RU2531399C2 - Reactors for continuous processing and methods of their use - Google Patents

Abstract

FIELD: machine building.

SUBSTANCE: invention relates to continuous processing reactors, the system containing such reactor, and the method of processing of fluid medium. The reactor contains the external tank with an internal surface, opposite to which the processed fluid medium can be located, internal tank, located inside the external tank and having an external surface, serving as a radiator surface for the processed fluid medium, and internal surface, designed so that to allow the heat exchange fluid medium to flow, in essence, above the uniform thin film, and the annular space formed between the external tank and the internal tank, to ensure the passing, along which the processed fluid medium can move, where the given annular space is designed so that to maintain a temperature difference between the external tank and internal tank, ensuring relatively high speed of movement of the fluid medium.

EFFECT: invention ensures uniform thin distribution of the processed fluid medium on the surface of processing, improvement of mixing of components, high speeds of transfer and high efficiency.

49 cl, 9 dwg, 6 ex

Description

FIELD OF TECHNOLOGY

The present invention relates to processing reactors and, more specifically, continuous processing reactors, which can impart high heat transfer, mass transfer, mixing speeds and other high transfer speeds to the process fluid.

BACKGROUND

A common problem in chemical reaction processes is achieving the required hydrodynamics in the reactor in order to efficiently produce the desired products. The reagents must be mixed so that the molecules of the components of the reaction come into contact with other components in the reaction, including catalysts. The presence of a gaseous reactant may additionally require an increase in the surface area at the interface between the gas and liquid components to increase the efficiency of the reaction.

To improve mixing and contact between the reaction components, thin-film reactors have been developed, including, but not limited to, applying a catalyst to the inner surface (i.e., treatment surface) of the treatment chamber. In addition, to enhance the adhesion of the catalyst to the treatment surface of the treatment chamber, the sol-gel technology or thincoat (washcoating) can be applied to the treatment surface. However, over time, the coating tends to suffer from abrasion and inevitably deactivate.

Addressing the need to increase the surface area between the components, certain thin-film reactors have been developed, including a rotary distributor, which can be used to distribute material, such as a process fluid, to the inner wall. However, since these reactors combine high-intensity heat transfer and a short residence time of the processed materials, this design can cause the materials to expand rapidly when materials enter the treatment chamber due to the sudden temperature difference between the treatment chamber and the source, causing uneven spraying of the material on the inner wall processing cameras.

Other thin-film reactors are equipped with one or more rotating brushes that can be applied to the inner wall of the treatment chamber by distributing the materials to be processed onto the inner wall (i.e., the treatment surface). However, direct contact of the brushes with the treatment surface can lead to contamination of the material, as well as undesirable wear of the brushes and the inner wall of the reactor. In addition, due to the necessary arrangement of brushes, obtaining a uniform thin film along essentially the entire length of the inner wall of the processing chamber remains a problem. In the presence of a viscous fluid, material may accumulate due to non-uniform flow. When this happens and the accumulated material is in contact with the brushes, the rotating system may lose mechanical balance and rotation may be disturbed.

Thin-film reactors are also equipped with a rotating disk, from which the processed fluid is distributed to the processing surface of the processing chamber. Unfortunately, such reactors are not adapted to provide a sufficiently long residence time and are not suitable for high capacities. In addition, the current design of thin-film reactors may be such that these thin-film reactors lack the ability to provide high transfer rates, i.e., relatively high rates of heat transfer, mass transfer or mixing, or a combination thereof, due to the fluid being treated.

Accordingly, there is a need for a thin-film reactor with a structure that can provide a substantially uniform fine distribution of the processed fluid or material on the treatment surface, which can enhance mixing and / or contact between the reaction components, which can provide a sufficiently long residence time, and which can provide relatively high transfer speeds, while ensuring high productivity.

SUMMARY OF THE INVENTION

According to one embodiment of the present invention, a fluid processing reactor is provided. This reactor includes an external reservoir having an inner surface, against which the process fluid may be located. The inner surface of the external reservoir, in one embodiment, can be designed to allow the process fluid to dip into a substantially uniform thin film, allowing the process fluid to have a relatively high rate of heat transfer, mass transfer, mixing, other transfer rates, or a combination thereof . The inner surface of the external reservoir may also be provided with a profiled pattern to create additional surface area over which the fluid to be treated can flow, facilitating one of the processing, processing, separation, extension of residence time, or a combination thereof. The reactor also includes an internal tank located inside the external tank and having an external surface serving as a heat exchange surface for the fluid being treated. The inner reservoir, in one embodiment, includes an inner surface, against which a heat exchange fluid may flow. The heat transfer fluid generally has a temperature that may differ from the temperature of the fluid being treated, causing a temperature difference between the outer surface of the inner reservoir and the inner surface of the outer reservoir. The reactor further includes an annular space defined between the external reservoir and the internal reservoir to provide a passage along which the process fluid may be supplied. The annular space, in one embodiment, can be designed to maintain a temperature difference between the external tank and the internal tank, giving the process fluid a relatively high transfer rate. In addition, the annular space may comprise a second fluid for interacting with the fluid being treated. In one embodiment, the second fluid may move countercurrently within the annulus relative to the flow of the fluid being treated. A layer of packed material can also be provided within the annular space to increase the surface area over which the volume of the fluid being treated can contact, to increase its transfer rates, and to ensure a substantially uniform temperature distribution over the annular space.

In another embodiment of the present invention, a method for processing a fluid is provided. This method includes first introducing the process fluid into the external reservoir and opposite its inner surface. At this stage, a substantially uniform thin-film flow of the fluid to be treated can be provided opposite the inner surface of the external reservoir, increasing the ability of the fluid to be processed, processed and / or separated, and also allowing the fluid to be processed to have a relatively high rate of heat transfer, mass transfer, mixing or a combination thereof. In one embodiment, the fluid to be treated may be rotationally distributed to form substantially thin droplets or filamentary elements on the inner surface of the external reservoir.

This method also includes providing, inside the external tank, an internal tank with a heat exchange surface with a temperature different from the temperature of the processed fluid. At this stage, a heat transfer fluid provided at a temperature different from the temperature of the process fluid may be distributed opposite the inner surface of the inner tank. The distribution of the heat exchange fluid can occur in a rotational manner, forming essentially thin drops or filamentary elements on the inner surface of the inner tank. This method further includes maintaining a temperature difference across the passage between the external tank and the internal tank, giving the process fluid therein relatively high transfer rates. The maintenance step, in one embodiment, includes providing a passage with a relatively short distance between the outer surface of the inner reservoir and the inner surface of the outer reservoir. In addition, the second fluid may be directed into a given passage and may be allowed to interact with the fluid being treated. In one embodiment, the second fluid may be allowed to move countercurrently with respect to the flow of the fluid being treated. To the desired degree, a layer of packing material can be placed inside this passage to increase the surface area over which the fluid to be treated can come into contact to increase transfer rates. In such an embodiment, the volume of fluid to be treated can be introduced into the external reservoir and into this passage.

The reactor and processing method of the present invention can be used for various applications, including fluid-fluid or solid-fluid-fluid interactions in connection with organic systems, distillation and evaporation, cooling of superheated steam, reactions initiated by ultraviolet and / or microwaves desalination and removal of carbon dioxide, among other things.

The reactors of the present invention can also be arranged in series, allowing multiple passes of the process fluid through each of the reactors to increase transfer rates. If desired, each reactor in the system can be designed for a different function. The reactor of the present invention, alternatively, may include a third reservoir inside the inner reservoir to provide another annular space between the third reservoir and the inner reservoir, allowing multiple passages of the process fluid through such a reactor. Additional tanks may be further provided, where each is sequentially inside the previous internal tank, if desired.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a longitudinal sectional view of a processing system having a continuous reactor for providing a fluid-fluid or solid-fluid-fluid reaction according to one embodiment of the present invention.

