The present invention relates to a process and reactor for carrying out a liquid compression chemical reaction. In this process and reactor according to the invention the reaction takes place in the gas phase, gas- solid phase, gas-liquid phase, and/or gas-solid-liquid phase and/or at the interphase of these phases, when increases (and decreases) of pressure and optionally

temperature are generated by applying force on a liquid phase of a reaction medium and transferring the pressure increase (and decrease) to at least the gas phase.

Preferably the process and the reactor are used such that the chemical reaction proceeds at high pressure and

optionally at high temperature.

Many processes in production (chemical, food) industries require high pressure and/or high temperature such that a chemical reaction takes place at economical rates of conversion. Short residence time and rapid cooling are often required.

Examples are synthesis gas production, cracking of hydrocarbons, hydrogenation, synthesis of ammonia, methanol, hydrocracking, hydrodesulfurization, polymerization

processes, phenol production and the like.

These processes are both energy and capital intensive. Energy required for the process is derived from combustion of high grade fuels (natural gas) in form of heat for heating of reactants to the reaction temperature or in form of electricity to drive compressors, and pumps. The energy of hot compressed reaction products is recovered by the use of various energy recovery devices such as heat recovery boiler-steam turbine unit. In spite of all these measures a significant percentage (sometimes up to 70 %) of the energy is lost.

Safety, environmental impact, production capacity and large size are other important problems associated with processes at extreme conditions (high pressure and/or temperature) . The higher the process pressure and/or

temperature the more severe the problems mentioned above are .

To overcome these problems typically relating to high-temperature and/or high-pressure processes, several alternative technologies for compression/expansion

accompanied by heating/cooling have been proposed.

Shock waves are used in a compression-expansion method for carrying out chemical transformations in shock tubes (e.g. for pyrolysis of methane) . However, this technique being useful for research is not practical because of the low energy efficiency. Furthermore, only gas phase processes with very short reaction time can be carried out by the use of this technique.

Processes for carrying out chemical reactions in the gas phase or gas-liquid phase in a turbine engine were proposed. But this technique provides only relatively low compression and the maximum temperature does not exceed temperatures achievable in conventional reactors (due to hot strengths and/or heat resistance of materials) .

It has been suggested to carry out chemical reactions under high pressure and temperature conditions by compressing a reactant gas under conditions approaching adiabatic compression until the desired temperature and pressure are obtained. A subsequent cooling of the reaction products is carried out by expansion as rapidly and as adiabatically as possible.

The industrial application of IC-engines as chemical reactors appeared to be impracticable because of oil lubrication and many inherent limitations on maximum pressures, temperatures, volume throughputs and the like.

Piston compression reactors have problems with wear and sealing of the piston in the cylinder under the severe conditions of a combination of high temperature, pressure and sliding speed. Inherent problems of these reactors are short circuit losses and mixing of products and feed. A reaction residence time in abovementioned reactors depends on feed initial pressure and mass of the moving parts/piston, i.e. size of reactor. High temperatures can be kept only during an extremely short time to avoid a high- temperature corrosion and heat resistance problems of the materials. The reactors of such a type cannot process multiphase feed, especially containing solid particles.

The present invention has for its object to substantially avoid the captioned problems and provide a new concept for carrying out at least one chemical reaction at high pressure and optionally high temperature. This new concept is based on the insight of compressing a reaction mixture by compression of the liquid phase (or one of the liquid phases) being a carrier liquid, liquid reactant, and/or a product of the chemical reaction. The compression of the liquid phase (being itself substantially non- compressible) transfers the pressure increase to the gas phase (and optionally the solid phase or other liquid phase dispersed in the gas phase) , so that due to the increased pressure (and optionally temperature) the chemical reaction or reactions takes place. Thus, use is made of liquids for performing compression and subsequent expansion of a gas phase. This gas phase may be a carrier gas, a reactant and/or a product of the reaction. The gas phase may have the form of gas entrapped in gas bubbles and/or gas plugs, or gas cavities in the reactor body/parts. The gas phase may contain dispersed liquids and/or solid particles. The increased pressure and optionally increased temperature provide the conditions at which the chemical reaction proceeds .

