electrochemical battery plant

Abstract

A system comprising an electrolytic cell stack connected to a water / gas separation vessel through an inlet pipe and an outlet pipe, wherein the separation vessel is configured to passively separate water and gas; the separation vessel includes a heat exchanger; and the separation vessel is composed of a polymer material.

Description

Technology Field

[0001] The present invention relates to an electrolytic cell system and the separation and cooling of water and gas. Background Technology

[0002] Conventional water electrolysis systems take hydrogen as a useful component while releasing oxygen and releasing heat into the atmosphere. This green hydrogen, produced through electrolysis from renewable sources, is being used in a continuously expanding group of applications. Examples of these applications include transportation fuels, long-term energy storage, and renewable chemistry.

[0003] Traditionally, electrolytic cell stacks are connected to heat exchangers and associated pumps via multiple pipes. The heat exchangers / pumps are then connected to gas separation towers. The water and oxygen produced by the electrolytic cell stacks are supplied through pipes to individual pumps / heat exchangers for cooling, and then supplied to individual gas separation towers. The cooled water is then supplied back to the electrolytic cell stacks through pipes. Traditionally, these components are located individually and connected by pipes covering long distances. This is because the industry prefers using large pumps (believing they are cheaper and simpler). In this system, water must be pumped back and forth over long distances, which can lead to pressure loss and incurs material costs due to the need for more piping. Such systems also involve many peripheral devices (balance of plant).

[0004] The fact that the components are located individually and that the distances between them are long also means that it is impossible to place a test facility in the same location as the pumps, heat exchangers, and electrolytic cell stacks. This is not optimal because it prevents testing before the final system is configured.

[0005] Therefore, the electrolytic cell system of the prior art includes components that cannot be manufactured with an efficient factory setup. Instead, these components require multiple links that must be assembled on-site without prior testing.

[0006] Oxygen and heat are also useful byproducts of electrolysis (hydrogen is not the only useful commodity). To extract these byproducts, components are being added rather than being efficiently integrated into the electrolytic cell system. These components are generally metal-based. The traditional manufacturing techniques typically relied upon—metal fusion welding, flange joint assembly using spanners, and on-site pipeline assembly that barely considers the number of placed components—cause significant manufacturing difficulties in modern plant layout designs.

[0007] Currently, when designing electrolysis plants, the field of process engineering arranges separate and general process equipment, including electrolytic cell stacks, pipes, heat exchangers (removing heat from process water), numerous pipes, 'knock-out' separation towers (separating water and oxygen gas), multiple flange joints (containing nuts, bolts, and connecting rods), pump skids, glycol tanks with pipelines, and associated airflow cooling (adjacent to primary cooling). Furthermore, massive assemblies are required to package these components together using trace heating, thermal compensation, and structural supports (weight hangers, braces, etc.), and to connect them to large-diameter water pipes. These are also complemented by new designs for oxygen recovery, compression of hydrogen and / or oxygen, gas storage, and heat recovery. In some cases, these components are deployed over long distances and contribute to large footprints, which in turn necessitates larger-diameter pipelines, assembly complexity, and high costs.

[0008] The present invention provides a system comprising a compact oxygen separation vessel that is strong and cost-effective to manufacture.

[0009] The present invention is an effective and environmentally sustainable complete water electrolysis system (cooling water and separating gas from water) that can be fully constructed as a repeatable unit in a factory setting. Furthermore, the system can be tested in the factory before deployment on-site, offering many advantages such as maintaining high cleanliness standards. The entire system is located in a single location, minimizing the distance water and gas travel. This provides economic and environmental benefits.

[0010] Accordingly, according to a first aspect of the present invention, the system comprises an electrolytic cell stack connected to a water / gas separation vessel through an inlet pipe and an outlet pipe, and

[0011] The above separation vessel is configured to passively separate water and gas;

[0012] The above separation vessel includes a heat exchanger; and

[0013] The above separation container is composed of a polymer material.

[0014] According to a second aspect of the present invention, a method for electrolyzing water uses the system defined above, water is contained in a gas / water separation vessel, an electrolytic cell electrolyzes the water to produce hydrogen and oxygen, then hydrogen and oxygen flow through a pipe to the separation vessel, and one or both of the hydrogen and oxygen are passively separated from the water and extracted from the system.

[0015] According to a third aspect of the present invention, an oxygen separation vessel for passively separating water from a mixture of oxygen and water is provided, the vessel comprising: a plurality of inlet nozzles for receiving the mixture of oxygen and water; a heat exchanger located within the vessel for cooling the mixture of oxygen and water; at least one oxygen outlet for discharging oxygen separated from the mixture of oxygen and water; and at least one water outlet nozzle for discharging water separated from the mixture of oxygen and water.

[0016] The vessel of the third embodiment may be used in combination with the system of the first embodiment and the method of the second embodiment, respectively. The vessel of the third embodiment may preferably be used in combination with an electrolytic cell stack, for example, an electrolytic cell stack for producing hydrogen.

[0017] The vessel of the third embodiment provides a strong, compact, and cost-effective oxygen separation vessel for manufacturing.

[0018] By providing multiple inlet nozzles, multiple mixture columns are created within the vessel during use, thereby significantly improving the oxygen / water separation rate for a given vessel height, which allows the vessel to be made much shorter than conventional oxygen separation vessels. For example, the vessel according to the present invention may have a height of about 2.5 m, whereas conventional vessels are generally about three times this height.

[0019] There may be 2 inlet nozzles, 3 inlet nozzles, 4 inlet nozzles, 5 inlet nozzles, or any other number of inlet nozzles greater than one. Preferably, there are 3 inlet nozzles to produce 3 mixture columns.

[0020] In addition, having oxygen separation including a heat exchanger (i.e., the heat exchange is inside the oxygen separation vessel) is not conventional technology and reduces the power required to pump water out of the vessel.

[0021] In a conventional system, the heat exchanger is located downstream of the oxygen separation vessel, and the pump is located between the oxygen separation vessel and the heat exchanger. In this conventional arrangement, the pump is positioned in front of the heat exchanger to overcome the pressure drop across the heat exchanger.

[0022] Placing a heat exchanger inside a vessel means that the pressure inside the vessel increases due to the oxygen pressure generated electrochemically (i.e., generated during electrolysis), which ultimately applies pressure to the free liquid surface of the wafer inside the vessel. This pressure helps to overcome the pressure drop across the heat exchanger, which ultimately means that the pump power can be reduced accordingly.

