BACKGROUND OF THE INVENTION

Many industrial processes utilize endothermic catalytic chemical reactions in gases or mixes of liqu ids and gases, typically occurring at high temperature and pressure. These reactions require external heat supply. One of the most important among such reactions is methane steam reforming, having chemical formula CH ₄ + H2O -> CO + 3H2. Two main types of plants are used by the industry in syngas production.

The first type is a tubular reformer, having multiple (typically hundreds) reaction tubes with a catalyst. The reaction tubes are placed inside of a furnace. Natural gas is burnt in the furnace, and heats up the methane/steam mix inside of the reaction tube. The temperature of the tube walls is higher than the temperature of the methane/steam mix. The tube walls have to be made of high temperature resistant alloys and are expensive and still limit the temperature of the reaction. The tubular reformer cannot be scaled down and cannot be moved.

Another type is an autothermal reformer, in which some of the gas is burnt in oxygen to supply heat directly to the methane/steam mix. This type of plant requires a separate oxygen plant. It is also expensive and even more difficult to scale down. Both types of the plants require burning natural gas in order to supply heat. The current invention is directed to solving the above mentioned shortcomings in the existing art and teaching a cost efficient system and method for effecting methane steam reforming, other catalytic endothermic chemical reactions and their applications.

SUMMARY OF THE INVENTION

The invention is directed to a system and a method for syngas production and performing other industrial chemical processes using mechanical energy from wind.

AWECS is an abbreviation of airborne wind energy conversion system. As used herein, AWECS means a wind energy conversion system, in which a wind engaging member(s) is (are) airborne and tethered to a fixed or moving member on the ground.

As used herein, the term "gas" includes mix of gases.

Syngas is an abbreviation for synthesis gas - a mix of CO and H2, possibly contaminated by significant presence of one or more of the following: C, CO2, H ₂ O, CH ₄ .

Some of the embodiments and variations of the invention are summarily described below in the following articles:

[Article 1 ] A method for performing a desirable endothermic chemical reaction in gas using a solid catalyst, comprising: providing a pressure vessel; providing the solid catalyst inside of the reaction vessel; delivering the gas to the pressure vessel; providing more than half of the energy required by the reaction by performing mechanical work on the gas; collecting at least most of the reaction products outside of the reaction vessel.

[Article 2] The method of Article 1 , wherein more than half of the energy required by the desirable reaction is released as heat from a physical process, selected from the group consisting of: gas compression, gas pressure drop, gas velocity drop, and combinations thereof.

[Article 3] The method of Article 1 , wherein more than half of the energy required by the desirable reaction is released as heat from a physical process, selected from the group consisting of: gas compression, gas friction with a solid surface, gas turbulence, and combinations thereof.

[Article 4] The method of Article 1 , wherein more than half of the energy required by the desirable reaction is released as heat from a combination of the gas compression and the gas pressure drop, the gas pressure drop occurring because of the gas friction with a solid surface and the gas turbulence.

[Article 5] The method of Article 1 , wherein more than half of the energy required by the desirable reaction is released as heat from the gas velocity drop.

[Article 6] The method of Article 5, wherein most of the gas velocity drop occurs because of the gas friction with a solid surface.

[Article 7] The method of any of Articles 1 -6, wherein most of the area of the solid surface inside of the reaction vessel is covered with the solid catalyst. [Article 8] The method of any of Articles 1 -7, wherein the form of the solid surface inside of the reaction vessel is optimized to increase the pressure drop or the velocity drop in the gas.

[Article 9] The method of any of Articles 1 -8, wherein substantially all energy required by the reaction is provided through heat release from the gas turbulence and the friction between the gas and a solid surface inside of the pressure vessel.

[Article 1 0] The method of any of Articles 1 -9, wherein the solid catalyst is provided in the form of pellets inside of a packed catalytic bed.

[Article 1 1 ] The method of any of Articles 1 - 1 0, wherein the gas passes over the solid catalyst multiple times.

[Article 1 2] The method of any of Articles 1 - 1 1 , wherein the gas is pumped into the pressure vessel continuously and the reaction products are removed

continuously.

[Article 1 3] The method of any of Articles 1 - 1 1 , wherein the gas is pumped into the pressure vessel in batches and the reaction products are removed in batches.

[Article 1 4] The method of any of Articles 1 - 1 3 , performed in an industrial plant.

[Article 1 5] The method of any of Articles 1 - 1 4, wherein the power for the mechanical work is supplied by a gas turbine or a steam turbine, mechanically driving a gas compressor or a rotor.

[Article 1 6] The method of any of Articles 1 - 1 4, wherein the power for the mechanical work is supplied by an electrical motor, mechanically driving a gas compressor or a rotor. [Article 1 7] The method of any of Articles 1 - 1 4, wherein renewable wind power or hydropower is used for the mechanical work.

[Article 1 8] The method of any of Articles 1 - 1 5 , wherein the desirable reaction is CH4 + H20 -> CO+ 3H2.

[Article 1 9] The method of Article 1 8, wherein the solid catalyst contains nickel as the main active component.

[Article 20] The method of Article 1 8, wherein the power for the mechanical work is supplied by a turbine, burning carbon containing fuels, and at least some C02 from the turbine exhaust is injected into the pressure vessel.

