WO2012014197A1 - Hydrogen generating system and apparatuses thereof - Google Patents

Abstract

The present invention is directed to a system for obtaining hydrogen and valuable byproducts by water split reaction using fuel metal as a consumer of oxygen and/or OH from water and aqueous alkali metal hydroxide solution as a catalyst and/or as a fuel metal oxide/hydroxide consumer; said system comprising at least one reactor, controlling programmable device, at least one element adapted for directing said reaction products, at least one element adapted for keeping given hydrogen output parameters during a given operation time, at least one element adapted to allow fast starting-up and/or breaking down the reaction, and at least one element for emergency situation.

Description

HYDROGEN GENERATING SYSTEM AND APPARATUSES THEREOF

FIELD OF THE INVENTION

The present invention is generally related to hydrogen production via water split reaction on metal partitions in a solution of alkali metal, and to a system for producing hydrogen gas by water split reaction with fuel metal consuming oxygen and forming metal oxide/hydroxide, alkali metal hydroxide serving as reaction catalyst and/or reagent consuming said fuel metal oxide/hydroxide and to an apparatuses for carrying out and controlling said reaction in particular.

BACKGROUND OF THE INVENTION

It is well known in the art that under certain conditions, aluminum, silicon and other metals react with water to generate hydrogen. It is also known, however, that this type of reaction is hard to control. A protective oxide layer exists on a metal surface and forms in contact with water at ambient temperature and inhibits the reaction. Therefore, the protective oxide layer should be efficiently and continuously removed before reaction, in starting period and in course of reaction. It is known also that the reaction can develop in spontaneous manner with strong self-heating what should be avoided.

A number of systems and reactors for hydrogen generation have been developed in the past. A short review of related patent documents is established below.

U.S. Patent No. 909,536 issued on Jan. 12, 1909, and U.S. Pat. No. 934,036 issued on Sep. 14, 1909, both issued to G. F. Brindley et al. These documents disclose several compositions for generating hydrogen. The compositions comprise any metal which can form a hydroxide when it is brought into contact with a solution of a suitable hydroxide. For example, aluminum is reacted with sodium hydroxide to release hydrogen and produce sodium aluminate.

U.S. Patent No. 2,721,789 issued on Oct. 25, 1955 to Q. C. Gill. This document discloses the structure of a hydrogen generator for reacting water with a measured dry charge of aluminum particles and flakes of sodium hydroxide. The reaction releases hydrogen gas and produces sodium aluminate. U.S. Patent No. 3,554,707 issued on Jan. 12, 1971 to W. A. Holmes et al. This document discloses a gas generator having bellows to raise or lower the level of water in response to the pressure inside the generator. As the level of water drops, the contact surface between the fuel cartridge and the water is lost and the reaction is terminated.

U.S. Patent No. 3,957,483 issued on May 18, 1976 to M. Suzuki. This patent discloses a magnesium composition, which produces hydrogen upon contact with water. The preferred magnesium composition comprises magnesium, and one or more metals selected from the group consisting of iron, zinc, chromium, aluminum and manganese.

JP 401,208,301 issued to Mito on Aug. 22, 1989. This document discloses a process for producing hydrogen. Aluminum is reacted with water under an inactive gas or water to release hydrogen gas and produce sodium aluminate.

U.S. Patent No. 6440385 Bl issued on Aug. 27. 2002 to A. Chaklader discovered that ball milling of aluminum with aluminum oxide results in producing significantly more hydrogen than the same aluminum without milling.

U.S. Patent No. 6582676 published on April 24, 2003 to A. Chaklader. This patent aimed hydrogen generation by reacting Aluminum (Al), Magnesium (Mg), Silicon (Si) and Zinc (Zn) with water provides a catalyst or other additive to prevent or slow down deposition of the reaction products on the metal surface that tends to passivate the metal and thereby facilitates the production of hydrogen.

According to U.S. Patent No. 7534275 issued on May 19, 2009 to Tonca, the anti- passivation material is selected from group consisting of alumina, ceramic compounds containing aluminum ions, carbon (C), calcium carbonate (CaCO.sub.3), calcium hydroxide (Ca(OH).sub.2), polyethylene glycol (PEG), and combination thereof, magnesium oxide (MgO), silicon dioxide (SiO.sub.2), and (ZnO).

Various other processes and reactors to produce hydrogen gas have been described in the art, as reacting water with magnesium, sodium, potassium, lithium, calcium, iron, zinc or steel.

The following disadvantages of the prior art should be noted: too slow start-up of reaction with following too sharp temperature rise, precipitation solid reaction products on fuel metal active surfaces, use the anti-passivation reagents what create difficulties with utilization the byproducts, use the methods for increasing fuel metal surfaces what is both expensive and forms relative high mass of oxide film.

Although the hydrogen production processes of the prior art are well studied as chemical, thermodynamic and engineering problems, it is believed that 3-phase (hydrogen - fuel metal solution) chemical, adsorption - desorption and hydrodynamic processes were not taken into account adequately especially for long-time operations. Thus, conditions leading to hydrogen release in a range from single bubble growing on the surface to massive bubbling and conditions of solid products precipitation should be known.

As such, it will be appreciated that the hydrogen generating system and apparatuses thereof will be designed with a glance on the complex of interactions among fuel metal surface, alkali metal hydroxide, alkali metal metalate solution and hydrogen under different conditions of temperature and pressure. The present invention is based mainly on the inventors' experimental findings.

SUMMARY OF THE INVENTION

Broadly stated, the process for producing hydrogen gas according to the present invention consists of splitting water to hydrogen and oxygen. The fuel metal is used to bond chemically the water's oxygen what allows hydrogen releasing but simultaneously the metal oxide/hydroxide forms. The alkali metal hydroxide is used as a catalyst of this reaction or as reagent which bonds chemically the freshly formed fuel metal oxide/hydroxide to form metalate, which is dissolved in water and shifts the water split reaction to hydrogen yield raise. From the inventors experience and literature data it is known that generated hydrogen can be dissolved in solution, form alkali - fuel metal tetrahydride, be absorbed by fresh metal surface and create aluminum hydride. The small hydrogen bubbles can merge into large ones which rise with high speed creating pressure fluctuations. The alkali metal metalate can decompose to fuel metal oxide and alkali metal hydroxide what accelerates the reaction rate. The reaction heat and temperature influence strongly on listed processes. These circumstances make the total process very complex as several chemical and physical processes go simultaneously. So set of means are foreseen to provide given hydrogen parameters. This process is advantageous for being applied to any reactive fuel metal of any partitions shape and for providing needed hydrogen yield both for short and long time demand.

In accordance with another feature of the present invention, all surfaces of the reactive fuel metal partitions are immersed in liquid-gas layer. This method is advantageous for providing the ability to control the intensity of the reaction between the solution and fuel metal because one of the process variables - surface is known. It can be calculated in course of metal dissolving and used for process control.

In accordance with another feature of the present invention, a fuel metal bed organizing and liquid-gas mixture movement provides control on reaction rate.