FIG. 2 is a longitudinal sectional view of another continuous reactor for providing fluid-fluid or solid-fluid-fluid reactions according to one embodiment of the present invention.

FIG. 3 is a longitudinal sectional view of yet another continuous reactor for providing fluid-fluid or solid-fluid-fluid reactions according to one embodiment of the present invention.

FIG. 4 is a longitudinal sectional view of another continuous reactor for providing a fluid-fluid or solid-fluid-fluid reaction according to one embodiment of the present invention.

FIG. 5 is a longitudinal sectional view of a continuous reactor for performing evaporation and / or distillation processes according to one embodiment of the present invention.

FIG. 6 is a longitudinal sectional view of a continuous reactor for cooling superheated steam according to one embodiment of the present invention.

FIG. 7 is a longitudinal sectional view of a continuous reactor for performing reactions initiated by UV and / or microwaves, according to one embodiment of the present invention.

FIG. 8 and 9 depict additional embodiments of the reactor of the present invention.

DESCRIPTION OF SPECIFIC EMBODIMENTS

According to one embodiment of the present invention, there is provided a processing system having a reactor for continuous processing of materials. This reactor can provide the processed materials with a sufficiently long residence time to increase mixing and / or contact between the reaction components, and can provide relatively high transfer rates, while at the same time providing high productivity.

The reactor generally includes an external tank containing materials (e.g., fluids and / or solids) processed or used in connection with them, an internal tank located inside the external tank, serving as an energy exchange surface, and an annular the space defined between the external and internal tanks and along which a temperature difference can be provided to cause relatively high transfer rates, while at the same time providing high productivity due to processing aemymi materials.

Reactor

Turning now to FIG. 1, according to one embodiment, the processing system of the present invention may be equipped with a reactor 10 for, inter alia, continuous processing. As depicted, the reactor 10 includes an external reservoir 11 for receiving processed fluids. The external reservoir 11, in one embodiment, includes a body 12, within which the processed fluid or fluids may be contained and, if desired, any material used in connection with this. In one embodiment, the body 12 may be substantially cylindrical in shape and may include an upper end 121 and a lower end 122. The body 12 may also include an inner surface 123 (i.e., a machining surface) and an opposite outer surface 124 extending between the upper end 121 and the lower end 122 of the body 12. The inner surface 123, in one embodiment, can be designed so that the fluid being processed can be opposite or on it. In one embodiment, the fluid to be treated may be able to flow down along the length of the inner surface 123 in the direction of the arrows 125 in a substantially uniform thin film. The substantially uniform flow of fluid along the inner surface 123, in one embodiment, can be facilitated, for example, by gravity. By allowing the fluid to flow substantially uniformly in the form of a thin film, the fluid can be well suited for processing and / or separation at a relatively high level of energy efficiency, while at the same time giving the fluid relatively high transfer rates (i.e., velocities heat transfer, mass transfer and / or mixing). According to one embodiment of the present invention, the thin film flow provided on the inner surface 123 of the outer reservoir 11 may have a thickness in the range of about 1.0 microns to about 1.0 cm. However, it should be understood that the thickness is less than the provided interval and greater than the provided the range is also considered depending on the specific application, since the reactor 10 of the present invention is not intended to be limited in this way.

Since the outer reservoir 11 can be designed to give the process fluid relatively high transfer rates to the extent that it is desirable to further increase the rates of heat transfer, mass transfer, mixing and / or other, relatively high transfer rates, the inner surface 123 can be profiled to create additional surface area over which the process fluid can flow. In particular, by providing an additional surface area over which the fluid to be treated can flow, the residence time or the period of time during which heat transfer can take place to or from the fluid can be increased. A profiled pattern of the inner surface 123 may also help increase the surface tension of the fluid flowing along the inner surface 123, and may help maintain a substantially thin and even film of fluid along the inner surface 123. An example of the profiled pattern for the inner surface 123 includes grooves. The grooves, in one embodiment, can be arranged horizontally, vertically, in a zigzag pattern, or with any other design. Although grooves can be provided along the inner surface 123, other shaped patterns can be provided, such as recesses, bulges, wavy irregularities, as long as these shaped patterns can help increase transfer rates.

In addition to, or instead of providing the inner surface 123 of body 12 with a profiled pattern, the inner surface 123 may include a coating to facilitate processing, processing and / or separation, while at the same time providing a flowing medium flowing along the inner surface 123 with relatively high transfer rates. In one embodiment, the coating may have any chemical, physical, electrical, magnetic or other properties known in the art.

It should be understood that although depicted is cylindrical in shape, the body 12 of the external reservoir 11 can be provided with any shape or configuration, for example, triangular, square, hexagonal, octagonal or any other geometric configuration with any desired length and diameter depending on the application. In addition, the body 12 can be made of any solid material, including metal, metal alloy, plastic, glass, quartz, ceramics or any other solid materials that can carry out heat transfer, remain at a certain temperature and / or carry out a temperature change, as necessary .

Referring again to FIG. 1, the outer reservoir 12 of the reactor 10 may also include a lower portion 13 designed to collect and remove, among other things, fluids that have been processed and that have passed along the inner surface 123 of body 12. In addition, the lower part 13 may also be designed to introduce another fluid or fluids into an external reservoir 11 for use in connection with a process fluid. The lower portion 13, in one embodiment, may be integrated with the body 12. Alternatively, the lower portion 13 may interchangeably attach to the body 12, providing a substantially tight seal thereto. In order to provide a substantially tight seal, the body 12 and the lower part 13 can be provided complementary to the inlet flanges 131, which can be fastened together using screws, nuts and bolts, or any other mechanisms known in the art. A rubber ring or other similar seals may also be provided between complementary inlet flanges 131 to increase the tight seal. Of course, other designs may be used, other than the use of flanges 131, while a substantially tight seal can be provided. In addition, to the desired extent, the lower part 13 can be pivotally attached to the body 12.

To allow removal of the treated fluid collected in the lower portion 13, at least one outlet 132 may be located at some location along the lower portion 13 so that the removal of the collected fluid can be sufficiently performed. In one embodiment, the fluid removed from the bottom 13 may be collected by a sump (not shown) located near the exit 132, and using any other means known in the art. Alternatively, to enter fluid into the external reservoir 11, an inlet 133 may be provided anywhere along the bottom 13 through which fluid may be introduced. In certain applications, in order to minimize interaction with other fluids that can be introduced into the reactor 10 through the lower portion 13, a divider 134 may be located near the outlet 132 to substantially prevent the fluid flowing along the inner surface 123 of the body 12 from flowing downstream 132 and down to lower portion 13, where other fluids may be present.

As depicted, the lower portion 13 may be parabolic in shape. However, it should be understood that the lower part 13 can be conical, flat or have any other geometric shape, which can correspond to the geometric profile of the lower end 122 of the body 12. Since the lower part 13 can be used to contain one or more fluids, it can be made of any solid material similar to the material of which the body 12 is made, including metal, metal alloy, plastic, glass, quartz, ceramics or any other solid materials that can be supported by a certain temperature and / or allow temperature change as necessary.

The outer reservoir 11 of the reactor 10 may further include an upper portion 14 for holding processable fluids within the outer reservoir 11. The upper portion 14, like the lower portion 13, may be integral with the body 12. Alternatively, the upper portion 14 may be removably attached to body 12, providing a substantially tight seal with it. In order to provide a substantially tight seal, the body 12 and the upper part 14 may be provided with complementary incoming flanges 141, which can be fastened to each other by using screws, nuts and bolts, or any other mechanisms known in the art. A rubber ring or other similar seals may also be provided between complementary inlet flanges 141 to increase the tight seal. Of course, other designs may be used, other than the use of flanges 141, while a substantially tight seal can be provided. In addition, to the desired extent, the upper part 14 can be pivotally attached to the body 12.