The liquid phase used for compression and expansion is selected and functions as:

(i) a carrier to transmit or create and transmit pressure to the gas phase;

(ii) a carrier with catalytic properties to transmit or create and transmit pressure to the gas phase, and to catalytically influence the chemical reaction;

(iii) one or more liquid reaction component (s) with or without solid phase which transmits or creates and transmits pressure to the gas phase, and participates together with or without solid phase in the chemical reaction;

(iv) the liquid phase being a feed component

(reactant to the chemical reaction) is converted to gaseous or liquid reaction product.

(vii) a heat carrier for providing heat to the chemical reaction.

A first aspect of the invention relates to a process for carrying out at least one liquid compression chemical reaction comprising the steps of:

i) providing a reaction medium comprising at least one liquid phase which is in contact with at least one gas phase and optionally at least one solid phase; and

ii) repeatedly performing a compression and expansion cycle on the reaction medium by applying force on the liquid phase, such that the chemical reaction takes place .

Thus, the chemical reaction is carried out in an elegant manner because high pressure in at least the gas phase is repeatedly generated by compressing the liquid phase. Such liquid phase is substantially incompressible so that the pressure increase (or decrease) is directly

transferred to the gas phase. In the gas phase, or at the interface with the liquid phase the chemical reaction proceeds, and/or in liquid phase after an adsorption of a gas feed component.

The compression and expansion may also result in a temperature change in the gas phase dependent on the

residing conditions. Thus, due to the frequency of the compression and expansion cycles, the size of the gas phase (gas bubbles, gas plugs, and gas cavities), the type of liquid in relation to heat exchange, hydrodynamic conditions and the like, the reaction may take place adiabatically, isothermally or any form in between. Accordingly, by

selecting the correct conditions and composition of the liquid phase and/or of the gas phase the reaction may be carried out at low, high or even extremely high temperatures and during long, short or extremely short periods of time.

The process of the invention provides various advantages of using a liquid phase (instead of a piston system) as compressing media, such as: (i) no gap ift between piston and cylinder i.e., positive sealing resulting in absence of leakage and accordingly no piston-cylinder wear; (ii) no (back) mixing between reactants and products, avoiding problems of replacement of products by feed, and no short-circuit losses; (iii) duration of the compression- expansion cycle can be controlled and does not depend on the initial pressure and properties of the gas phase, reactor scale-up, reaction characteristics such as heat effects of chemical reactions, and change of number of moles between reactants and reaction products; (iv) solid and liquid reactants can be used which are considered difficult in relation to evaporation or preheating to a desired

temperature before entering the reactor, such as bio-oil, oil sands, oil shales, oil residues, pyrolysis oil and the like; (v) liquid used for compression can be (or contain) catalyst or reactant; (vi) duration of the

compression/expansion cycle can easily be controlled; (vii) compression can be isothermal, adiabatic or between; (viii) the liquid phase can be used as a heat exchange medium; (ix) the liquid used for compression can conform to an irregular chamber volume, the surface area to volume ratio in the gas chamber can be optimized; extremely high temperatures and pressures are possible (in bubbles); (x) in case entrained bubbles (gas plugs and/or cavities) are subjected to

compression-expansion problems of the reactor wall

overheating, involving hot corrosion and side reactions caused by hot spots are eliminated; (xi) technically simpler than solid piston reactor, industrial implementation can be made much faster.

As stated above the chemical reaction and the nature of the reactant may have an effect on the form of the gas phase. According to a preferred embodiment the gas phase has the form of gas bubbles and/or gas plugs, or gas

cavities .

