kg, and decreases the entropy of the working fluid to 0.367.2 kj/kgK (see step “D”). The working fluid may then pass through the compressor  11 , which elevates the pressure of the working fluid to 150 psi and may change to the state of the working fluid to a complete liquid state, when returning to step “A” to repeat the cycle. Fluids other than water may yield different results (e.g., pressures, temperatures, enthalpy and entropy) than water in Rankine Cycles, and are encompassed within the scope of the present disclosure. 
       FIG.  2 E  is an illustration of a Carnot Cycle that can be implemented by an integrated green energy and selective molecular separation system, according to an embodiment.  FIG.  2 E  illustrates the relationship between pressure and volume of the working fluid in a Carnot Cycle, and maps generally how the pressure and volume of the working fluid change from the compressor  11  to the heat exchanger  2 , from the heat exchanger  2  to the turbine/generator  4 / 5 , from the turbine/generator  4 / 5  to the condenser  9 , and from the condenser  9  to the compressor  11 . 
       FIG.  2 F  is another illustration of a Carnot Cycle that can be implemented by an integrated green energy and selective molecular separation system, according to an embodiment.  FIG.  2 F  illustrates the relationship between temperature and entropy of the working fluid in a Carnot Cycle, and maps generally how the temperature and entropy of the working fluid change from the compressor  11  to the heat exchanger  2 , from the heat exchanger  2  to the turbine/generator  4 / 5 , from the turbine/generator  4 / 5  to the condenser  9 , and from the condenser  9  to the compressor  11 . 
     The green energy portion of the integrated systems discussed herein may implement one or more of the thermodynamic cycles shown in Table 3. Table 3 shows the type of Compression, Heat Addition, Expansion and Heat Rejection of each thermodynamic cycle, along with the corresponding steps shown in  FIGS.  2 A,  2 B and  2 D to  2 F . For instance, in the Rankine Cycle the heat exchanger  2  implements an isobaric heat addition (Steps A→B). The turbine  5  implements an adiabatic expansion (Steps B→C). The condenser  9  implements an isobaric heat rejection (Steps C→D). The compressor  11  implements an adiabatic compression (Steps D→A). That is, for the Rankine Cycle: Heat Exchanger (Isobaric)→Turbine (Adiabatic)→Condenser (Isobaric)→Compressor (Adiabatic). In the Carnot Cycle the heat exchanger  2  implements an isothermal heat addition (Steps A→B). The turbine  5  implements an isentropic expansion (Steps B→C). The condenser  9  implements an isothermal heat rejection Steps (C→D). The compressor  11  implements an isentropic compression (Steps D→A). That is, for the Carnot Cycle: Heat Exchanger (Isothermal)→Turbine (Isentropic)→Condenser (Isothermal)→Compressor (Isentropic). 
     
       
         
           
               
             
               
                 TABLE 3 
               
             
            
               
                   
               
               
                 Thermodynamic Cycles Implemented by the Integrated Green 
               
               
                 Energy and Selective Molecular Separation Systems 
               
            
           
           
               
               
               
               
               
            
               
                   
                 Compression 
                 Heat Addition 
                 Expansion 
                 Heat Rejection 
               
               
                 Cycle 
                 Steps D → A 
                 Steps A → B 
                 Steps B → C 
                 Steps C → D 
               
               
                   
               
               
                 Bell Coleman 
                 adiabatic 
                 isobaric 
                 adiabatic 
                 isobaric 
               
               
                 Carnot 
                 isentropic 
                 isothermal 
                 isentropic 
                 isothermal 
               
               
                 Ericsson 
                 isothermal 
                 isobaric 
                 isothermal 
                 isobaric 
               
               
                 Rankine 
                 adiabatic 
                 isobaric 
                 adiabatic 
                 isobaric 
               
               
                 Hygroscopic 
                 adiabatic 
                 isobaric 
                 adiabatic 
                 isobaric 
               
               
                 Scuderi 
                 adiabatic 
                 Variable pressure 
                 adiabatic 
                 isochoric 
               
               
                   
                   
                 and volume 
               
               
                 Stirling 
                 isothermal 
                 isochoric 
                 isothermal 
                 isochoric 
               
               
                 Manson 
                 isothermal 
                 isochoric 
                 isothermal 
                 Isochoric, then 
               
               
                   
                   
                   
                   
                 adiabatic 
               
               
                 Stoddard 
                 adiabatic 
                 isobaric 
                 adiabatic 
                 isobaric 
               
               
                 Atkinson 
                 isentropic 
                 isochoric 
                 isentropic 
                 isochoric 
               
               
                 Brayton 
                 adiabatic 
                 isobaric 
                 adiabatic 
                 isobaric 
               
               
                 Diesel 
                 adiabatic 
                 isobaric 
                 adiabatic 
                 isochoric 
               
               
                 Humphrey 
                 isentropic 
                 isochoric 
                 isentropic 
                 isobaric 
               
               
                 Lenoir 
                   
                 isochoric 
                 adiabatic 
                 isobaric 
               
               
                 Otto 
                 isentropic 
                 isochoric 
                 isentropic 
                 isochoric 
               
               
                   
               
            
           
         
       
     