In one embodiment, the upper part 14 may be equipped with at least one exhaust 142, providing removal of any fluid, including liquid and gas, which can be used in connection with the processing of the fluid flowing along the inner surface 123 of the body 12. Exhaust 142 can also be used to release any gas that can be used by increasing the pressure of the external reservoir 11 during processing of the flow medium along the inner surface 123. As shown, the upper part 14 may be parabolic th form. However, it should be understood that the upper part 14 may be conical, flat or have any other geometric shape, which may correspond to the geometric profile of the upper end 121 of the body 12. In addition, since the upper part 14 may have to withstand high pressure, it may be desirable to do top 14 of any solid material similar to the material of which body 12 is made, including metal, metal alloy, plastic, glass, quartz, ceramics, or any other solid materials that can support vatsya at a certain temperature and / or allow a change of temperature as needed.

It should be noted that, although referred to as exhaust, inlet or outlet, these openings or apertures can be used to introduce or remove fluid from the external reservoir 11.

Referring again to FIG. 1, in addition to the outer reservoir 11, the reactor 10 may further include an inner reservoir 15 located inside the outer reservoir and designed to provide a heat exchange surface for the fluid flowing along the inner surface 123 (i.e. processing surface) of the outer reservoir 11. The inner reservoir 15, in one embodiment, may be substantially cylindrical in shape and concentrically located inside the outer reservoir 11, so that the inner ervuar 15 and outer tank 11 may be substantially axially aligned with each other. In addition, the inner reservoir 15 can be provided with a significantly smaller diameter relative to the diameter of the outer reservoir 11, so that an annular space 16 can be defined between the inner reservoir 15 and the outer reservoir 11, providing a passage along which fluid can be processed along the inner surface 123 of the outer reservoir 11. In one embodiment, the size and diameter of the inner reservoir 15 and the outer reservoir 11 or the ratio of one reservoir to another may vary and may be beyond Ana, depending on the particular application. In order to maintain the inner reservoir 15 in its position inside the outer reservoir 11, the inner reservoir 15 may be located on the uprights or legs 151. Since the legs 151 may be located inside the bottom 13 of the outer reservoir 11, where fluid flow may be required everywhere, the legs 151 may be porous to allow the flow of fluid to occur everywhere.

As depicted, the inner reservoir 15 may include a body 17 designed to serve as a heat exchange surface inside the reactor 10. In particular, the body of the inner reservoir 17 may include an outer surface 171 and an inner surface 172 along which the heat exchange fluid may flow in the direction of arrows 173. In one embodiment, the heat transfer fluid flowing along the inner surface 172 of the inner tank 15 may be provided at a different temperature relative to the process fluid flowing along the inner surface 123 of the outer reservoir 12. By providing a heat exchange fluid with a different temperature, temperature differences can occur across the annular space 16 between the inner surface 123 of the outer reservoir 11 and the outer surface 171 of the inner reservoir 15, contributing to relatively high transfer rates during processing, processing and / or separation of the fluid flowing along the inner surface 123 of the outer tank 12. Examples of heat transfer fluid s medium include water, oil, glycol mixture, Dow Therm _TM or any fluid capable of performing heat exchange.

The inner surface 172 of the inner reservoir 15, like the outer surface 123 of the outer reservoir, in one embodiment can be designed so that the heat transfer fluid can flow down along the length of the inner surface 172 in a substantially uniform thin film. The substantially uniform flow of the heat exchange fluid along the inner surface 172, in one embodiment, can be facilitated, for example, by gravity. According to one embodiment of the present invention, the thin film flow provided on the inner surface 172 of the inner reservoir 15 may have a thickness in the range of about 1.0 microns to about 1.0 cm. However, it should be noted that the thickness is less than the provided interval or greater than the interval provided is also considered application-specific, since the inner tank 15 of the present invention is not intended to be limited in this way.

To help increase the relative surface tension to maintain a substantially thin and uniform film of fluid along the inner surface 172 of the inner reservoir 15, the inner surface 172 may be provided with a profiled pattern (not shown), similar to the pattern provided along the inner surface 123 of the outer reservoir 11. Examples of a profiled pattern for the inner surface 172 of the inner reservoir 15 include grooves. The grooves, in one embodiment, can be arranged horizontally, vertically, in a zigzag pattern, or with any other design. Although grooves can be provided along the inner surface 172, other shaped patterns can be provided, such as recesses, bulges, wavy irregularities, as long as these shaped patterns can help increase the uniformity of the thin-film flow.

It should be understood that although depicted is cylindrical in shape, the body 17 of the inner reservoir 15 can be provided with any shape or configuration, for example a triangular, square, hexagonal, octagonal or any other geometric configuration with any desired length and diameter depending on the application. In addition, the body 17 can be made of any solid material, including metal, metal alloy, plastic, glass, quartz, ceramics or any other solid materials that can carry out heat transfer, remain at a certain temperature and / or carry out a temperature change, as necessary in order to generate a temperature difference across between the inner surface 123 of the outer tank 11 and the outer surface 171 of the inner tank 15.

The inner tank 15 of the reactor 10 may also include a lower end 18 for collecting and removing heat transfer fluid that can move downward from the inner surface 172 of the body 17. The lower end 18, in one embodiment, can be integrated with the body 17, providing an essentially tight seal with the body 17. To perform removal of the collected fluid from the lower end 18, an outlet channel 181 may be provided. In one embodiment, the outlet channel 181 may be in fluid communication with the bottom 13 of the outer reservoir 11, so that the heat transfer fluid can exit from the inner reservoir 15 to the lower part 13 of the outer reservoir 11, where it can then be removed through the outlet 182. As shown, the lower end 18 may be conical in shape. However, it should be noted that the lower end 18 may be parabolic, flat, or any other geometric shape as long as it can direct the heat transfer fluid to the outlet channel 181.

The inner reservoir 15 of the reactor 10 may further include an upper end 19 for holding the heat exchange fluid inside the inner reservoir 15. The upper end 19, in one embodiment, may be integral with the body 17, providing a substantially tight seal with the body 17 Like the lower end 18, the upper end 19 of the inner reservoir 15 may be conical in shape. However, it should be understood that the upper end 19 may be parabolic, flat, or any other geometric shape as long as it can act while holding the heat-exchange fluid inside the inner tank 15.

In one embodiment of the present invention, the upper end 19 and lower end 18 of the inner reservoir 15 may be made of any solid material similar to that provided for the body 17 of the inner reservoir. Examples of such a material include metal, metal alloy, plastic, glass, quartz, ceramics, or any other solid materials that can carry out heat transfer, remain at a certain temperature, and / or carry out a temperature change as necessary.

As indicated above, the annular space 16 may be located between the inner surface 123 of the outer tank 11 and the outer surface 171 of the inner tank 15, maintaining a temperature difference between them to facilitate processing, processing and / or separation, while at the same time allowing fluid to flow along the inner surfaces 123 with relatively high transfer rates. In one embodiment of the present invention, since the annular space 16 provides a passage along which fluid processing can take place along the inner surface 123 of the outer reservoir 11, the annular space 16 can be provided with a structure allowing at least a second fluid (t ie gas or liquid) enter the annular space 16 for contact and interaction with the descending process fluid. The second fluid, in one embodiment, may be able to move upward (ie, upward flow) within the annular space 16 and along the direction of the arrows 161 in countercurrent with respect to the downward flow of the fluid being processed along the direction of the arrows 125. By creating a countercurrent flow between the upward the second fluid and the downward fluid to be treated fluid the contact points at the interface between the second fluid and the process fluid may increase above the relative but a larger surface area, causing a relatively high transfer rate.