The process of the invention allows the selection of the composition of the gas phase dependent on the nature of the reaction. Thus the gas phase may comprise only a carrier gas which is substantially inert to the reactants and reaction products, and does not take place in the chemical reactions. Otherwise, the gas phase may further comprise or consists substantially only of at least one reactant. Finally the gas phase may entail solid particles and/or liquid droplets, such as catalyst particles and/or can be also feed or feed component.

Similarly, according to a preferred embodiment the liquid phase may comprise at least one reactant for the chemical reaction, or a catalyst, such as in the form of liquid metal or metal alloy.

Another advantage of the process is that if desired the gas phase and/or the liquid phase comprises the product of the chemical reaction.

If it is preferred according to the invention that in the chemical reaction solid particles are used as

catalyst or reactant or reaction product then the gas phase and/or the liquid phase may comprise solid particles being a reactant and/or catalyst for the chemical reaction or a reaction product.

The general concept of the invention requires that the compression and expansion of the gas phase proceeds via the liquid phase. But the invention is not limited to any particular form or manner of compressing and expanding a gas phase. According to preferred embodiments the compression and expansion cycle is carried out with the at least one piston system, by hydraulic ramming, by centrifugal

compression and expansion and/or by cavity compression and expansion by cyclic submersion into a liquid phase,

preferably a liquid subjected to inertial forces e.g., to a rotating liquid layer.

Another aspect of the invention relates to a reactor for carrying out the process of the invention. This reactor in its general concept comprises (i) at least one reactor vessel provided with an inlet for the liquid phase and for the gas phase and/or for the solid phase, and/or for liquid containing solids, and an outlet for the reaction product; and (ii) means for repeatedly compressing and expanding the reaction medium by applying pressure to the liquid phase. It is noted that the reactor may be reaction vessel, a reaction volume, and/or reaction compartment.

This reactor may have various different forms dependent on the type of reaction to be carried out and also on the nature and the combination of the gas phase, the liquid phase and/or the solid phase and/or the reaction product ( s ) .

According to a first embodiment the reactor comprises a reaction vessel, and the compression and

expansion means comprise a piston system and closing means for closing the reaction vessel during compression and expansion, and which piston system is in direct or indirect contact with the liquid phase. If circumstances desire the piston system may be used for carrying out the compression and expansion cycle in two or more reaction vessels

concomitantly or consecutively. The closing means may be any mechanical means for partially or completely interrupting the flow of the liquid phase resulting in a change in pressure in a liquid phase which is in contact with the gas phase. The closing means may be selected as desired as long as the compression and expansion may be carried out so that the reaction proceeds. The closing means may comprise actuators for actuating (closing and opening) valves which close the reaction vessel during compression and expansion. The piston means may be in direct contact with the liquid phase. If the nature of the liquid phase does not allow such direct contact then a separating medium, such as a membrane or separating liquid may be used. Obviously, means may be present for controlling and determining the size and the number per volume of the bubbles, characteristics of gas phase, such as size and volume fraction of bubbles and gas plugs in liquid.

According to another embodiment the reactor comprises a hydraulic ramming system comprising pump means for generating a flow of the liquid phase, and ramming means (such as valving system and the like) for abruptly stopping liquid phase flow. Such hydraulic ramming system generally comprises pump means for generating a flow of the liquid phase, preferably in a circulating manner. Such circulation cycle may preferably comprise a storage tank functioning as a hydraulic accumulator for the liquid phase and a tank for separating the product from the liquid phase being in the form of a gas, liquid or solid. Furthermore, any type of ramming means may be used for abruptly stopping the flow of liquid whereby the compression of the gas phase takes place. Any type of closing valve or flow stopper is suitable.