     The following explanation for each process in Table 3 may be helpful. Adiabatic: No energy transfer as heat (Q) during that part of the cycle (Q=constant, δQ=0). Isothermal: The process is at a constant temperature during that part of the cycle (T=constant, δT=0). Isobaric: Pressure in that part of the cycle will remain constant (P=constant, δP=0). Isochoric: The process is constant volume (V=constant, δV=0). Isentropic: The process is one of constant entropy (S=constant, δS=0). Isenthalpic: process that proceeds without any change in enthalpy or specific enthalpy (H=constant, δH=0). 
       FIG.  3 A  is a schematic illustration of another type integrated green energy and selective molecular separation system (“Green Energy Blue”). The integrated system of  FIG.  3 A  includes some of the component parts of the systems discussed above with respect to  FIGS.  1 A to  1 D , and the component parts identified with the same reference numerals in the figures may be the same and operate in the same manner unless indicated otherwise below. In the integrated system of  FIG.  3 A , the energy source is an inlet fluid  25 A that possesses relatively high kinetic energy. The inlet fluid  25 A may be a gas or a liquid. In an embodiment, the inlet fluid  25 A may include wind containing polluted air from the surrounding environment; and/or exhaust flue gas from a flame, a flare and/or an engine. In any of these cases, the inlet fluid  25 A may contain predetermined molecules of greenhouse gas (carbon dioxide (CO 2 )), carbon monoxide (CO), nitrogen oxides (NO X ), hydrogen sulfide (H 2 S), and/or other gases as discussed above. The kinetic energy of the inlet fluid  25 A exerts a force on a series of blades mounted on a shaft of the turbine  5 . The force turns the blades, which rotates the shaft to drive the turbine  5  as discussed above. In some embodiments, the turbine  5  may be a windmill. The shaft of the turbine  5  may be mechanically connected to the rotor of an electricity generator  6  so that rotation of the shaft rotates the rotor of the electricity generator  6  to generate electricity  7  via electromagnetic induction as discussed above. After driving the turbine  5 , the inlet fluid  25 A enters the separation portion  15  of the selective molecular separation unit  15 ,  16 . The predetermined molecules of the greenhouse gases in the inlet fluid  25 A are selectively separated from other molecules of the surrounding environment in the selective molecular separation unit  15  in the manner discussed above (i.e., via a sorption process and/or a molecular sieve membrane). Meanwhile, the electricity  7  produced can be extracted from the electricity generator  6 , and a portion of the electricity  7  may be utilized to power the electrical heater in the desorption unit  16  which provides the heat to perform the desorption process of the separated predetermined molecules in the selective molecular separation unit  15 ,  16 , as discussed above. Another portion of the generated electricity  7  may be sent to an electrical grid for commercial distribution and use, as discussed above. The predetermined molecules captured in the desorption process can be conveyed from the selective molecular separation unit  15 ,  16  for storage  17  in a storage tank (not shown). The other molecules, such as oxygen (O 2 ) and nitrogen (N 2 ), which have been separated from the predetermined molecules of the inlet fluid  25 A may be released from the separation portion  15  to be released as outlet fluid  25 B into the surrounding environment. 
       FIG.  3 B  is a schematic illustration of a first variation of the integrated green energy and selective molecular separation system of  FIG.  3 A . The integrated system of  FIG.  3 B  includes the component parts of the system of  FIG.  3 A , and the component parts identified with the same reference numerals in the figures may be the same and operate in the same manner unless indicated otherwise below. The integrated system of  FIG.  3 B  adds a compressor  11  before the turbine  5 , such that the inlet fluid  25 C (which may be the same as the inlet fluid  25 A in  FIG.  3 A ) is compressed by the compressor  11  before entering the turbine  5 . The compressor  11  may be a pump when the inlet fluid  25 C is a liquid. The compressor  11  increases the pressure of the inlet fluid  25 C, which increases the kinetic energy of the inlet fluid  25 C. The increased kinetic energy of the inlet fluid  25 C drives the turbine  5  with greater force, which in turn drives the electrical generator  6  faster to produce more electricity  7 . Further, the electricity  7  generated by the electrical generator  6  can be used to power the compressor  11 , in addition to the electrical heater in the desorption unit  16 , as shown in  FIG.  3 B . In other embodiments, the compressor may be powered by the rotating shaft of the turbine  5 . After driving the turbine  5 , the inlet fluid  25 C enters the separation portion  15 . The predetermined molecules of the greenhouse gases in the inlet fluid  25 C are selectively separated from other molecules of the surrounding environment in the separation portion  15  in the manner discussed above (i.e., via a sorption process and/or a molecular sieve membrane). Meanwhile, the electricity  7  produced can be extracted from the electricity generator  6 , and a portion of the electricity  7  may be utilized to power the electrical heater which provides the heat to perform the desorption process of the separated predetermined molecules in the desorption unit  16 , as discussed above. Another portion of the generated electricity  7  may be sent to an electrical grid for commercial distribution and use, as discussed above. The predetermined molecules captured in the desorption process can be conveyed from the selective molecular separation unit  15 ,  16  for storage  17  in a storage tank (not shown). The other molecules, such as oxygen (O 2 ) and nitrogen (N 2 ), which have been separated from the predetermined molecules of the inlet fluid  25 C may be released from the separation portion  15  to be released as outlet fluid  25 D into the surrounding environment. 