[0023] This configuration can reduce pump power by 18%, leading to significant energy savings. Since the power used by the pump during electrolysis is 'parasitic' power, this reduction effectively lowers the cost of hydrogen production. This is particularly important in low-power scenarios, such as when powering the electrolyzer with solar panels on cloudy days or with wind turbines on calm days. In these low-power scenarios, the power required by the pump can account for a significant portion of the total power consumed.

[0024] Preferably, the container (i.e., the body of the container) is made of a plastic / polymer material. The container may be made of partially cross-linked linear low-density polyethylene 'LLDPE' (e.g., ICORENE® LLDPE). Alternatively, the container may be made of high-performance hexane high-density polyethylene.

[0025] Preferably, the inlet nozzles are positioned at or near the top of the oxygen separation vessel. Being near the top means that the nozzles are positioned in an area defined by the top 25% of the vessel at use, more preferably within the top 10% of the vessel.

[0026] The fact that the inlet nozzles are positioned close to the top of the vessel means that the multiple mixture columns generated by the inlet nozzles become larger / taller, thereby improving water / oxygen separation.

[0027] The container may further include at least one through hole for accommodating a transversal bracing element, and preferably, at least one through hole has a substantially rectangular or substantially elliptical cross-section.

[0028] A through hole may also be referred to as a through hole, a through channel, or something similar.

[0029] Through holes enable the provision of transverse elements to the vessel that reinforce / strengthen it. During use, the vessel experiences high pressures that would otherwise lead to buckling or failure. Furthermore, the through holes themselves also provide a bridge between the sidewalls, improving the vessel's strength and providing vacuum stability against vacuums that may result from the negative head of suction of the pump (i.e., the through holes provide a reinforcing effect even in the absence of bracing elements).

[0030] Using through holes with a rectangular or square cross-section is particularly desirable because it simplifies manufacturing by promoting wall thickness homogeneity of the polymer / plastic liner during manufacturing.

[0031] Preferably, the vessel further comprises a transverse bracing element received in at least one through hole. Each through hole may have a transverse bracing element. The transverse bracing element is preferably made of steel. The transverse bracing element may be a tie rod or something similar. Alternatively, the bracing element may be referred to as a reinforcing element or something similar.

[0032] Preferably, the vessel further comprises an outer sheet cladding covering at least a portion of the outer surface of the vessel. Preferably, the cladding is made of steel, such as steel plate (e.g., EN10028 P460 pressure steel plate). The cladding may also be provided with glass fiber reinforcement. Glass fiber reinforcement, also known as glass reinforced plastic (GRP), may be used with a linear low-density polyethylene (LLDPE) liner, a medium-density polyethylene (MDPE) liner, a polypropylene (PP) liner, or a high-density polyethylene (HDPE) liner.

[0033] Cladding strengthens the vessel and increases the pressure it can withstand.

[0034] While cladding and transverse bracing elements each provide significant reinforcement individually, using them in combination helps distribute the load applied to the sidewalls of the vessel. Consequently, the load that the vessel can withstand before failure or buckling increases, thereby enhancing the reinforcement effect.

[0035] Alternatively, the vessel may have at least one circumferential groove to accommodate a circumferential bracing element. For example, this circumferential bracing element may be a steel ring or something similar that reinforces the vessel.

[0036] Preferably, the container further includes two outer end plates disposed at opposite ends of the container, and the outer end plates are joined by one or more longitudinal bracing elements.

[0037] These end plates and longitudinal bracing elements provide additional reinforcement to the vessel. Preferably, the end plates are made of steel, such as EN10028 P460 pressure steel, P350 steel, or 300-series stainless steel of appropriate thickness. It is also preferable that the bracing elements be made of steel. The bracing elements may be connecting rods or similar.

[0038] Optionally, a plurality of inlet nozzles and at least one water outlet nozzle may be integral with the container and may be composed of the same material as the container, and preferably the nozzles are connected to the pipe by polymer fusion, which is very cost-effective.

[0039] Preferably, the inlet nozzles are positioned at substantially the same height (i.e., at the same height when in the direction in which gas separation is used). Substantially means at the same height within a 10% deviation of the total height of the vessel.

[0040] Preferably, the container is rotationally molded in a single one-shot process.

[0041] Preferably, the container has a flat elliptical cross-section in which the flat side walls are positioned vertically when in use.

[0042] More preferably, the inlet nozzles are positioned to direct the fluid flow toward the (preferably flat) sidewalls of the vessel during use, thereby creating a cyclone effect. This increases the efficiency of the water / oxygen separation process, and consequently, makes the vessel more compact.

[0043] In other words, the inlet nozzles can be arranged so that, when in use, the fluid flow is directed toward the opposite side wall along the curvature of one side wall of the vessel, thereby improving the separation of the fluid and gas mixture using centrifugal force.

[0044] Preferably, the container is made of high-performance hexane high-density polyethylene. This provides a clean, rigid, and high environmental stress crack resistance. Alternatively, the container may be made of other materials such as partially cross-linked linear low-density polyethylene.

[0045] Alternatively, the vessel may include a tapered collector positioned between the heat exchanger and at least one water outlet nozzle. This increases the velocity of the fluid flow through the water outlet nozzle.

[0046] Optionally, the heat exchanger may be a tubular heat exchanger.

[0047] Preferably, the oxygen separation vessel further includes a sleeve disposed around a tubular heat exchanger, and preferably, the sleeve is made of a polymer material.

[0048] Preferably, the sleeve comprises an inlet, an outlet, and one or more baffle plates arranged to allow the fluid to flow in a cross-flow direction around the heat exchanger during use. The baffle means that the fluid is maximized at the boundary layer between the fluid and the heat exchanger to enhance heat exchange. Cross-flow means that the fluid flows in a direction having a non-zero component perpendicular to the tubular range of the heat exchanger.

[0049] According to a fourth aspect of the present invention, a hydrogen generation system comprising an electrolytic cell stack connected to an oxygen separation vessel of the third aspect is provided.

[0050] Preferably, the hydrogen generation system further includes a pump connected to at least one water outlet nozzle, and the pump is located downstream of the oxygen separation vessel. As previously discussed, placing the pump downstream of the gas separation vessel reduces pump power, thereby saving electricity. The pump drives the flow of water out of the oxygen separation vessel. Brief explanation of the drawing

[0051] FIG. 1 illustrates a schematic diagram of a preferred embodiment of the present invention. Figure 2 is a graph showing that pump power saving in a 2 MW system is up to 1.5% of total power consumption. When the plant is idle and the pump is operating, this can save up to 70% of the current plant power. FIG. 3 is a schematic diagram showing fluid flow in a preferred embodiment of the present invention (only the container is shown). FIG. 4 is a schematic diagram illustrating a preferred embodiment of the present invention. FIGS. 5a to 5c illustrate the first configuration of the container. FIGS. 6a to 6d illustrate the second configuration of the container. FIGS. 7a to 7d illustrate the third configuration of the container. FIGS. 8a to 8d illustrate the fourth configuration of the container. Specific details for implementing the invention

[0052] As used herein, electrolytic cell stack and water / gas separation vessel (or tower) are terms used in the art. A stack comprises a plurality of electrolytic cells.