In another aspect of the present invention, the own hydrogen produced and/or external gas bubbling through the bed create a liquid - gas stream which tears away from the surface small hydrogen bubbles, creates movement of metal partitions and takes away from the metal surface the forming non gaseous products. Therefore, there is no needs in anti-passivation means thus high cleanness both hydrogen and byproducts is provided.

In yet another aspect of the present invention there are means provided to remove solid byproducts and prevent fuel metal surface passivation: The means include overflow receptacle(s) for separation solid products of reaction from circulating solution, the distance between fuel metal partitions and bottom of reactor, plates and cartridges as well filter between reactors. The removed products can be treated with obtaining valuable byproducts, as will be described in the following.

An important economical aspect of the present invention is obtaining molecular sieves both known types and novel family synthesized under hydrogen partial pressure; these syntheses operational pressure and heat can be utilized from hydrogen production.

The system of the present invention uses the hydrogen output, pressure and temperature of a reaction occurring between a fuel metal and the water contained therein to control the intensity of the reaction by feeding water and/or alkali metal hydroxide solution and/or alkali metal metalate solution, by external gas flow or/and liquid circulation rate and direction. The processes and system according to the present invention are practical and safe for much energy, heat and pressured hydrogen customers in different situations for example, in remote locations either floated or on shore, where electricity is not available.

Furthermore, the method and system according to the present invention use metals waste readily available in domestic garbage and transient stations. Accordingly, the invention relates also to an environmental protection issue.

The large amount of metal waste of constant quality from the metal working shops can be used for preparing such valuable products as metal hydrides, metal oxides, hydroxides, alkali metal metalates, zeolites and catalysts simultaneously with hydrogen, pressure and heat. In case of aluminum shop the hydrogen production byproduct, aluminum hydroxide, can be used as adding to bauxite (recycled).

Thus, it is the aim of the present invention to provide a system for obtaining hydrogen and valuable byproducts by water split reaction using fuel metal as a consumer of oxygen and/or OH from water and aqueous alkali metal hydroxide solution as a catalyst and/or as a fuel metal oxide/hydroxide consumer; said system comprising at least one reactor, controlling programmable device, at least one element adapted for directing said reaction products, at least one element adapted for keeping given hydrogen output parameters during a given operation time, at least one element adapted to allow fast starting-up and/or breaking down the reaction, and at least one element for emergency situation.

It is a further aim of the invention to provide a system for obtaining hydrogen and fuel metal valuable byproducts by water split reaction using fuel metal and aqueous alkali metal hydroxide solution, wherein at least part of said hydrogen obtained is re-circulated into said reaction medium to intensify the removal of reaction products from said fuel metal surface so as to prevent passivation and further to push away both small hydrogen bubbles and solid particles attached to said fuel metal surface.

The advantages and novel features of the present invention will become apparent from the following detailed description of the preferred embodiment. BRIEF DESCRIPTION OF THE DRAWINGS

Preferred embodiments of the present invention selected by way of examples will be described now with reference to the accompanying drawings, in which:

Figure 1 is a schematic diagram of a preferred hydrogen production system in accordance with variations of the present invention illustrating all stages of the hydrogen production process including usage of external gases for process controlling.

Figure 2 is a schematic cross-section view of a reactor in accordance with variations of the present invention, illustrating an optional mode of operation thereof, when the fuel metal partitions are hanged up, reactor has a helmet, a solid products receptacle in form of packed bed of plastic rings and an external gas input.

Figure 3 is XRD diffractogram of a byproduct obtained in Example 1. The byproduct has Bayerite structure.

Figure 4 is a schematic illustration of the dependence of the reaction rate on reaction time in reactor without circulation means. The figure illustrates a typical view of such dependencies with slow start-up followed with sharp temperature rise.

Figure 5 is a schematic illustration of the dependence of the reaction rate on the reaction time, wherein the reactor comprises means for solution circulating. In comparison with the results illustrated in Figure 4, the results illustrated in figure 5 shows smoothing of the reaction rate.

Figure 6 is a graphic illustration of pressure (bar), and hydrogen output (mL/min) vs. time (min) (2-nd stage of NaOH input). The results represent a typical evolution of the reaction rate in time.

Figure 7 is XRD diffractogram of the byproduct obtained in Example #8. The mixture of Bayerite and Gibbsite was obtained.

Figure 8 is a schematic block diagram of hydrogen gas and liquid and byproducts applications. DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS

While this invention can be realized in many different embodiments, there is shown in the drawings and will be described in details herein a specific variations and examples of the system and methods according to the present invention, with the understanding that the present disclosure is to be considered as an example of the principles of the invention and is not intended to limit the scope of the invention to the embodiment illustrated in any way.

It is the aim of the present invention to provide a system for obtaining hydrogen and valuable byproducts by water split reaction using fuel metal as a consumer of oxygen and/or OH from water and aqueous alkali metal hydroxide solution as a catalyst and/or as a fuel metal oxide/hydroxide consumer; said system comprising at least one reactor, controlling programmable device, at least one element adapted for directing said reaction products, at least one element adapted for keeping given hydrogen output parameters during a given operation time, at least one element adapted to allow fast starting-up and/or breaking down the reaction, and at least one element for emergency situation. Elements adapted for keeping given hydrogen output parameters may affect for example the flow rate, the pressure, the temperature, and the humidity of the reaction during a given operation time. An emergency situation in accordance with the present invention may include without limitation a fire, an explosion, gas leakage, gas reception interruption.

In accordance with the system provided herein, fuel metal may be selected from the group consisting of aluminum (Al), chromium (Cr), iron (Fe), magnesium (Mg), manganese (Mn) silicon (Si), zinc (Zn), mixtures and alloys thereof, while alkali metal may be selected from the group consisting of: sodium (Na), potassium (Mg), lithium (Li) and calcium (Ca) or mixture thereof.

The reactor may be filled with at least one fuel metal partition selected from the group consisting of: porous and non-porous powders, flakes, rods, strips, spirals, multi- layered materials, tubes, plates, slabs and profiled articles. The number and shape of the fuel metal partitions, hydrodynamic regime of liquid-gas mixture's movement, and composition of solution are functionally chosen to provide a given reaction rate (mL/min cm2).

In accordance with variations of the invention, the elements adapted for keeping given hydrogen output parameters during a given time may include at least the following: water supply, current solution supply, concentrated alkali metal hydroxide solution supply, alkali metal metalate solution supply, hydrogen receiver equipped with pressure regulator, back flow preventing device, heater, pulsator, liquid and/or gas circulators, and an external gas input. The water, current solution, concentrated alkali metal hydroxide solution, and alkali metal metalate solution tanks may functionally be connected with the reactor in both gas and liquid spaces.

In accordance with variations of the system provided herein the interior arrangement of the reactor functionally allows directing of said reaction products. The interior arrangement of the reactor may comprise a deposition of fuel metal partitions in a manner minimizing formation of dead spaces on fuel metal surfaces for both hydrogen bubbles and solution. Deposition of special inactive articles functionally allows reception of solid reaction products. In such variation, the fuel metal partitions may have a shape that functionally provides vertical channels adapted for liquid-gas mixture movement, such as a honeycomb form, a cone-like or prismatic-like form positioned by narrow end downwards. Preferably, at least one fuel metal partition is suspended or uplifted so that there is enough space between its lower end and a receptacle for collecting solid reaction products. The receptacle may be a bed of inactive media. In such scenario, the rector's bed is self-supporting during fuel metal dissolving being composed as a bundle of fuel metal and inactive material tube-like partitions.