[Article 21 ] The method of any of Articles 1 - 1 8, further comprising a step of re ^¬ using waste heat.

[Article 22] An industrial system for performing an endothermic heterogeneous catalytic reaction in gas, comprising: a pressure vessel, having an inlet and an outlet; a mechanical means for increasing either a pressure or a velocity or both the pressure and the velocity of the gas in the pressure vessel, configured to provide at least half of the power, required for the endothermic reaction; a solid catalyst, facilitating the desirable endothermic reaction, the catalyst being placed inside of the pressure vessel.

[Article 23] The system of Article 22 , wherein the area of the surfaces inside of the reactor, including the surface of the catalyst, is sufficient to ensure sufficient drop of the pressure and the velocity of the gas to provide more than half of the power, required by the desirable endothermic reaction. [Article 24] The system of any of Articles 22-23 , wherein the area of the su rfaces inside of the reactor, including the surface of the catalyst, is sufficient to ensure sufficient drop of the pressure of the gas to provide more than half of the power, required by the desirable endothermic reaction.

[Article 25] The system of any of Articles 22-23 , wherein the area of the su rfaces inside of the reactor, including the surface of the catalyst, is sufficient to ensure sufficient drop of the velocity of the gas to provide more than half of the power, required by the desirable endothermic reaction.

[Article 26] The system of any of Articles 22-25 , wherein the mechanical means for increasing the pressure or the velocity of the gas is a gas compressor.

[Article 27] The system of any of Articles 22-24, wherein the mechanical means for increasing the pressure or the velocity comprises: a motor and a rotating member, coupled to the motor and placed inside of the pressure vessel.

[Article 28] The system of any of Articles 22-27, wherein most of the area of the surfaces inside of the reactor is covered with the catalyst.

[Article 29] The system of any of Articles 22-28, wherein most power required by the endothermic reaction is provided through heat release from the gas

turbulence and the friction between gas and solid surface inside of the pressure vessel.

[Article 30] The system of any of Articles 22-28, wherein substantially all power required by the endothermic reaction is provided through heat release from the gas turbu lence and the friction between gas and solid surface inside of the pressure vessel.

[Article 31 ] The system of any of Articles 22-30, wherein the catalyst is provided in the form of catalytic pellets in a packed bed.

[Article 32] The system of any of Articles 22-30, wherein the catalyst covers flat surfaces, placed in the reaction vessel.

[Article 33] The system of any of Articles 22-32 , wherein a plurality of the reaction vessels and a plurality of the mechanical means for increasing pressure or velocity of the gas are provided.

[Article 34] The system of any of Articles 22-32 , further comprising gas pipes or vessels connecting the outlet of the reaction vessel to an inlet of the same or another reaction vessel in order to perform multiple passes of the gas over the catalyst.

[Article 35] The system of any of Articles 22-34, wherein the mechanical means for increasing the pressure or the velocity of the gas is driven by an electrical motor.

[Article 36] The system of any of Articles 22-34, wherein the mechanical means for increasing the pressure or the velocity of the gas is driven by a turbine, burning carbon containing fuel.

[Article 37] The system of any of Articles 22-36, wherein the endothermic reaction is CH4+H20 -> CO+ 3 H2. [Article 38] The system of Article 37, wherein at least some of the carbon dioxide from the fuel burning is added to the gas.

[Article 39] A synthetic fuel plant, comprising the system from any of Articles 22- 38.

[Article 40] An ammonia plant, comprising the system from any of Articles 22-38.

[Article 41 ] A method of methane steam reforming, repeatedly performing a process comprising steps of: compressing gas, comprising substantial amounts of methane and water steam; passing the compressed gas over a catalyst,

accelerating rate of the endothermic reaction CH4+ H20 -> CO+ 3 H2 ; wherein more than half of the required energy is supplied to the gas by compression.

[Article 42] The method of Article 41 , wherein the compression is performed by a compressor, driven by renewable energy of wind or water.

[Article 43] The method of Article 41 , wherein the compression is performed by a compressor, driven by electrical energy.

[Article 44] The method of Article 41 , wherein the compression is performed by a compressor, driven by a gas turbine or a steam turbine.

[Article 45] The method of any of Articles 41 -44, wherein carbon dioxide is added to the gas for stoichiometry adjustment.

[Article 46] An industrial system for synthesis gas production, comprising: a pressure vessel with an inlet and an outlet; a catalyst, accelerating rate of the reaction CH4+H20+energy -> CO+ 3H2; the catalyst is placed inside of the pressure vessel; a gas compressor, connected to the pressure vessel inlet, the gas compressor is adapted to compress a reacting gas, containing methane, and output the compressed gas into the pressure vessel; wherein the gas compressor has sufficient power to provide more than half of the energy, required for the synthesis gas production within the pressure vessel.

[Article 47] The system of Article 46, wherein the pressure vessel outlet is connected to the gas compressor to facilitate multiple passes of the reacting gas through the compressor.

[Article 48] The system of any of Articles 46-47, further comprising a wind turbine or a water turbine, coupled to the compressor.

[Article 49] The system of any of Articles 46-47, further comprising an electrical motor, coupled to the compressor.

