WO2008115662A2 - Carbon dioxide sequestering fuel synthesis system and use thereof - Google Patents

Abstract

A carbon dioxide sequestering, fuel synthesis system comprises an electrolyzer to electrolyze saltwater for producing hydrogen and metal hydroxide. The hydroxide solution obtained by the electrolysis is passed to an osmotic exchanger, for flow within channels defined by gas permeable walls of the osmotic exchanger. External surfaces of the permeable walls are exposed to atmosphere fluid flow, wherein carbon dioxide of the atmosphere permeates the permeable walls for sequestering via reaction with the metal hydroxide.

Description

CARBON DIOXIDE SEQUESTERING FUEL SYNTHESIS SYSTEM

AND USE THEREOF

RELATED DATA

[0001] This non-provisional application claims priority and benefit of United States Provisional Application Ser. No. 60/903,439 filed February 25, 2007, which is hereby incorporated by reference in its entirety.

TECHNOLOGICAL FIELD

[0002] The present disclosure relates to fuel synthesis systems and more particularly to carbon dioxide sequestering fuel synthesis systems and related alternative fuel, power conversion and propulsion systems.

BACKGROUND

[0003] Fossil fuels may be perceived by certain members of the community as generally available today in large quantities and with high energy density. Accordingly, the coal- based and diesel and/or gasoline types of fossil fuels are commonly used in engine and energy conversion applications. More recently, however, its long term viability is coming under greater scrutiny; given that these fossil fuels may appear to be of diminishing supply within deposits of limited geographic extent. Accordingly, a portion of the industry is becoming more active in exploring alternative fuels, their synthesis and energy conversion systems.

[0004] A negative trait commonly attributed to consumption of hydrocarbon-based fuels has been the emission of carbon dioxide. Coupled to this concern, portions of the industry subscribe to theories of "Global Warming" and are now looking actively to avenues that may ease concerns of carbon dioxide emissions.

[0005] In the case of hydrogen systems, hydrogen may be used as an alternative fuel to drive hydrogen engines and/or to fuel fuel-cell energy conversion systems. However, some artisans of this industry suggest that neither it's compressed gaseous nor liquefied form may be sufficiently economical or practical for lending feasibility as a stand-alone alternative fuel solution. [0006] Relative to bio-diesel types of alternative fuels for spark ignition engines, the fuel may be recognized as a form of vegetable oil treated with ethanol or methanol. While offering an alternative to the limited sources of the more customary fossil fuel derivatives, the bio-diesel type of alternative fuel may be recognized as being dependent upon the available surplus of agricultural product, and would compete with demands for food production.

[0007] Ammonia (NH₃) represents another type of alternative fuel, which is nitrogen- based as opposed to being carbon based. When used for powering combustion systems, the ammonia exhibits a low flame propagation velocity relative to that of the more conventional hydrocarbon based fuels, and therefore requires certain design consideration. Further, the ammonia as a stand-alone fuel delivery system may be recognized to poise certain safety risks.

[0008] Anhydrous ammonia is a toxic substance. As a gas, ammonia can present a danger to health with a threshold level of 500 parts per million by volume in ambient air. To store a quantity of ammonia equivalent to fueling an automobile or a truck with an equivalent of 60 gallons of gasoline may require about 342 kg of ammonia. If an accidental rupture were to occur, a toxic clod of the ammonia could develop over a volume of atmosphere as great as 1,000,000 cubic meters.

[0009] Also nitrogen based, urea is also received some attention as an alternative fuel. It is known to be relatively safe, at least relative to the ammonia delivery models. When consumed as a fuel, the urea may be hydrolyzed with water to release ammonia and water (for example, on demand at the energy conversion system) as represented by equation (1) as follows:

CO(NH₂)₂ + H₂O → 2NH₃ + CO₂ (1)

[0010] Guanidine too offers another type of nitrogen-based alternative fuel. The inventors of the present application in a former international application No. WO2005/108289 published November 17, 2005 (from International Appl. Ser. No. PCT/US2005/015920, filed May 3, 2005) teach of guanidine as an alternative fuel that may ease some of the concerns with emissions of greenhouse gases. Additionally, while the conventional fuels are known to pose certain carcinogenic risks that often required expensive procedures for clean-up of spills; guanidine, on the other hand, may be characterized in liking with a fertilizer, wherein accidental spills may be handled with greater ease.

[0011] The present disclosure, according, proposed novel technologies for fuel synthesis and energy conversion systems and associated methods.

SUMMARY

[0012] According to an embodiment of the invention, a carbon dioxide fuel synthesis system comprises an electrolyzer to electrolyze saltwater or brine for producing hydrogen and metal hydroxide. In a further embodiment, the electrolyzer also produces HCl. An osmotic exchanger may receive the metal hydroxide solution from the hydrolyzer for flow within channels defined by permeable walls of the osmotic exchanger. The osmotic exchanger is operatively disposed to expose the external surfaces of the permeable walls to an atmospheric fluid flow, for sequestering carbon dioxide of the atmosphere.

[0013] In a further embodiment, a discharge housing may receive discharge solution from the osmotic exchanger. The discharge housing may be operatively configured to dehydrate the discharged solution to yield carbonate/bicarbonate product for subsequent handling external the system - e.g., as a soda byproduct.

[0014] In a further embodiment, the system may comprise an osmotic controller that controls at least one of (i) the flow of the ambient atmosphere fluid flow to the external walls of the osmotic exchanger, (ii) the ratio of metal hydroxide to water supplied to the osmotic exchanger, or (iii) the rate of discharge of the solution from the osmotic exchanger; based upon at least one of a concentration of the metal carbonate/bicarbonate in the solution for discharge.

[0015] In a further embodiment, the permeable walls of the gas-to-solution transfer network of the osmotic exchanger may be supported by walls of a tower to a wind turbine.

[0016] In a further embodiment, the permeable walls to the osmotic exchanger may be defined at least in part by micro, mesa or macro-porous membrane. In a particular example, the membrane material may comprise a hydrophobic GORE-TEX ® micro- porous material.

[0017] In accordance with another embodiment, a method of sequestering carbon dioxide in fuel synthesis includes producing hydrogen by electrolysis of saltwater or brine. Metal hydroxide resulting from the electrolysis is then exposed to an atmospheric flow via an osmotic exchange network for sequestering carbon dioxide. In a particular example, the metal hydroxide solution flows within an osmotic conduit of the exchange network that is defined at least in part by walls of gas permeable material. The external surfaces of the gas permeable material are exposed to an atmospheric gaseous fluid flow, wherein carbon dioxide of the atmosphere may pass through the walls of the permeable material for reaction with metal hydroxide within the osmotic conduit.

[0018] In a further embodiment, the fuel synthesis may include reacting hydrogen produced by the electrolysis with nitrogen to form ammonia. This ammonia may then be used in a further embodiment to react with carbon dioxide to produce urea, which in turn may be further reacted with further portions of the ammonia to produce guanidine.

[0019] In a further embodiment, at least a portion of the carbon dioxide necessary to react with the ammonia to produce the urea may be scavenged, salvaged or recovered from the metal carbonate/bicarbonate resulting from the carbon dioxide sequestering. In such embodiment, HCl produced from the electrolysis of the saltwater/brine may be reacted with at least a portion of the carbonates/bicarbonates from the sequestering to produce recovered carbon dioxide. This carbon dioxide recovered may then be passed to the urea synthesis vessel to react with ammonia for producing the urea.

[0020] In a further embodiment, a method of producing guanidine may comprise exposing urea to ammonia while irradiating the urea with light. The light irradiation may use a wavelength less than about 1240 nm.