[0053] As used herein, heat exchanger is a term known in the art. In relation to electrolytic cells, they cool the water flowing through the electrolytic cell system.

[0054] The inventors have devised an electrolytic cell system comprising a multi-purpose vessel that combines bulk clean water storage, separation of oxygen and / or hydrogen from water, heat exchange, optional fabrication-less porting (i.e., eliminating the need to manufacture and add additional ports), and enhanced cleanliness in a single module.

[0055] The advantage of the present invention is that, in contrast to conventional technology where the electrolytic cell must be assembled on-site with pipes, separation towers, and pumps and then tested, it enables the realization of multiple self-sufficient electrolysis modules, i.e., repeatable and manageable units.

[0056] In addition, the oxygen separation vessel of the present invention is smaller in size compared to conventional separation vessels, making transportation and installation easier and allowing it to be installed in more limited spaces.

[0057] The core of the present invention involves two modifications to existing systems. First, by placing a heat exchanger inside the gas separation tower, the number of balance of plants is reduced and efficiency is increased. Second, the efficiency of the system is increased because the integrated heat exchanger and gas separation unit can be connected to the electrolyzer over a short distance (because the components are compatible). Previously, due to the large number of balance of plants, electrolyzer stacks had to be connected to large water / gas separation towers and separate heat exchangers over much longer distances. This made field assembly and testing very difficult.

[0058] The gas separation vessel is composed of a polymer material. Preferably, the gas separation vessel is composed of a plastic material.

[0059] The gas separation vessel may be constructed of partially cross-linked linear low-density polyethylene 'LLDPE' (e.g., ICORENE® LLDPE) or high-performance hexane high-density polyethylene. Additionally, the gas separation vessel may have a multi-walled structure with pressure steel plates (e.g., EN 10028 P460 or P350 steel of appropriate thickness or 300-series stainless steel) as an outer liner or cladding. Alternatively, the outer liner or cladding may be glass fiber reinforcement.

[0060] It is preferable that the separation vessel includes multiple nozzles for connecting the inlet pipe and the outlet pipe, and the pipes are integral with the vessel and composed of the same polymer material as the vessel. This offers many manufacturing advantages.

[0061] In a preferred embodiment, the vessel includes at least four nozzles configured such that at least two nozzles are in fluid communication with each pipe.

[0062] More preferably, the system includes at least six nozzles configured such that at least three nozzles are in fluid communication with each pipe.

[0063] Preferably, the vessel (preferably including nozzles) is injection molded or rotationally molded from a polymer material in a single one-shot process. More preferably, the pipe is also made of a polymer material. This is advantageous because various components can be connected by polymer fusion. This eliminates the need for complex metalworking and flanges, as is required in the composite technology.

[0064] The reduction in the number of parts in the system of the present invention leads to design efficiency and ease of placement, which can be achieved in the proposed invention by rotational forming technology that creates up to 15 ports / nozzles directly on the vessel wall itself. The nozzles can then be directly connected to the pipework through automated polymer fusion welding, which eliminates the need for traditional fusion welder qualifications, flanges, spanners, gaskets, nuts, bolts, and washers, and also ensures leak-tightness.

[0065] The placement of conventional isolated auxiliary devices (towers and related equipment) far from the hydrogen generation (stack) entails the calculation of many components (due to their associated large diameters, forces, and weight), which leads to difficulties in managing flow and cleanliness. For example, assembly involves lifting heavy objects on-site, during which pipe ends may be exposed to elements of the construction site.

[0066] The system of the present invention is illustrated in FIG. 1. In the system of the present invention, water from the electrolytic cell stack(s) is supplied to an integrated gas separation and heat exchanger unit. In this integrated unit, the heat exchanger serves to cool the surrounding water by being submerged in the water flowing into the gas separation tower during use. The water thus cooled is supplied back to the electrolytic cell.

[0067] In a preferred embodiment, the electrolytic cell stacks are connected to the separation vessel over a short distance, so they can be located in the same building, preferably in close proximity to each other. The reduction in distance between the integrated heat exchanger and gas separation unit and the electrolytic cell stacks avoids various disadvantages of the prior art, such as economic derivative problems associated with transporting and pumping water over long distances.

[0068] The present invention integrates the auxiliary functions of electrolysis into the smallest common denominator (module) that establishes all manufacturing and testing under a controlled environment within a single factory roof, using design and assembly rules associated with lean assembly (small number of parts, reasonable interface). Forming the product with this architecture benefits the organization in several ways, such as: first, the auxiliary functions being standardized with an emphasis on compatibility; second, parts inventory being reduced and quality being improved (e.g., a single pump part number); and third, inventory (and all management tasks) and manufacturing cycle times being reduced, and field installation time being minimized. The present invention enables the use of 'snap and go' piping by having the pipework composed of polymer materials. The system can then be connected via integrated nozzles, and small-diameter pipes with a diameter of less than 50 mm can be used, thereby reducing the burden on workers and the need for heavy equipment, which is now best described as trivial piping work. This stands in stark contrast to the use of a 350 mm bore in conventional technology, which is best illustrated by heavy industrial operations. Because the invention can be assembled in a factory setting, it reduces occupied space, pump loss, and the tendency for dirt to enter.

[0069] The present invention is preferably manufactured by a one-shot injection molding method. This has the advantage of easy manufacturing. It is preferably formed through rotational molding. This enables rapid manufacturing.

[0070] In a preferred embodiment, the container is isolated to enable preheating, convenient instrument fitting (measurement of water conductivity, water level, and temperature), as well as prevention of microbial growth. In a preferred embodiment, the polymer container of the present invention comprises an antimicrobial or antifungal agent. Such formulations are known in the art. The formulation may be provided by including an additive in a molding process, preferably in a single-step, fragment-free, recyclable thermoplastic mold.

[0071] The vessel of the present invention enables complete factory assembly, integration, and testing in close proximity to stacks. As a result, the diameter can be smaller, and the pipe length can be shorter with less head loss, avoiding the fabrication of flanges and ports. Consequently, assembly time is saved, the possibility of leakage is reduced, head pressure is lowered, and the need for flow management is reduced. This is because the elements of the system are no longer far apart from the electrolytic cell stacks and are not far apart from each other.