       FIG.  3 C  is a schematic illustration of an integrated green energy and selective molecular separation system according to another embodiment. The integrated system of  FIG.  3 C  includes the component parts of the system of  FIG.  3 A , and the component parts identified with the same reference numerals in the figures may be the same and operate in the same manner unless indicated otherwise below. The integrated system of  FIG.  3 C  includes the compressor  11  of  FIG.  3 B  and includes a combustor  24  between the compressor  11  and the turbine  5 . In some embodiments, the combustor  24  may be part of an engine or a gas turbine. The inlet fluid  25 E (which may be the same as the inlet fluid  25 A in  FIG.  3 A ) may be compressed by the compressor  11  before entering the combustor  24 . The compressor  11  may be a pump when the inlet fluid  25 C is a liquid. The compressor  11  increases the pressure of the inlet fluid  25 E, which increases the kinetic energy of the inlet fluid  25 E. The combustor  24  may include an ignition source, such as a flame or a spark, and receives the compressed inlet fluid  25 E along with a fuel  27 . The ignition source may ignite the fuel  27  in the combustor  24  to produce a combusted inlet fluid that has a greater thermal and/or kinetic energy than the inlet fluid  25 E. The greater thermal and/or kinetic energy combusted inlet fluid is used to drive the turbine  5  with a greater force than non-combusted inlet fluid. The greater force in turn drives the electrical generator  6  faster to produce more electricity  7 , which can be used to power the compressor  11  and the electrical heater in the desorption unit  16 , while also being sent to an electrical grid for commercial distribution and use, as discussed above. After combustion, the combusted inlet fluid enters the separation portion  15 . The predetermined molecules of the greenhouse gases in the combusted inlet fluid are selectively separated from other molecules of the surrounding environment in the separation portion  15  in the manner discussed above (i.e., via a sorption process and/or a molecular sieve membrane). Meanwhile, the electricity  7  produced can be extracted from the electricity generator  6 , and a portion of the electricity  7  may be utilized to power the electrical heater which provides the heat to perform the desorption process of the separated predetermined molecules in the desorption unit, as discussed above. Another portion of the generated electricity  7  may be sent to an electrical grid for commercial distribution and use, as discussed above. The predetermined molecules captured in the desorption process can be conveyed from the selective molecular separation unit  15 ,  16  for storage  17  in a storage tank (not shown). The other molecules, such as oxygen (O 2 ) and nitrogen (N 2 ), which have been separated from the predetermined molecules of the combusted inlet fluid may be released from the selective molecular separation unit  15  to be released as outlet fluid  25 F into the surrounding environment. 
       FIG.  3 D  is a schematic illustration of a second variation of the integrated green energy and selective molecular separation system of  FIG.  3 A . The integrated system of  FIG.  3 D  includes the component parts of the system of  FIG.  3 A , and the component parts identified with the same reference numerals in the figures may be the same and operate in the same manner unless indicated otherwise below. The integrated system of  FIG.  3 D  additionally includes a heat exchanger  26 , which may be provided between the electricity generator  6  and the selective molecular separation unit  15 . The inlet fluid  25 A turns the blades of the turbine  5  via kinetic energy, which rotates the shaft and drives the electricity generator  6  to generate electricity  7  as discussed above. In some embodiments, the turbine  5  may be a windmill. The inlet fluid  25 A then enters the heat exchanger  26 . The heat exchanger  26  may exchange thermal energy of the inlet fluid  25 A with the sorbent and/or molecular sieve membrane which reduces the temperature of the inlet fluid  25 A. The reduced-temperature (e.g., cooled) inlet fluid  25 A then passes through the separation portion  15  to undergo the sorption process in which the predetermined molecules (e.g., of the greenhouse gases) in the reduced-temperature inlet fluid  25 A are selectively separated from other molecules, as discussed above. The reduced-temperature of the inlet fluid  25 A actually improves the sorption process. The other molecules which are not separated by the sorbent material, and for molecular sieve membrane, such as oxygen (O 2 ) and nitrogen (N 2 ), may be released from the separation portion  15  as outlet fluid  25 B into the surrounding environment. 
     Meanwhile, heat from the exchange of thermal energy in the heat exchanger  26  is used to desorb the sorbent having the separated predetermined molecules from the sorption process. That is, the heat is used to capture the predetermined molecules, such as carbon dioxide (CO 2 ), carbon monoxide (CO), and nitrogen oxides (NO X ) from the sorbent in a desorption process as discussed above. The captured predetermined molecules can be conveyed from the desorption unit  16  for storage  17  in a storage tank (not shown). The electricity  7  produced by the electricity generator  6  may be sent to an electrical grid for commercial distribution and use, as discussed above. 
       FIG.  3 E  is a schematic illustration of a third variation of the integrated green energy and selective molecular separation system of  FIG.  3 A . The integrated system of  FIG.  3 E  is similar to the integrated system of  FIG.  3 D , but relocates the heat exchanger  26  to be provided before the turbine  5 . The remaining component parts identified with the same reference numerals in  FIGS.  3 D and  3 E  may be the same and operate in the same manner as discussed above. 