[0021] In accordance with another embodiment, an osmotic apparatus comprises a conduit defined by walls of permeable walls forming a channel therethrough. Fibers of hydrophilic material may be disposed within the channel of the conduit. In a particular example, the diameter of the channel may be defined with dimension for the lumen of about 1 mm to 100 mm. Further, the fibers of hydrophilic material may pack the channel with a density of about 20 to 90%.

[0022] In accordance with another embodiment, a method of energy conversion comprises reacting guanidine for producing ammonia and/or hydrogen. The ammonia/hydrogen may drive a solid oxide fuel cell (SOFC), wherein hydrogen oxidation within the fuel cell produces electricity along with the release of heat and water in the form of steam. At least a portion of the steam released is used to drive a steam turbine-generator pair for generating further electrical energy. At least a portion of the steam passed through the turbine is recovered and returned to the guanidine hydrolysis process. In a particular embodiment for the energy conversion, the energy conversion system may be used to drive at least one of an electrical motor or power grid.

[0023] In a particular embodiment, heat produced by the SOFC is used to assist the decomposition or disassociation of the ammonia when received therein into its hydrogen and nitrogen components.

[0024] In a further embodiment, the electrical energy produced by the energy conversion system is used to drive a propulsion system to a vessel, boat, aircraft, locomotive or vehicle.

BRIEF DESCRIPTION OF DRAWINGS

[0025] Subject matter for embodiments of the present invention may be further understood by reference to the following detailed description when read with reference to the accompanying drawings, in which:

[0026] Fig.l is a simplified cross-section view of a portion of a carbon dioxide sequestering osmotic lumen and flow diagram associated with its use, in accordance with an embodiment of the invention.

[0027] Fig.2 is a simplified schematic diagram showing a carbon dioxide sequestering fuel synthesis system in accordance with another embodiment of the invention, and showing a saltwater/brine electrolysis unit for sourcing (i) hydrogen to the fuel synthesis module and also for sourcing (ii) metal hydroxide to a carbon dioxide sequestering, osmotic module. [0028] Fig.3 is a further simplified diagram to the carbon dioxide sequestering fuel synthesis system in accordance with a particular embodiment, showing a wind turbine for the energy source driving the electrolysis unit.

[0029] Fig.4 is a simplified schematic diagram to an example of an electrolysis subsystem that may be used for the electrolysis chamber in fuel synthesis embodiments of the present invention.

[0030] Fig. 5 is simplified block diagram showing a fuel synthesis system in accordance with another embodiment of the present invention, showing light irradiation of urea in the presence of ammonia for producing guanidine.

[0031] Fig. 6 is a simplified block diagram showing a fuel synthesis system in accordance with another embodiment of the present invention, showing ammonia bubbling through molten urea and light irradiation of urea in the presence of the ammonia bubbled therethrough.

[0032] Fig. 7 is a sketched rendering of a chemical reaction of urea with ammonia, and showing light incident upon the urea, as may be used to assist an understanding of an embodiment of the present invention.

[0033] Fig. 8 is a simplified block diagram of an energy conversion system in accordance with an embodiment of the present invention, showing guanidine feeding a solid oxide fuel cell power plant for producing electricity, and showing steam being recovered from the turbine-generator for routing back to the guanidine hydrolysis chamber.

[0034] Figs. 9-12 are simplified schematic diagrams of propulsion systems in accordance with further embodiments of the present invention, showing incorporation of energy conversion systems of Fig. 8.

DESCRIPTION

[0035] In the description that follows, readily established structures for the exemplary embodiments may be disclosed in simplified form (e.g., simplified reaction vessels, fluid lines, valves, sensors, wind turbines and/or simplified description) to avoid obscuring an understanding of the embodiments with excess detail and where persons of ordinary skill in this art can readily understand their structure and formation by way of the drawings and disclosure. For the same reason, identical components may be given the same reference numerals, regardless of whether they are shown in different embodiments of the invention.

[0036] As used herein, the term "vessel" may be used to reference alternative meanings. In the context of the embodiments for synthesis, the term may be understood from context to reference a housing, chamber or chemical reaction type of "vessel." In further embodiments of different contexts in connection with transportation systems, the term "vessel" may refer to boats, barges, water-craft or submarine and/or may further be understood from context to suggest reference to other transportation systems such as locomotive, vehicle, airplane, truck, bus and transportation "vessels."

[0037] Similarly, the expression HCl may refer to hypo- and/or hydro-chloric acid in certain context in this disclosure.

[0038] Likewise, in context of the steam recovery and recirculation to the hydrolysis chamber, the reference to "water" in some context may be understood to reference water of its liquid form and/or of water in vapor form such as steam.

[0039] In accordance with an embodiment of the present invention, referencing FIG. 2, carbon dioxide sequestering fuel synthesis system 200 comprises electrolysis unit 204 powered by a power source 202. Electrolysis unit or electro lyzer 204 is operable to electro lyze a solution of saltwater or brine to produce electrolysis product such as hydrogen and metal hydroxide. And in some embodiments, it may further produce chlorine and/or HCl of hypo- or hydro-chloric acid. The metal hydroxides may comprise sodium hydroxide, potassium hydroxide or magnesium hydroxide. Typically, the more abundant metal hydroxide is sodium hydroxide.

[0040] Further referencing Fig. 2, the metal hydroxide is passed from electrolyzer 204 by line 208 to metal hydroxide solution reservoir 214. It may be understood that the metal hydroxide may be passed to the reservoir in solution of water as provided from the electrolyzer. In further embodiments, a particular pH may be desired within the reservoir 214 for passage to the osmotic exchanger. If the pH of the solution may be too great by excess concentration of hydroxides, additional water may be added to the reservoir by way of optional source 254 via control valve 258. [0041] Progressing to the carbon dioxide sequestering module of the fuel synthesis system 200, further referencing Fig. 2, the metal hydroxide solution from reservoir 214 may be passed through line 216 via valve 218 to pump 220. The pump, in turn, may drive the fluid input line 222 to the osmotic exchanger 100 via valve 226. In some alternative embodiments, the pump could be removed and the fluid could be propagated through the osmotic network of exchanger 100 under the influence of gravitational forces.

[0042] More commonly, however, pump 220 may be used in combination with the various valves as illustrated for representing examples for the osmotic module. These pumps and valves may be understood to lend greater control for the establishment of pH levels and for the sequestering efficiencies of the sequestering module for the fuel synthesis system 200.

[0043] To assure that the pressure at the input line 222 does not exceed a certain level, a pressure sensor 224 may be used to deliver a pressure signal 223 to the controller 258. Controller may then govern the operation of pump 220 and valves 218, 226 based upon the pressure sensed and the efficiencies of the flow of fluid through the osmotic exchanger 100. With the assistance of valves 226, 232, the pressure within osmotic exchanger 100 may be kept at a certain predetermined level via regulation by controller 258 based on the pressure sensed by sensor 224. For example, the pressure may be kept close to atmospheric pressure to enable free passage of CO2 through the permeable membrane material. Normally, the pressure may need to be slightly higher at the input end than at the output end so as to maintain a slow flow rate. It may further be recognized that use of pressures near atmospheric levels may reduce the strength requirements of the membrane material.