If the liquid phase or the gas phase comprises a solid material then it is preferred to use another

embodiment of the invention. In this preferred embodiment the reactor comprises a rotor provided with rotor blades and which rotor is rotationally mounted in a rotor housing, and the inlet and the outlet are arranged each at a side and near the centre of the rotor axis. Such reactor is suitable for a chemical reaction comprising a liquid phase and a gas phase or a gas phase and a solid phase, or a gas phase, liquid phase and solid phase. The liquid phase passes through a rotor and is temporarily subjected to a high centrifugal force compressing the gas phase. Subsequently, when the reactants and/or reaction products move from the periphery to the center, the centrifugal force decreases resulting in an expansion of the gas phase. Typically can be used as feed for such reactor: (i) gas, gas-liquid, gas- solid, or gas-liquid-solid bubbles in a liquid carrier; or (ii) gas-liquid or gas-liquid-solid without a liquid

carrier. Such a reactor is very suitable for multi-phase reaction systems prone to stratification or phase

separation .

According to another embodiment of the invention the reactor comprises at least one rotational reactor channel of which the distance to a rotation axis increases and decreases between the reactor channel inlet and outlet, and preferably the reactor channel is at least partly formed within a cylindrical rotor. This embodiment is based on the concept that by passing through a rotating reaction channel with an increase and subsequent decrease of the distance to the rotational axis the reaction mixture comprising the gas phase, flowing through the reaction channel is temporarily subjected to compression and thereafter to expansion. By selecting the shape, cross-section of the channel and the rotational speed the extent of compression and expansion and law of compression-expansion can be controlled in elegant manner .

A further embodiment of the invention relates to a reactor comprising an in cross section non-round, preferably oval reaction chamber. The reaction chamber may be round in which the rotor has an off-centered rotational axis, so that in the rotational direction the distance from the rotor to the reaction chamber wall changes. The rotor is rotationally mounted and provided with rotor cavities, and further the liquid phase, such that upon rotation of the rotor a liquid layer is formed on the (non-round) rotation chamber wall filling the rotor cavities dependent on the distance to the reactor chamber wall. This reactor comprises cavities of which the gas phase volume is changing with the distance to the chamber wall and thus the filling of the cavity by the liquid layer present on the wall of the reactor chamber during rotation.

Evidently, the process and reactor of the invention based on the concept of liquid phase based

compression is much wider than that of the compression reactors using solid pistons. The process and reactor can be applied for chemical processes such as synthesis gas

production, (hydro ) cracking, hydrogenation, and the like. Application is also possible for various gas-liquid, gas- solid and gas-liquid-solid high pressure and/or high

temperature processes, including catalytic processes, such as methanol synthesis, hydrogenation of for instance biomass and biomass derived products, oil residues, coal, oil sands, and oil shales, polymerization processes, Fisher-Tropsch synthesis and the like.

Materials with a high density and a low melting point, such as metals, like lead and bismuth, and alloys, such as Rose's alloy and the like, can be used as the liquid phase .

Mentioned and other features of the process and reactor of the invention will be further elucidated by reference to various embodiments that are given only for information purposes and not with the intention to limit the invention in any respect. Thereto reference is made to the following drawings wherein:

Figure 1A shows schematically a first reactor and process of the invention;

Figure IB is a variant of the piston system of figure 1A;

Figure 2 shows another embodiment of the reactor and process of figure 1A;

Figure 3 shows a variant using a hydraulic ramming system; Figure 4 shows a variant using a centrifugal compression and expansion system;

Figure 5A, 5B, and 5C show another variant using a centrifugal compression and expansion system, wherein figure 5C is a cross section over the line A-A in figure 5B; and

Figures 6A, 6B, and 6C show a variant using a submerging compression system, wherein figure 6B is a cross section over the line A-A in figure 6A, and figure 6C is a cross section over the line B-B in figure 6A.

Figure 1 shows a reactor according to the invention. The reactor comprises a standing reactor vessel 1 with lower inlet valve 2 and upper outlet valve 3. Shape of the reactor vessel 1 may be different, preferably a straight tube or column, although bended tubes may be used in order to decrease a footprint or to slow down the bubbles rising speed, or tube of variable cross-section. Both of inlet valve 2 and outlet valve 3 comprise an internal chambers 2a and 3a and actuators 2b and 3b, respectively. The actuators 2b and 3b can be of any suitable type, such as actuators based on electrical, pneumatic, hydraulic, electro

hydraulic, mechanical principles.