[0072] The present invention reduces the number of parts, complexity, and pumping energy consumption. Several factors contribute to significant pump power savings. A typical embodiment of the present invention will reduce losses to a greater extent than would be possible without the present invention through the arrangement of heat exchangers (see FIG. 2), shorter lengths of ducting (a beneficial aspect being reduced friction losses), and the ability to use multi-stage pumps that allow for energy-saving adjustments.

[0073] In a preferred embodiment, the vessel has a flat elliptical cross-section in which the flat sidewalls are positioned vertically when in use. This embodiment is illustrated in FIG. 3. Preferably, nozzles are positioned to direct the fluid flow toward the (preferably flat) sidewalls of the vessel when in use to create a cyclone or centrifugal effect. The nozzles direct the fluid flow toward the opposite sidewall along the curvature of one sidewall of the vessel. This is also illustrated in FIG. 3. Preferably, the fluid flow is directed at an angle of about 45 degrees to the sidewalls to create a turbulent region or cyclone. This enables efficient water / gas separation. The angle of the nozzle (i.e., inlet nozzle) may be 30 to 60 degrees, more preferably 35 to 55 degrees, even more preferably 40 to 50 degrees, and most preferably about 45 degrees (i.e., 44 to 46 degrees).

[0074] A wire brush may be positioned within at least one of the nozzles so that the kinetic energy of the fluid stream collapses during use.

[0075] In a preferred embodiment, a vortex breaker, a vortex spoiler, or a demister pad is located within at least one of the pipes.

[0076] In a preferred embodiment, the ratio of the vessel is such that the ratio of the vessel's height to its width is 3:1 or less than 2:1, or preferably about 1:1. To explain without being bound by theory, this may be made possible by a nozzle that directs the fluid flow toward the sidewall to create a cyclone / centrifugal effect. This enables more effective water / gas separation, which means that the separation vessel does not need to be as tall as that of the prior art.

[0077] Containers of the prior art have a height-to-width ratio of 6:1, primarily in the vertical direction, for the precise separation of gas and water. This is intended to prevent the water-gas mixture from flowing back into the pump inlet. Polymer-based and fusion-welded containers with a 6:1 ratio are difficult to handle in terms of ergonomics and manufacturing methods. Such containers are brittle and prone to breakage, thus entailing other costly necessary precautions. In a preferred embodiment of the present invention, by means of split ports (multiple nozzles) and a 1:1 ratio, ease of manufacturing of the container itself is achieved by a rotational molding process, and cleanliness is achieved in terms of process because no burr is generated by connecting flanges or manually drilling or de-burring the plastic (these functions are essential for molding in a 'one-shot' process).

[0078] The gas separation 'knockout' tower used in the conventional technology system has a diameter of 1 m and a height of 6 m (total 4.8 m). 3 It includes a column of which is impractical to handle and manufacture in a fully equipped factory, and is difficult to export (export via road or sea transport) or assemble on-site. This reduces the range for effectively arranging a series of units. In contrast, the typical aspect ratio of a typical embodiment of the proposed invention is 2.6 m x 2.6 m x 1 m (total 6.8 m 3 It is a rectangular prism, which allows it to effectively handle much more actual load.

[0079] In conventional technology, many flanges are connected one by one and bolted to the tower on-site (because the completed assembly is too large to transport as a single part), which entails inefficient execution and tools, and the flanges are prone to significant leakage, at least initially, which must be resolved on-site.

[0080] For use in the present invention, a tubular heat exchanger is preferred. This heat exchanger functions by supplying a coolant, preferably cold water, that flows through the interior of the tubular structure to cool the outer metal surface, and this cooled outer metal then cools the surrounding water within the gas separation tower supplied from the electrolytic cell stack. The process fluid is drawn into the pump inlet through the shell side, while the tube side of the heat exchanger is connected to the refrigerant circuit. In modern technology, the heat exchanger is located downstream of the pump. In the present invention, the heat exchanger is located upstream of the process pump. In the present invention, the pressure drop across the heat exchanger is overcome by the electrochemically generated oxygen pressure, particularly by the absolute pressure applied to the free liquid surface of the suction vessel. Thus, pump power can be reduced accordingly. A reduction in pressure drop of 0.6 to 1 bar g leads to a reduction in pump power of about 10 to 16%. (In such a system, the total pressure drop is about 6 bar).

[0081] The present invention significantly reduces the occupied space and number of parts, and also increases manufacturing capacity through a number of jointless nozzles. The present invention allows for various coolant types through the selection of heat exchanger types (enabling multiple downstream integration possibilities), and allows for the substantial elimination of pump head loss from the primary cooling side to avoid pump 'parasitic loss' in a reduced regime, as well as an integrated antimicrobial means that ensures oxygen pressure capacity and maximum cleanliness during idle time.

[0082] In a preferred embodiment, the heat exchanger, preferably a tubular heat exchanger, is positioned in the highest flow region of the vessel, thereby avoiding significant resistance to flow on the vessel 'shell' side compared to conventional plate heat exchangers. This reduces pump losses compared to conventional plate heat exchangers (made of multiple narrow fluid impact holes). Head pressure savings were evaluated using the pump affinity law controlling centrifugal pump-based water circulation and yielded a minimum pump energy savings of 14%, a figure that can be achieved through pressure head reduction via floating tubular heat exchangers alone. In addition, the tubular heat exchanger is made as a single fabrication part, in contrast to plate heat exchangers which generally include multiple plates, seals, end plates, studs, washers, and nuts.

[0083] The robustness and versatility of the selected heat exchanger type can be explained by its chemical life, chemical salt resistance, tolerance to debris, and 'contamination,' along with its low pressure drop. The coolant stream is located on the tube side (flowing internally on the tube side). This is unusual and actually reduces the heat exchange coefficient (the ability to conduct heat), which is not traditionally adopted. However, the reduction in the heat exchange coefficient is very gradual and does not constitute significant damage. Since larger pumps and flow are located on the electrolysis side, other factors are more than beneficial in compensating for this, which is more than a balance to this negative aspect. This arrangement allows for the use of a certain range of coolant types on the tube side (internally), such that the shell side cannot accommodate equipment on the secondary cooling side, and consequently, the number of such equipment is significantly reduced.