[0044] Further referencing Fig. 2 in association with Fig. 1, osmotic exchanger 100 in accordance with an embodiment of the present invention comprises walls of permeable membrane material 101 that define the osmotic conduit with a channel therethrough. Metal hydroxide solution passing through the channel of the osmotic conduit may flow along inwardly facing surfaces 103 of walls 101 of the permeable material. Thus, gases of the external atmosphere may permeate the walls for interaction with the solution within the channel. For example, referencing the exploded view of Fig. 1, carbon dioxide may pass through external face 105 of permeable wall 101 and beyond inwardly facing surface 103 for reaching and interacting with metal hydroxide of the solution within the lumen. As the solution further flows through the channel defined by the permeable walls, additional carbon dioxide of the atmosphere may react with additional hydroxide of the solution for producing metal carbonates and/or metal bicarbonates. Thus, the downstream portion 134 of the osmotic exchanger 100 may exhibit a concentration of carbonate greater than that proximate input 122 of the osmotic exchanger.

[0045] In accordance with a further embodiment of the present invention, further referencing Fig. 1, the permeable walls 101 of osmotic exchanger 100 may comprise at least one of microporous, mesoporous, and macroporous membrane material. The pore size freely passes atmospheric gases, including CO2, while excluding liquid such as water from entering or exiting the membrane. For relative understanding, microporous may refer to a pore size of less than about 2 nm. Mesoporous may be understood to refer to a pore size of greater than about 2 nm and less than about 50 nm. Whereas, macroporous may reference a pore size of greater than 50 nm. It may be theorized that a pore size smaller than ~1 μm could be sufficient to exclude the liquid water. In a particular embodiment, none the less, a microporous membrane was selected as a material that was hydrophobic, so at to prevent the membrane from being wetted by the water. For example, the material selected was a GORE-TEX ® microporous membrane material.

[0046] Further referencing Fig. 1, the interior channel defined by the inwardly facing surface 103 of the membrane material 101 may be filled with a hydrophilic material to increase the effective surface area of the absorbing solution. A cellulose fiber or nylon fiber may be used to pack the lumen. For example, in a particular embodiment, the fibers of hydrophilic material may be disposed within the channel with a density therein of up to 20% to 90% of the channel volume. Accordingly, the permeable walls defining the lumen to the channel of the osmotic conduit may be wrapped around the hydrophilic fibers and thus retain better structure and/or rigidity. Likewise, the osmotic conduits may be capable of formation with diameter greater than that which might otherwise be required. And similarly, the over-all osmotic network might therefore be realized with lower fabrication cost than that otherwise expected with narrow diameter lumens.

[0047] It may be further theorized, merely for purposes of facilitating understanding, that perhaps the hydrophilic fibers within the lumen may be effective for enhancing the turbulence of the solution within the channel so as to thus enhance the exchange of gases permeating the walls of the osmotic conduit and thereby enhance the sequestering operability of the solution within the osmotic conduit.

[0048] In a particular embodiment, the osmotic conduits for the exchanger may be formed with channel diameter(s) from 1 mm to about 100 mm. The length of these lumens could be formed with an extent up to, for example, 10 to 20 meters long.

[0049] Returning with further reference to Fig. 2, the osmotic exchanger 100 could be understood to comprise multiple osmotic conduits as described relative to Fig. 1. Accordingly, the plurality of tubes or lumens as defined by the permeable materials may be referenced as an osmotic exchange network. The osmotic exchange network may be disposed to expose the external walls for communication with an atmospheric fluid flow. In operation, the flow of atmospheric gases to the external walls of the osmotic exchange network may allow carbon dioxide to permeate the pores of the walls for interaction with the metal hydroxides of the solution within the osmotic conduits.

[0050] Further referencing Fig. 2, as the solution propagates to the exit of the osmotic exchanger, a pH sensor 230 may monitor the pH and send a signal to controller 258 regarding the pH. Based upon the pH determined, controller 258 may control valve 232 via line 231 for opening or closing the valve for either recirculation path 236 or discharge port 234. Accordingly, the portion of solution initially passed through the osmotic exchanger may be recalculated. That is, it may be passed back for further reprocessing via fluid path 236, pump 248 and line 250 via valve 252 for return to metal hydroxide reservoir 214. As may be recognized, pump 248 may be used to counter gravitational forces and likewise to counter pressure within reservoir and/or for establishing sufficient pressure by which to punch-through check valve 252.

[0051] By such recirculation control, the controller 258 may be able to regulate the flow of the absorbing solution through the membrane exchange network. Additionally, the return loop may allow the fluid to make multiple passes through the osmotic network as may be required to meet a given level of pH via the sequestering of carbon dioxide from the atmospheric conditions. Once the level of pH has been established, the controller 258 may enable the valve 232 for discharge of sent solution via discharge line 234. In one example of operation, the input pH may be in the range near pH = 14 (perhaps 13 - 15) proximate sensor 228. The desired target range for the pH at the output is about 8.2 for enabling ocean disposal. For given processes where it is desirable to have the solution consist primarily of carbonates, the pH solution may be alternatively targeted for a range greater than 10.3, e.g., perhaps 10.3 to 12.3.

[0052] In accordance with a further particular embodiment, the discharge may be realized along path 238 for release to an external body of water 240 such as, for example, an ocean. In such embodiment, controller 258 may monitor 241 the pH of the ocean by way of, for example, sensor 242. The controller may thus regulate the release along path 238 based upon the comparison of the pH of the ocean relative to that of the solution for discharge. For example, the pH of the solution for discharge may be monitored for a pH slightly higher than that of the external body of water. Upon so determining, the controller 258 may enable discharge of the solution into the external body of water. Thus, upon establishing a level of pH of 8.2 as being slightly more basic that the ocean pH of 8.1, the discharge may be effected and likewise may serve to assist stabilization of the ocean pH.

[0053] In an alternative embodiment, further referencing Fig. 2, the discharge from the osmotic exchanger is routed to dehydrator 244 by way of discharge line 239. As thus implied, the dehydrator 244 may dehydrate the carbonate solution for metal bicarbonate and carbonates byproduct, which may then be released to land dumps and/or for external handling or transport - e.g., as washing soda product.

[0054] In further embodiments, as the dehydrator dehydrates the discharged carbonate solution, a portion of the water may be recovered and routed back to the optional water source reservoir 256 via fluid line 246. It may be understood that line 246 inherently may include a pump and valves (not shown) operable to assist the circulation of the recovered water back to the optional water reservoir 256. It may similarly be understood that such recovery module may further include a condenser (not shown) that may condense the steam recovered from the dehydrator.

[0055] Further referencing Fig. 2, the fuel synthesis by one perspective and embodiment, could be understood to be defined by the generation of the hydrogen gas at fluid line 206. However, as mentioned earlier herein, this form of elemental hydrogen may be understood to pose certain practical limitations in application as the raw fuel for transport and/or application in propulsion systems. Accordingly, in a further embodiment of the present invention, the hydrogen is passed 206 to an ammonia synthesis vessel 210.

[0056] In ammonia synthesis vessel 210, the hydrogen is combined with nitrogen to form ammonia. This vessel may incorporate known methods of synthesis such as that of the Haber process wherein the reaction of the hydrogen with nitrogen may be facilitated by a catalyst as known, such as for example a catalyst of an iron catalyst and/or via further promoters such as aluminum oxide (Al₂O₃) and potassium oxide (K₂O).