In addition, the residence time or the period of time during which contact between the descending fluid and the ascending fluid within the annular space 16 can occur can be substantially increased by providing one or both of the inner surface 123 of the outer reservoir 11 and the outer surface 171 of the inner reservoir 15 profiled pattern. A profiled pattern may be used, such as that of figure 174 shown on the outer surface 171 of the inner reservoir 15. Alternatively, other profiled patterns such as grooves, protrusions, recesses, and undulations may be used. Each of these patterns can also be arranged horizontally, vertically, in a zigzag pattern, or with any other design mentioned above. For illustrative purposes, the shaped profile shown 174 may be performed on each of the inner surface 123 of the outer reservoir 11 and the inner surface 172 of the inner reservoir 15. By increasing the residence time of the process inside the annular space 16, this process, in one embodiment, can be provided with a relatively higher energy and processing efficiency than others.

The annular space 16 according to one embodiment of the present invention may have a width in the range of about 0.2 cm to about 2 cm. However, it should be understood that the annular space with any size of width can be used. Due to the relatively short distance across the annular space 16, the difference or temperature gradient that can be created inside the annular space 16 can also lead to relatively higher energy and processing efficiency. In addition, due to the design of the reactor 10, the annular space 16 can be maintained under vacuum in connection with certain applications to improve reaction kinetics. It should be understood that, since the second fluid can be directed into the annular space 16, the size and design of the divider 134 located near the outlet 132, can allow the divider 134 to extend into the annular space 16, at the same time without coming into contact with the inner tank 15 Thus, the presence of the divider 134 makes it possible to introduce a second fluid into the annular space 16, while maintaining a sufficient length to direct the fluid from the inner surface 123 of its reservoir 11 through the outlet 132.

In order to further impart and increase the transfer rates of the process fluid along the inner surface 123 of the outer reservoir 11, an energy source, such as a heat pump casing 111, can be provided around the circumference of the body 12 of the outer reservoir 11, acting as a source of heating or cooling of the fluid flowing along the inner surface 123. For example, if the interaction between the downward process fluid and the upward second fluid inside the annular space 16 leads to a noticeable and When changing the temperature of the downward fluid, the casing 111 can be used to adjust the temperature of the downward fluid up or down, as required, until the desired temperature is reached.

The casing 111 in one embodiment may be any commercially available heat pump and may include inductive, resistive, or conductive elements. The casing 132 may further include additional components to improve heat production. Alternatively, instead of a heat pump, the casing 111 may be designed to allow fluid to pass through it at a relatively elevated temperature or at a relatively cold temperature to act as a source of heating or cooling of the fluid flowing along the inner surface 123 of the outer reservoir 11. When this, the casing 111 may include channels 112 that allow gases, liquids or fluids to enter or exit the casing 111. In one embodiment, the casing 111 may be made of m metal, metal alloy, plastic, glass, quartz, ceramics or any other materials that can maintain and cause warm or cold temperatures.

One of the advantages of the reactor 10 of the present invention is the ability to provide a substantially uniform thin film along the inner surface 123 of the external processing tank 11. To do this, the reactor 10 uses, according to one embodiment, the fluid distribution system 101 of FIG. 1. The distribution system 101, in one embodiment, may include a passage 102 designed to introduce a process fluid from a source (not shown) into the interior of the external reservoir 11. The distribution system 101 may also include a first rotational element 103, such as a disk, in fluid communication with the passage 102, so that fluid from the passage 102, if desired, can be continuously directed to the first rotational element 103 and then distributed to it on the inner surface 123 of the outer reservoir 11.

It should be understood that the element 103, in one embodiment, can be designed so that its rotation causes a centrifugal action, causing the fluid received from the passage 102 to be directed outward to the periphery (ie, the edge) of the element 103. The rotation of the element 103 may further cause the fluid at the periphery of the element 103 to continuously spin from the element 103 into substantially thin droplets or filamentary elements onto the inner surface 123 of the outer reservoir 11. Continuous supply of substantially thin drops or filaments 's elements on the inner surface 123 allows the formation of a substantially uniform thin film when processed fluid descends along the inner surface 123.

In the embodiment shown in FIG. 1, the element 103 may be located on top of the long pipe 104 inside the external reservoir 11 and at a distance from the passage 102. The illustrated long pipe 104 can extend through and from the lower part 13 of the external reservoir 11 to the internal reservoir 15 and through the upper end 19 of the inner tank 15, so that it is essentially axially aligned with the passage 102. In one embodiment, the pipe 104 may concentrically be located inside the outlet 182, through which the exit fluid from inner tank 15.

The distribution system 101 may also include a second rotary element 105 in fluid communication with the pipe 104 and located inside the inner reservoir 15. The second rotational element 105, in one embodiment, can be used to distribute a substantially uniform thin film of heat transfer fluid to the inner surface 172 of the inner reservoir 15. As shown, the second element 105 may be perforated so that fluid directed along the pipe 104 can be distributed from the second element 105.

Like the first rotary element 103, the second rotational element 105 can also be designed so that its rotation causes a centrifugal action, forcing the fluid received from the pipe 104 to be directed outward to the periphery (ie, the edge) of the element 105. Rotation of the second element 105 may additionally cause the fluid at its periphery to be continuously distributed through its perforations in the form of substantially thin droplets or threadlike elements on the inner surface 172 of the inner reservoir 15. Continuous over Acha substantially fine droplets or filiform elements to the inner surface 172 allows the formation of a substantially uniform thin film when processed fluid descends along the inner surface 172.

The distribution system 101 may further include a motor (not shown) designed to cause rotation of the pipe 104, for example, in the direction shown by arrow 106, and thus the rotation of the elements 103 and 105. This motor, in one embodiment, can be attached to the end of the pipe 104, the opposite end, on which the element 103 is located, and can be designed to rotate at a sufficient speed. In one embodiment, the rotational speed of the motor can be adjusted so that the rotational speed can be changed as desired. For example, a given velocity may vary to ensure uniform distribution of the thin film when the flow velocity of the fluid may vary.

Although depicted being located at a distance from the passage 102, the position of the first rotational element 103 inside the distribution system 101, as shown in FIG. 2, may be such that the rotational element 103 can be substantially in contact and in fluid communication with the passage 102. In the embodiment shown in FIG. 2, the passage 102 may be a continuation of the pipe 104 and may remain substantially axially aligned with the pipe 104. In other words, the pipe 104 can be extended so that it can extend extending from the upper end 19 inside the early reservoir 15 and through the upper part 14 of the outer reservoir 11. The first rotational element 103, on the other hand, may include holes (not shown) around its periphery, so that the fluid directed into the rotational element 103 can be distributed from the element 103 through these openings to the inner surface 123 of the outer reservoir 11. A motor (not shown) can be connected to the end of the pipe 104 extending from the upper part 14 of the outer reservoir 11 and can cause the tube 104 to rotate in the direction of arrow 20. Of course, if desired, yes The motor may alternatively be connected to the opposite end of the pipe 104 near the bottom 13 of the outer reservoir 11.

The first rotational element 103 shown in FIG. 2 may be a hollow disk, a hollow tube, or any other design as long as it is rotational and capable of being provided with holes around its periphery for distribution purposes. However, it should be understood that, as shown in FIG. 3, the rotary element 103 may also be provided with a design similar to the second rotational element 105. More specifically, the rotational element 103 may be provided with a plurality of perforations such that a fluid is guided along the pipe passage 102 104 may enter and be distributed from the rotary element 103.