[0084] The system of the present invention opens up the possibility of using natural waterways or seawater as a coolant in electrolysis processes. In heating large swimming pool complexes or zones, or industrial spaces, the heat exchanger can be resistant to chlorinated water or inhibitors, and can recover heat to increase overall efficiency compared to fully passive system standards. Test results have shown that energy efficiencies exceeding 95% can be achieved in some cases. A key advantage of the present invention is the acceptable types and specifications of coolants, allowing the use of any fluid that is roughly filtered and provided at temperatures ranging from above freezing to 40°C. Coolants such as seawater or waterways, which were generally unimaginable, have become possible with the present invention. This overcomes narrow concerns regarding heat exchange performance, special handling system integration, and occupied space. Cooling primary process water is particularly attractive in marine applications, such as offshore wind turbines as a non-limiting example, as it offers significant space reduction and shows a path toward future wind turbine integration. The size of the stack module(s) associated with the module can also be very carefully selected to match the wind turbine 'Type IV' DC link voltage of 690 V (suitable for electrolysis). Accordingly, the system of the present invention can be customized to have 300 to 350 electrochemical cells as standard. It is important to match the DC voltage of the electron donor (wind turbine) with the load voltage (electrolyzer). The present invention can define a container volume that matches the stacks to be accommodated.

[0085] In the present invention, the required length of ducting or pipework is reduced due to the juxtaposition and merging of auxiliary components. As a result, a significant amount of parts and space are saved (while pipe length is obvious, elbows, unions, flanges, isolation valves, strainers, filters, metal bellows, pipe hangers, anchors, lagging, and thermal tracing all add to head loss, etc.), leading to a minimum pump power reduction of 1% (this is a conservative estimate as it considers only the reduction in pipe length). With a pressure drop reduction of 0.6 to 1 bar for 6 bar (typical in PEM electrolytic cell stacks) and the pressure head generated above the liquid surface in the tank due to the relocation of the heat exchanger harness, pump power will be reduced by 10 to 16%. The ideal situation is to achieve the maximum possible bore over the shortest possible length. This represents the path for true optimization development regarding head loss and parasitic head loss. This approach is unnatural to many engineers, for whom adding parts rather than reducing them is a natural tendency.

[0086] In a preferred embodiment, a centrifugal pump, preferably a multi-stage centrifugal pump, is used in the present invention. A preferred location of the pump is illustrated in FIG. 1, namely within the pipe discharging from the separation vessel to the electrolytic cell stack. In the present invention, a multi-stage centrifugal pump is preferred because it offers better ‘turndown’ capability than a single-impeller pump and provides the best energy-saving synergy. ‘Turndown’ is generally performed when hydrogen demand is low and the required primary coolant flow rate is reduced. When hydrogen demand is partial or reduced, it is necessary to pump less fluid around the system, which is referred to as ‘turndown’. The general concept is that lowering the pump speed reduces power consumption, which is very beneficial because pump applications consume 20% of the world's electricity and eco-friendly systems must set an example in energy conservation. This is even more relevant for widely deployed electrolysis systems using very large pumps, as in the system of the present invention. It also brings significant operating cost savings to the client and provides a competitive advantage.

[0087] In a preferred embodiment, the pump is capable of achieving a lower shaft speed for the same output flow. This is referred to as load balancing capability; in other words, it is desirable for the pump of the present invention to have excellent load balancing capability. If load balancing is properly planned, it is expected to save up to 40% of pump energy consumption.

[0088] Multistage centrifugal pumps allow for greater load regulation when controlling the pump using speed, and according to the law of affinity, a greater reduction in speed results in a greater reduction in kilowatt-hours used. The synergy between the present invention and the pump selection reduces head pressure and, consequently, allows for the optimization of the number of pump stages (from 6 stages to 3 stages, see FIG. 2) as well as the benefit of load regulation capability (typically 37% for multistage pumps compared to 5% for single impellers), which is claimed to constitute the advantage of this feature by reducing the power used beyond the general norm achievable with multistage pumps or single impeller pumps.

[0089] There is a wide variety of separation technologies in the field of two-phase gas-liquid separation. The vertical knockout tower, as previously mentioned, is the simplest and most common form of modern technology, but it has the problem of being the slowest and taking up the most space among them. This is because the vertical knockout tower relies on gravity and the residence time of the gas-water mixture (and the minimum column height required to accommodate it) to cause the water to 'fall' and the gas bubbles to 'rise' from the collection outlet toward the top of the vessel.

[0090] FIG. 1 shows three nozzles connected to each pipe. Thus, this preferred embodiment divides the flow and height into a maximum of three possible parts, leading to the typical 2.6 m height selection mentioned above. This leads to more efficient separation.

[0091] In one embodiment, the present invention includes a Schoepentoeter device that divides a mixed-phase feed stream into a series of lateral flow streams and a curved flow stream. These curved streams disperse the kinetic energy of the streams to facilitate entry into a vessel and provide centrifugal acceleration to promote the separation of liquid from gas.

[0092] In some embodiments, a tangential cyclone is created within the separation vessel. This separates gas and water by relying on centrifugal acceleration. FIG. 3 shows how this can be achieved, namely by orienting the fluid flow at a constant angle to the side wall of the separation vessel.

[0093] In a preferred embodiment, nozzles are provided tangentially or nearly tangentially to generate centrifugal acceleration (this mechanism increases separation efficiency). This is illustrated in FIG. 3. The nozzles direct the flow against the walls of the vessel, and once the flow hits the bottom, it wraps around or vortices around the heat exchanger along the low curvature of the vessel, mimicking the effect of baffles placed around traditional cooling heat exchangers. Vortices and turbulence around the tubular heat exchanger are beneficial.

[0094] The vessel of the present invention may have a large number of nozzles. However, this does not add complexity because the nozzles are formed as part of a unique rotational molding vessel.

[0095] In a preferred embodiment, the present invention includes using a demister pad composed of a fine mesh or mesh grid to further remove mist from steam when separation is affected. Additional features also include a vortex breaker and a vortex spoiler.

[0096] In one embodiment, the kinetic energy of the stream is broken down by a set of wire brushes positioned coaxially at the inlet nozzle. This type of brush is known to be cost-effective in small air-gas separators.