[0057] For purposes of assisting understanding, a comparative analysis may be theorized for an existing method of synthesis relative to some more customary methods of synthesis. When the ammonia is otherwise derived from more classic natural gas synthesis processes, the process itself might be recognized as exacerbating certain global warming difficulties via the hydrocarbon combustion process of, e.g., the Haber-Bosch process. For certain embodiments of the present invention, however, the hydrogen may be derived from the electrolysis of salt water, wherein the production of ammonia as fuel need not necessarily exacerbate the problem of global warming. Further, the sequestering of carbon dioxide via the hydroxides may be understood to further ease the concerns relative to global warming, which may be represented simplistically via the equation (2):

H₂O + 2NaCl + CO₂ → H₂ + Cl₂ + Na₂CO₃ (2)

[0058] From this basis, it may be theorized that approximately 22 tonne of carbon dioxide may be captured in washing soda for about every tonne of hydrogen produced. In other words, about 3.9 tonne of carbon dioxide may be referenced as being captured for every tonne of ammonia produced. It may also be recognized that perhaps the washing soda may be applied to various other uses, as in liking to other parts of the world where it is otherwise obtained by mining various deposits in arid regions. Thus, the production can be heaped up in arid regions to sequester the carbon much more securely and economically than various schemes that have been proposed, e.g., such as those that have been proposed for the injecting of gaseous carbon dioxide into given geologic structures.

[0059] It may be further theorized that the sequestering of about 1,000,000,000 MT of carbon dioxide will require about (10^Λ9) (59/44)/ N tonnes of guanidine, wherein N is between 4.5 and 9, depending on whether bicarbonate or carbonate is formed in the sequestering process. If the carbonate or bicarbonate is stored on dry land, then the value of N would be 9; while, on the other hand, if it is used to de-acidify the ocean, a match of the bicarbonate/carbonate ratio may be obtained relative to the ocean. For this ocean release, it may be provided with a slightly more carbonate to bicarbonate ratio as may be used to assist reversing the acidification of the oceans.

[0060] Returning to further embodiments of the present invention, with further reference to Fig. 2, the ammonia as similarly referenced for the hydrogen earlier might similarly be viewed per a given embodiment as the resulting fuel of the fuel synthesis system. In some applications, this could be deemed feasible. However, as mentioned previously herein, the ammonia as a stand-alone fuel could be recognized as being a bit impractical alone, e.g., given its toxic nature if accidentally released by accidental spill. Accordingly, in a further embodiment of the invention, the ammonia from ammonia synthesis vessel 210 may be further passed to urea/guanidine synthesis vessel 212.

[0061] It may thus be recognized that the synthesis of urea from ammonia requires a combination of ammonia with carbon dioxide by which to form the urea molecule, as represented by the equation (3) as follows:

2NH₃ + CO₂ → CO(NH₂)₂ + H₂O (3)

[0062] Before moving forward with various urea or guanidine synthesis system embodiments, a further optional embodiment for the present invention is now disclosed indirectly with reference to Fig. 2 as associated with the requirements for the generation of urea. In most geographic realms, it may be estimated that the amount of carbon dioxide found in the atmospheric conditions may be sufficient for enabling the production of urea in quantities capable of keeping up with the amount of hydrogen available from the electrolysis unit 204.

[0063] For purposes of assisting an exemplary analysis, the power source 202 is assumed with realization as a wind turbine. Thus, the quantity of carbon dioxide within the flux of wind associated with generating the electricity generated by the wind turbines can be deemed of quantity sufficiently vast by which to further enable extraction for the synthesis of the urea. The amount of carbon dioxide within the air passing through the diameter/area effective for rotating the rotor-blades of the wind turbine may be referenced relative to the diameter/dimensions of the rotor and its rotation. This analysis may be performed assuming use of, for example, a wind turbine such as that of ENERCON, GMBH of 6 MW (Megawatt) - i.e., the model El 12. This particular turbine has a rotor dimension of 112 m. It is further rated to produce 6 MW with wind speeds from about 14 to 24 m/s. Assuming a 20 m/s windspeed, the airflow may be calculated as follows:

Pi* 112*112*20/4 => 233,798 (m³/s)

[0064] Of this volume of air, in normal geographic territories, the percentage of carbon dioxide may be known at about 390 ppm by volume. This may further be expressed for the carbon dioxide as about ^ 91.2 (m³/s) for the carbon dioxide (CO2).

[0065] Given that the density of CO2 at standard temperature and pressure (STP) is about 44 gm/ 22,400 cm3, which corresponds to about 0.044 kg/0.0224 m³, which in turn corresponds to about 1.96 kg/m³; the mass of carbon dioxide CO₂ passing through the wind turbine may be determined as about 179 (kg/s), which may be expressed alternatively as 645 (tonne/hr). To sequester 3.4 tonne of CO₂ for each tonne of guanidine produced, the amount of CO₂ would accordingly correspond to 190 tonne of guanidine per hour.

[0066] In the same hour, the turbine produces 6,000 kWhr of electrical energy. Assuming that the electrical energy required to produce 1 tonne of guanidine is 30 GJ, then this may result in a further determination of (30*10^Λ9)/(3.6*10^Λ6) = 8,333 kWhr per tonne of guanidine. Thus, the turbine may be theorized to provide the energy to produce 0.72 tonne of guanidine. Therefore, the volume Of CO₂ passing through the wind turbine may be recognized for normal geographic realms of the world to vastly exceed the amount that might be sequestered in the production of guanidine. Again, this is noted relative to a normal geographic realm of the world.

[0067] However, in certain regions, the available quantity of carbon dioxide may be more limited. Accordingly, to facilitate the urea production from the guanidine, the carbon dioxide might be initially thought as having to be sourced from an external source. Alternatively, in accordance with a further embodiment of the present invention hereby disclosed, a process may be used for recovering carbon dioxide from the metal carbonates formerly sequestered by the osmotic exchanger.

[0068] For such embodiment, the metal carbonate discharged from the sequestering osmotic exchanger may be treated with HCl (hypo- or hydro-chloric acid) for releasing carbon dioxide and the associated metal salt. In a particular example for the electrolysis unit 204, referencing Fig. 2, the HCl may be sourced as one of the byproducts (not shown specifically in Fig. 2) resulting from the electrolysis of saltwater. This HCl may be used as the acid for reaction with the metal carbonate resulting from the sequestering osmotic exchanger. The resulting carbon dioxide recovered may then be passed to the urea synthesis vessel 212 for assisting the formation of urea when combined with the ammonia. It may be recognized, therefore, that such optional embodiment of the present invention may permit the carbon dioxide sequestering fuel synthesis system to be employed in geographic territories/regions of the world of low concentration of carbon dioxide.

[0069] Moving forward with reference to Fig. 3, in accordance with a particular embodiment of the present invention, the power source 202 as referenced in Fig. 2 may be recognized as a wind turbine power source. Wind of an atmospheric fluid flow may drive the turbine blades of the wind turbine 302 by which to provide electricity for powering the electrolysis unit 304. Again, the electrolysis unit 304 may produce product of metal hydroxide for output 314 and hydrogen that is delivered via fluid line 306 to ammonia synthesis vessel 310. This ammonia is in turn passed to urea/guanidine synthesis vessel 312. [0070] Tower 370 supports the wind turbine 302 at a height sufficient to allow rotation of the turbine blades. Supported and extending along a partial height of the tower 370, osmotic exchanger 200' may receive and flow the metal hydroxide solution within the osmotic exchange network of the osmotic exchanger 200'. It may be recognized that this osmotic exchange network may comprise an embodiment such as that described previously herein relative to Fig. 2. Again, discharged solution may feed a discharge collection reservoir 339. This concentration of this collection reservoir may be kept at a pH via a concentration of the carbonate/bicarbonate dependent upon the rate of metal hydroxide feeding the osmotic exchange network and the level of recirculation within the osmotic exchange network and rate of sequestering from the ambient atmospheric fluid flow. Again, in particular embodiments, the concentration of metal hydroxide that feeds the osmotic exchanger along with the circulation and recirculation within the osmotic exchanger may be controlled by a controller for establishing a ratio of carbonates/bicarbonates for a predetermined level of pH in the discharge reservoir. With a given level of pH established in the discharge reservoir 339, the solution may then be released to the external body 340 of water (e.g., ocean) via line 338.