Turning now to FIG. 4, for certain applications, instead of containing a thin film of fluid, the annular space 16 of the reactor 10 can be filled with the volume of the fluid being processed. In such an embodiment, the continuous reactor 10 of the present invention can be provided with a layer of packing material 40 within the annular space 16. A layer of packing material 40 can be used to increase the surface area over which a given volume of the fluid to be treated can come into contact to increase transfer rates. In one embodiment, the packing material 40 may include sieve-like materials, balls, monolith, or any other material that can provide a substantially tortuous passage through which the fluid to be processed must pass, increasing the residence time or the period of time during which fluid can be processed. In such an embodiment, the reaction may include countercurrent gas introduced into the annular space 16 in the presence of the fluid being treated. By introducing it, countercurrent gas can form bubbles in the volume of the fluid, which can be directed upward through the layer of packing material 40. In addition, the presence of a winding path within the layer of packing material 40, as well as packing material 40 can act by splitting or splitting each bubble into multiple smaller bubbles. Thus, an increase in surface area can be caused over a much larger number of bubbles for reaction with the fluid being treated. In one embodiment, when smaller bubbles are formed, the packed bed 40 can act to substantially uniformly distribute the bubbles within the fluid volume in the annular space 16.

Optionally, the packing material 40 may be coated with a catalyst layer to facilitate processing, processing and / or separation, while at the same time adding a relatively high transfer rate to the fluid flowing through the annular space 16. In one embodiment, the packing material 40 may be heated or cooled, for example, by a casing 11 through the inner surface 123 of the outer reservoir 11 and / or by heat exchange fluid through the outer surface 171 of the inner reservoir 15, depending on the particular application. In addition, when heating or cooling, the presence of packing material inside the annular space 16 can provide a substantially uniform temperature distribution through the annular space 16.

Work

In operation, referring again to FIG. 1, the fluid to be processed can generally be substantially continuously introduced into the external reservoir 11 of the reactor 10 through the passage 102. The fluid to be processed can then be directed to or into the first rotational element 103, where, in as a result of centrifugal force due to the rotation of the element 103, it can be directed outward to the periphery (ie, the edge) of the element 103. The rotation of the element 103 additionally causes the fluid on the periphery to be continuously distributed from the element 103 in the form of essentially thin drops or threads dnyh elements on the inner surface 123 of the outer tank 11. The continuous flow of substantially fine droplets or filiform elements to the inner surface 123 allows the formation of a substantially uniform thin film when processed fluid descends along the inner surface 123.

While the process fluid is introduced through passage 102, the heat transfer fluid at a temperature different from the temperature of the process fluid may be substantially continuously introduced into the inner tank 15 through the pipe 104. This heat transfer fluid can then be directed to a second a rotational element 105, where, again as a result of the centrifugal force exerted by the rotational element 105, the heat exchange fluid is directed to the periphery of the element 105. Then, as with the first rotational element 103, the heat oobmennaya fluid can be continuously distributed in a substantially fine droplets or filiform elements to the inner surface 172 of the inner tank 15, allowing a substantially uniform thin film flow along the inner surface 172.

In certain applications, for example in a gas-liquid reaction, countercurrent fluid (i.e. gas) can be introduced into the annular space 16 through an inlet 133 at the bottom 13 of the outer reservoir 11. Such a fluid can be directed upward in the annular space 16 along the outer the surface 171 of the inner reservoir 15 and allow it to interact with a downward process fluid (i.e., liquid) moving along the inner surface 123 of the outer reservoir 11. The presence of a countercurrent process fluid along the rings Vågå space 16 may increase reaction efficiency, handling, processing or for separation downstream fluid. Such an increase in efficiency may result from an increase in the points of contact with the descending fluid and / or an increase in the surface area at the interface between the descending fluid and the ascending countercurrent fluid. In such applications, a resulting reaction based on a continuous interaction between the descending fluid and the ascending countercurrent fluid can affect or influence the temperature of each fluid (for example, an exothermic reaction). In this regard, the temperature of the countercurrent fluid along the outer surface 171 of the inner tank 15 can be controlled by a heat exchange fluid moving along the inner surface 172 of the inner tank 15, while the temperature of the downstream fluid can be controlled by the casing 111, if necessary.

Once the descending treated fluid reaches the bottom 13 when it flows along the inner surface 123 of the outer reservoir 11, it can be directed to the outlet 132 and removed from the reactor 10. Similarly, the descending heat transfer fluid when it reaches the lower end 18 of the inner reservoir 15 can be directed through the outlet channel 181 and removed from the reactor 10 through the outlet 182.

As a result of this design of the reactor 10 of the present invention, together with the ability of the reactor 10 to provide a substantially uniform thin-film flow of the treated fluid, an increase in surface area, as well as residence time or interaction time between the treated fluid and the countercurrent fluid, and the ability to cause a difference temperatures between the thin-film processed fluid and the heat-exchange fluid, forming a thermal gradient across a narrow annular space nstva 16, the reactor 10 of the present invention can improve the handling, processing and / or separation of the processed fluid, at the same time giving a relatively high fluid transport rate, such as the heat transfer rate of mass transfer and / or stirring speed. In addition, due to the ability to continuously provide a substantially uniform thin film of fluid over a substantially large surface area, the reactor 10 of the present invention can provide substantially high processing capacities for the involved fluid or fluids.

Example 1: fluid-fluid or solid-fluid-fluid reactions

As shown in the embodiments depicted in FIGS. 1, 2, 3, and 5, the reactor 10 of the present invention may be applicable for fluid-fluid or solid-fluid-fluid reactions in connection with organic systems. It should be understood that the term fluid, as used here and in this application, includes gas and liquid. Thus, the reactor 10 may be applicable, for example, for gas-liquid, liquid-liquid, solid-gas-liquid reactions, or any other combination.

The reactor 10 of FIGS. 1, 2 and 3, in one embodiment, has particular applications for organic systems where higher pressures and temperatures are used, for example, hydrogenation, oxidation, polymerization, dealkylation, alkylation, methylation, carboxylation, decarboxylation and reaction Fischer-Tropsch, among other things. This application may additionally be useful, for example, in the preparation of organic products from a coal suspension or in the preparation of dimethyl ether (DME) using natural gas, methanol or other organic liquids or a mixture of gases as raw materials. It can additionally be applicable in the production of biodiesel and raw materials with low free fatty acid for diesel, using transesterification and esterification processes.

In FIGS. 1-3, in a liquid-gas reaction, the liquid to be treated may first be continuously introduced through the passage 102 into the first rotational element 103. This liquid may include water, a solvent, chemicals, a disinfectant, an oil product, salt water, methanol, ethanol, a liquid catalyst, a suspension type catalyst, or any other type of fluid. On the rotary element 103, the centrifugal force from the rotary element 103 acts by continuously distributing the liquid in the form of essentially thin drops or filamentary elements to the inner surface 123 of the outer reservoir 11 so as to create a continuous, substantially uniform thin film of fluid on the inner surface 123. While the fluid to be treated is introduced through passage 102, countercurrent gas can be introduced into the annular space 16 via an inlet 123 on the external reservoir 11. This gas can directed into the annulus 16 along the outer surface 171 of the inner container 15 and to be able to interact with the descending liquid, moving along the inner surface 123 of the outer tank 11. Examples of such gas may include hydrogen, oxygen, air, synthesis gas, CO _2, nitrogen or any other reactive or non-reactive gases.