[0097] In a preferred embodiment, the vessel walls may comprise a three-wall structure composed of expanded insulation (intended to reduce radiant heat during off-time) and polypropylene, expanded foam, and polypropylene. Lighter weight, easier handling, cleanliness, antimicrobial properties, and deployability in specific environments of varying sizes (e.g., container packaging or inside a single-story building facilitated by an appropriate aspect ratio) define utility features, and since multiple modules are efficiently connected by small-diameter pipes, they can serve all market segments. The reduction in the number of parts is significant. A single vessel is designed for applications with the most demanding requirements. Modules can be manufactured in a factory at a speed several times faster than current technology (reducing the four days currently required to manufacture an equivalent vessel to a few hours and avoiding long burr cleaning steps (reduced from two weeks to zero)). Current alkali units of the prior art inherit heavy industrial construction methods, partial-concentration design, corrosive systems, and outdated chemistry. For example, while designs such as the conversion of chloro-alkali via water electrolysis have been successfully attempted by many competitors, they are outdated in that, when formulated into a single design, little consideration was given to lean manufacturing—which is unique to the chemical / process industry, highly self-limiting, and rarely seen. Outdated plants are merely relocated and repurposed while maintaining previous physical implementations with modified electrode chemistry or coatings, with the rest being logical but temporarily adjacent. The volume of fusion welding fabrication and the weight of the steel structures used are truly enormous, reaching up to 7 meters in height—a maximum of three stories—compared to 2.6 meters according to conventional practice. Its suitability for the purpose is questionable, and it appears merely confusing when faced with the challenge of deploying hydrogen on a large scale in a rapidly changing world.

[0098] The energy cost for oxygen-air separation is 6.6 kWh / kg. Oxygen as a byproduct of hydrogen generation is not typically collected. Therefore, net economic benefits can be obtained when oxygen is pressurized. Decarburization in the steel industry, oxygen fuel, or even fish farms are just a few of the possible applications. In some embodiments, to maintain pressure, the vessel includes a composite outer structure covering a polymer wall obtained by rotational molding. Thus, in some embodiments, a metal, preferably aluminum, shell is rolled around the vessel of the present invention and secured by rivets. Preferably, at least two structural members are arranged longitudinally and perpendicularly to support and mitigate the inevitable creep of the polymer vessel under pressure.

[0099] In some embodiments, the vessel of the present invention includes ports for sensor level control (e.g., 3 ports), ports for sensor pressure control (e.g., 1 port), ports for conductivity control (e.g., 1 port), ports for deionized water circulation (e.g., 2 ports, an inlet and an outlet), ports for oxygen discharge (e.g., 1 port), ports for oxygen pressure relief (e.g., 1 port), ports for a heat exchanger (e.g., 2 ports, inside and outside), ports for a pump outlet (e.g., 1 port), ports for the return of the mixed phase (x3 in a typical embodiment), and ports for drainage (e.g., 2 ports). In total, up to 17 ports are provided, constituting a reduction over the prior art.

[0100] Preferably, the vessel for use in the present invention includes a tapered collector positioned below the heat exchanger. It is preferably connected directly to the heat exchanger. It is preferably made of a polymer material. FIG. 4 illustrates a tapered collector. Item 13 is a tapered collector (preferably made of a polymer) that is securely fastened directly below the heat exchanger and connected to the main pump inlet to channel water passing through the heat exchanger and thereby increase the velocity of the water. The pump (3) is connected to the pump outlet of the vessel and has a suction force to vigorously draw the flow through the heat exchanger to maximize the cooling duty.

[0101] The velocity homogeneity of the cross-flow through the heat exchanger is controlled by a provided taper that reduces the velocity as it approaches the pump discharge port and increases the velocity as it moves further away from the discharge port (towards the blunt end) (effectively reducing the longitudinal variation of the cross-flow) and lowers the longitudinal variation of the velocity.

[0102] Alternatively, a vessel for use in the present invention comprises a sleeve positioned around a heat exchanger. The sleeve is made of a polymer material. The sleeve comprises baffle plates arranged to maximize heat exchange by making the fluid direction around the tubes 'cross-flow' to maximize the breakdown of the boundary layer between the tubes and the fluid. The baffles, tube spacings, and tube lengths are configured to design the heat exchanger pressure drop characteristics according to FIG. 8b.

[0103] FIGS. 5a to 5c illustrate the first configuration of an oxygen separation vessel (1a). FIG. 5a illustrates a side view of the vessel (1a), FIG. 5b illustrates an end view of the vessel (1a), and FIG. 5c illustrates a cross-sectional view of the vessel (1a) through the cross-sectional line CC.

[0104] The illustrated container (1a) has three inlet nozzles (6a), five outlet nozzles (6b), a series of circumferentially parallel grooves (17), a coolant inlet port (18), and a coolant outlet port (19).

[0105] The groove (17) is formed in a shape to accommodate a bracing element, such as a metal reinforcing ring. This bracing element provides additional strength to the container (1a), thereby mitigating the risk of the container (1a) buckling due to high pressure applied to the inside of the container (1a) during use.

[0106] As illustrated in FIGS. 5b and 5c, the inlet nozzles (6a) are positioned at a predetermined angle (about 45 degrees in the illustrated example) so that when in use, the fluid flow is directed toward the (flat) side wall of the container to create a cyclone / centrifugal force effect (as previously described).

[0107] As illustrated in FIG. 5c, an internal conduit (20) is formed between the coolant inlet port (18) and the coolant outlet port (19). This internal conduit allows the coolant to flow through the vessel (1a) and may have additional channels (which may be connected to one or more outlet nozzles (6b)) to allow other fluids, such as water separated from the water / oxygen mixture, to flow. The internal conduit (20) may also function as a heat exchanger (or accommodate a heat exchanger) and may have additional components not illustrated that allow it to function as such a heat exchanger (e.g., the one in FIG. 8b) or accommodate such a heat exchanger.

[0108] A second configuration of the container (1b) is illustrated in FIGS. 6a to 6d. FIG. 6a illustrates a graphic projection of the container (1b), FIG. 6b illustrates a side view of the container (1b), FIG. 6c illustrates a bottom view of the container (1b), and FIG. 6d illustrates an end view of the container (1b).

[0109] The vessel (1b) has three inlet nozzles (6a), five outlet nozzles (6b), two oxygen outlets (22) located at the top of the vessel (1a), a coolant inlet (18), and a coolant outlet (19). Unlike the vessel (1a) of FIGS. 5a through 5c, the vessel (1b) of FIGS. 6a through 6d does not have grooves, but instead has a plurality of transverse through holes (21) between the side walls of the vessel (1b). The illustrated through holes (21) have a cross-section that is (substantially) circular. The exemplary vessel (1b) has nine holes spaced at regular intervals, but alternative numbers of holes, such as four, six, or eight, may be used.