[0071] Referencing Fig. 4, an electrolysis unit 404 may comprise a four chamber electrolysis circuit. Such electrolysis unit may be used for that of the embodiments described previously herein relative to Figs. 2 and 3. In this example, further referencing Fig. 4, the electrolysis unit comprises four chambers #1, #2, #3 and #4. These chambers are separated by respective cation or anion exchange membranes. A cation exchange membrane 474 separates the first and second chambers #1 and #2 respectively. Anion exchange membrane 472 separates the second and third chambers #2 and #3. While the cation exchange membrane 470 separates the third and fourth chambers #3 and #4.

[0072] Initially, a given level of metal hydroxide such as sodium hydroxide may be provided in the first chamber #1 to serve as a starting basis for the electrolysis unit. Additionally, filtered seawater or brine may be placed in the second chamber #2 to assist its initial starting condition. The third chamber #3 may be primed with a given level of HCl for its starting condition; while the fourth chamber #4 may be primed with a predetermined level of sulfuric acid. It may be understood that the sulfuric acid in the fourth chamber may be used to increase the electrical conduction for a sulfate without risk of release of the sulfate ion.

[0073] Once primed, power may be applied to the electrolysis unit for operation. The cathode (-) 468 will attract the hydrogen ions for gaining electrons at the electrode and thereby combine to form hydrogen gaseous molecules H₂ from the chamber, for subsequent output as the hydrogen source 406. At the opposite anode (+) electrode 466, the sulfuric acid assists in the preferred affinity of oxygen ions to the electrode for release of electrons and combination as oxygen molecules O₂. These oxygen molecules, in turn, are released f from the fourth chamber #4 at oxygen output 476. As the reaction further ensues within the four chamber electrolysis unit, it may be understood that hydrogen ions may pass through the cation exchange membrane from the fourth chamber into the third chamber. In this third chamber, the hydrogen ions may thereby combine with chlorine ions that have been passed from the second chamber to the third chamber via anion exchange membrane 472. Accordingly, the hydrogen and the chorine combine to form the HCl at the hypo-/hydrochloric acid output 478 from the third chamber.

[0074] At chamber one, while hydrogen may be released at hydrogen output 406; it may further be understood that the metal hydroxides will be output from the hydroxide output port 416 of the first chamber. As this reaction is sustained, further filtered seawater may be sourced to the input port 464 of the second chamber of the four chamber electrolysis unit 404.

[0075] Moving forward in accordance with a further embodiment, referencing Fig. 5, a urea/guanidine synthesis system 500 receives ammonia by way of valve 598 and carbon dioxide via valve 599, which in turn are collectively input to reaction vessel 580 via fluid input line 597. The reaction vessel is heated to a temperature greater than 100° C, while the gases of ammonia and carbon dioxide move upward into the reaction vessel 580. In further embodiments, the reaction vessel 580 may be kept at temperature sufficient for sustaining molten state of the guanidine/urea in the collection reservoir at the bottom. For example, the temperature may be kept at a level of 32° C to 150° C.

[0076] The upward flow of gases in the reaction vessel 580 is facilitated by gas circulatory circuit defined at least in part by exhaust line 584, which in turn passes the gases to condenser housing 586. The condenser housing includes an ammonia and carbon dioxide gas recycle line 590 that can be kept in a forward flow through the recycle line via at least one of a Venturi effect at the junction of line 590 relative to the further recycled line 596 and/or in combination with a similar Venturi effect proximate the input line 597 acting upon the junction of recycle return line 596.

[0077] During synthesis, as the ammonia and carbon dioxide move upward in the reaction vessel 580, they encounter reactor baffles 582 which may serve to agitate the gases together with the enhanced temperatures so as to react and facilitate the urea formation from the gas reactions. As the urea then begins to move downward under the influence of gravitational forces, the urea is further exposed to ammonia and may thus further react for producing guanidine. To enhance this reaction of the urea with ammonia for enhanced efficiencies in the production of guanidine, a light may be irradiated into the chamber to strike the urea and to excite its molecular state for stimulating its further reaction with ammonia.

[0078] In a particular embodiment, the light source 503 may comprise at least one of a light emitting diode or solid state laser of energy of about 1 eV, which may be of a wavelength less than 1240 nm. In the case of a solid state laser such as a gallium arsenide solid state laser, the monochromatic light may be of wavelength less than 1240 nm and greater than 800 nm, and may be directed an incident beam 505 into the chamber for acting upon particles of urea in the environment of ammonia. Accordingly, the oxygen double bond, with reference to Fig. 7, may be exited to a state more conducive for reaction with ammonia. It may be theorized that a major limiting factor in the formation of guanidine from urea may be due to its normal planar geometry. However, by way of the present embodiment of the invention, the molecular structure of the urea may be excited for transition to a tetrahedral or pyramidal geometry, as opposed to its planar geometry for the unexcited urea molecule. Similarly as revealed by Lopez, et. al. in J Phys. Chem. A 2003, 107, 2304-2315, as represented by computer simulations of amide bonds (which in turn correspond to those present in urea), the tetrahedral geometry has been represented with an energy of approximately 0.9 ev (~ 20 kcal/mole) relative to the ground planar state for the molecule. At the temperatures typically used for organic chemical reactions, only a very small fraction (e.g., less than 1 in 1 billion) of the molecules would be in the excited state operable for enabling the reaction with ammonia to form guanidine. This explains, therefore, the slow reaction rates that have been encountered by certain artisans. But, by way of the presently proposed embodiment, the chemical reaction rate may be dramatically increased by exciting the urea molecules with the light of appropriate energy, wherein the "delocalized amide bond" may be partially broken and the urea molecule may transition to its alternative tetrahedral or pyramidal orientation. This change in shape, likewise, brings forward a change in its electron density as may be contrasted to its simpler amide molecule structure so as to make the reaction with ammonia more readily available.

[0079] In actual applications, the urea molecules will have a range of energy levels, due to molecular vibrations and rotations, and complexes with adjacent molecules, so there will be a range of light energies, near 0.9 eV, that will be suitable for exciting the urea molecules. By certain embodiments of the present invention, light-emitting diodes (LEDs) or solid state lasers that emit light with energy near 1 ev, or equivalent to a wavelength below 1240 nm may be proposed with suitable energy. For example an infrared Ledtech UT 1883 Infrared LED emits infrared light with a peak at 940 nm. Gallium Arsenide lasers may provide peak wavelengths in the range of 890 nm. In practice an array of infrared lasers or LEDs may be mounted outside a section of the reaction vessel 580 that is to contain the ammonia and urea in a solvent that is either water or an alcohol or may contain the urea in its molten form without any added solvent. If mounted external the reaction vessel, the portion of the vessel may comprise a window that is essentially transparent to infrared light. Alternatively, the arrays or lights can be mounted inside the reaction chamber and kept cooled to a temperature below the maximum operating temperature of 85 C.

[0080] Further referencing Fig. 5, as the urea and guanidine forms, it falls to the bottom of the reaction vessel 580 as a solution of molten guanidine/urea. The resulting water vapor and excess un-reacted ammonia and carbon dioxide gases that do react during a first passage may exit through an exhaust gas line 584 and be passed to condenser chamber 586. In the condenser housing, cooling coils 587 may cool the exhaust gases, which in turn may condense water while keeping the majority of the exhausted ammonia and carbon dioxide in their gas state; although, a certain amount will be dissolve into the recovered water. The water condensed will accumulate within the collection tank 588 within the condenser 586. Gas passages in the walls of the condenser chamber 586 permit the escape of the carbon dioxide and the ammonia to the recycle line 590.