In accordance with one another variation of the invention, the reactor may be a tray column having at least one perforated plate supporting fuel metal partitions. The plate is preferably made of inactive material, and more preferably the reactor is a multi- plate reactor. In yet a further variation, the perforated plate has at least one overflow channel with overflow receptacle for solid byproducts. The reactor may further have at least one external gas input below partitions to intensify the removal of reaction products from said fuel metal surface, so as to prevent surface passivation. Preferably, the reactor has at least one external gas distributor below partitions. The external gas may be either one of hydrogen, nitrogen, argon and helium, and mixtures thereof.

One product produced by the system provided herein may be a hydrogen-nitrogen mixture. This product may be adapted for either one of ammonia production or hydrogen burning, or both.

In a preferred variation, the external hydrogen is part of the system's own product provided by gas circulation means. However, the external hydrogen for circulating the components comprised in the reactor may be produced by one another reactor under pressure higher than the pressure in the first reactor.

In accordance with additional variation of the system presented herein the reactor may comprise at least one plate consisting of perforated tubes that are functionally adapted to allow external gas distribution so as to constantly avoid surface passivation and push small hydrogen bubbles out the surface). In a preferred variation, the reactor comprises more than one plate having an external gas feeding. Also, the reactor may have insulation and gas or liquid circulation for minimizing effect of ambient temperature fluctuation on the reaction rate during the day time.

The system provided herein may further comprise at least one heater either inside the reactor or an external heater. The heater functionally allows intensifying the reaction rate.

In accordance with the system of the present invention, the controlling programmable device is functionally adapted for keeping at least the product gas flow rate, pressure and temperature inside the reactor in given ranges, by feeding said reactor with either one of an external gas, water, hydroxide solution, alkali metal metalate solution, and mixtures and combinations thereof. Keeping product gas flow rate, pressure and temperature inside the reactor in given ranges may further be obtained by using either one of a heater, a circulating compressor, a reversible circulating pump, a pulsator, and combinations thereof. The controlling programmable device may further allow filling the reactor with water when it is free from solution to allow storage of the remained fuel metal under water. It may further allow cleaning of the reactor by dissolving solid byproduct and drainage of the solution out of the system. The controlling programmable device may further be adapted to allow operation of the system along with the emergency situation element. The emergency situation element may comprise at least one of the following components: a nitrogen supplier, current solution tank, alkali metal metalate reservoir, a torch, flame arrestor, drainage tank and bypass between said reactor and receiver.

The system may further comprise bypass between reactor and pressure vessel as an emergency situation element for increasing gas volume within the reactor in case of drainage of liquid from the reactor to the current alkali metal hydroxide solution tank.

The controlling programmable device may further allow operation of the system provided herein together with a start-up element that may include at least one of the following components: special helmet in the topmost of reactor, high-surface partitions, start-up reactor, nitrogen supplier, alkali metal solution reservoir, alkali metal metalate reservoir, a torch, a flame arrestor and a drainage tank.

In accordance with one another variation the system comprises at least two reactors wherein solution is periodically being transferred from one reactor to the other and back trough a media collecting solid byproducts. In such variation, first reactor is adapted to produce hydrogen and byproducts from synthesis of molecular sieve or catalyst, while second reactor is functionally adapted for processing the byproducts of the first reactor. Byproducts from first reactor may be delivered to the second reactor either by pump or simply by gravitation force. The byproducts are either one of aluminum oxide and/or Boehmite, Gibbsite, Bayerite.

The products produced within said second reactor may consist of the following: fuel metal oxide, fuel metal hydroxide, molecular sieve and fuel metal containing catalyst. Specific examples for such products produced within the second reactor are either one of zeolite and fuel metal containing catalyst such as Ni-Al mixed catalyst for N20 decomposition, Cu-Al catalyst for oxidation of phenol aqueous solutions.

In a preferred variation of the invention, all features of hydrogen generation system are optimized to obtain clean target byproduct. The target byproduct may be either one of the group consisting of: sodium metalate, metal hydroxide, and metal oxide.

The system of the present invention may functionally be used as a gas supplier for fuel cell, either on board or on shore. Such fuel cells may be used for example for driving pump and/or pulsator and/or compressor.

The system presented herein may further be used a gas supplier for production of liquid hydrogen.

The system presented herein may further be used as an energy supporting system for energetic systems depending on current climate conditions such as photovoltaic and wind. In fact, the system of the present invention may functionally be used as a remote and decentralized source of energy, preferably, by using water as hydrogen/energy safe storage.

The present invention is further aimed to provide a system for obtaining hydrogen and fuel metal valuable byproducts by water split reaction using fuel metal and aqueous alkali metal hydroxide solution, wherein at least part of said hydrogen obtained is re-circulated into said reaction medium to intensify the removal of reaction products from said fuel metal surface so as to prevent passivation and further to push away both small hydrogen bubbles and solid particles attached to said fuel metal surface.

The present invention is further aimed to allow producing green fuels energy (G F E) by recycling at least part of said byproducts obtained in by the system presented herein. The green fuel energy may functionally allow to handle environmental pollution by using molecular sive and/or zeolites which can be replaced by cations . Reference is now made to Figures 1, 2 and 3. Figure 1 is a schematic illustration of one variation of a system for long-time autonomous operation with given H₂ output, pressure, duration and one-time loading of the chemicals in accordance with the present invention. Fuel metal, alkali metal hydroxide and water are the porous aluminum rods with stainless steel ringbolts, sodium hydroxide and tap water correspondingly. The system may comprise a controlling programmable device (not shown) with level, pressure, temperature and amount of produced hydrogen sensors for keeping given hydrogen output, for adjusting water and sodium hydroxide solution addition in the reactor during the operation. The system includes a reactor, receiver, tanks, and a fuel cell, and it is driven by it circulation compressor (Fig. 1). The fuel cell illustrated is onboard fuel cell, however an on shore fuel cell may also be used mutatis mutandis.

In accordance with one variation of the invention, Reactor Rl (Fig.l) that is illustrated in more details in figure 2, is an apparatus with a sealed housing 10 and an interior upper support grid 20 to which aluminum rods 30 are hanged up. Preferably, all surfaces of reactor Rl are inactive surfaces: inner walls of reactor, support grid and ringbolts excluding bottom solution output that are being protected by plastic films 40. To the end of operation this plastic film is covered with film of solid products. Lower part of the reactor is loaded randomly with 6 mm polypropylene Raschig rings 50 adapted for reception of solid reaction products precipitated from the solution. The waste chips 60 of the same aluminum (start-up mean) are preferably placed above rings 50. External gas is supplied to distributor 70. Reactor can be vertical or horizontal. A helmet 80 is foreseen in the topmost of the reactor; due to its small volume the gas pressure inside helmet raises rapidly and supplying a consumer with gas of needed pressure in start-up period accelerates.