[Article 50] The system of any of Articles 46-47, further comprising a gas turbine, coupled to the compressor.

[Article 51 ] A system for producing electric power and synthetic fuel, comprising: a source of gas, containing methane; a gas turbine, connected to the source of gas; an electrical generator, coupled to the gas turbine at least a part of the time; a methanol plant, comprising: a syngas sub-plant, producing synthesis gas from the methane; a liquid fuel sub-plant, producing liquid fuel from the syngas from the syngas sub-plant; a compressor, coupled to the gas turbine at least a part of the time; a control system, comprising logical elements: to determine current demand for electrical power; to establish a pre-defined demand threshold; if the current demand is above the threshold, generate more electrical power and less synthesis gas or synthetic fuel; else generate less electrical power and more synthesis gas or synthetic fuel.

Various objects, features, aspects, and advantages of the present invention will become more apparent from the following detailed description of preferred embodiments of the invention, along with the accompanying drawings in which like numerals represent like components.

The description uses prior patent applications by the inventor:

PCT/US1 2 /66331 (01 -PCT)

PCT/US1 2 /671 43 (02-PCT)

PCT/US1 3 /73766 (1 0-PCT)

61 /839,001 (APPL-PPA-45)

61 /877,994 (APL-PPA-48)

61 /890,690 (APPL-PPA-49)

61 /91 6,91 5 (APPL-PPA-51 )

61 /91 9,786 (APPL-PPA-52)

All referenced patents, patent applications and other publications are

incorporated herein by reference, except that in case of any conflicting term definitions or meanings the meaning or the definition of the term from this disclosure applies.

BRIEF DESCRIPTION OF THE DRAWINGS The accompanying drawings illustrate the invention. The illustrations omit details not necessary for understanding of the invention, or obvious to one skilled in the art, and show parts out of proportion for clarity. In such drawings:

Fig. 1 shows a side view of one embodiment of a system for syngas production, utilizing wind power, harnessed by airborne wind energy system.

Fig. 2 shows a top view of details of a pressure vessel and mechanical energy transfer elements in that system.

Fig. 3 schematically shows a plant for producing methanol and/or liquid fuel using a system for syngas production with mechanical power supply.

Fig. 4 schematically shows a plant for producing hydrogen and/or ammonia using the system for syngas production with mechanical power supply.

Fig. 5 shows a top sectional view of details of a pressure vessel in an embodiment of a system for endothermic catalytic reactions with traditional compressor.

Fig. 6 shows a natural gas power plant modified to produce methanol in addition to the electrical power.

Fig. 7 shows a cross section of a system for performing endothermic catalytic reactions using a mechanical power source and gas friction between rotor and stator blades.

Fig. 8 shows a cross section of a catalyst covered blade.

Fig. 9A shows a cutaway view of a system for performing endothermic catalytic reactions using a mechanical power source and gas velocity drop with a

centrifugal compressor and helical blades for gas acceleration. Fig. 9B shows a cross section of the same embodiment, viewed from the side of the centrifugal compressor.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

In one preferred embodiment of the invention is a system for industrial syngas production from methane by steam reforming. In such system, the main reaction is CH ₄ + H2O = CO + 3 H2, which is performed at high temperature and pressure and requires presence of a catalyst. This reaction is highly endothermic, so significant amount of energy needs to be supplied from outside. In this

embodiment, the energy is supplied in a form of a mechanical energy, significant part of which is converted into heat on or near the catalytic surfaces.

FIG. 1 shows a side view of one variation of this embodiment, driven by wind energy. It comprises a pair of airborne wings 1 01 , harvesting wind energy by moving cross wind in a helix. Wings 1 01 are attached to a tether 1 02 by relatively short cables and a twist prevention device. Motion of wings 1 01 pulls tether 1 02 with little sideways motion of tether 1 02. Other elements of the construction, shown in FIG. 1 and described below, are installed on the ground. Particulars of attachment of the elements to the walls, ground and other su pporting structures are not shown to avoid clutter. There is a ring 1 03, installed on a slightly elevated structure. Another ring 1 04 is installed on top of ring 1 03 on ball bearings and is capable of horizontal rotation to accommodate changes in the direction of the wind. A vertical pulley 1 05 is installed on ring 1 04. Tether 1 02 wraps around pulley 1 04 and drops inside of rings 1 03 and 1 04, so that it remains vertical no matter how ring 1 04 with pulley 1 05 rotate. Tether 1 02 goes around a vertical pulley 1 06, as shown in FIG. 1 , so that it comes out horizontally. A perforated belt (or a chain) 1 07 is attached at the end of tether 1 02 and winds on / unwinds from a spool 1 08, which is placed at some distance from pulley 1 06. In the working phase tether 1 02 pulls belt 1 07, which unwinds from spool 1 08 and moves to the right. A pressure vessel 1 09 is set horizontally on the ground. There is a stop 1 1 0 and a spring 1 1 1 A, stopped by stop 1 1 0 and pushing one of cylinder rods, as described below. A control system 1 1 2 is provided for automatic operation of the system. Control system 1 1 2 comprises at least one microprocessor, multiple sensors and actuators. It can be distributed, with a part of it being carried by wings 1 01 . Wing 1 01 can be of flexible or rigid construction, with appropriate control surfaces and actuators. A kite or a glider can be used as wing 1 01 , with addition of an appropriate control surfaces and actuators. Tether 1 02 can be manufactured from ultra-high molecular weight polyethylene fibers, aramids, para-aramids or another strong fiber. Belt 1 07 can be made of aramids, para- aramids, high or ultra-high molecular weight polyethylene fibers and other sufficiently strong and flexible materials. Optionally, a single wing system can be used. More enabling details are in the referenced publications.