       FIG.  3 F  is a schematic illustration of a fourth variation of the integrated grant energy and selective molecular separation system of  FIG.  3 A . The integrated system of  FIG.  3 F  is similar to the integrated systems of  FIG.  3 D , and includes the compressor  11  before the turbine  5 . As discussed above, the compressor  11  increases the pressure of the inlet fluid  25 C, which increases the kinetic energy of the inlet fluid  25 C. The increased kinetic energy of the inlet fluid  25 C drives the turbine  5  with greater force, which in turn drives the electrical generator  6  faster to produce more electricity  7 . The remaining component parts identified with the same reference numerals in  FIGS.  3 D and  3 F  may be the same and operate in the same, manner as discussed above. 
       FIG.  3 G  is a schematic illustration of a fifth variation of the integrated green energy and selective molecular separation system of  FIG.  3 A . The integrated system of  FIG.  3 G  is similar to the integrated system of  FIG.  3 F , but relocates the heat exchanger  26  to be provided between the compressor  11  and the turbine  5 . The compressor  11  may increase the pressure of the inlet fluid  25 C before entering the heat exchanger  26 . The remaining component parts identified with the same reference numerals in  FIGS.  3 F and  3 G  may be the same and operate in the same manner as discussed above. 
       FIG.  3 H  is a schematic illustration of a first variation of the integrated green energy and selective molecular separation system of  FIG.  3 C . The integrated system of  FIG.  3 H  is similar to the integrated system of  FIG.  3 F  and includes a combustor  24  between the compressor  11  and the turbine  5 . In some embodiments, the combustor  24  may be part of an engine or a gas turbine. The inlet fluid  25 E (which may be the same as the inlet fluid discussed above) may be compressed by the compressor  11  before entering the combustor  24 . The compressor  11  may be a pump when the inlet fluid  25 C is a liquid. As discussed above, the compressor  11  increases the pressure of the inlet fluid  25 E, which increases the kinetic energy of the inlet fluid  25 E. The combustor  24  may include an ignition source, such as a flame or a spark, and receive the compressed inlet fluid  25 E along with a fuel  27 . The ignition source may ignite the fuel  27  in the combustor  24  to produce a combusted inlet fluid that has a greater thermal and/or kinetic energy than the inlet fluid  25 E. The greater thermal and/or kinetic energy combusted inlet fluid is used to drive the turbine  5  with a greater force than a non-combusted inlet fluid. The greater force in turn drives the electrical generator  6  faster to produce more electricity  7 , as discussed above. In addition, the integrated system of  FIG.  3 H  includes the heat exchanger  26  as in  FIG.  3 F . The remaining component parts identified with the same reference numerals in  FIGS.  3 H and  3 F  may be the same and operate in the same manner as discussed above. 
       FIG.  3 I  is a schematic illustration of a second variation of the integrated green energy and selective molecular separation system of  FIG.  3 C . The integrated system of  FIG.  3 I  is similar to the integrated system of  FIG.  3 H , but relocates the heat exchanger  26  to be provided between the combustor  24  and the turbine  5 . As discussed above, the combustor  24  produces a combusted inlet fluid that has a greater thermal and/or kinetic energy than the inlet fluid  25 E. The greater thermal and/or kinetic energy combusted inlet fluid provides greater thermal energy to the heat exchanger  26 . The greater thermal energy may enhance the desorption process of the separated predetermined molecules in the desorption unit  16  by providing greater heat to capture the predetermined molecules, such as carbon dioxide (CO 2 ), carbon monoxide (CO), and nitrogen oxides (NO X ) from the sorbent and/or molecular sieve membrane as discussed above. The remaining component parts identified with the same reference numerals in  FIGS.  3 H and  3 I  may be the same and operate in the same manner as discussed above. 
     It is noted that the integrated green energy and selective molecular separation systems of  FIGS.  3 C,  3 H and  3 I , which use the combustor  24 , may implement the thermodynamic Brayton Cycle, and may be part of or integrated with an engine or a gas turbine.  FIG.  3 J  illustrates one embodiment of a combustion process that may occur in the integrated systems of  FIGS.  3 C,  3 H and  3 I . In Step  1 , inlet air  25 E is received into the compressor  11 , which increases the pressure of the inlet fluid  25 E. The increased pressure increases the thermal and kinetic energy of the inlet fluid  25 E. In Step  2 , the compressed inlet air  25 E is conveyed to the combustor  24 . A combustible fuel  7  is also fed into the combustor  24 . The combustor  24  may include an ignition source, such as a flame or a spark, which ignites the fuel  27  in the combustor  24  to produce a combusted inlet fluid that has a greater thermal and/or kinetic energy than the inlet fluid  25 E. In Step  3 , the combusted inlet fluid is convoyed turbine  5  to drive the turbine  5  to produce work (e.g., to rotate the shaft of the turbine  5 ). In Step  4 , exhaust gases from the combusted fluid exiting turbine  5  may be directed to the separation portion  15 .  FIG.  3 J  further illustrates two graphs showing that the combustion process follows a standard thermodynamic Brayton Cycle. The first graph plots how the pressure (P) and volume (V) of the inlet fluid  25 E changes in Steps  1  to  4 . The second graph plots how the temperature (T) and entropy (S) of the inlet fluid  25 E changes in Steps  1  to  4 . 