A gas receiver R2 (fig. 1) is calculated on daily production and assigned for smoothing the fluctuations of hydrogen output from the reactor. Receiver R2 is functionally connected with reactor Rl by three lines. One of them is the gas output from reactor Rl with back pressure device vl preventing passing gas from receiver to reactor when reactor's pressure becomes lower than receiver's one. The second connection is a bypass of back pressure device, from receiver to reactor; valve v2 opens when liquid is drained from reactor Rl; gaseous space of the reactor increases, pressure drops but should be compensated. The third line serves for draining water or liquid, which can be separated in the receiver from the gas, to reactor; that can be performed by valves v3 and v4 when pressure in reactor becomes lower than in receiver. The receiver is equipped with over-pressurization relief valve v5 after which gas passes a flame arrestor R3 and torch R4 for popping. The given product gas pressure is kept by gas regulator v6.

A water tank Tl is equipped with level sensor; it is positioned over reactor Rl and can supply water by gravitation force: to the reactor trough valves v7, v4, to gas receiver R2 (in start-up period) trough valves v7, v4 and to current solution tank T2 trough valves v7, v8. Tl is connected with reactor Rl by gas space through valves v9, vlO.

The current solution tank T2, which is also positioned above reactor Rl but below Tl and connected by gas phase with reactor Rl through valves v9, vl 1 feeds periodically the reactor over the operation time through valves vl2, vl3. The current solution tank T2 and connected with T2 by two lines in its upper (valve vl4) and bottom (valves vl5, vl6) parts.

In emergency situation such as fire, an explosion, gas leakage, gas reception interruption and any other situation that may endanger the system existence and functionality and threat the environment or human life, the current solution from the reactor Rl is transferred by hydrogen pressure through valves v4, v8 and if any by nitrogen pressure (through valve vl7) into tank T2. The bottom of the latter has layer of plastic rings to retain the precipitate from current solution when it comes from reactor. All vessels have nitrogen input and lines to flame arrestor (not shown).

Before system starts, receiver R2 is filled with water up to level that is a little below the line of gas input and output to have small gaseous space. The lines connecting reactor and all tanks are closed (valves v4, v9 and vl3). AH tanks are blown off with nitrogen up to oxygen absence; valve vl8 is closed and nitrogen pressure rises to 2-3 bar. The alkali metal solution of the concentration known from the model studies is prepared in tank T2. It is loaded into reactor Rl by valves vl2, vl3 up to helmet underside's level; and the reaction starts. Nitrogen input (vl7) begins to blow off the air from the reactor and receiver (trough flame arrestor and torch), to propagate solution in the reactor and create its circulation. The blowing is performed until oxygen absence. Then nitrogen valve vl7 is closed and pressure rises only due to reaction of aluminum chips. Under 2-3 bar pressure the gas is sent in turn to all tanks. Its release continues till nitrogen absent will be fixed. Then all gas valves of the tanks and before torch (vl8) are closed again. The hydrogen output and pressure in reactor (in the helmet) and receiver are enhanced to a level allowing putting in operation small on board fuel cell CI, which in turn activates a circulating compressor C2. The compressor takes gas from a product line and injects it through external gas input (valve vl9) of the reactor and distributer within it. This gas propagates solution, creates its circulation what prevents sitting on the active surfaces and growth of the hydrogen bubbles, removes the latter while they are small and takes away the solid products from the aluminum surface. As a result gas generation rises; when its pressure comes to a given level (the valves of gas exit from all tanks and reactor are closed), gas pressure in the receiver and all tanks comes to given level and hydrogen is sent to consumer. Excess of gas is used to force away water from receiver to water tank. Then valves v9, vlO, vl 1 and vl4 are sequentially open and gas fills the upper parts of Tl, T2 and T3 tanks.

Preferably, in a course of normal operation a computer calculates cumulative hydrogen output, losses of weight and surface of aluminum, losses of water and sodium hydroxide; when real increments exceed programmed ones the reaction rate is lowered. The hydrogen output and pressure are being controlled by water or sodium hydroxide solution feeding, as well by circulating compressor activation. If pressure in reactor comes to upward value, the solution is lifted from reactor to current solution tank; when it comes to lower limit, the solution comes back.

After aluminum depletion, the solution is sent (drained) to sodium aluminate solution tank T4 (valve v20). This solution after settling can be used in the next operation as initial solution. It can be circulated by pump, heated and used for washing out the solid product in reactor and current solution tank. The solid product can be extracted from reactor also mechanically together with plastic films and plastic rings and then treated. Before opening, the reactor needs to be blown with nitrogen until H₂ concentration in exhaust will be less than 4% then air can be used. Another variation of the present invention relates to reactors for producing molecular sieves or catalysts. The two hydrogen producing reactors 1, 2 are working in cycling mode when pressure in one reactor periodically becomes more than in the other, and solution is transferred from first reactor to second reactor trough a reactor 3, which serves in this time as a sedimentation tank. Then the accumulated solid product is treated to get target product as mentioned above. For example, aluminum hydroxide is dissolved in concentrated solution of NaOH, silica source is added and zeolite Na-A, P, X, Y, etc. are obtained depending on reaction temperature, pressure and duration. The hydrogen generation heat can be accumulated by silica source which is stored in separate indirect heated tank. A zeolite synthesis is carried out under either hydrogen or/and water vapor pressure.

One another variation of the present invention relates to catalyst and sorbents in situ obtaining. The reactor is constructed as paced bed column; fuel metal is a component of an alloy. After leaching the fuel metal by an alkali metal solution and collecting solid byproduct in sedimentation tank, the self-supporting bed of a reduced skeletal catalyst ready to catalytic reaction is obtained. Close up view to such case is presented in Example 8 that illustrates a self-supporting bed that is obtained from a bundle of tubes. The solid reaction product resulted from fuel metal dissolution can be treated in situ to get a filter, sorbent or catalyst.

Still, one more variation of the present invention relates to small particles of fuel metal loaded on a conical plate with overflow channel. The particles have high surface area and generated hydrogen lifts them and creates boiling solid-liquid-gas mixture. In the upper part of the plate remained only gas - liquid layer; gas separates above the plate and in upper part of overflow channel; liquid flows down to receptacle.

A series of experiments was carried out to study the behavior of the hydrogen gas bubbles forming on the surfaces of different fuel metals, the metal partitions, in different reactors with different alkali metal hydroxide concentrations, etc. The solid byproducts occurring were studied as well.

Example 1 This example refers to storing of aluminum wires. Two pieces of electric wires were placed on bottom of two glass vials and flooded with distilled (vial # 1) and tap (vial #2) water. After two days small bubbles occur on the upper generatrix of wire in vial #2 only. Two weeks later wires in both vials were clean and bright; no bubbles were observed. Thus, the fuel metal may be stored under tap water.

Three fresh pieces of the wires were submersed into glass vials ## 3, 4, and 5 with 10 mL of NaOH solutions of 0.01, 0.1 and 0.5 N concentration correspondingly. Hydrogen bubbling, appearance of wires, solid reaction products and vials walls' transparence walls were observed in 8 minutes, 24 hours and 2 weeks.