FIG. 2 shows in details most ground based elements of the system. Pressure vessel 1 09 has a form of a tubular horseshoe with open ends and walls 201 .

Walls 201 of pressure vessel 1 09 are thermally isolated from outside to minimize energy losses. A fixed catalyst bed 202 is inserted in the middle part of the horseshoe. Catalyst 202 is formed from many small nickel rings. The ring can have 1 0mm in both diameter and height with a 5mm hole. Alternatively, catalyst 202 can be formed from many spheres having diameter 5- 1 0 mm or even less, 1 - 2 mm. The form of the catalyst elements, their size and amount is selected in order to increase pressure drop on the surface of the catalyst, as well as to increase the catalytic surface. The desirable reaction happens on catalyst 202 inside pressure vessel 1 09. Gas tight pistons 203A and 203B are inserted into the tubular ends of pressure vessel 1 09, piston rods 204A and 204B are attached to respective pistons. Mechanical devices 205A and 205B for engaging /disengaging belt 1 07 are attached to piston rods 204A and 204B, respectively. At any time in the working phase only one piston rod engages belt 1 07. There is an inlet 206 for the source gas - a mix of methane and steam at high temperature and high pressure. The inlet pressure is below preferable reaction pressure. There is an outlet 207 for the reaction outcome, containing syngas.

In the operation, alternate motion of pistons 203A and 203B moves gas in pressure vessel 1 09 through catalyst bed back and forth and supplies energy in the form of heat. The outside energy is required, because reaction of producing syngas from methane and water steam is endothermic. The energy is harvested from the wind by motion of wings 1 01 and transferred by belt 1 07 to pistons 203A and 203 B. The heat is generated in two places in reaction tube 1 09: when the engaged piston compresses the gas under it and when the pressure of the gas mix falls in the catalyst bed as result of the gas-catalyst friction and turbulence.

The whole system operates in long cycles (which should be distingu ished from short piston cycles; one system cycle will typically contain 1 0 - 30 piston cycles, each cycle consisting of both pistons completing their motion from left to right). Focusing on the action outside of pressure vessel 1 09, each system cycle consists of a working phase and a returning phase. The working phase starts when most of belt 1 07 is wound around spool 1 08, and wings 1 01 are at the closest position to the ground installation. Wings 1 01 flies cross wind in a helix pattern, using aerodynamic lift to pull tether 1 02. Tether 1 02 pulls belt 1 07, which unwinds from spool 1 08 and brings in motion pistons 203A and 203B alternately. FIG. 2 shows piston 203A engaged. In the working phase belt 1 07 moves from left to right. After one piston moves to extreme right position, belt 1 07 disengages it and engages another piston, which has arrived to its extreme left position by that time. Springs 1 1 1 A and 1 1 1 B prevent the disengaged piston from gaining too much speed on its way from the right to the left. The upper part of tether 1 02 typically has angle of 20 ^° - 40 ^° to the horizon. The typical tangential speed of tether 1 02 is 1 /3 to 2/3 of the scalar value of the projection of the wind velocity on the upper tether part. Arrows in FIG. 1 show the direction of the motion of belt 1 07 and tether 1 02 in the working phase. The working phase ends when much of belt 1 07 is unwound from spool 1 08. The returning phase starts. In the

returning phase, both pistons 203A and 203B are disengaged from belt 1 07. An external electrical motor (not shown) rotates spool 1 08 in the opposite direction, winding belt 1 07 back on spool 1 08. These operations are performed under command of control system 1 1 2. Belt 1 07 pulls tether 1 02, which pulls wings 1 01 closer to the ground installation, toward their original positions. In the returning phase, wings 1 01 are controlled to minimize drag. After the returning phase ends, new working phase starts. Before the beginning of the working cycle, a portion of compressed pre-heated methane and water steam enter pressure vessel 1 09 through inlet 206, either as a mix or separately. In the working cycle, pistons 203A and 203 B push the mixed gas through the catalyst bed 202 multiple times, until most of the gas reacts. The desirable reaction here is methane steam reforming:

CH ₄ + H ₂ 0— > CO + 3 H ₂

The temperature of the gas in pressure vessel 1 09 increases within the working cycle, as well as concentration of syngas. Concentration of the methane decreases in the same time. In the returning cycle, the outcome of the reaction ("dirty" syngas) is removed through outlet 207 and is sent to either purification or to the next step of the production cycle.

The number of piston cycles in one system cycle can be estimated from a formula

_ l kH

N ^~ 2 ^~ RT

Where N - the number of the piston cycles; H - the heat of the reaction, J/mol; R - universal gas constant, J/(mol*K); T - absolute temperature in pressure vessel 1 09 (K); k - ratio of volume of gas at average pressure inside of pressure vessel 1 09 to the product of length of the piston movement to the sectional area of the piston, typical values are 0.5< k<2.0. The sizing of the airborne wings and length of belt 1 07 can be easily computed using Loyd's formula.