Inlet chamber 2a has inlet 2c connected to feed gas line. Outlet chamber 3a has a product outlet 3c. The reactor comprises a gas distributor 4 for dispersing and distributing gas in the liquid.

The reactor vessel 1 is connected to the means for repeatedly compressing and expanding the reaction medium in the reactor vessel 1 by applying force on the liquid phase, and comprises piston means in the form of a hydraulic cylinder 5 with reciprocating piston 6 inside. The piston 6 may be driven using a mechanical transmission (crank gear, swash plate and the like) or hydraulically, pneumatically, and the like. To provide a more even compression-expansion along the reaction vessel there can be several connection lines between hydraulic cylinder 5 and reaction vessel 1, also several hydraulic cylinders may be used.

The reactor is filled with a liquid. The upper chamber 3a is also partly filled with the liquid phase. The liquid phase serves to transmit pressure to the gas phase and may function as heat carrier, catalyst and the like.

Depending on the application, and the conditions and nature of the chemical reaction (s), the hydraulic cylinder 5 may be connected either directly to the reactor or by a pipeline placed sufficiently far to provide low operational temperature of piston seals and guiding

surfaces. If a liquid phase carrier has poor lubrication properties, the piston 6 may compress a more suitable liquid, for instance, hydraulic oil and then transmit the force generated via a membrane or diaphragm 7 (see figure IB) to the liquid phase carrier. In case of non-mixing liquids with different densities, such as combinations of oil/water, oil/liquid metal, an interface between two phases may serve as the diaphragm.

The reactor performs a cyclic operation. In operation a gas feed is supplied to the inlet port 2c. At a certain moment both the valves 2 and 3 open and the feed gas bubbles through the liquid column 1 up to the outlet chamber 3a. Valves 2 and 3 can, to certain extent, open and close independently of each other. Before gas bubbles reach the outlet valve 3 both the valves close and the piston 6 compress the liquid phase. The liquid phase carrier

transmits pressure from the piston 6 and compresses the gas bubbles generating pressure (and temperature) sufficient to perform a target reaction. Then, during back stroke of the piston 6, product gas bubbles expand, and piston recuperates a part of the expansion energy to use it in the next cycle. Then the inlet valve 2 and outlet valve 3 open and the gas bubbles penetrate to outlet chamber 3a and then, trough the outlet port 3c to the product line. Subsequently, the next portion of bubbles is supplied and the cycle is repeated.

The compression and expansion cycle of the same portion of bubbles present in the vessel 1 can be performed as many times as desired dependent on the column residence time .

Depended on the size of the bubbles, properties of the liquid phase, and speed of the piston movement, the compression can be accompanied by a temperature rise or to be almost isothermal.

To maintain the optimal diameter of bubbles different gas distributors such as packings/static mixers may be installed in the reactor.

The production capacity of the reactor is based on the gas bubble formation and on the speed of bubble rise in a liquid phase carrier.

Figure 2 shows the reactor 8 with an increased product capacity. The reactor 8 comprises two reaction vessels 1 with an inlet 2 and an outlet 3 provided with the valves 2a and 3a. The reaction vessels 1 can be of different shape. They can be bended and/or curved, and positioned in different ways.