[0081] The water collected in the bottom of the collection tank 588 is then passed to the water reclamation vessel 594 via fluid line 591 and pressure reducing valve 592. The water passed into the water reclamation housing 594 may experience a reduced pressure operable to outgas gases such as any ammonia and carbon dioxide that may have been dissolved therein. The out-gassing of carbon dioxide and ammonia may be pumped via pump 595 via return line 596 back to the gas input line 597 for the reaction vessel 580. It may be recognized that the pump 595 may be operable to establish a low pressure atmosphere within the water recovery out-gassing chamber 594 at least relative to the operability of the pressure reducing valve 592. Water 507 reclaimed in the bottom of the reclamation housing 594 may then be released to the waste reservoir 511. As the level of the molten guanidine/urea reaches a certain threshold within the reaction vessel 580, valve 501 may be opened to release and source the guanidine/urea for external use.

[0082] In accordance with an alternative embodiment of the present invention, referencing Fig. 6, a guanidine synthesis system 600 receives urea from a bulk urea tank 627 via valve 629 for entry to reaction vessel 680. Ammonia may be supplied to the reaction vessel 680 from input 615 via valve 613. Ammonia passes to an ammonia chamber of the reaction vessel 680. From the ammonia chamber, it may pass into the urea through a gas permeable wall 617. As passed through the permeable barrier wall, the ammonia bubbles through the molten urea/guanidine reservoir 681.

[0083] As the ammonia bubble through the urea, light from a light source 603 may be irradiated into the molten solution for assisting the reaction of the urea with the ammonia for producing the guanidine. As represented earlier for embodiments described relative to Fig. 5, the light may comprise at least one of a light emitting diode or a solid-state and/or gallium arsenide solid state laser of energy greater than about 0.9 eV, as may be associated with wavelength less than 1240 nm. In further embodiments, the light may be of wavelength less than about 1240 nm and greater than 800 nm. [0084] As the ammonia reacts with the urea to form guanidine, it may yield water vapor which is then exhausted out of the reaction vessel 680 by way of exhaust line 684 via pressure sensitive valve 631. Additionally, the excess ammonia that does not react may similarly be exhausted though the exhaust line. This recovered gas is passed to the condenser 686.

[0085] Further referencing Fig. 6, the gases passed to condenser 686, similarly as describe before relative to Fig. 5, may be cooled by the condenser coil 687 for recovering water droplets 689 that may collect into the water collection tank 688 near the base of the condenser chamber 686. Ammonia gases may exit the condenser chamber via the recirculation pump 621 in recovery line 690, 623. This recovery line may pass the ammonia back to the ammonia chamber of the reaction vessel 680. The water recovered in the collection tank 688 of the condenser chamber 686 may be passed to the water reclamation housing 694. Again, the pressure may be reduced in this housing to assist out-gassing of dissolved ammonia for reclamation of the water 607. The out-gassed ammonia may likewise be pumped back to the ammonia chamber of the reaction vessel 680 via pump 695 in recovery line 696. The water reclaimed may then be released via valve 609 to an external water discharge reservoir 611.

[0086] The guanidine produced in the reaction vessel may pool at the bottom of the reaction vessel. Accordingly, it may then be output as guanidine/urea output product via output valve 625. As output, it may then be used in subsequent external applications.

[0087] In accordance with a further embodiment of the present invention, referencing Fig. 8, a solid oxide fuel cell (SOFC) energy conversion system 800 may be fueled by a guanidine based fuel. The SOFC 806 will release heat during the oxidation of hydrogen therein. The oxidation of the hydrogen will form water within the SOFC, which will result in steam in view of the heat generated in the SOFC. The steam 810 from the SOFC 806 may be passed to a steam turbine 812, for turning generator 816 for generating electricity 817 as a dual producer with that 807 produced by the SOFC. At least a portion of the steam passed through the turbine 812 may be recovered by condenser 814 for return to guanidine hydrolysis chamber 804. In this embodiment, the returned water may facilitate further hydrolysis of the guanidine for producing ammonia that may further fuel the SOFC 806.

[0088] It may be noted that only a portion of the water released in the combustion and oxidation will be recovered in certain embodiments. To assist such understanding, it may be theorized that for each mole of guanidine that is decomposed and combusted, 4.5 moles of water are produced; of which, only two moles are required for the decomposition. In other words, when guanidine is decomposed and combusted, a lesser amount is required than that which is given off. Accordingly, recovery of about 33% to 44% of the water may be deemed sufficient for enabling realization of a self-sufficient energy conversion system.

[0089] In a particular embodiment, the electricity 807 form the SOFC 806 and that 817 generated by generator 817 may be combined to drive an electrical device collectively such as electrical motor 808. The motor likewise may be coupled to an external mechanical system for delivering mechanical energy to the external system. For example, it may drive a propulsion system to a vehicle, or other mechanical systems for rudder, pump, oscillation system, worm gear and the like.

[0090] In alternative embodiments, the electricity delivered by the solid oxide fuel cell (SOFC) may drive one device independently of that driven by the generator. For example, the SOFC could be used to drive an electric motor 808 (e.g., referencing Fig. 10) for the propulsion systems of the air craft while the generator could be used to drive alternative electrical systems on board the aircraft 1000.

[0091] In a further embodiment, returning with further reference to Fig. 8, the SOFC 806 and generator 816 may deliver the electricity to an energy storage system (not shown) which may be operatively configured in a parallel arrangement to the electrical motor of the normal load application. Accordingly, a system controller (not shown) may govern when the energy from the energy conversion system is to be delivered to the electric motor or alternatively to the storage system. Likewise, the controller could drive the load via the storage system in the absence of continuous operation of the energy conversion system of SOFC and generator. Or, both could be applied simultaneously for peak demands; wherein power could be delivered from both the energy storage system as previously stored therein and per the capability of the duel SOFC and turbine-generator pair.

[0092] In a further embodiment, further referencing Fig. 8, the SOFC is operatively configured with thermal coupling to the fuel input chamber for enabling heat generated by SOFC 806 to assist in decomposition of the ammonia received into its nitrogen and hydrogen elements. For example, the SOFC may comprise a stack such as that taught by Gardner in US Pat. No. 5,595,833, hereby incorporated herein by reference. In the SOFC stack, for the present embodiment, a fuel intake manifold may receive the ammonia and is thermally coupled to receive at least a portion of the heat generated by the SOFC during oxidation of the hydrogen therein. With this thermal coupling, the heat may be used to assist in the decomposition of the ammonia when received in the intake manifold.

[0093] In further embodiments, known catalyst(s) may further be disposed within the fuel intake manifold to the SOFC to further catalyze and assist in the decomposition of the ammonia when received in the fuel intake manifold. In a particular example, the catalyst may comprise any of the catalytic materials used in the commercial synthesis of ammonia, e.g., either ruthenium on silica or magnetite (Fe₃O₄), which is reduced and promoted with oxides of aluminum (Al) and potassium (K).

[0094] As further operable, e.g., as in liking to that of the stack of Gardner, a turbo may be able to be driven by hot exhaust gases from the spent fuel within a given collection manifold of the SOFC stack. In other words, as the spent fuel and spent oxidant are collected in the collection manifold, a portion of the spent oxidant may be re-circulated into the oxidant supply manifold, while an additional portion may be exhausted external to the SOFC and used to drive, e.g., turbine 812 of the energy conversion system 800 in accordance with embodiments of the present invention as described herein relative to Fig. 8. In this fashion, the portion of the collected oxidant in the collection manifold that is re-circulated may be understood to assist the preheating of the fuel that may be delivered and received in the fuel intake manifold.