In 8 minutes, large bubbles were sitting on the upper surface of the wire in 0.01 N solution but small ones were both sitting and rising in 0.1 and 0.5 N ones.

After 24 hours, hydrogen generation stopped in 0.01 and 0.1 N solutions but continued in 0.5 N one. In 0.01 N solution wire had brown shell; in 0.1 N the wire had initial appearance; in 0.5 N black powder was observed on the vial's bottom. 2 mL of the solutions were taken from vials; one drop of sodium silicate solution was added to them.

The two weeks solutions remained clear, while spent 0.5 N solution gave immediately white gel precipitate which was a zeolite precursor.

The 0.01 N solution was replenished with water; after 24 hours the shell of the wire did not changed. Then vials # 3 and #4 were filled with fresh 0.01 and 0.1 N solutions correspondingly. In 30 minutes the shell on the wire surface in 0.01 N solution disappears and bubbling started; in 0.1 N solution bubbling started immediately and bubbles take up the small grains of precipitate.

After two weeks in 0.01 N solution the wire was covered with black film, the vial's walls were transparent; the white powder was observed on the bottom of the vial and on upper surface of the wire. This powder separates easily from the glass and aluminum surfaces by handy shaking. XRD test of dry powder showed Bayerite structure as illustrated in Figure 3) that represents a diffractogram of the byproduct obtained in Example #1 above. In 0.1 and 0.5 N solutions the wires disappeared; black-grey powder was on the bottom of the vials. The vial's walls were opaque due to either leaching glass with NaOH or the solid product deposition. All solution were clear, their densities were measured (Table 1). For comparison literature data for NaOH solutions densities are placed in the table. Besides 1 wt % of NaA102 solution's density was measured and was 0.9982 g/mL.

Table 1. Densities of Spent NaOH Solutions After Storing Aluminum

It is shown in Table 1 that Hydrogen solubility in water at 25°C is 0.00155 g per kg, i.e. 0.0000155 g in 10 mL or 0.0000155*22400/2 = 0.173 mL, and solution density should be 9.91/(10 + 0.173) = 0.974 g/mL. Thus, it may be suggested that hydrogen in the solutions exists not only in dissolved form but also in a form of colloidal-size bubbles, which are invisible in solution. That is very important for an assessment of a state of reaction mixture in the course of process controlling.

Example 2

The sitting on the surfaces hydrogen bubbles create dead space for solution and stimulate precipitation of solid reaction products. According to current invention the bubbles growth on the surfaces should be limited. Three aluminum electric wires of 2.6 mm diameter, 40 mm length and 0.71 g weight were placed into three polycarbonate cylinders of 10 mm diameter and filled with 6.7 ml of distilled water and 0.268 g (1 M), 0.804 g (3 M) and 1.608 g (6 M) NaOH solutions what corresponds to 1, 3 and 6 normal (N) concentrations. In all cases forming hydrogen created liquid-gas bubbling mixture in which wires were immersed completely; confined space creates intrinsic circulation. Reaction was performed under adiabatic conditions for 60 minutes. Aluminum conversion and reaction rate are shown in Table 2 below. Table 2. Effect of NaOH Concentration on Aluminum Conversion Under Adiabatic Condition and Intrinsic Circulatio.

Table 2 above demonstrates a strong dependence of aluminum conversion on solution concentration which can be used for reaction control. However the most impressive is the appearance of the wires: all wires were bright, demonstrate surface evenness and thickness equality along wires lengths samples.

Example 3

Unlike the experiment illustrated in Example 2 above, the only variable in this example was water amount; Na/Al ratio was constant (1.6) and close to stoichiometric (1.48). Reaction was performed under isothermal conditions. The electric aluminum wires were contacted with NaOH in two types of reactors: in staying position in 10 mm tubes (with intrinsic circulation) and lying on the bottom of large bottles (without circulation). Table 3 demonstrates differences in aluminum weight losses both with and without circulation.

Table 3. Comparison of Aluminum Weight Losses Under Circulation and Without Circulation

Example 4

The experiment was performed to repeat the known David Belitskus reaction of Aluminum with Sodium Hydroxide Solution as a Source of Hydrogen (J. Electrochem. Soc,: Electrochemical technology. August 1970, 1097-1099). Data under current invention conditions (in confined space). Two pieces of electric wire having total surface 10 cm² (diameter 0.26 cm, length 12.25 cm) and total weight 2.08 g were placed into polycarbonate cylinder, 10 mm inner diameter), filled with 3.52 g of NaOH dissolved in 8.8 ml of tap water (10 N solution); reaction temperature was 25°C. In 60 minutes aluminum weight's loss was 0.17 g that corresponds to 0.17*33.6/27 = 0.211 L = 211 ml hydrogen generation. Again the wires had surface evenness and thickness equality. The reaction rate was 21 1/(60* 10) = 353 mL/min cm². Under similar conditions Beliskus had obtained 140 mL of hydrogen. That means that H₂ generation under circulation was 100*(21 1-140)/140 = 50 % more than without circulation.

Example 5

This experiment was performed in order to test the walls of waste aluminum can for comparison with Martinez-2005 data (Susana Silva Martfnez, Wendy Lo^' pez Beni'tes, Alberto A. A ' lvarez Gallegos, P.J. Sebastia'n. Recycling of aluminum to produce green energy. Solar Energy Materials & Solar Cells 88 (2005) 237-243).

A waste soft drink can was dipped into a concentrated sulfuric acid to remove the paint and plastic film. Two curved platelets 35 x 50 mm, total weight 1 g, were placed in transparent plastic glass in vertical position (height 35 mm) by convex sides one to another and separated with horizontal plastic tube. In such state due to cushioning they bear against glass walls and kept themselves. NaOH/Al mol ratio 1.1 and reaction time 60 minutes were chosen from cited article; amount of water needed to cover aluminum was 60 mL. 1.63 g of NaOH household grade was dissolved in this amount of tap water beforehand and had room temperature. The solution was poured into glass which was shielded. Due to even aluminum surface and transparent glass walls the next stages of total process were observed visually: 1) 2-3 mm diameter swellings occur along whole surface; apparently surface pitting of aluminum oxide film by NaOH led to water penetration through the formed pores to the fresh aluminum surface; filled by hydrogen swellings are formed under A1₂0₃ film; 2) with swellings growing, the cracks appeared on the film surface and large (3-4 mm diameter) hydrogen bubbles were grew in static conditions on the crack's edges; when buoyancy force becomes more than surface tension, the bubble tears off from the surface and lifts. The self-cleaning of the surfaces of vertical platelets from the bubbles begins from the lower zone and then spreads upwards; on the horizontal surfaces (lower edge of platelets) and in the points of contact with walls the large bubbles can exist long time; 3) very small bubbles appear on the surfaces cleaned from large ones; fractional gas holdup increases; the upper part of gas- liquid layer becomes opaque; 4) in 30 minutes small grains of powder are lifted by bubbles; they go down collecting in peripheral parts of bottom evidencing dropping solution along reactor's wall, i.e. its circulation. After 60 minutes 0.47 g aluminum remained; the aluminum loss was 0.53 g what corresponds to 0.53*33.6*1000/27 = 659 mL of generated hydrogen. Under similar conditions in the cited work 1 g of small strips (i.e. with larger surface) gave 308 mL. Thus organizing circulation of the solution increased hydrogen output to 100*(659 - 308)/308 = 114 %.