It should be noted, that compression of the gas increases internal energy of the gas, increasing both its pressure and temperature. As the gas moves through the catalytic bed, the pressu re drops, releasing additional heat. This system can be modified in various ways, including replacement of the airborne wind energy system with another power system, producing mechanical energy and capable of driving a compressor. Continuous gas conversion can be used instead of cyclical gas conversion.

The system described above, with or without modifications, has many advantages over the existing steam reforming industrial systems for syngas production from natural gas. The highest temperature in the pressure vessel is achieved on the catalyst, where reaction happens, and the lowest temperature is on the walls; this allows cheaper construction of the pressure vessel from lower grade steel and/or higher temperature of the gas. The walls of the pressure vessel can be covered from inside by heat resistant materials, such as ceramics, able to withstand significantly higher temperature than alloys, currently used in the reaction tube walls. The higher temperature of the reacting gas leads to higher rate of the reaction. One pressure vessel can replace multiple tubes of a standard steam reformer. The described system can achieve higher conversion rate because of higher temperatures and higher velocity of the gas. No furnace or heater is required, further decreasing capital expenditures to build the plant. If renewable energy is used to drive the compressor, there is also economy of the natural gas, which is not burnt to provide energy. The resu lt is large savings compared with the existing steam reforming plants. These advantages are shared by other examples of syngas production systems, described below.

The reaction can be performed in multiple stages, each stage with its preferable pressure and temperature. For example, two pressure vessels 1 09 can be utilized, with output from the first one (a partially reacted gas mix) serving as an input to the second one. The temperatures and pressures in these pressure vessels can differ to minimize the cost of the system. The internal volumes, wall materials and other parameters of these two vessels will differ, respectively.

Typically, the temperature in second pressure vessel 1 09 will be higher for syngas production.

Another embodiment of the invention is a system for producing synthetic fuel using an airborne wind energy harvesting subsystem or another source of mechanical energy. FIG. 3 shows such a system. In it, natural gas is injected into a pre-processing subsystem 301 , where sulfur is removed from it. Methane or methane-C02 mix from pre-processing subsystem 301 is injected into pressure vessel 1 09, together with water steam (arrow 305). Operation of pressure vessel 1 09 is described above. The "dirty" syngas from pressure vessel 1 09 is sent into a post-processing subsystem 302 , where optional water shift reaction is performed and gases other than CO and H2 are removed from the mix. The "clean" syngas from post-processing subsystem 302 is sent into a methanol synthesis subsystem

303 , where methanol is produced from syngas using Fischer-Tropsch process. The produced methanol can be removed (arrow 306) and used as a vehicle fuel or in other purpose, or it can be sent for further processing into gasoline converter

304, where it is converted into gasoline. The gasoline is removed (arrow 307). Alternatives for pressure vessel 1 09 are described below.

This system for manufacturing liquid fuel has lower capital expenditure and operating costs than existing plants because of lower costs of syngas production. Further, it can be made relatively easy for assembling, disassembling and move, resulting in a moveable plant. Such moveable plant can be delivered to locations of stranded natural gas or offshore gas fields. Once re-assembled, it can convert the stranded gas into liquid fuel, especially methanol, relatively inexpensive to deliver to where it is consu med without need to build pipelines.

Another embodiment of the invention is a system for producing hydrogen and/or ammonia using an airborne wind energy harvesting subsystem. FIG. 4 shows such a system. In it, natural gas is injected into a pre-processing subsystem 301 , where su lfur is removed from it. Methane from pre-processing subsystem 301 is injected into pressure vessel 1 09, together with water steam (arrow 305).