Both inlet valve 2 and outlet valve 3 include an internal chambers 2a and 3a and actuators 2b and 3b,

respectively. The actuators 2b and 3b can be also based on electrical, pneumatic, hydraulic, electro hydraulic

principles. The outlet valves 3 have outlet ports 3c, and the inlet valves 2 have inlet ports 2c. Both reactor columns 1 are connected to the hydraulic cylinders 5 with

reciprocating pistons 6 inside. In the reactor 8 the inlet ports 2c and outlet ports 3c are connected to a two-phase feed manifold 9, and product gas manifold 11. The inlet manifold 9 has mixing unit 10 to mix a gas feed and liquid. Both reactor columns 1 perform the same cyclic operation but with a phase lag. At the same time both inlet valves 2 and outlet valves 3 are open in one reactor vessels, and closed in the other reactor vessels 1. When a pair of valves 2, 3 is open a gaseous feed in form of bubbles in the liquid phase is supplied to the reactor vessel 1. Subsequently, actuators 2b, and actuators 3b close inlet valves 2, and outlet valves 3, the piston 6 compresses the gas bubbles in the liquid phase carrier and a target chemical reaction takes place. During back stroke of the piston 6 bubbles containing reaction products expand. At the same time the inlet valve 2 and outlet valve 3 of the other reactor vessel 1 are open and reaction products are displaced there by new portion of feed or a new portion of feed bubbles in the liquid. Therefore, compression in one reactor vessel 1 is accompanied by expansion in the other reactor vessel 1, and expansion energy in one reactor vessel 1 is used to provide compression in the other reactor column 1.

The gas-liquid mixture leaving valve chambers 3a through the outlet ports 3c goes to a separator. Hereafter product gas goes to downstream processing whereas the liquid carrier is recycled to the feed gas manifold 9.

The pistons 6 can be driven using mechanical transmission (a crank gear, a swash plate and the like as well as hydraulically or pneumatically. Both pistons 6 operate with a phase lag, i.e. compression in one reactor vessel 1 is accompanied by expansion in the other reaction 1. In case of a sufficiently high exothermicity of the chemical reactions the operation does not require an external energy source to actuate the pistons 6 and a piston driving mechanism is used only for start-up.

Depending on the application, the hydraulic cylinder 5 can be connected both directly to the reactor column or placed sufficiently far to provide low operational temperature of piston seals and guiding surfaces. Also the abovementioned diaphragm pressure transmission or non-mixing liquids interface principles can be used.

The reactor 8 can have many inlet and outlet valves as well as a number of pistons/cylinders. Gas feed can be supplied into the reactor vessels 1 not only via inlet manifold 9, in form of a mixture with carrier liquid but also injected separately, directly to the reactor vessel 1 .

The twin reactor 1 is shown as an example. A multi vessel reactor is also possible. Multi-vessel designs can easily provide shock free flows in the feed manifold 9.

Packing or static mixers inside the reactor 8 can also be used to maintain/control the bubble size, as well as keep the gas feed in form of gas plugs rather then the bubbles.

One of the advantages of the reactor 8 of the invention is that it does not require substantially vertical position. Moreover the reactor vessels 1 can be bended to different curves such as spirals and the like. Reactors of such a kind can also have cooling or heating jackets, internal heat exchangers. The reactors based on compression of the gas phase by a liquid phase transmitting pressure can operate at any speed of compression-expansion. A combination of bubbles size, properties of liquid carrier and speed of compression can give any compression-expansion laws in the range from isothermal to adiabatic ones. Also any profile of compression-expansion or any dependence of compression speed on time during the cycle can be performed, such as rapid compression and rapid expansion, rapid compression and slow expansion, rapid compression then holding at high pressure and rapid expansion etc.

The reactor 8 can work not only with gas phase, but also with two-phase gas-liquid feed, wherein the liquid is dispersed in a gas phase.

For very rapid gas-phase reaction, when selectivity strongly depends on reaction time, hydraulic ram phenomena can be applied (see figure 3) . The installation is shown in figure 3 and comprises a hydraulic accumulator 14, reactor tube 15, feed inlet manifold 19 with inlet valve 18, outlet valve 16 with valve chamber 17 playing in this particular case also a role of a product collector and separator. The valve chamber 17 and accumulator 14 are communicated by a circulation loop 60 provided with

circulation pump 13. In operation a liquid phase carrier is circulated through a pump 13, hydraulic accumulator 14, a reactor tube 15, and then, through outlet valve 16 into a chamber 17 and then back to pump 13.