Example 6

The aim of the experiment was to check the apparatus of the present invention in a long-time operation without circulation means. An Arkal Company (Israel) plastic filter equipped with manometer was used as a reactor. Total volume of the filter is 1 L, allowed pressure and temperature are 6 bar and 80°C correspondingly. The 1 N solution of NaOH was prepared beforehand from 20 g household grade NaOH and 500 mL of tap water. The inner surface of reactor was lined by plastic packet of food grade. Aluminum electric wires, 2.6 mm diameter and ~ 70 mm length, total weight 60.11 g and surface area 250 cm were placed in the packet and flooded with solution. Reactor was sealed. Hydrogen generation was measured by pressure raise. Each additional bar means that 500 mL of hydrogen was produced. When pressure reached 6 bars, part of the gas was allowed to release to get 4 bars. Then the cycle was repeated. Increment of time spent to generate increment of pressure (volume) was fixed. Fig. 1 illustrates initial part of aluminum dissolving.

Reference is now made to Figure 4 that graphically illustrates dependence of reaction rate on reaction time in reactor without circulation means. Two features should be noted: the too slow raise of reaction rate in initial (induction) period, what is usual for such reactions, and too high reaction rate for long-time applications. Reaction was stopped, gas released and reactor was opened. The wires were partially covered by thick layer of grey byproduct. Example 7

The same reactor as used in Example 6 was used in the current experiment. In this experiment NaOH concentration was reduced a little by dissolving the same 20 g NaOH in 600 mL of water (0.83 N solution). The plastic packet was placed inside reactor. Polypropylene (PP) transparent cylinder was set inside packet; distance between PP cylinder and reactor walls was provided by 4 plastic tubes positioned around the cylinder in 90°. The cylinder had latticed bottom and 6 legs below lattice. In top part of cylinder the 4 holes were drilled. Aluminum wires were placed in vertical position inside cylinder below holes and stayed on the lattice. The NaOH solution was poured inside PP cylinder; its level was a little above lower edge of the holes. It was expected that in course of reaction these holes, latticed bottom and legs should provide circulation of solution; gas separation from liquid in a liquid-gas upper surface; separation the solid product from liquid in the bottom of reactor. The reaction was started immediately. The reaction rate change is shown in Figure 2.

Figure 5 is a graphical presentation of the dependence of the reaction rate on the reaction time (reactor with means for solution circulating). In starting period the reaction rate did not rise as expected from solution circulation. After 130 minutes, the reactor was opened and it was found that the latticed bottom was fully clogged up with solid byproduct. Thus, distance should be foreseen between fuel metal partitions and the bottom.

Example 8

In accordance with the present invention, another variation of the reactor interior was investigated. A long-time hydrogen generation was modeled. The initial data was as follows: hydrogen output 60 L/min, pressure 6 bar, and duration 90 days were accepted for modeling. The total aluminum weight to be loaded into industrial reactor is approximately 6.3 ton. Approximately 300 g of aluminum was loaded into model reactor. Scale-up coefficient is 6.3*10⁶/302 ~ 20,000; thus, average H₂ output should be 60,000/20,000i.e., 3 mL/min. The methods for controlling the output were studied. The aluminum used was 26 tubes with external and inner diameters of 10 and 7 mm correspondingly, average length 14.2 cm, total weight - 302 g, total surface area 1991.6 cm ; the tubes were bundled by straps together and placed into transparent pressure reactor 2 L volume. One rigid plastic tube in the center of the bundle and 3 elastic plastic tubes around the bundle were fixed. Plastic Raschig rings 5 - 7 mm were laid on the bottom of the reactor to prevent forming an integer cemented body of the solid reaction product and provide the rings layer's permeability for the solution. Lengths of the external plastic tubes were more than aluminum ones such as bundle stand on the legs of external plastic tubes. These tubes kept also a distance between bundle and reactor inner walls providing (together with central plastic tube) solution's circulating. It was assumed that in this configuration the aluminum tubes will provide confined space for generated hydrogen what creates rise of liquid-gas mixture but plastic tubes will provide an overflow of solution. The questions were: in what direction the tubes will dissolve and where the solid product will accumulate? Reactor had detachable cap with manometer and valve for gas output and a bottom liquid output valve. The manometer was served as hydrogen generated volume measuring instrument; when the reactor worked without pressure, a gas burette 10 mL volume and stopwatch were used. The reactor's parts had the following volumes: cap 180 ml; volume of solution when it covers aluminum tubes - 802 ml; cylinder's upper part (gas phase) above solution 121 ml; wherefore, total gas phase volume was 180 +121 ~ 300 ml.

Running ahead one can note that the whole aluminum was dissolved during 19 days with output fluctuation from 1.2 to 150 L/min. Details of the process are shown below:

1 -st NaOH input.

The calculations were made on the basis of equation

Al + NaOH + H₂0 = NaA10₂ + 1.5 H₂ i.e. 27 g of aluminum and 40 g of NaOH produce 33.6 L of hydrogen.

To enlarge pressure to 5 bar in the closed reactor, the 5*300 = 1.5 L of H₂ must be generated. That corresponds to 1.5*27/33.6 = 1.2 g of aluminum loss; to dissolve 1.2 g aluminum 1.2*40/27 = 1.79 g NaOH are needed. This amount was added to 800 mL tap water. The solution's concentration was 1.79*1000/(800*40) = 0.055 N and ratio NaOH/Al wt/wt = 1.79/302 ~ 0.006 (i.e. very far from stoichiometric 40/27 = 1.48). The solution was poured into reactor. In 5 minutes the external surface of the tubes was covered with "frost". The liquid above tubes became opaque; the cloud of small bubbles rose above upper ends of tubes. The manometer moved. The bubbles between neighboring tubes became larger. Seldom bubbles rose in the peripheral space between reactor and bundle. The cloud was seen in upper part of the peripheral ring. In 15 minutes the pressure came to 1 bar; in next 35 minutes the pressure came up to 1.3 bars and then its rise stopped. Pressure was lowered to zero but process was not started again. Many large bubbles sitting on the all sorts of surfaces: tubes, reactor walls and straps inside solution could be seen. Thus, H₂ amount entering gas space was only 300* 1.3 = 390 mL but not expected 1.5 L. It was visually proved that large amount of generated hydrogen was held by liquid and inner parts of the reactor.

The process activation by NaOH concentration increasing was tested (about intensification by circulation see experiment 9 below). 100 ml of solution was drained from reactor and 3.26 g of NaOH was dissolved in it; the solution was cooled to room temperature; reactor was opened and the solution was poured into reactor (2-nd NaOH input). Total NaOH amount was 1.77 + 3.26 = 5.03 g. The ratio NaOH/Al = 5.03/302 = 0.016, i.e. it was 3 times more than previous one. In 3.5 hours the pressure came up to 6 bars. Output fluctuates were from 37.5 to 2.4 mL/min. The results are graphically presented in Figure 6 that presents pressure, bars, and hydrogen output, (mL/min) vs. time (min) with reference to second stage of NaOH input. As shown in the figure, the pressure was dropped, the reactor was allowed to work almost all day long without pressure; hydrogen was released to atmosphere through a water seal. At the second day the valve of gas output was closed and in 24 minutes the pressure reached 6 bars and the reactor showed output from 60 to 150 mL/min. In the next days under similar conditions this range decreases and in 7 days output became less than 3 mL/min. Thus, adding NaOH should be smoother and reaction pressure is also parameter allowing controlling hydrogen output.