Operation of pressure vessel 1 09 is described above. The "dirty" syngas from pressure vessel 1 09 is sent into a water shift subsystem 402 , where water shift reaction is performed to increase amount of hydrogen in the mix. The "hydrogen enriched" syngas from water shift subsystem 402 is sent into a purification subsystem 403 , where gases other than hydrogen are removed. The produced hydrogen can be removed (arrow 406) and used, or it can be sent for further processing into ammonia synthesis subsystem 404, where it reacts with nitrogen, producing ammonia (Haber-Bosch process). The ammonia is removed (arrow 407) and used, for example, as fertilizer. Alternatives for pressure vessel 1 09 are described below. This system for manufacturing hydrogen and/or ammonia has lower capital expenditure and operating costs than existing plants because of lower costs of syngas production. FIG. 5 shows a top sectional view of another embodiment of the invention, a reactor for endothermic catalytic reactions with mechanical energy supply. In it, the reaction occurs within a toroid pressure vessel having walls 501 . Walls 501 are thermally isolated from outside to minimize energy losses. A fixed catalyst bed 502 occupies most of the space in the vessel. Parameters of catalyst bed 502 is selected for high pressure drop similarly to catalyst bed 202 , discussed above. The catalyst can be provided in the form of spherical pellets with diameter 1 -2 mm. A gas compressor 503 , driven by a motor 505 directly or through a mechanical transmission 504 compresses the gas (the working mix), thus supplying energy, necessary for the endothermic reaction. Significant amount of the internal energy of the gas becomes heat in the catalyst bed as a result of the pressure drop because of the gas friction and turbulence, caused by the catalyst pellets. Thus the temperature of the gas near the catalyst surface is higher than the temperatu re of the tube walls, allowing use of cheaper materials for the walls. There is an inlet 506 for the source gas - a mix of methane and steam at high temperature and high pressure in the case of methane steam reforming - and an outlet 207 for the reaction outcome, containing syngas. Gas compressor 503 can be of a conventional type, such as a centrifugal compressor, an axial compressor, a vane compressor, a reciprocating compressor etc. Motor 505 can be driven by electricity (i.e., be an electrical motor), by wind energy (possibly obtained from an airborne wind energy system), by hydro power, compressed air, high pressure steam (steam turbine), hot gases (for example, the motor can be a gas turbine, possibly using the same natural gas source that supplies methane to the reaction itself) or other available source. If motor 505 uses electrical energy, this electrical energy can be generated locally using solar, wind, nuclear or another renewable or local energy resource. If the source of energy is coal or natural gas, then CO2 from this process can be added to the reaction to change CO/ H2 ratio in the output. The source of the energy can be some exothermic reaction in the same plant. Surface per volume ratio of the catalyst bed 502 can vary along the circular path inside the toroid to better accommodate dropping pressure and speed of the gas mix. Multiple gas compressors can be installed in multiple points of the vessel for more uniform gas parameters along the length of catalyst bed 502. In most practical cases, the gas passes multiple times through the compressor and the catalytic bed (in either the same vessel, or different vessels or both the same and different vessels), but a single pass reactors are possible as well. In some embodiments, small amount of air or oxygen can be added to the gas mix inside of the vessel in one or multiple points in order to allow some methane to burn, providing additional energy and shifting CO/ H2 ratio in the output syngas. The catalyst can be nickel on alumina or spinel support.

Sample parameters of this embodiment for methane steam reforming: Length of the catalyst bed - 2 m, Diameter of the catalyst bed - 0.5 m, Catalyst pellet diameter - 2 mm, Pressure in front of the catalyst bed - 60 bar, Pressure behind the catalyst bed - 40 bar, Temperature average - 850 ^° C, Gas velocity in front of the catalyst bed - 3 m/s, Compressor power - 3 MW, Methane conversion rate in one pass - 4%.

FIG. 6 shows a natural gas power plant modified to produce methanol in addition to the electrical power. It comprises a pressure vessel 600, similar to one, described in the explanations to Fig. 5, with a gas compressor 503. There is a gas turbine (turbo-shaft) 601 , having a shaft 602 , and an electrical generator 603. Each of electrical generator 603 and gas compressor 503 receive power from gas turbine 601 through shaft 602 and (optionally) a reductor or a gearbox. Electrical generator 603 is connected to the grid by an electric cable 604. Natural gas arrives through a pipe 605 , which splits. Some of the gas goes to the gas turbine 601 , where it is burnt, and some of it passes through a purification system 606. A relatively pure methane from purification system 606 goes through a pipe 607 and enters pressure vessel 600, where it is mixed with steam and undergoes methane steam reforming reaction. Resulting syngas exits pressure vessel 600 through a pipe 608 and enters a post processing facility 609, which uses that syngas to produce methanol. Produced methanol is removed through a pipe 61 0. Thus, the described system can produce both liquid fuel and electricity in the same time. Further, it can be arranged to react in real time to changes in the demand for electricity, producing more electricity or only electricity) in times of higher demand for electricity, and producing more methanol (or only methanol) in times of lower demand for electricity. The changes in the demand can be reflected in the changes in the electricity prices. This is done using a

programmable element 608, which works as follows. When the demand for electricity is low, most of the power from gas turbine 601 is sent to gas

compressor 603, which works at full capacity. When demand for electricity is high, most or all of the power is sent to electrical generator 603, which works at fu ll capacity. Accordingly, very little or no methane is sent through purification system 606 and very little or no methane/steam mix enters pressure vessel 600. When demand for electricity drops, the system reverts back to produce mostly methanol. This system can act as a peak load power plant. In this system, CO2 from the turbine exhaust can be separated and used in the post processing facility 609 to produce additional methanol by reacting with excess H2 from the syngas:

CO2 + 3H ₂ → CH3OH + H ₂ 0

Gas turbine 601 can be combined with a steam turbine in a combined cycle gas turbine. The steam turbine can use exhaust heat from gas turbine 601 and/or heat from the methanol synthesis reaction for electricity production. The plant from Fig. 6 can be used for producing methanol from natural gas in stranded gas locations or offshore locations. In these case, electrical generator 603 is small or omitted altogether, cable 604 is omitted or not connected to the grid, and programmable element 608 is not used.

An existing gas or coal power plant can be modified to produce syngas and then methanol from that syngas. If coal plant is used, a steam turbine is used instead of gas turbine 601 and there should be a separate supply line for natural gas.