In this liquid-gas reaction, in certain cases, an exothermic reaction can occur. In this regard, the temperature of the downward liquid can be controlled by the casing 111, in order to maintain the downward liquid at the desired temperature. As for the ascending countercurrent gas, in order to control its temperature, the heat exchange fluid at a temperature different from the temperature of the descending fluid can be substantially continuously introduced into the inner tank 15 through the pipe 104. This heat exchange fluid can then be directed to the second rotational element 105, where, as a result of the centrifugal force caused by the rotational element 105, is continuously distributed in the form of essentially thin drops or threadlike elements on the inner surface 172 Cored oil tank 15 to form a continuous, substantially uniform thin film along the inner surface 172.

Once the descending treated fluid reaches the bottom 13 when it flows along the inner surface 123 of the outer reservoir 11, it can be directed to the outlet 132 and removed from the reactor 10. Similarly, the descending heat transfer fluid as soon as it reaches the lower end 18 of the inner reservoir 15 can be guided through the outlet channel 181 and removed from the reactor 10 through the outlet 182. As for the upstream countercurrent gas, it can be removed through the exhaust 142. If desired, a condenser can be provided so that ndensirovat remote countercurrent gas for efficient collection. In addition, if necessary, the reaction along the annular space 16 can be maintained in vacuum to improve reaction kinetics.

In another embodiment, the reactor 10 shown in FIG. 4 can be used in a solid-fluid-fluid reaction and may include a layer of packing material 40 within the annular space 16. A layer of packing material 40 can be used to increase surface area, over which the downward volume of the treated fluid can come into contact, further increasing the transfer rate. In addition, the packing material 40 may provide a substantially tortuous passage through which the descending fluid must pass and / or extend the period of time during which the descending fluid can be processed. In this regard, the packing material 40 may act to further facilitate processing, processing and / or separation, while at the same time additionally imparting relatively high transfer rates to the descending liquid. The packing material 40 may also be heated or cooled, for example, by a casing 11 and / or by means of a heat exchange fluid inside the inner tank 15, depending on the particular application. When heating or cooling, the presence of packing material inside the annular space 16 can provide a substantially uniform temperature distribution through the annular space 16.

Example 2: Evaporation and Distillation

As shown in the embodiment of FIG. 5, the reactor 50 of the present invention can be used in evaporation and distillation processes. Evaporation and distillation processes include, for example, the removal of water from petroleum products, ethanol, methanol, glycerol or other compounds. In addition, such processes may include the removal of light organics from heavy organics, such as light sulfur-free oil from heavy oil, methanol from a mixture of biodiesel and glycerol, methanol from glycerol, and light organics from heavy oil. In addition, such processes may include the removal of organic solvents, such as ethyl acetate, from the polymer dispersion, or the removal of organic solvents or monomers during depolymerization processes. It can also be used to desalinate water, concentrate fruit juice, concentrate food materials such as soup, milk, remove light organics from groundwater, remove dissolved organics from treated water (i.e. industrial wastewater), and remove dissolved gases from a liquid such as carbon dioxide from a hot amine solution, hydrogen sulfide from water, concentration of the suspension, as well as in many other applications.

In an application for removing light organics from heavy organics, the inner surface 123 of the outer reservoir 11 may be heated, for example, by a casing 111, while the outer surface 171 of the inner reservoir 15 may be cooled by substantially cooled fluid flowing along the inner surface 172 of the inner reservoir 15. In addition, the annular space 16 between the outer reservoir 11 and the inner reservoir 15 can be maintained under vacuum to accelerate the reaction kinetics.

Under the conditions provided above, in one embodiment, a liquid containing light organic matter or material that is vaporized or distilled can be introduced through passage 102 and distributed using the first rotary element 103 evenly along the heated inner surface 123 of the outer reservoir 11. When a thin film of liquid descends down the heated inner surface 123, vapors can occur along the inner surface 123 and then can come into contact with a relatively colder outer surface 17 1 of the inner reservoir 15. Upon contact with the relatively colder outer surface 171, the vapors may condense and change phase to liquid. This condensed liquid can then flow down along the outer surface 171 of the inner reservoir 15, where it can collect at the bottom 13 of the outer reservoir 11. This phase change from vapor to liquid can occur over a substantially short distance within the annular space 16, typically a distance between the inner surface 123 of the outer tank 11 and the outer surface 171 of the inner tank 15. One advantage of this configuration is that it provides an energy-efficient way to separate lighter components from heavier components.

In order to further improve the energy efficiency or conservation of energy involved in this particular process, the processed fluid can also be used as a heat transfer fluid. In particular, a relatively cold, processed fluid may be directed into the inner reservoir 15 through the pipe 104 and along the inner surface 172. When it descends along the inner surface 172, vapors generated from the downward process fluid along the inner surface 123 of the outer reservoir 11 may enter contact with the outer surface 171 of the inner tank 15. The heat energy from the vapors can then be absorbed by a relatively cold, processed fluid, descending along the inner surface 172 of the inner reservoir 15. This fluid along the inner surface 172, now at elevated temperature, can collect at the lower end 18 of the inner reservoir 15 and be directed to the inner surface 123 of the outer reservoir 11 through the passage 102 and the first rotational element 103. When it descends along the inner surface 123, its vapors again come into contact with the relatively colder outer surface 171 of the inner reservoir 15, heating the fluid along the inner surface 172 of the inner reservoir 15. Like only Once this cycle has been established, the casing 111 can be turned off to save energy, and the process described here can proceed in an energy-efficient manner.

For any non-condensed vapors that can travel to the upper part 14 of the external reservoir 11, a condenser can be provided to condense such remaining vapors. In one embodiment, the capacitor may be located outside the external reservoir 11 and in fluid communication with the exhaust 142 to receive non-condensed vapors directed through the exhaust 142. Alternatively, the condenser may be located inside the external reservoir 104. In one embodiment, the capacitor may be in the form of a spiral 51 located inside the exhaust 142.

It should be noted that not all liquid distributed on the heated inner surface 123 of the outer tank 11 can evaporate. In this regard, such a liquid may be able to drain down the inner surface 123 and directed outward through the outlet 132 in the lower part 13 of the outer tank 11. If desired, such a liquid can be returned back through the passage 102 for reprocessing.

Alternatively, sumps may be located beneath reactor 50 to collect liquid removed from outlet 132 of lower portion 13. For condensed liquid that has passed down the outer surface 171 and which has accumulated in lower portion 13, a separate sump may be provided to collect such fluid Wednesday through input 133.

Example 3: cooling superheated steam

In the embodiment shown in FIG. 6, the reactor 60 of the present invention can be used in connection with cooling superheated steam or deheating steam. Both the inner surface 123 of the outer reservoir 11 and the outer surface 171 of the inner reservoir 15 can be maintained at a temperature noticeably lower (i.e. colder) relative to the superheated steam.

In order to maintain the inner surface 123 of the outer reservoir 11 at a relatively cold temperature, relatively cold liquid may be introduced through the passage 102 distributed by the first rotational element 103 on and substantially uniformly along the inner surface 123 of the outer reservoir 11. Additionally or alternatively, the casing 111 may be set to a predetermined temperature level, while maintaining the inner surface 123 at such a relatively low temperature. In order to maintain the outer surface 171 of the inner tank 15 at a similar, relatively low temperature, a relatively cold liquid can be introduced through the pipe 104 into the inner tank 15. This fluid is then sent to the second rotary element 105 and then distributed on and substantially uniformly along the inner surface 172 of the inner tank 15.

Under the conditions provided above, superheated steam can be introduced into the external reservoir 11 through the exhaust 142 at the top 14 of the external reservoir 11. In one embodiment, superheated steam can be provided in the form of precipitation of water particles in the range, for example, from the microrange to the nanoscale. The steam can then be directed into the annular space 16, where it collides, on the one hand, with the relatively cold inner surface 123 of the outer tank 11, and on the other hand with the relatively cold outer surface 171 of the inner tank 15. In addition, as soon as the superheated steam enters the relatively cold annular space 16, it is faced with a cold fluid distributed from the first rotational element 103. A meeting with a relatively cold fluid distributed from the first rotational element element 103, acts by cooling superheated steam to a certain level. Then, when the steam moves along the annular space 16, it can further be cooled and condensed into a collection fluid.