The next portions of NaOH were dissolved in drained solutions and returned to reactor. It was found that under 4 - 6 bar the output did not changed notable, so when pressure came to 6 bar the pressure was dropped to 4 and such cyclic regime provides small hydrogen output fluctuation. When H₂ output was only 1.63 mL/min (less than needed 3 mL/min) a medical electric heater was applied to one side of the reactor. That resulted in growing output to 2.22 mL/min.

The effect of ambient temperature on H₂ output was studied and the results are presented in Table 4 below.

Table 4. Effect of Ambient Temperature on Hydrogen Output

As shown in Table 4, even in moderate range the effect of ambient temperature is notable. This problem can be solved by: i) reactor insulation; and ii) using receiver with back-pressure preventing device between receiver and reactor.

A control of hydrogen output by draining solution from reactor, i.e. by decreasing contact surface between solution and aluminum, was studied. The last 4 days the output was 9 - 14 mL/min.

The first 200 mL of solution was drained from the reactor's bottom; in 10 minutes the output was 14.3 mL/min. Then attempt was made to drain remained solution but only 78 mL exited; in the next 10 minutes reaction showed 13.7 mL/min. The new attempt was made to drain liquid but only 10 mL exited but drop wise; gas bubbles grew from the drops. All this time hydrogen generation (bubbling in water seal) continued. Spent solution was filtered outside of reactor.

The reactor was opened; all tubes both aluminum and plastic as well reactor's walls were covered with solid products. The drained filtered solution was returned into reactor; as it did not cover the upper ends of the tubes 175 mL of tap water were added to fill reactor. The total volume of liquid poured was 205 + 78 + 10 = 293 mL. Initial volume was 800 mL; apparently the volumes difference is due to a volume occupied by the solid reaction products.

The product precipitated in space between tubes, fulfills them and creates cemented struts which hold the tubes while they passed dissolving. The product was XRD tested and has been identified as a mixture of Bayerite and Gibbsite- Al₂0₃x3H₂0 what explains the loss of water. Results of XRD test are demonstrated in Figure 7 that represents a diffractogram of the byproduct obtained in Example #8 above.

Example 9

The aim of the following experiment was to check H₂ bubbling effect on Aluminum dissolving rate. Initial conditions of Example # 8 (0.055 N NaOH aqueous solution, Na Al = 0.006) were repeated but without pressure and with H₂ bubbling. Two plastic centrifugal tubes by 50 mL volume, 2.7 cm inner diameter and 11.3 cm height were used as reactors. Two electric aluminum wires, diameter 0.26 cm, weight 1.02 g, length 7.12 cm and surface area 5.8 cm², were submerged into 37 mL of 0.055 N solution of NaOH household grade. Hydrogen from installation of Example #8 was feed into reactor #1 through plastic tube 10 mm inner diameter which was submerged in solution close to the bottom. Hydrogen input was 9.1 mL/min, it was passed in a form of large bubbles with periodicity of 5 - 6 sec. Closed plastic tube of the same diameter was submerged in the reference reactor # 2 also to make the same cross-section area for liquid in both reactors. Ambient temperature was 22°C. Reaction lasts 84 minutes. Aluminum weight loss was minor in both cases but sample #1 (with H₂ bubbling) had bright surface while the surface of sample # 2 had large spots of solid products. To intensify the reaction, the experiment was repeated with fresh wires of the same weights in more concentrated, 1 N, solution and during 200 minutes. Ambient temperature was 22°C. Results of the experiment are shown in Table 5 below evidencing the notable effect of solution propagation.

Table 5. Effect of Solution Propagation On The Reaction Rate.

1 0.072 89.6 0.448 0.077

2 0.050 66.2 0.331 0.054

Reference is now made to Figure 8 that illustrate a schematic block diagram of hydrogen gas and liquid and byproducts possible applications. As shown in the diagram one option of using the hydrogen gas is the production of liquid hydrogen. The process occurring by using the provided system results in a very clean water that may be used for the production of heavy water and for scientific laboratories and pharma industry for example, where a highly clean water are required. Another target byproduct is Alumina (aluminum oxide) that may be used for aluminum recycling. Another profitable option is to produce the alumina for zeolite production, both, catalytic zeolites and/or standard zeolites.

Thus, it is one another aims of the present invention to produce a Green Fuels Energy (G F E) by recycling the byproducts of the process provided herein back to production of hydrogen and synthetic fuel. These procedures may save all the energy produced nowadays by the Bayer process that is the principal industrial means of refining bauxite to produce alumina (http://en.wikipedia.org wiki/Baver process).

The system of the present invention will allow the industrial world to avoid all the environmental pollution occurring as a result of the Bayer process (as well as pollution created by other processes such as Hall-Heroult process).

While some embodiments of a method and of one apparatus have been described herein above, it will be appreciated by those skilled in the art that various modifications, alternate materials, compositions and equivalents may be employed without departing from the true spirit and scope of the invention. Therefore, the above description and illustrations should not be construed as limiting the scope of the invention which is defined by the appended claims. Zeolites may further be used as catalyst for production of synthetic fuel and or for hydrogen production from natural gas. One another target byproduct is carbon dioxide that may further be used for example in food industry, chemical industry or for water treatment, and for the production of synthetic fuels such as dimethyl ether (CH30CH3) that may serve as a substitute for gasoline and diesel oil.

Claims

CLAIMS What is claimed is:

1. A system for obtaining hydrogen and valuable byproducts by water split reaction using fuel metal as a consumer of oxygen and/or OH from water and aqueous alkali metal hydroxide solution as a catalyst and/or as a fuel metal oxide/hydroxide consumer; said system comprising at least one reactor, controlling programmable device, at least one element adapted for directing said reaction products, at least one element adapted for keeping given hydrogen output parameters during a given operation time, at least one element adapted to allow fast starting-up and/or breaking down the reaction, and at least one element for emergency situation.

2. The system of claim 1 wherein said fuel metal is selected from the group consisting of aluminum (Al), chromium (Cr), iron (Fe), magnesium (Mg), manganese (Mn) silicon (Si), zinc (Zn), mixtures and alloys thereof.

3. The system of claim 1 wherein said reactor is filled with at least one fuel metal partition selected from the group consisting of: porous and non-porous powders, flakes, rods, strips, spirals, multi-layered materials, tubes, plates, slabs and profiled articles.

4. The system of claim 1 wherein the alkali metal is selected from the group consisting of: sodium (Na), potassium (Mg), lithium (Li) and calcium (Ca) or mixture thereof.