When an inlet valve 18 opens a portion of gas phase feed is injected through inlet manifold 19 to the liquid carrier flow in the reactor tube 15. When a portion of gas bubbles almost reach the outlet valve 16, then the outlet valve 16 abruptly is closed. This an entire or partial closure causes a compression of the reaction media (hydraulic ram, or hammer phenomena) . The inertia of the liquid phase carrier rapidly compresses the bubbles and a target chemical reaction takes place. The compression of the bubbles is followed by their expansion and cooling of reaction products. Then the outlet valve 16 opens and the portion of bubbles containing reaction products goes to the chamber 17, where gas and liquid are separated. The

expansion can take place also after and as a result of opening valve 16. Then expansion energy is used to provide flow of products to chamber 17. Gas products go to a

downstream processing, liquid carrier returns to the pump 13.

The reactors 1, 8, and 12 are not optimal for carrying out the processes in which the reaction mixture comprises a solid phase. Valve seats do not fit well for operation with solid particles. A reactor 20 according to the invention intended for operation with a two phase system (gas-liquid, and gas solid) and three phase system (gas- liquid-solid) is shown schematically in figure 4.

The reactor 20 comprises housing 21 with an inlet 22 and an outlet 23. A rotor 24 with blades 25 is rotatable in bearings 26 placed inside the housing 21. The bearings 26 are sealed with sealing units 27.

In operation the rotor rotates with a high speed. A feed is introduced into the reactor 20 through the inlet 22, accelerated by the rotor blades 25 and reaches a

peripheral speed of the rotor 24 near internal peripheral wall of the housing 21. Centrifugal force reaches a maximum in this area creating a hydrostatic pressure compressing the bubbles, and/or gas plugs formed in between the rotor blades to the optimal reaction pressure and temperature. The thickness of the rotor can be made as large as necessary for the desired reaction residence time.

Then the reaction mixture flows in back direction, towards rotational axis 28. During the following flowing the speed and acceleration of the mixture and accordingly the hydrostatic pressure drops down. Gas in the bubbles or gas plugs expands and then the mixture leaves the reactor 20 through the outlet 23 for a separation. Therefore the left, feed side of the rotor 24 works as a compressor whereas the right, product side does as a turbine. A part of the work spent on compression (and heating) of the feed is recovered and used for the

compressive heating of a next portion of feed. Some energy losses in form of heat can be used in chemical reaction.

The rotation of the rotor 24 may be provided by means of electric motor, gas or steam turbine, directly by steam or by means of use of feed stream energy. The reactor rotor 24 may contain additional actuation blades, or a part of the rotor blades 25 can be used for the actuation.

For instance, the pressure P depends on reaction mixture density p and peripheral speed v approximately as P = pv ² /2. If a high density liquid such as Rose's alloy (density about 9440 kg/m ³ ) is used then at small volume gas content and v = 300 m/s, the pressure will be about 4200 bar. Maximum practicable pressure is restricted only by mechanical strengths of the reactor.

A second embodiment of a reactor 29 using

centrifugal force to compress-expands a feed is shown in figures 5A and 5B . The principle is illustrated in figure 5A.

The reactor 29 comprises a curved pipe 30 which rotates around axis XX. A two- or three-phase mixture flows through the pipe 30 and experiences a centrifugal force. A pressure generated by the centrifugal force compresses bubbles and gas plugs inside the liquid flowing through the pipe 30. When the mixture flows in radial outward direction from the axis XX, the pressure increases. Then the mixture flows parallel to the axis XX the pressure remain constant. This is reaction zone 31, where pressure and temperature reach a maximum, optimal for a target chemical reaction. Afterwards, the radial inward flow of the mixture in the direction towards the axis XX, is accompanied with a

decrease of the centrifugal force and pressure. Reaction products expand and leave the reactor 30. Shape and size of the bended pipe 31 determine and influence the pressure-time and temperature-time history. Both should be selected in accordance with the desired reaction path to influence conversion and selectivities .