In particular, when superheated steam passes in the annular space 16 and through a relatively cold, distributed liquid, in one embodiment, the steam can transfer part of its thermal energy (i.e. heat) to the distributed liquid and can be pushed out by the distributed liquid to the inner surface 123 of the outer reservoir 104. In one embodiment, the dispensed liquid may act to cover vapor particles, i.e. the in-situ coating process, and pushing the steam onto the inner surface 123. When the steam is pushed onto the inner surface 123 of the outer tank 11, it can be cooled again with a relatively cold temperature that is maintained along the inner surface 123. In addition, since the steam transfers its heat to the distributed liquid in the annular space or along the inner surface 123, an increase in temperature may cause the liquid to vaporize. Vapors, when formed in the annular space 16, can condense using the relatively cold outer surface 171 of the inner reservoir 15. This continuous interaction with the distributed fluid, the inner surface 123 of the outer reservoir 11 and the outer surface 171 of the inner reservoir 15 can quickly cool the superheated steam . The cooled vapor can then condense and flow along the outer surface 171 of the inner tank 15 and the inner surface 123 of the outer tank 11 down to the bottom 13 of the outer tank 11 where it can be collected.

It should be understood that, although the cooling of superheated steam can be performed with the same flow, as described above, it can also be performed in the design with a countercurrent flow. That is, steam can be introduced in a countercurrent direction to a relatively cold fluid distributed from the first rotational element 103.

Example 4: reactions initiated by UV or microwave

As shown in the embodiment of FIG. 7, the reactor 70 of the present invention can be used in connection with ultraviolet (UV) initiated reactions, such as photopolymerization, treatment or disinfection of water, or organic reactions to produce clinical drugs. In addition, the reactor 70 can also be used in connection with reactions initiated by microwaves. In particular, microwave energy can be used as a source for providing heat and as a stimulating agent for organic reactions, especially for reactions including cold suspension, liquid organics, pharmaceuticals, and the conversion of sawdust and other wood-based products into cellulose. Microwave energy can also be used for energy-efficient evaporation of water, desalination, capture and isolation of carbon dioxide. You may notice that energy from, for example, microwaves and UV waves can act to destroy pathogens and bacteria in the fluid. Other energy sources also possible in this invention should not be considered so excluded.

For use in desalination and water treatment using microwaves, the reactor 70 may be tuned in substantially the same manner as described in connection with FIG. In one embodiment, the salty liquid may be introduced through the passage 102 and distributed by the first rotational element 103 on the heated inner surface 123 of the outer tank 11 and evenly along it. At the same time, relatively cold liquid can be introduced through the pipe 104 into the inner reservoir 15. This fluid can then be directed to the second rotational element 105 and then distributed on and substantially evenly along the inner surface 172 of the inner reservoir 15.

When a substantially uniform thin film of salt liquid extends along the inner surface 123 of the tank 11, an energy source such as a microwave generation device 71 located near the body 12 of the external tank 11 can be activated by transmitting microwave radiation through the walls of the body 12, heating the salty fluid a medium flowing along the inner surface 123 of tank 11. This causes a thin film of salty fluid to evaporate. It should be understood that when using an energy source such as a microwave generator 71, when the energy must act on the processed fluid in the external tank 11, but should not act on the heat transfer fluid in the internal tank 15, the body 12 of the external tank 11 can be made of material that allows such energy to pass through it, while the inner reservoir 15 can be made of material that can be impervious to such energy.

The generated vapor can then pass through the annular space 16 to the relatively cold outer surface 171 of the inner reservoir 15. Upon contact with the relatively cold outer surface 171, the vapor can condense into liquid and can pass to the bottom of the outer surface 171 of the inner reservoir 15. The condensed liquid can then collect the lower part 13 of the external reservoir 11. In one embodiment, this process can be performed in the annular space 16 in a vacuum. Alternatively, the process may be performed under atmospheric or approximately atmospheric pressure.

It should be understood that not all fluid is heated by microwave radiation. Thus, the heated fluid flowing along the inner surface 123 of the outer tank 11 can collect through the outlet 132 at the bottom 13 and return back to the outer tank 11 through the passage 102. Thus, after this process is initiated, not much energy can be required from the microwave source 71 to heat the saline fluid being treated. As a result, this design can provide a substantially energy-efficient distillation system.

In certain cases, in addition to using microwave radiation, ultraviolet (UV) radiation can also be used to destroy pathogens or bacteria that may be present in the treated fluid.

Example 5: carbon dioxide removal

For use in capturing and isolating carbon dioxide, any of the reactors shown above, including those shown in FIGS. 1, 2, and 3, can be used in substantially the same manner as described above.

In one embodiment, using a liquid (eg, an amine solution) capable of absorbing carbon dioxide gas, a certain volume of such a liquid may be in contact with an environment containing carbon dioxide gas to absorb carbon dioxide into the liquid and remove it from the environment. After being saturated with carbon dioxide, this fluid can be introduced through passage 102 and distributed via the first rotational element 103 onto the heated inner surface 123 of the outer reservoir 11 and uniformly along it. At the same time, a downward countercurrent gas stream capable of absorbing carbon dioxide can be introduced into the annular space 16.

When a substantially uniform thin film of saturated liquid extends along the inner surface 123 of the reservoir 11, a heating device 71, such as microwaves or fluid pipes located near the body 12 of the outer reservoir 11, can be activated by heating the saturated fluid flowing along the inner surface 123 of tank 11. Countercurrent gas flow, on the other hand, can be maintained at a relatively low temperature. To do this, relatively cold liquid can be introduced through the pipe 104 into the inner reservoir 15. This fluid can then be directed to the second rotational element 105 and then distributed on and substantially uniformly along the inner surface 172 of the inner reservoir 15.

When an upstream countercurrent gas stream comes into contact with a heated saturated liquid, the countercurrent gas can interact with the saturated liquid and absorb carbon dioxide from the liquid. The fluid can then continue to move downward along the inner surface 123 and out through the outlet 132 at the bottom 13 of the outer reservoir 11, where it can collect or return back to the passage 102. As for the upward countercurrent gas stream, now saturated with carbon dioxide, it can be removed through the exhaust 142 in the upper part 14 of the external reservoir 11. The gas stream saturated with carbon dioxide can then be mixed with other liquids or materials to produce a carbonate product.

Example 6

In one embodiment, shown in Fig. 8, reactors 80, like any of the reactors shown in Figs. 1-7, can be arranged in series and arranged to be in fluid communication with each other, so that any of the applications described above can be performed continuously sequentially or allow multiple passages of fluid through a reactor of the same or similar design. It should be noted that any possible combination of reactors can be installed in series, and these sequences are not limited to any maximum number of reactors.

In a further embodiment, as shown in FIG. 9, instead of providing a sequence of reactors, the reactor 10 of the present invention may be designed to include at least a third reservoir 90, which may be located inside the inner reservoir 15, providing a second annular a space 91 between the outer surface of the third reservoir 90 and the inner surface 172 of the inner reservoir 15. In this design, fluid and / or gas flowing along the annular space 16 between the outer the reservoir 11 and the inner reservoir 15, being outside this annular space 16, can be guided into the annular space 91 located between the inner reservoir 15 and the third reservoir 90 inside the inner reservoir 15. Redirection can be performed through holes 92 at the upper end 19 and holes 93 on the lower the end 18 of the inner tank 15. This design may allow the process fluid to make many passes through the reactor 10, increasing the transfer rate. It should be noted that the fourth tank may also be located inside the third tank, providing a third annular space. This design can be repeated with additional fifth, sixth or any additional tanks, if necessary.