       FIG.  3 K  is an exemplary implementation of an integrated green energy and selective molecular separation system of  FIGS.  3 A,  3 B and  3 C  in a jet engine, according to an embodiment. The jet engine may include several components akin to the green energy portion of the integrated system in  FIG.  3 C . For instance, the jet engine may include a compressor  11 , a combustor  24  and turbine  5 . The inlet fluid  25 E may be polluted atmospheric air from the surrounding environment and/or heat. The heat may be derived from: gas flares resulting from the burning of natural gas associated with oil extraction; exhaust fumes; and combustion. The inlet fluid  25 E may be compressed by the compressor  11  before entering the combustor  24 . The compressor  11  increases the pressure of the inlet fluid  25 E, which increases the kinetic energy of the inlet fluid  25 E. The combustor  24  includes an ignition source, such as a flame or a spark, and receives the compressed inlet fluid  25 E along with a fuel (see  FIG.  3 J ). The ignition source may ignite the fuel in the combustor  24  to produce a combusted inlet fluid that drives the turbine  5 . The jet engine may be equipped with an electricity generator  6  that is driven by the turbine  5  to generate electricity  7 , as discussed above. And, the jet engine may be equipped with a selective molecular separation unit  15  and an electrical heater in a desorption unit  16 . The electricity  7  can be used to power the compressor  11  and the electrical heater, and/or other components of the aircraft having the jet engine. In addition, the electricity  7  may be stored in storage device (not shown) for future use in an electrical and for commercial distribution and use, as discussed above. 
     After exiting the turbine  5 , the inlet fluid enters the selective molecular separation unit  15  to perform a sorption discussed above. The electrical heater in the desorption unit  16  may be used to perform a desorption process discussed above via the electrical heater. After desorption, the captured predetermined molecules (greenhouses gas (carbon dioxide (CO 2 )), carbon monoxide (CO), and nitrogen oxides (NO X )) can be stored  17  in a storage unit (not shown). The other molecules, such as oxygen (O 2 ) and nitrogen (N 2 ), which have been separated from the predetermined molecules of the inlet fluid  25 E may be released from the jet engine as outlet fluid  25 F into the surrounding environment. 
       FIG.  4    is an embodiment of an absorption and a desorption process that may occur in the integrated green energy and selective molecular separation systems discussed above. As discussed above, the absorption process occurs in the separation portion  15  of the selective molecular separation unit  9 ,  15 ,  16 , and the desorption process occurs in the desorption unit  16 . In the absorption process, one or more vessels may contain a liquid absorbent material, such as, for example, ethanol amine, mono ethanol amine (MEA), di ethanol amine (DEA), methyl di ethanol amine (MDEA) and tetra ethylene pent-amine (TEPA). Other liquid absorbent materials not listed here are encompassed within the scope of the present disclosure. An inlet fluid containing the predetermined molecules, such as greenhouse gas, is passed through the liquid absorbent in the vessels in which the predetermined molecules, such as carbon dioxide (CO 2 ), carbon monoxide (CO), and nitrogen oxides (NO X ), of the greenhouse gases are absorbed by the liquid absorbent in a chemical process. Absorption of the predetermined molecules, such as greenhouse gas (carbon dioxide (CO 2 )), carbon monoxide (CO), and nitrogen oxides (NO X ) by the liquid absorbent separates the predetermined molecules from other molecules of the inlet fluid which are not absorbed by the liquid absorbent. The other molecules, such as oxygen (O 2 ) and nitrogen (N 2 ), which have been separated from the predetermined molecules in the inlet fluid and which do not constituted greenhouse gas may exit the vessels to be released as outlet fluid into the surrounding environment, e.g., such as atmospheric air. 
       FIG.  4    further shows that the desorption process uses thermal energy to break a bond between the separated predetermined molecule (e.g., carbon dioxide (CO 2 ), carbon monoxide (CO), and nitrogen oxides (NO X )) and the absorbent material. The thermal energy used in the desorption process comes from the green energy portion of the integrated system, and in  FIG.  4    is used to capture the predetermined molecules contained in the liquid absorbent material. The liquid absorbent material may be desorbed in the same vessel used in the absorption process, or may be transferred to another vessel for the desorption process. As discussed above, when only one vessel is used, the sorption, and desorption processes are implemented in an alternating sequential intervals. That is, the one vessel accommodates the sorption process in one interval without heat in the desorption process, and in the next interval is heated in the desorption process without accommodating the sorption process. The intervals then repeat as a batch process. Alternatively, the one vessel may undergo both the sorption and desorption process at the same time. When two or more vessels or a set of several vessels are used, the vessels may alternate undergoing the absorption and desorption process. That is, one vessel may accommodate the absorption process while the other vessel undergoes the desorption process. After a predetermined amount of time, the one vessel undergoes the desorption process while the other vessel accommodates the absorption process. In this manner, a continuous absorption and desorption process may occur. 
       FIG.  5 A  shows embodiments of several types of solid adsorbent materials that may be used in an adsorption process of an integrated green energy and selective molecular separation system. As discussed above, the solid adsorbent material may be one or more of: Zeolite, Layered double hydroxide (LDH), Silica, Metal-organic framework (MOF), Activated carbon, Activated carbon fibers (ACF), DOF, Alkali-metal-based materials, ordered porous carbon, Graphene, Carbon molecular sieves (CMS), and combinations thereof (see  FIG.  5 A ). 