[0095] In yet a further embodiment, further referencing Fig. 8, the hydrolysis chamber 804 may be operable to react guanidine with water to produce ammonia and may similarly be configured with operable thermal coupling to the SOFC. By this thermal coupling, at least a portion of the heat generated by the oxidation within the SOFC may be used to facilitate the reaction of the guanidine with water to produce the ammonia available for driving the SOFC. Further, it may be recognized that the steam that may be recovered upon passage through turbine 812 may have a given elevated temperature that may similarly be used to assist the heating of the hydrolysis reaction of the guanidine in hydrolysis chamber 804.

[0096] In some embodiments where the steam recovered from the turbine is not too excessively hot, the recovered steam may be delivered directly back to the hydrolysis chamber 804.

[0097] In accordance with further embodiments, further referencing Figs. 5 and 6, the guanidine and urea solutions may be obtained from the synthesis reactors formulated to given powdered and/or granular states. Because the guanidine is much less stable than urea within the presence of water, for some embodiments therefore the urea may be coated over the guanidine grains. In a particular method, grains of guanidine may be exposed to ammonia and carbon dioxide at given temperature and pressure to form a surface layer of the urea on the guanidine. Thereafter, additional layers of guanidine may be formed thereon and again the urea. In a further optional embodiment, a thin film of anti-clumping material may finally be applied to the grains.

[0098] In accordance with further embodiments of the present invention, referencing Figs. 9-12, the Solid Oxide Fuel Cell energy conversion systems such as of the embodiments described previously herein with reference to Fig. 8, may be incorporated into the power plant for the propulsion system of a boat, aircraft, vessel or vehicle. With reference to Fig. 9, a guanidine fuel tank 802 may feed guanidine to a hydrolysis chamber 804 which in turn may supply ammonia to the SOFC in a manner such as that disclosed for the embodiments describe previously herein relative to Fig. 8. The electricity 808 A produced by the SOFC may be used to drive electric motor for powering and delivering mechanical energy to the locomotive 900. Additionally, steam from the SOFC may be delivered to a steam turbine 812 and utilized for driving generator for generating additional electricity 808B. Steam and water recovered from passage through the turbine may then be routed back via recovery line 814 to the guanidine hydrolysis chamber 804. [0099] Moving forward with reference to FIG. 10, the energy conversion system 800 may be employed in an aircraft 1000. Guanidine tanks 802 may be configured in wing fuselages. These may be coupled to feed the guanidine to hydrolysis chamber 804, which in turn may supply the ammonia to the SOFC for generating the electricity and steam. The steam can be used by the steam turbine-generator pair 812 for generating further electricity. The steam passed through the turbine may be recovered and passed back to the hydrolysis chamber 804 via the water recovery line 814. The electricity generated from the SOFC and the Generator may be used to drive electric motors 808A and 808B for the aircraft propulsion.

[00100] Figs. 11 and 12, in accordance with further embodiments of the present invention, similarly show use of the energy conversion systems 800 in different respective embodiments for a water vessel or boat. The guanidine tank 802 is configured to feed guanidine to the hydrolysis chamber 804. The hydrolysis chamber supplies ammonia to the SOFC for oxidation and generation of electrical energy. Steam from the SOFC is used to drive the Turbine-generator 812 pair for generating additional electrical energy. The steam passed through the turbine may again be recovered and passed back to the hydrolysis chamber 804 by way of fluid recovery line 814. The electricity generated from the SOFC and the Generator may be used to drive electric motors 808 for the craft's propulsion systems.

[00101] In further aspects for these embodiments, vibration dampers 820 may be used to dampen vibrations of the vehicles relative to the SOFC stacks. As may be understood, the SOFC stacks may comprise ceramic plates of numerous quantity and potential fragile vulnerabilities. Accordingly, the vibration dampers may be used to assist in dampening of vibrations to the SOFC stack.

[00102] While certain exemplary features of the embodiments of the invention have been illustrated and described above, it may be understood that various modifications, substitutions, changes and equivalents may now occur to those skilled in the art. It is, therefore, to be understood that the appended claims are intended to cover all such embodiments and changes as fall within the spirit of the invention.

Claims

What is claimed is:

1. A system comprising:

an electro lyzer to electro lyze saltwater and produce product consisting of at least hydrogen and metal hydroxide; and

an osmotic exchanger operatively configured to flow metal hydroxide solution from the electro lyzer within permeable walls of the osmotic exchanger;

the osmotic exchanger operatively disposed to expose external surfaces of the permeable walls for gaseous fluid communication with ambient atmosphere.

2. The system according to claim 1, further comprising a discharge housing to receive solution discharged from the osmotic exchanger.

3. The system according to claim 2, in which the discharge housing comprises a dehydrator to dehydrate the discharged solution to produce dehydrated product of metal carbonate/bicarbonate for external release and handling.

4. The system according to claim 2, the discharge housing operatively configured to enable external release of at least a portion of the solution received.

5. The system according to claim 1, further comprising an osmotic controller operatively configured to influence at least one of (i) the flow of the ambient atmosphere in fluid communication with the external surfaces of the permeable walls, (ii) a ratio of the metal hydroxide to water in the solution fed into the osmotic exchanger and (ii) the rate of discharge from the osmotic exchanger based upon at least one of the concentration of metal carbonate and/or the concentration of metal bicarbonate in the solution discharged from the osmotic exchanger.

6. The system according to claim 5, further comprising a pH-sensor to determine a pH level of an external body of water, wherein the osmotic controller is further operatively configured to base said influence at least in part on the pH level determined.

7. The system according to claim 6, further comprising another pH-sensor to determine a pH level of the solution discharged, wherein the osmotic controller is operatively configured to enable release of the solution from the discharge housing when it has pH higher than the pH determined for the external body of water.

8. The system according to claim 1, further comprising a power source of the group consisting of at least one of solar, geothermal, hydro, hydrocarbon or wind-based energy generators to generate electricity for powering the electrolysis of the electrolyzer.

9. The system according to claim 1, further comprising a tower; and

a wind-turbine supported by the tower to generate electricity, wherein at least a portion of the electricity generated is available to power the electrolyzer; and

the permeable walls define a gas-to-liquid transfer network of the osmotic exchanger that is supported and extends along at least a partial height of the tower.

10. The system according to claim 9, further comprising a reservoir to receive water and metal hydroxide from the electrolyzer for the solution, the reservoir to supply the solution to the gas-to-liquid transfer network of the osmotic exchanger under the influence of at least one of a pump and gravitational forces.

11. The system according to claim 1 , in which the permeable walls of the osmotic exchanger comprise at least one of micro-, meso- and macro-porous membrane material.

12. The system according to claim 11, in which the membrane material comprises a hydrophobic, GORE-TEX ® micro-porous material.

13. The system according to claim 1, in which the osmotic exchanger further comprises hydrophilic material disposed within an interior of the osmotic exchanger between inwardly facing surfaces of the permeable walls, the hydrophilic material operatively disposed therein for increasing an effective surface area of the solution flow for absorbing the CO2.

14. A CO2 sequestering method of fuel synthesis, comprising:

producing hydrogen by electrolysis of saltwater/brine; and

sequestering CO2 with metal hydroxide byproducts resulting from the electrolysis of the saltwater.

15. The method according to claim 14, in which the sequestering comprises:

flowing solution of the metal hydroxide through osmotic conduit(s) defined at least in part by liquid barrier walls of gas permeable material; and

exposing outwardly facing surfaces of the liquid barrier walls of the osmotic conduit(s) to an atmospheric fluid flow.