FIG. 7 shows a cross section of the first preferred embodiment. The central part of it is a reactor 701 . Reactor 701 comprises a cylindrical pressure vessel 703 , having mu ltiple perforations in its walls. Pressure vessel 703 is placed inside of an external tube 704. A cylindrical internal tube 702 , having multiple

perforations as well, is placed inside of pressure vessel 703. Internal tube 702 is coaxial to pressure vessel 703 and installed on bearings 705. This installation is gas tight. One end of internal tube 702 is closed and attached to a shaft 706, which is connected to an engine 707, so that engine 707 can rotate internal tube 702 around its axis. The other end of internal tube 702 is open at least partially. Circular rotor blades 708 are installed along most of the length of internal tube

702 , their diameter is slightly less than the internal diameter of pressure vessel

703. Circular stator blades 709 with cut out centers are installed inside and along most of the length of pressure vessel 703. The cut out diameter is slightly larger than the external diameter of internal tube 702. Rotor blades 708 and stator blades 709 alternate, and have small distance between them. FIG. 8 shows a fragment of a section of a blade 708 or blade 709. The blade's core 801 is made of a strong and temperature resistant alloy, such as a nickel-chromium alloy. On the outside, it is covered with a catalyst support 802 , which can be made of alumina or spinel. A layer of catalyst 803 , such as nickel, is placed on top of catalyst support 802. Nickel catalyst is usually covered by nickel oxide before reduction. Going back to FIG. 7, a gas compressor 71 0 is attached to external tube 704. Gas compressor 71 0 pumps the reacting gas, such as methane/steam mix with molar ratio 1 : 3 , into external tube 704 under pressure. Through the perforations, the gas enters the pressure vessel 703. Internal tube 702 with attached blades 708 rotates on shaft 706 with high RPM, driven by engine 707. Blades 709, attached to pressure vessel 703 , are stationary. The compressed gas between adjacent rotor blades 708 and stator blades 709 undergoes significant friction with rotor blades 708 and stator blades 709, which converts the

mechanical energy, supplied by engine 707, into heat. The friction is mostly between the gas and the blades' surfaces. Thus the energy is supplied for the endothermic reaction. One of the key benefits is that the mechanical energy is converted to the heat in the place where it is utilized: at the catalyst surface. The product of the reaction, containing syngas, is removed through the perforation in internal tube 702 and then through its open end. Flow of gases is shown in white arrows in FIG. 7. The operation is controlled by an electronic control system 71 1 . External tube 704 is thermally insulated and the external surface of reactor tube 703 is treated to minimize radiative and other thermal losses.

Engine 707 is the source of mechanical energy for the system operation. Engine 707 may be anything of the following: an electrical motor, a gas turbine, a steam turbine, a nuclear powered turbine, an engine, driven by mechanical energy of falling water or wind etc. If an electrical motor is used, it may be powered by a dedicated power plant of any of known types or by electricity from the grid.

Amount of electrical power, used by engine 707, may vary depending on the current electricity demand or price as follows: use less power, when electricity price increases, and use more power, when electricity price decreases. If engine 707 is a gas turbine, it may use the same gas feed for both combustion and methane source for steam reforming. The gas turbine can be combined with an electrical generator, connected to the grid and vary its power output to the grid depending on the current electricity demand or price. If a fossil fuel based power source is used, the CO2 created in the combustion of the fossil fuel may be added as an input for steam reforming to decrease H2/CO ratio of the reaction product, if it is used in a methanol production plant. Compressor 71 0 may be driven by engine 707 or by a separate engine.

Sample parameters of the reactor 701 : Length - 1 0 m, Diameter of reactor tube 703 - 1 m, Diameter of internal tube 702 - 0.25 m, RPM - 5,000, Pressure inside reactor tube 703 - 40 bar, H20/CH ₄ ratio in the source mix - 3 : 1 , Gas temperature inside pressure vessel 703 - increasing from 600 ^° C near the wall of pressure vessel 703 to 800 ^° C near the wall of internal tube 702. In the described system, the ratio of unreacted methane decreases from the periphery (the wall of reactor tube 703) to the internal tube 702. Correspondingly, the rate of reaction decreases as the ratio of the gases in the mix approaches chemical equilibrium. But the amount of heat that is created by rotation, also decreases toward the center, because it is proportional to the linear speed of the blades in a given point, which is proportional to the distance from the center.

This system has multiple benefits compared with conventional steam methane reformer. If a not very expensive source of mechanical energy is available, the cost of the syngas from this system is less than the cost of syngas from a conventional reformer. The invented system is especially effective for small scale syngas production. It can be delivered to and deployed in remote areas where stranded gas is present, including offshore locations. Produced syngas can be converted to methanol which can be economically transported. If there are oil sand reserves close by, the hydrogen from syngas can be used to upgrade the bitumen by catalytic hydrocracking.

This system can be used for other catalytic endothermic reactions, not only for syngas production. This system can be modified in a variety of ways. For example, rotor blades 708 and stator blades 709 can have trapezoid (trapezium) section, being wider at the bases and narrower at the ends. In another example, the source gas is pumped through internal tube 702, and the products of the reaction removed through external tube 704. In this case, rotor blades 708 preferably have trapezoid section, while stator blades 709 have rectangular section. Thus, the distance between them increases with increasing distance from the center, decreasing amount of heat generated per unit of volume.