       FIG.  5 B  illustrates an embodiment of an adsorption process using an adsorbent material that may occur in an integrated green energy and selective molecular separation system. In the embodiment, Zeolite is the adsorbent material and is impregnated with some cations such as Calcium (Ca 2+ ). The Calcium (Ca 2+ ) cations attract carbon dioxide (CO 2 ) molecules of the predetermined greenhouse gas molecules. The attraction of the carbon dioxide (CO 2 ) molecules to the Calcium (Ca 2+ ) molecules causes the carbon dioxide molecules (CO 2 ) to attach to the oxygen atoms of the aluminate (AlO 4 ) and Silicate (SiO 4 ) and thus be captured by the impregnated Zeolite. 
       FIG.  5 C  illustrates another embodiment of an adsorption process using an adsorbent material that may occur in an integrated green energy and selective molecular separation system. In this embodiment, the Zeolite, as the adsorbent material, is impregnated with either Sodium (Na + ) or Zinc (Zn 2+ ) cations. The Sodium (Na + ) or Zinc (Zn 2+ ) cations attract carbon dioxide (CO 2 ) molecules of the predetermined greenhouse gas molecules. The attraction of the carbon dioxide (CO 2 ) molecules to the Sodium (Na + ) or Zinc (Zn 2+ ) cations causes the carbon dioxide molecules (CO 2 ) to attach to the oxygen atoms of the aluminate (AlO 4 ) and Silicate (SiO 4 ) and thus be captured by the impregnated Zeolite. 
       FIG.  5 D  illustrates different types of molecular bonding that may occur in an integrated green energy and selective molecular separation system. The desorption process in the desorption unit  16  uses heat to break the bond, as discussed above. The bonding may be ionic bonding of the predetermined molecules using a cation-anion attraction method, for example Sodium Chloride (NaCl). In another example, the bonding may be covalent bonding of the predetermined molecules using a nuclei-shared electron attraction method, for example Hydrogen (H 2 ). In a further example, the bonding may be a metallic bonding of the predetermined molecules using a cations-delocalized electron attraction method, for example iron (Fe). Intermolecular (non-bonding) methods as shown in  FIG.  5 D  may also be used and are encompassed within the scope of the present disclosure. 
       FIG.  6    illustrates an embodiment of an adsorption process using a solid adsorbent material that may occur in the selective molecular separation unit  15 , and illustrates an embodiment of a desorption process of the solid adsorbent material using the heater of the desorption  16  discussed above. While the illustrated example shows that a solid adsorbent material is used in the processes, a molecular membrane(s) with the sorbent materials discussed above impregnated or grafted in the molecular membrane(s) may also be used or used in combination with the solid adsorbent material. In such a case, the impregnated or grafted in the molecular membrane(s) can be also subjected to a desorption process. In the embodiment of  FIG.  6   , ambient air as the inlet fluid may enter a container that includes the solid adsorbent material therein. In the embodiment, the solid adsorbent material may have a planar structure. While only one solid adsorbent material is illustrated in the figure, the container may have multiple solid adsorbent materials provided in series along a flow path of the ambient air. The ambient air may contain predetermined molecules, such as greenhouse gas (carbon dioxide (CO 2 )), carbon monoxide (CO) and nitrogen oxide (NO X ) molecules. For simplicity,  FIG.  6    only shows the carbon dioxide (CO 2 ) molecules in the ambient air. As the ambient air in the container passes through the solid adsorbent material, predetermined molecules such as carbon dioxide (CO 2 ) are adsorbed and chemically bonded to the surface of the solid adsorbent material, while other molecules, such as oxygen (O 2 ) and nitrogen (N 2 ) pass through the solid adsorbent material. The solid adsorbent material thus physically and/or chemically separates the predetermined molecules of greenhouse gases (e.g., carbon dioxide (CO 2 )) from the other molecules of the surrounding environment. 
     Once the solid adsorbent material is saturated with the predetermined molecules such as greenhouse gas, the solid adsorbent material may be heated to, e.g., approximately 100 degrees Celsius in a desorption process to capture the predetermined molecules (e.g., greenhouse gas) from the solid adsorbent material, and regenerate or recycle the solid adsorbent material. As discussed above the desorption process uses thermal energy (e.g., heat) to break a bond between the separated predetermined molecule (e.g., carbon dioxide (CO 2 ), carbon monoxide (CO), and nitrogen oxides (NO X )) and the solid adsorbent material. As discussed above, the thermal energy used in the desorption process comes from the green energy portion of the integrated systems discussed herein. The predetermined molecules captured from the adsorbent material can be collected and conveyed to a storage container as shown in  FIG.  6    for further usage. 
       FIG.  7    illustrates an example of a sorption process in which one or more liquid absorbents are passed through one or more solid adsorbent materials that may occur in an integrated green energy and selective molecular separation system. In the embodiment, the sorption process uses a combination of liquid absorbents and solid adsorbent materials to separate the predetermined molecules, such as greenhouse gas (carbon dioxide (CO 2 )), carbon monoxide (CO), hydrogen sulfide (H 2 S), and nitrogen oxides (NO X ), from the inlet fluid. The liquid absorbent material may be, for example, ethanol amine, mono ethanol amine (MEA), di ethanol ammo (DEA), methyl di ethanol amine (MDEA) and tetra ethylene pent-amine (TEPA), as discussed above. Other liquid absorbent materials not listed here are encompassed within the scope of the present disclosure. The liquid absorbent material, indicated in  FIG.  7    with drops of liquid, is passed through a solid adsorbent material. The solid adsorbent material may include molecular membranes such as discussed above, and/or adsorbents such as Zeolite, Layered double hydroxide (LDH), Silica, Metal-organic framework (MOF), Activated carbon, Activated carbon fibers (ACF), DOF, Alkali-metal-based materials, ordered porous carbon, Graphene, Carbon molecular sieves (CMS), and/or combinations thereof (see  FIG.  5 A ). Other solid adsorbent materials not listed here are encompassed within the scope of the present disclosure. 