16. The method according to claim 15, further comprising conditionally re-circulating the solution in the osmotic conduit(s) dependent at least in part on the pH of solution passed therethrough.

17. The method according to claim 16, releasing at least a portion of solution from the osmotic exchange network.

18. The method according to claim 17, wherein the solution is conditionally released into an external body of water when a pH of the solution for release is higher that that of the external body of water.

19. The method according to claim 16, further comprising mixing the metal hydroxide byproduct resulting from the electrolysis with water for circulation as said solution in the osmotic exchange network.

20. The method according to claim 15, further comprising reacting nitrogen with the hydrogen produced from the electrolysis to form ammonia.

21. The method according to claim 20, further comprising reacting the ammonia with carbon dioxide to produce urea.

22. The method according to claim 21, in which the electrolysis further produces HCl, said method further comprising:

reacting at least a portion of the HCl produced by the electrolysis with at least a portion of the carbonates and bicarbonates produced by the sequestering to produce carbon dioxide; and

passing the carbon dioxide recovered from the carbonates to the urea production process as a source for at least some of the carbon dioxide in the reacting with ammonia.

23. The method according to claim 21, further comprising reacting the urea with ammonia to produce guanidine.

24. The method according to claim 23, further comprising irradiating the urea with light of wavelength less than about 1240 nm to facilitate the reaction of the urea with ammonia in the producing of guanidine.

25. The method according to claim 24, wherein the irradiating uses a light of wavelength less than about 1240 nm and greater than about 800 nm.

26. A method of producing guanidine comprising:

exposing urea to ammonia; and

irradiating the urea with light during at least a portion of the exposure to ammonia.

27. The method according to claim 26, wherein the irradiating uses a light of wavelength less than about 1240 nm.

28. The method according to claim 27, wherein the irradiating uses a light of wavelength less than about 1240 nm and greater than about 800 nm.

29. The method according to claim 27, further comprising sourcing the light from a light source of the group consisting of light-emitting diodes, and solid state and/or GaAs- based solid state lasers.

30. The method according to claim 29, using light energy of at least about 0.9 eV for the irradiating with light.

31. The method according to claim 27, wherein the irradiating illuminates urea when the urea is in an environment comprising ammonia.

32. The method according to claim 31 , wherein the urea is suspended within a solvent during the exposure to ammonia and light irradiation.

33. The method according to claim 27, wherein the urea is molten;

the exposing to ammonia comprises bubbling ammonia through the molten urea; and

the irradiating comprising directing the light into the molten urea during at least a portion of the bubbling of the ammonia.

34. The method according to claim 26, further comprising:

recovering carbon dioxide from a metal carbonate by reacting the metal carbonate with HCl to recover carbon dioxide and produce salt;

combining the ammonia with the carbon dioxide produced to yield said urea.

35. The method according to claim 34, further comprising:

electrolyzing saltwater or brine to produce electrolysis product that includes metal hydroxide and HCl;

exposing metal hydroxide to an atmospheric flow to sequester carbon dioxide from the atmosphere, the sequestering defined at least in part by reacting the metal hydroxide with the carbon dioxide from the atmosphere to produce metal carbonate; and using the metal carbonate produced by the sequestering and at least a portion of the HCl produced by the electrolysis in the reacting of the carbonate with the HCl.

36. The method according to claim 35, in which the electro lyzing further produces hydrogen, and the method further comprises:

reacting the hydrogen with nitrogen to produce ammonia; and

using the ammonia produced for that to which the urea is exposed.

37. An osmotic apparatus, comprising:

a conduit comprising walls of permeable material defining a channel; and

fibers of hydrophilic material disposed in the channel of the conduit.

38. The osmotic apparatus according to claim 37, in which the permeable walls define the lumen for the channel with a diameter of greater than about 1 mm and up to about 100 mm.

39. The osmotic apparatus according to claim 38, in which the fibers of hydrophilic material pack the channel for a density therein of about 20 to 90%.

40. The osmotic apparatus according to claim 38, in which the permeable walls comprise at least one of micro, meso and macro-porous hydrophobic membrane material.

41. A method of energy conversion comprising:

reacting guanidine with water to produce at least one of hydrogen and ammonia;

using the at least one of hydrogen and ammonia to drive a Solid Oxide Fuel Cell, wherein the oxidation of the hydrogen in the SOFC produces electrical energy, heat and steam;

using at least a portion of the steam produced by the SOFC to drive a steam turbine- generator for generating further electrical energy; recovering at least a portion of steam or water passed through the turbine-generator; and

passing at least a portion of the steam or water recovered back to the reacting process for further hydrolysis of guanidine.

42. The method according to claim 41, further comprising driving at least one of an electrical motor or power grid with at least a portion of the electrical energy produced and generated.

43. The method according to claim 41, further comprising using the electrical energy to drive a propulsion system for propelling a vessel of the group consisting of a vehicle, boat, aircraft, locomotive and transport device.

44. The method according to claim 41, in which at least a portion of the heat produced by the SOFC is used to facilitate the reacting of the guanidine.

45. The method according to claim 44, in which the heat produced by the oxidation in the SOFC is further used to assist disassociation of ammonia to produce hydrogen and nitrogen.

46. An energy conversion system comprising:

a hydrolysis vessel to receive guanidine and react the guanidine with water to produce at least one of ammonia and hydrogen;

a solid oxide fuel cell (SOFC) operable to receive the at least one of the ammonia and hydrogen from the hydrolysis vessel for oxidation to produce electrical energy, heat and steam;

a turbine-generator operably configured to be driven by the steam produced by the SOFC and to generate further electrical energy; and

a condenser to recover at least one of steam and water from the turbine-generator for forwarding to the hydrolysis vessel.

47. The system according to claim 46, in which the hydrolysis vessel is thermally coupled to the SOFC to enable use of at least a portion of the thermal energy produced by the SOFC to assist in the hydrolysis of the guanidine.

48. The system according to claim 47, in which the SOFC comprises a fuel intake manifold operatively configured to enable heating of ammonia received therein to facilitate the disassociation of the ammonia into its constituent elements of nitrogen and hydrogen.

49. The system according to claim 48, in which the SOFC further comprises a catalyst in the intake manifold operable to assist the heated decomposition of the ammonia.

50. The system according to claim 46, in which the energy conversion system defines at least in part the power plant to at least one of the group consisting of a vehicle, boat, vessel, aircraft and locomotive, and said system further comprises an electric motor operatively configured to propel said at least one of a vehicle, boat, vessel, aircraft and locomotive when driven by the electricity generated and produced by the SOFC and turbine-generator.

51. A method of fuel synthesis, comprising:

combining carbonate(s) with HCl to obtain product of carbon dioxide and salt; and

reacting ammonia with the carbon dioxide to produce urea.

52. The method according to claim 51 , further comprising reacting the urea with ammonia to produce guanidine.

53. The method according to claim 51, further comprising:

electrolyzing saltwater or brine to yield at least one of hydrogen, metal hydroxide, and HCl;

sourcing at least a portion of the HCl obtained by the electrolysis to the combining with carbonates; exposing the metal hydroxide obtained by the electrolysis to an atmospheric fluid flow to sequester carbon dioxide from the atmosphere and produce at least one of metal carbonate and metal bicarbonate; and

reacting nitrogen with the hydrogen obtained from the electrolysis to produce ammonia for use as said ammonia in the reacting with carbon dioxide;

wherein the at least one of the carbonate and bicarbonate obtained from the sequestering is used in the reaction with the HCl for the obtaining of the carbon dioxide product.