[0110] Each hole (21) is provided to accommodate a bracing element, such as a connecting rod or similar, capable of maintaining tensile strength. When in use, the bracing element reinforces the vessel (1b) against high internal pressure, thereby preventing the vessel (1b) from buckling or otherwise breaking / deforming. Using through holes instead of grooves (as in FIGS. 5a through 5c) means that the sidewalls of the vessel (1b) can be manufactured smoothly while maintaining the strength and integrity of the vessel (1b). Since having smooth sidewalls is easier to manufacture than grooved sidewalls, the use of through holes (21) further allows for easier and cheaper production than grooved vessels.

[0111] FIGS. 7a through 7d illustrate other alternative containers (1c). FIGS. 7a through 7d correspond to FIGS. 6a through 6d, respectively.

[0112] The vessel (1c) is similar to the vessel of FIGS. 6a through 6d, except that the nine circular through holes are replaced with six through holes (21) having a substantially square cross-section. It should be understood that the through holes may have other cross-sections, such as (substantially) elliptical, (substantially) rectangular, etc., and may be selected according to tool requirements during manufacturing and / or the type of bracing element to be used. Similarly, there may be more or fewer through holes. In any case, it is desirable that the through holes (21) be regularly spaced to ensure a uniform distribution of the load by the transverse bracing elements.

[0113] FIGS. 8a to 8d illustrate the container (1b) of FIGS. 6a to 6d provided with reinforcing elements. FIGS. 8a to 8d correspond to FIGS. 6a to 6d, respectively.

[0114] The vessel (1b) is provided with an outer sheet cladding (23), preferably made of EN 10028 P460 pressure steel or an equivalent steel. The cladding (23) helps maintain the integrity of the vessel during use and mitigate the risk of buckling or similar buckling by reinforcing the vessel (1b).

[0115] Additionally, the container is provided with transverse bracing elements (24) that are received within the through hole (21) in the form of transverse connecting rods. These bracing elements (24) are preferably made of steel, and alternative transverse bracing elements may be used instead of connecting rods.

[0116] Although the cladding (23) and the transverse bracing element (24) each provide a significant reinforcing effect individually, when the cladding (23) and the transverse bracing element (24) are used in combination, the bracing element (24) helps to distribute the load applied to the side wall of the container (1b), and consequently, the load that the container (1b) can withstand before it breaks or buckles is increased, thereby further enhancing the reinforcing effect.

[0117] In addition to the cladding (23), the vessel (1b) is provided with two end plates (25), each of which is located at opposite ends of the vessel (1b). The end plates (25) are connected by longitudinal bracing elements (26), which may be connecting rods or similar and are preferably made of steel. The longitudinal bracing elements (26) extend between the end plates (25) and are joined at each end to one of the end plates (25). In this way, the end plates (25) combined with the longitudinal bracing elements (26) provide reinforcement to the vessel (1b) and prevent the vessel from buckling or breaking due to high internal pressure experienced during use. Preferably, there are four longitudinal bracing elements (26), for example, joining each corner portion of one end plate (25) to the corresponding corner portion of the opposite end plate (25).

[0118] The end plate (25) is made of steel, such as EN10028 P460 pressure steel or an equivalent.

[0119] Although the cladding (23), bracing elements (24, 26), and end plates (25) have been described in relation to the vessel (1b) illustrated in FIGS. 6a through 6d, they may also be used with other vessels such as those shown in FIGS. 7a through 7d. To use the transverse connecting rod (24), the vessel must have a through hole (21), but the cladding and end plates may be used with vessels that do not have a through hole.

[0120] Alternatively, the rolled aluminum or steel shell form can be replaced with a glass fiber semi-cylindrical shell form (responding to lightweight and tensile stresses on the circular part of the vessel), while the sidewalls (responding to bending stresses) can be manufactured of ductile steel or aluminum.

[0121] FIGS. 5a through 5c, FIGS. 6a through 6d, FIGS. 7a through 7d, and FIGS. 8a through 8d are technical drawings and depict a vessel at actual scale, that is, at an actual scale where the proportions of the drawings are accurate. All dimensions provided in these drawings are provided in millimeters (mm). The dimensions illustrated in these drawings are preferred values ​​but should not be construed as limiting unless otherwise indicated in the claims.

[0122] It should be understood that in any of the above examples, the number of inlet nozzles (6a) can be changed. In the above examples, there are three nozzles, but alternatively, there may be one, two, four, or more nozzles. However, it is preferable to have more than one inlet nozzle because the inlet nozzles can create multiple columns of mixture within the vessel, thereby greatly improving the separation speed for a given vessel height, which can make the vessel much shorter than a conventional oxygen separation vessel.

[0123] Not all exemplary vessels are depicted with an oxygen outlet (22), but the oxygen outlet has been omitted for the sake of simplicity in the drawing and it should be understood that each vessel is intended to have at least one oxygen outlet.

[0124] Any of the containers of FIGS. 5a to 5c, FIGS. 6a to 6d, FIGS. 7a to 7d, and FIGS. 8a to 8d can be used in combination with the system described above with reference to FIGS. 1 to 4.

[0125] The vessel may be referred to interchangeably as a gas separation vessel or an oxygen separation vessel. A preferred embodiment of the vessel is as an oxygen separation vessel for separating oxygen from a mixture containing oxygen and water (particularly in the context of green hydrogen generation from renewable electricity), but it is also possible to separate other gases from other mixtures. Generally, due to the unstable / volatile nature of the oxygen / hydrogen mixture, oxygen and water are separated in several stages. Explanation of the symbols

[0126] 1. Phase-separated heat exchange O2 pressure one-shot molded vessel (1a, 1b, and 1c represent various vessel configurations) 2. Secondary cooling circuit 3. Pump 4. Electrolysis stack(s) 5. Heat exchanger 6. Molding nozzle (6a is the inlet nozzle / port, 6b is the outlet nozzle / port) 7. Low temperature supply 8. High-temperature exhaust outlet 9. Water / Oxygen Mixture 10. Pressure Reduction Section 11. Primary Cooling Circuit 12. Maximum 3-story wall 13. Composite Material Pressure Shell 14. Antimicrobial additives 15. Generated turbulent region 16. H2O Collector 17. Container Home 18. Coolant Inlet Port 19. Coolant drain port 20. Internal conduit 21. Penetrating hole 22. Oxygen outlet 23. External Cladding 24. Crossing connecting pole 25. End plate 26. Longitudinal connecting rod