5. The system of claim 1 wherein said elements adapted for keeping given hydrogen output parameters during a given time include at least the following: water supply, current solution supply, concentrated alkali metal hydroxide solution supply, alkali metal metalate solution supply, hydrogen receiver equipped with pressure regulator, back flow preventing device, heater, pulsator, liquid and/or gas circulators, and external gas input.

6. The system of claim 5 wherein water, current solution, concentrated alkali metal hydroxide solution, and alkali metal metalate solution tanks are functionally connected with said reactor in both gas and liquid spaces.

7. The system of claim 1 wherein the interior arrangement of said reactor functionally allows directing of said reaction products.

8. The system of claim 7 wherein said interior arrangement of said reactor comprises a deposition of fuel metal partitions in a manner minimizing formation of a dead spaces on fuel metal surfaces for both hydrogen bubbles and solution, and wherein deposition of special inactive articles functionally allows reception of solid reaction products.

9. The system of claim 8 wherein said fuel metal partitions have a shape that functionally provides vertical channels adapted for liquid-gas mixture movement.

10. The system of claim 8 wherein said fuel metal partition has a honeycomb form.

11. The system of claim 8 wherein said fuel metal partitions have a cone-like or prismatic-like form positioned by narrow end downwards.

12. The system of claim 8 wherein at least one fuel metal partition is suspended or uplifted so that there is enough space between its lower end and a receptacle for collecting solid reaction products.

13. The system of claim 12 wherein said receptacle is a bed of inactive media.

14. The system of claim 13 wherein said rector's bed is self-supporting during fuel metal dissolving being composed as a bundle of fuel metal and inactive material tube-like partitions.

15. The system of claim 7 wherein said reactor is a tray column having at least one perforated plate supporting fuel metal partitions.

16. The system of claim 15 wherein said perforated plate has at least one overflow channel with overflow receptacle for solid by-products.

17. The system of claim 7 wherein said reactor has at least one external gas input below partitions to intensify the removal of reaction products from said fuel metal surface.

18. The system of claim 17 wherein said reactor has at least one external gas distributor below partitions.

19. The system of claim 17 wherein said external gas is selected from the group consisting of: hydrogen, nitrogen, argon and helium.

20. The system of claim 19 wherein said product is a hydrogen-nitrogen mixture.

21. The system of claim 20 wherein said hydrogen-nitrogen mixture is adapted for either one of ammonia production or hydrogen burning, or both.

22. The system of claim 21 wherein said external hydrogen is part of the system's own product provided by gas circulation means.

23. The system of claim 21 wherein said external hydrogen for circulating the components comprised in said reactor is produced by one another reactor under pressure higher than the pressure in the first reactor.

24. The system of claim 1 wherein said reactor comprises at least one plate consisting of perforated tubes that are functionally adapted to allow external gas distribution.

25. The system of claim 24 wherein said reactor comprises more than one plate having an external gas feeding.

26. The system of claim 1 further comprising at least one heater either inside said reactor or an external heater, wherein said heater functionally allows intensifying said reaction rate.

27. The system of claim 3 wherein number and shape of fuel metal partitions, hydrodynamic regime of liquid-gas mixture's movement, and composition of solution are functionally chosen to provide a given reaction rate (mL/min cm2).

28. The system of claim 1, wherein the reactor has insulation and gas or liquid circulation for minimizing effect of ambient temperature fluctuation on the reaction rate during the day time.

29. The system of claim 1 wherein said controlling programmable device is adapted for keeping product gas flow rate, pressure and temperature inside the reactor in given ranges by feeding said reactor with either one of an external gas, water, hydroxide solution, alkali metal metalate solution, and mixtures and combinations thereof.

30. The system of claim 29 wherein keeping product gas flow rate, pressure and temperature inside the reactor in given ranges may further be obtained by using either one of a heater, a circulating compressor, a reversible circulating pump, a pulsator, and combinations thereof.

31. The system of claim 17 having a bypass between reactor and pressure vessel as emergency situation element for increasing gas volume within reactor in case of drainage liquid from reactor to the current alkali metal hydroxide solution tank.

32. The system of claim 1, wherein said controlling programmable device functionally allows filling said reactor with water when it is free from solution to allow storage of the remained fuel metal under water.

33. The system of claim 1 wherein said controlling programmable device further allows cleaning of said reactor by dissolving solid byproduct and drainage of the solution out of the system.

34. The system of claims 1, 31 wherein said controlling programmable device is adapted to allow operation of said system with said emergency situation element, and wherein said emergency situation element comprises at least one of the following components: a nitrogen supplier, current solution tank, alkali metal metalate reservoir, a torch, flame arrestor, drainage tank and bypass between said reactor and receiver.

35. The system of claim 1 wherein said controlling programmable device functionally allows operation of said system with said start-up element that include at least one of the following components: special helmet in the topmost of reactor, high-surface partitions, start-up reactor, nitrogen supplier, alkali metal solution reservoir, alkali metal metalate reservoir, a torch, a flame arrestor and a drainage tank.

36. The system of claim 1 wherein said system comprises at least two reactors and wherein solution is periodically being transferred from one reactor to the other and back trough a media collecting solid byproducts.

37. The system of claim 36 wherein first reactor is adapted to produce hydrogen and byproducts from synthesis of molecular sieve or catalyst, and wherein second reactor is functionally adapted for processing byproducts of first reactor.

38. The system of claim 37 wherein said byproducts are either one of aluminum oxide and/or Boehmite, Gibbsite, Bayerite.

39. The system of claim 37 wherein products produced within said second reactor consisting of the following: fuel metal oxide, fuel metal hydroxide, molecular sieve and fuel metal containing catalyst.

40. The system of claim 39 wherein said products produced within said second reactor are either one of zeolite and fuel metal containing catalyst such as Ni-Al mixed catalyst for N20 decomposition, Cu-Al catalyst for oxidation of phenol aqueous solutions.

41. The system of claim 1 wherein all features of hydrogen generation system are optimized to obtain clean target byproduct.

42. The system of claim 41 wherein said target byproduct are either one of the group consisting of: sodium metalate, metal hydroxide, metal oxide.

43. The system of claim 1 functionally used as a gas supplier for fuel cell.

44. The system of claim 1 functionally used a gas supplier for production of liquid hydrogen.

45. The system of claim 1 functionally used as energy support system for energetic systems depending on current climate conditions: photovoltaic and wind.

46. The system of claim 1 functionally using water as hydrogen/energy safe storage.

47. The system of claim 1 functionally used as remote and decentralized source of energy.

48. A system for obtaining hydrogen and fuel metal valuable byproducts by water split reaction using fuel metal and aqueous alkali metal hydroxide solution, wherein at least part of said hydrogen obtained is re-circulated into said reaction medium to intensify the removal of reaction products from said fuel metal surface so as to prevent passivation and further to push away both small hydrogen bubbles and solid particles attached to said fuel metal surface.

49. A system according to claims 1, 48 that further allow producing green fuels energy (G F E) by recycling at least part of said byproducts obtained in said reaction.

50. A system according to claim 50 wherein said green fuel energy functionally allows to handle environmental pollution by using molecular sive and/or zeolites which can be replaced by cations.