Another possible modification is to change reactor 701 from radial one to axial one. In such axial reactor, one base of a cylindrical reactor is rotating, and another base is static. The blades have a form of coaxial cylindrical surfaces. The rotor blades are attached to the rotating base, and the stator blades are attached to the static base. The rotor blades and the stator blades alternate. The source gas is pumped in through one of the bases, and the product mix exits through another base.

In another modification, the blades can be perforated in order to make them lighter and add turbulence to the gas. In the turbulent gas, mechanical energy is converted into heat not only through friction, but also through turbulence.

FIG. 9A shows a cutaway section of another embodiment of the invention. There is shaft 706, described above. The reacting gas is compressed by centrifugal compressor 901 , comprising an impeller 902 , sitting on shaft 706, and a diffuser 903. A cylindrical pressure vessel 904 is attached to compressor 901 , so that the compressed gas exiting compressor 901 enters it from the left. A rotor 905 with helical (auger like) blades 906 is installed on shaft 706. FIG. 9B shows a cross section of reactor 904. Multiple helical rotor blades 906 may be installed on rotor 905. Rotor blades 906 are preferably curved as shown in FIG. 9B. Rotor 905 rotates in such direction (shown by arrow on Fig. 6B) that its rotation pushes the gas toward walls of reactor 904, to the right along the axis of reactor 904, and provides rotation to the gas in reactor 904. Thin stator sheets 907 are attached to the walls of reactor 904. Stator sheets 907 are made of heat resistant metal and are covered by the catalyst support and catalyst. Stator sheets 907 have the form of helix with an angle, optimal to accommodate gas flow from rotor blades

906 (i.e., that the gas flow from rotor blades 906 is parallel to stator sheets 907). The twist rate of rotor blades 906 may be 1 :3 (one turn per three diameters of the external edge of the blade). Corresponding twist rate of stator sheets 907 may be 3: 1 (three turns per one diameter of the internal edge of the blade). Stator sheets

907 should have small distance between them (such as 1 mm) in order to maximize the catalytic surface and heat generation, so there are multiple helix like blades overlapping. Rotor sheets 906 should be fairly close to stator blades 907, but not that close as to require high tolerances. Additional sheets 908, covered by the catalyst support and the catalyst, may be installed inside of diffuser 903. The wall of reactor 904 and the wall of diffuser 903 are thermally insulated from the environment. Sample parameters of reactor 904: Length - 1 0 m, Reactor diameter - 5 m, Internal diameter of stator blades 907 - 0.75 m, External diameter of rotor blades 906 - 0.72 m, Diameter of rotor 905 - 0.4 m, RPM - 5,000, Pressure inside reactor tube 904: 40 bar, H ₂ 0/CH ₄ ratio in the source gas mix - 3: 1 , Gas temperature inside reactor tube 904: 800°C.

The operation of this embodiment is somewhat similar to that of the embodiment in FIG. 7. Pre-compressed and pre-heated source gas mix enters centrifugal compressor 901 , which further compresses and heats it to the working temperature and pressure. Some of the methane reacts inside of diffuser 903. The gas mix enters reactor 904, where fast rotation of rotor 905 with rotor blades 906 continuously adds energy to the gas mix. This energy is initially in the form of high velocity of the gas, accelerated by blades 906. As the velocity of the gas drops (mostly through friction between the gas and stator blades 907), this energy converts into heat, and the generated heat sustains steam methane reforming reaction. High speed of gas flow also improves transport of reacting components to and from the surface of the catalyst. When the gas mix exits reactor 904 on the right, most of the methane has already reacted, producing syngas. The syngas is utilized in any desired way. Shaft 706 is driven by engine 707 as described above. This embodiment has an advantage over the

embodiment on FIG. 1 , that the stator blades are not interspersed with the rotor, so they may be spaced more closely without fear of collision with the rotor blades.

Geometry of the system can vary. For example, twist rate of either or both rotor blades 906 and stator blades 907, diameters of rotor 905, rotor blades 906 and/or stator blades 907 may vary along the length of reactor 904 to

accommodate changing reaction rates. Stator sheets 907 may be perforated or equipped with other turbulence inducing features. The system can be used for other catalytic endothermic reactions, not only for syngas production.

Another embodiment of the invention is a plant for producing liquid fuel from natural gas, comprising: a sub-plant for production of methanol from syngas; a pressure vessel for syngas production by methane steam reforming; a catalyst inside of the pressure vessel; a gas compressor, adapted to compress a gas inside of the pressure vessel; where most of the energy necessary for methane steam reforming is supplied by the gas compressor compressing the gas. The

compressor can be driven by a gas turbine, driven by the natural gas. The compressor can also be driven by an electric motor. The electric motor can use electricity, produced by a gas turbine from the natural gas.

Another embodiment of the invention is a plant, producing either of hydrogen, methanol, ammonia or another product, utilizing mechanically powered syngas production facility with optional waste heat re-use and optional production curtailing in times of high electricity demand.

Thus, a system and a method for performing endothermic chemical reactions, syngas production and related matters are described in conjunction with one or more specific embodiments. While above description contains many specificities, these should not be construed as limitations on the scope, but rather as exemplification of several embodiments thereof. Many other variations are possible.