     When the inlet fluid containing the predetermined molecules, such as greenhouse gas (carbon dioxide (CO 2 )), carbon monoxide CO), hydrogen sulfide (H 2 S), and nitrogen oxides (NO X ), discussed herein passes through the solid adsorbent material, the predetermined molecules are adsorbed by the solid adsorbent material and absorbed by the liquid absorbent material. That is, the predetermined molecules are separated from other molecules of the inlet fluid by both an adsorption and an absorption process. The inlet fluid passes through the combined absorbent/adsorbent material as outlet fluid that is free of the predetermined molecules, such as greenhouse gas (carbon dioxide (CO 2 )), carbon monoxide (CO), hydrogen sulfide (H 2 S), and nitrogen oxides (NO X ). The separated predetermined molecules (e.g., carbon dioxide (CO 2 ), carbon monoxide (CO), hydrogen sulfide (H 2 S), and nitrogen oxides (NO X )) can then undergo a desorption process as discussed herein. 
       FIG.  8    illustrates embodiments of a separation process using a molecular sieve membrane  19  that may occur in an integrated green energy and selective molecular separation system. The molecular membranes  19  shown in  FIG.  8    may be used to separate predetermined molecules from inlet fluid (e.g. flue gas or feed gas). In either case, the molecular sieve membranes  19  filter the gas to physically separate larger molecules from smaller molecules. For example, the membrane(s)  19  may physically separate larger oxygen (O 2 ) and nitrogen (N 2 ) molecules from the smaller carbon dioxide (CO 2 ) molecule. The membrane(s)  19  may have microscopic apertures that are sized to allow only the selected carbon dioxide (CO 2 ) molecules, carbon monoxide (CO) molecules, hydrogen sulfide (H 2 S), and nitrogen oxide (NO X ) molecules to pass through, while the other inlet fluid molecules  13 , such as oxygen (O 2 ) and nitrogen (N 2 ) molecules, are deflected and subsequently be directed to, e.g., an outlet of the selective molecular separation unit  9 ,  15 ,  16  as outlet fluid  14 , and released back into the atmosphere (surrounding environment). In the integrated green energy and selective molecular separation systems discussed above, the smaller carbon dioxide (CO 2 ) molecules may then pass through one or more additional molecular sieve membranes  19  for further separation from larger oxygen (O 2 ) and nitrogen (N 2 ) molecules. In order to enhance the separation (filtration) process, one of the sorbent materials discussed above may be impregnated or grafted in the molecular sieve membrane(s). 
       FIG.  9 A  illustrates an embodiment of a mixing water (H 2 O) molecules with carbon monoxide (CO) molecules in an integrated green energy and selective molecular separation system, according to an embodiment. This process may be implemented by the carbon monoxide (CO) reduction unit  22 . As discussed above, water (H 2 O) molecules may be added to carbon monoxide (CO) molecules to produce chemically carbon dioxide (CO 2 ) molecules and hydrogen (H 2 ) molecules. The mixture may then pass through a molecular sieve membrane to separate hydrogen (H 2 ) molecules and carbon dioxide (CO 2 ) molecules. The water (H 2 O) molecules may be fed from a source outside the carbon monoxide (CO) reduction unit  22  or may be derived from another component of the selective molecular separation unit  9 ,  15 ,  16 , such as the selective catalytic reducer (SCR)  20 . The hydrogen (H 2 ) molecules can be separated from the carbon dioxide (CO 2 ) molecules via a molecular sieve membrane and pass the carbon dioxide (CO 2 ) through the selective molecular separation unit  9 ,  15 ,  16 . The carbon dioxide (CO 2 ) molecules can be conveyed from the desorption unit  16  of the selective molecular separation unit  9 ,  15 ,  16  for storage  17  in a storage tank (not shown) as discussed above. 
       FIG.  9 B  illustrates an embodiment of the catalytic converting unit (DOC)  21  that may be implemented in an integrated green energy and selective molecular separation system. As discussed above, the catalytic converting unit (DOC)  21  may contain palladium and/or platinum, and/or rhodium. This unit converts particulate matter (PM), hydrocarbons (i.e., unburnt and partially burned fuel), and carbon monoxide (CO) to carbon dioxide (CO 2 ) and water (H 2 O). The catalytic converting unit (DOC)  21  can therefore be used to reduce hydrocarbon and carbon monoxide from the surrounding environment. The oxidation of carbon monoxide to carbon dioxide may occur as follows: 2 CO+O 2 →2 CO 2 . The oxidation of hydrocarbons to carbon dioxide and water may occur as follows: C x H 2x+2 +[(3x+1)/2] O 2 →x CO 2 +(x+1) H 2 O. 
     The foregoing integrated systems may be utilized in processes of generating electricity and selectively separating and capturing predetermined molecules present in a surrounding environment. The processes may include providing a kinetic energy working fluid derived from an energy source to drive a turbine  5  by rotating a shaft of the turbine  5  as discussed herein. An electricity generator  6  may be driven via rotation of the shaft of the turbine  5  to generate electricity  7  by electromagnetic induction as discussed herein. In the processes, at least one of (i) the kinetic energy fluid exiting the turbine  5  and (ii) electricity  7  generated by the generator  6  may be supplied to a selective molecular separation unit  9 ,  15 ,  16  as discussed herein. The processes further include intaking the predetermined molecules into the separation portion  15  of the selective molecular separation unit  9 ,  15 ,  16  and selectively separating at least one predetermined molecule from other molecules of the surrounding environment as discussed herein; and then capturing the at least one predetermined molecule via a desorption process of the at least one predetermined molecule in the desorption unit  16  of the selective molecular separation unit  9 ,  15 ,  16  using heat from thermal energy of at least one of (i) the kinetic energy fluid and (ii) an electrical heater powered by the electricity  7  generated by the generator  6  as discussed herein. 