To provide sufficient strength and balancing the reactor, another embodiment is shown in figure 5B . The reactor 32 is a cylindrical rotor 33 comprising a central body 34, two covers 35 and an external reinforcing liner 36. The liner 36 is preferably made of high-strength low-density fiber reinforced material. The rotor 33 has a plurality of channels 37 inside. Each channel 37 represents the rotating, curved pipe 30 described above. The rotor 33 rotates on bearings 38. An external housing is not shown for the sake of simplicity.

There are two ports 39 intended to deliver feed inside the rotor 33 and remove reaction products. The ports 39 are sealed with sealing units 40. To maintain a certain size of bubbles and/or plugs, static mixers 41 can be installed inside the rotor channels 37.

A rotation of the rotor 33 can be provided by electric motor, gas and steam turbine. Also the rotor 33 itself can be used as a rotor of electric motor or turbine. In the latter case it can have blades on the external surface. Blades machined or fixed inside the covers can be also used. In this case energy of feed stream can be use to provide the rotation.

In operation the rotor 33 rotates in bearings 38.

A two- or three-phase mixture is delivered inside one of the covers trough the inlet port 39, distributed between the channels 37, and flows in radial outward direction, then parallel to the axis of rotation and afterwards from the periphery to the axis of rotation and the outlet port 39.

Figure 6 shows an embodiment of the invention in which the cycle of compression-expansion by liquids can be performed not only inside the bubbles or gas plugs but also in relatively big cavities formed in a solid body. Such cavities may be bigger than the bubbles and provide less heat losses and accordingly make the process closer to adiabatic. This principle of such reactor 44 is shown in figure 6. The reactor 44 comprises a casing 45 closed by two covers 46 and 47. The covers 46 and 47 have inlet 48 and an outlet 49 ports. The casing 45 has an oval working chamber

50 with rotor 51 inside rotating on bearings 52. The rotor

51 has several identical clove-shaped slots or gas cavities 53 (eight slots 53 in figure 6A) . The slots 53 function as reaction chambers where a feed is compressed by a liquid 54. The working chamber 50 is partly filled with an appropriate liquid. When the rotor 51 rotates the liquid forms an oval ring 56 on the internal surface 55 of the working chamber 50. The liquid layer in operation plays the role of a piston compressing gas cavities inside the slots 53. During every 180 degree rotation of the rotor 51, three phases can be distinguished for each slot 53 depending on its angular position :

- gas, gas-solid or gas liquid feed can freely flow through the slot 53 (small arrows 57 in figure 6B) . This position of the slot 53 is shown as a gas exchange phase when the feed fills in the slot 53 and displaces reaction products.

- the feed is trapped inside the slot 53 and subsequently is compressed by the liquid 54. An ultimate stage of the compression is shown in section B-B of figure 6A. If rotational speed of the rotor 51 is sufficiently high the compression occurs rapidly and results in an increase of temperature and pressure of the feed providing optimal conditions for many chemical reactions.

- products expand rapidly when the liquid leaves the slot. The expansion is accompanied by a rapid cooling (quenching) of products.

Chemical reactions take place at the end of the compression and before the expansion when the pressure and temperature of compressed media are sufficiently high.

For some reactors liquid carriers of very high density (such as low melting point metal alloys like Rose's alloy with melting point below 47°C and the like) can be used to influence/control the process. In case of a

feed/product containing solid particles main or especially intended auxiliary seals can be permanently blown with a pressurized pure liquid to avoid penetrating particles through seals. A wearless operation of solid pistons and bearings in the aforementioned reactors especially at high temperature can be achieved via application of the

contactless hydrostatic bearing technology. In that case liquid carrier or liquid feed/product component itself can be used as a working liquid for hydrostatic bearing.

Draining of this pressurized bearing working liquid directly to reaction chamber can protect the hydrostatic bearing from penetration of solid particles.