Claims

Claim 1 A system comprising an electrolytic cell stack and a water / gas separation vessel connected through an inlet pipe and an outlet pipe, wherein the separation vessel is configured to passively separate water and gas; wherein the separation vessel includes a heat exchanger; wherein the separation vessel is composed of a polymer material; wherein the separation vessel includes a plurality of inlet nozzles for receiving a mixture of water and gas, and wherein the plurality of inlet nozzles are arranged at an angle between 30 and 60 degrees with respect to the side wall of the separation vessel, such that when in use, the fluid flow is directed toward the opposite side wall along the curvature of the side wall of the separation vessel to produce a cyclone effect. Claim 2 A system according to claim 1, wherein the separation container further comprises a plurality of discharge nozzles for connecting each of the discharge pipes, and the inlet and discharge nozzles are integral with the container and are composed of the same polymer material as the container. Claim 3 In paragraph 2, the system comprises at least four nozzles configured such that at least two nozzles are in fluid communication with each pipe. Claim 4 A system according to paragraph 2, comprising at least six nozzles configured such that at least three nozzles are in fluid communication with each pipe. Claim 5 In claim 1, the system wherein the container is rotationally molded from a polymer material in a single one-shot process. Claim 6 In claim 1, the system, wherein the pipes are composed of a polymer material. Claim 7 In paragraph 2, the above nozzles are connected to a pipe by polymer fusion, in a system. Claim 8 In claim 1, the container is a system having a flat elliptical cross-section in which the flat side walls are positioned vertically when in use. Claim 9 delete Claim 10 A system according to paragraph 2, wherein a wire brush is positioned coaxially within at least one nozzle so as to cause the kinetic energy of the fluid stream to collapse during use. Claim 11 A system according to paragraph 2, wherein a vortex crusher, a vortex spoiler, or a demister pad is located within at least one of the inlet pipe and the outlet pipe. Claim 12 A system according to claim 1, wherein the ratio of the container is such that the ratio of the height to the width of the container is less than 3:1 or 2:

1. Claim 13 In claim 1, the system, wherein the container comprises an antibacterial or antifungal additive. Claim 14 In paragraph 1, the system wherein the heat exchanger is a tubular heat exchanger. Claim 15 In claim 1, the system is configured such that the heat exchanger uses water, for example, seawater, as a coolant. Claim 16 In claim 1, at least one pipe comprises a pump for enabling fluid flow around the system when in use, a system. Claim 17 In Clause 16, the above pump is a centrifugal pump, in the system. Claim 18 In claim 1, the system comprises a container having ports for sensor level control, sensor pressure control, conductivity control, deionized water circulation, oxygen pressure relief, or connection to a heat exchanger. Claim 19 A system according to claim 1, having a tapered collector positioned between the heat exchanger and the discharge pipe from the vessel to increase the fluid flow velocity to the discharge pipe during use. Claim 20 A method for electrolyzing water using a system according to any one of claims 1 to 8 and claims 10 to 19, wherein water is contained in a gas / water separation vessel, an electrolytic cell electrolyzes the water to produce hydrogen and oxygen, and then the hydrogen and oxygen flow through a pipe to the separation vessel, and one or both of the hydrogen and oxygen are passively separated from the water and extracted from the system. Claim 21 An oxygen separation vessel for passively separating water from a mixture of oxygen and water, comprising: a plurality of inlet nozzles for receiving the mixture of oxygen and water; a heat exchanger located within the vessel for cooling the mixture of oxygen and water; at least one oxygen outlet for discharging oxygen separated from the mixture of oxygen and water; and at least one water outlet nozzle for discharging water separated from the mixture of oxygen and water, wherein the plurality of inlet nozzles are arranged at an angle between 30 and 60 degrees with respect to the side wall of the separation vessel, so as to direct the fluid flow toward the opposite side wall along the curvature of the side wall of the separation vessel during use to produce a cyclone effect. Claim 22 In claim 21, the oxygen separation container, wherein the container is composed of a polymer material. Claim 23 An oxygen separation vessel according to claim 21, wherein the inlet nozzles are located in an area defined by the upper 25% of the oxygen separation vessel. Claim 24 An oxygen separation vessel according to claim 21, further comprising at least one through hole for accommodating a transverse bracing element. Claim 25 An oxygen separation vessel according to claim 24, further comprising a transverse bracing element received in at least one through hole. Claim 26 An oxygen separation vessel comprising an outer sheet cladding in paragraph 21. Claim 27 In paragraph 26, the above-mentioned outer sheet cladding is an oxygen separation vessel made of steel. Claim 28 An oxygen separation vessel according to claim 21, wherein the vessel comprises at least one circumferential groove for accommodating a circumferential bracing element. Claim 29 An oxygen separation vessel according to claim 21, further comprising two outer end plates disposed at opposite ends of the vessel, wherein the outer end plates are joined by one or more longitudinal bracing elements. Claim 30 In paragraph 29, the above outer end plate is an oxygen separation vessel made of steel. Claim 31 An oxygen separation container according to claim 21, wherein the plurality of inlet nozzles and the at least one water outlet nozzle are integral with the container and are made of the same material as the container. Claim 32 In paragraph 21, the oxygen separation vessel, wherein the plurality of inlet nozzles are located at substantially the same height. Claim 33 In Clause 21, the oxygen separation vessel, wherein the above-mentioned vessel is rotationally molded in a single one-shot process. Claim 34 In claim 21, the oxygen separation vessel having a flat elliptical cross-section in which the flat side walls are positioned vertically when in use. Claim 35 In paragraph 34, the oxygen separation vessel, wherein the inlet nozzles are positioned to direct the fluid flow toward the flat sidewall of the vessel when in use to produce a cyclone or centrifugal effect. Claim 36 An oxygen separation vessel according to claim 21, wherein the inlet nozzles are positioned to direct the fluid flow toward the opposite side wall along the curvature of one side wall of the vessel when in use. Claim 37 In claim 21, the oxygen separation container, wherein the container is composed of high-performance hexane high-density polyethylene. Claim 38 An oxygen separation vessel according to claim 21, further comprising a tapered collector positioned between the heat exchanger and the at least one water outlet nozzle. Claim 39 In Clause 21, the above heat exchanger is an oxygen separation vessel that is a tubular heat exchanger. Claim 40 An oxygen separation vessel comprising, in addition to the sleeve disposed around the tubular heat exchanger in paragraph 39. Claim 41 An oxygen separation vessel according to claim 40, wherein the sleeve comprises an inlet, an outlet, and one or more baffle plates arranged to allow fluid to flow in an orthogonal direction around a heat exchanger during use. Claim 42 A hydrogen generation system comprising an electrolytic cell stack connected to an oxygen separation vessel according to any one of claims 21 to 41. Claim 43 A hydrogen generation system according to claim 42, further comprising a pump connected to at least one water outlet nozzle, said pump located downstream of the oxygen separation vessel.

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