     In the processes, at least one predetermined molecule is selectively separated via at least one of a sorption process and a molecular sieve membrane in the separation portion  15  of the selective molecular separation unit  9 ,  15 ,  16  as discussed herein. The desorption process in the desorption unit  16  regenerates at least one of a sorbent material used in the sorption process and the molecular sieve membrane as discussed herein. In the desorption process, the thermal energy is sufficient to break a bond between the separated predetermined molecule and at least one of the sorbent material and the molecular sieve membrane to regenerate the at least one of the sorbent material and the molecular sieve membrane for a next cycle of selective separation of another predetermined molecule of the surrounding environment as discussed herein. The sorption process in the separation portion  15  may utilize at least one of an absorption process and adsorption process as discussed herein. In addition the sorbent material may be impregnated or grafted in the molecular sieve membrane as discussed herein. The processes may also include storing  17  the at least one predetermined molecule in a storage unit after capturing the at least one predetermined molecule in the desorption process, as discussed herein. In the processes, the turbine  5  may be a windmill. As discussed herein, the energy source used in the processes may be at least one of: a combustion process which produces the kinetic energy fluid; a burning process which produces the kinetic energy fluid; and the surrounding environment including wind which produces the kinetic energy fluid. The combustion process may occur in one of an engine and a gas turbine as discussed herein. The burning process may occur in one of a flare, a water heater and a furnace as discussed herein. 
     Furthermore, in the processes of generating electricity and selectively separating and capturing predetermined molecules present in a surrounding environment, the heat may be generated via at least one of: (i) one or more of: a Rankine Cycle; a Carnot Cycle; a Brayton Cycle; a Diesel Engine Cycle, an Otto Cycle; an Ericsson Cycle; a Hygroscopic Cycle; a Scuderi Cycle; a Stirling Cycle; a Manson Cycle; a Stoddard Cycle; an Atkinson Cycle; a Humphrey Cycle; a Bell Coleman Cycle and a Lenoir Cycle; and (ii) the electrical heater powered by the generator in combination with the one or more Cycles in (i), as discussed herein. 
     It is within the scope of the present disclosure that the processes of generating electricity and selectively separating and capturing predetermined molecules present in a surrounding environment may implement any combinations of the components of the systems as discussed herein, and include operation of the systems discussed herein and any combinations of the components of the systems as discussed herein. 
     The present disclosure integrates an energy generation system/process with a greenhouse gas capturing system/process, which have conventionally been two separate and discrete systems/processes. The present disclosure provides an improvement over known systems and processes for generating green energy, and over known systems and processes for capturing greenhouse gases, because the present disclosure integrates different types of energy systems, such as thermal, solar, wind, combustion, and kinetic energy systems, with a selective molecular separation (e.g., greenhouse, gas capturing) system (“Green Energy Blue”). An important aspect of the integration is the utilization of the output (e.g., thermal energy) of the energy generating portion of the system in the selective molecular separation portion of the system, and the utilization of the output (e.g., a reduced temperature working fluid) of the selective molecular separation portion the energy generating portion. Each portion of the system utilizes the other to form one unitary system that produces green energy (i.e., electricity) while also separating and capturing predetermined molecules (e.g., greenhouse gas) from the surrounding environment. Moreover, the integrated green energy and selective molecular separation systems and processes discussed herein can generate electricity while removing greenhouse gas (carbon dioxide (CO 2 ) from the air with zero emissions. That is, the systems and processes discussed herein can generate electricity from any energy source (such as thermal, solar, wind, combustion, and kinetic energy) with zero emissions while at the same time capturing greenhouse gas (carbon dioxide (CO 2 ) in an integrated manner. 
     The present disclosure is thus an integrated solution to both reducing the production of fossil fuels and global warming (“Green Energy Blue”). Generating energy from the energy sources discussed above and incorporating such with a selective molecular separation unit (e.g., greenhouse gas capturing unit) can help preserve the Earth&#39;s atmosphere and provide a sustainable living environment for the foreseeable future. 
     It should be understood that the foregoing description provides embodiments of the present invention which can be varied and combined without departing from the spirit of this disclosure. Although several embodiments have been illustrated in the accompanying drawings and describe in the foregoing specification, it will be understood by those of skill in the art that additional embodiments, modifications and alterations may be constructed from the principles disclosed herein. Those skilled in the art should, in light of the present disclosure, appreciate that many changes can be made in the specific embodiments which are disclosed and still obtain a like or similar result without departing from the concept, spirit and scope of the present disclosure.