Of course, if multiple passages are desired, fluid and / or gas trapped from the annular space 16 in any of the reactors of FIGS. 1-7 can return back to the annular space 16 for as many passages as required.

Although the present invention has been described with reference to certain embodiments, it will be understood by those skilled in the art that various changes may be made and equivalents may be substituted without departing from the true spirit and scope of the present invention. In addition, many modifications can be made to suit the specific situation, indication, material and composition of the substance, process steps or steps, without departing from the spirit and scope of the present invention. All such modifications are intended to be within the scope of the appended claims.

Claims (49)

1. A reactor containing:
an external reservoir having an inner surface opposite which the process fluid may be located;
an inner reservoir located inside the outer reservoir and having an outer surface serving as a heat exchange surface for the fluid to be treated, and an inner surface designed to allow the heat exchange fluid to flow in a substantially uniform thin film; and
an annular space defined between the external reservoir and the inner reservoir to provide a passage along which the process fluid may be supplied, where this annular space is designed to maintain a temperature difference between the external reservoir and the internal reservoir, imparting relatively high transfer rates to the process fluid. 2. The reactor according to claim 1, where the inner surface of the external tank is designed to allow the processed fluid to fall into a substantially uniform thin film. 3. The reactor according to claim 2, where this essentially uniform thin film allows the process fluid to be well suited for processing, processing and / or separation. 4. The reactor according to claim 2, where this essentially uniform thin film provides the processed fluid with a relatively high speed of one of heat transfer, mass transfer, mixing, or a combination thereof. 5. The reactor according to claim 1, where the inner surface of the external tank can be provided with a profiled pattern that creates additional surface area over which the processed fluid can flow, facilitating one of the processing, processing, separation, increase the residence time inside the annular space, or a combination thereof . 6. The reactor according to claim 1, where the inner surface of the external tank may be coated to facilitate the processing, processing and / or separation of the processed fluid. 7. The reactor according to claim 1, where the external tank also includes a lower part designed to collect and remove the processed fluid that has descended on the inner surface. 8. The reactor according to claim 1, where the inner reservoir includes an inner surface along which heat exchange fluid may flow. 9. The reactor of claim 8, where the heat transfer fluid has a temperature different from the temperature of the processed fluid, causing a temperature difference between the outer surface of the inner tank and the inner surface of the outer tank. 10. The reactor of claim 8, where the inner surface of the inner tank can be provided with a profiled pattern to increase surface tension, in order to provide and maintain a substantially thin and uniform film of heat transfer fluid. 11. The reactor of claim 8, where the inner tank also includes a lower end, designed to collect and remove heat transfer fluid that has descended on the inner surface. 12. The reactor according to claim 1, where the annular space is designed to allow directing the second fluid into the annular space for interaction with the processed fluid. 13. The reactor of claim 12, wherein the second fluid may act by increasing contact points at the interface between the second fluid and the process fluid over a relatively large surface area within the annular space, giving the process fluid a relatively high transfer rate. 14. The reactor according to claim 1, where the annular space is designed so as to allow the second fluid to be directed into the annular space in countercurrent with respect to the process fluid to interact with the process fluid. 15. The reactor according to claim 1, where the annular space is provided with a relatively short distance between the inner surface of the outer tank and the outer surface of the inner tank to give the processed fluid a relatively high transfer rate. 16. The reactor according to claim 1, further comprising a fluid distribution system allowing introduction of the process fluid onto the inner surface of the outer tank and the inner surface of the inner tank. 17. The reactor according to clause 16, where the fluid distribution system includes a rotational element inside the external reservoir for the formation of essentially thin droplets or filamentary elements from the processed fluid, so that a substantially uniform thin film of the processed fluid can be provided on the inner surface of the outer element. 18. The reactor according to clause 16, where the fluid distribution system includes a rotational element inside the inner tank for the formation of essentially thin drops or filamentary elements from the heat transfer fluid, so that a substantially uniform thin film of heat transfer fluid can be provided on the inner surface of the inner element. 19. The reactor according to claim 1, further comprising an energy source provided near the external reservoir, acting as a source of heating or cooling of the process fluid along the inner surface of the external reservoir. 20. The reactor according to claim 1, further comprising a layer of packed material inside the annular space to increase the surface area over which the volume of the processed fluid can contact to increase its transfer rates. 21. The reactor according to claim 20, where this layer of packed material can provide essentially uniform temperature distribution across the annular space. 22. The reactor according to claim 1, further comprising a third tank located inside the inner tank so as to provide another annular space between the third tank and the inner tank, allowing the processed fluid to repeatedly pass through the reactor, increasing the transfer speed. 23. A fluid processing system in which a plurality of reactors according to claim 1 are connected in series, allowing the fluid to be processed to repeatedly pass through the reactors, increasing transfer rates. 24. The system according to item 23, where each reactor is designed to process the processed fluid in a different way. 25. A method of processing a fluid, where:
injecting the process fluid into the external reservoir and opposite its internal surface;
provide, inside the external tank, an internal tank with a heat exchange surface with a temperature different from the temperature of the processed fluid;
imparting a substantially uniform thin film flow to the heat exchange fluid along the inner surface of the inner tank; and
maintain the temperature difference across the passage between the external tank and the internal tank, giving the process fluid therein relatively high transfer rates. 26. The method according A.25, where at the stage of introduction provide essentially uniform thin-film flow of the processed fluid opposite the inner surface of the external reservoir. 27. The method according to p. 26, where at this stage of providing, essentially uniform thin-film flow enhances the ability of the fluid to process, process and / or separation. 28. The method according to p. 26, where at this stage of providing allow the processed fluid to have a relatively high speed of heat transfer, mass transfer, mixing, or a combination thereof. 29. The method according to p. 26, where at this stage of providing rotationally distributed inside the external reservoir, essentially thin drops or filamentary elements of the processed fluid. 30. The method according A.25, where at the stage of introduction give the inner surface of the external tank a profiled pattern, forming an additional surface area over which the processed fluid can flow, facilitating one of the processing, processing, separation, increase the residence time of the processed fluid inside the passage or a combination thereof. 31. The method according A.25, where at the stage of introduction cover the inner surface of the external tank to facilitate the processing, processing and / or separation of the processed fluid. 32. The method according A.25, where at the stage of providing distributed opposite to the inner surface of the inner tank heat transfer fluid at a temperature different from the temperature of the processed fluid. 33. The method according to p, where at the stage of distribution create a temperature difference between the outer surface of the inner reservoir and the inner surface of the outer reservoir. 34. The method according to clause 29, where at the stage of distribution rotationally distribute inside the inner tank, essentially thin droplets or threadlike elements of the heat transfer fluid. 35. The method according A.25, where at the stage of providing provide the inner surface of the inner tank with a profiled pattern to increase surface tension to provide and maintain a substantially thin and uniform film of heat transfer fluid. 36. The method according A.25, where additionally direct the second fluid into the passage between the external tank and the internal tank, allowing interaction with the processed fluid. 37. The method according to clause 36, where at this stage, the directions increase the contact point at the interface between the second fluid and the process fluid over a relatively large surface area inside this passage, giving the process fluid a relatively high transfer rate. 38. The method according to clause 36, where at this stage, directions allow the second fluid to move inside this passage in countercurrent relative to the processed fluid. 39. The method according A.25, where at the stage of maintenance provide this passage with a relatively short distance between the outer surface of the inner reservoir and the inner surface of the outer reservoir, to give the processed fluid a relatively high transfer speed. 40. The method according A.25, where further heated or cooled processed fluid along the inner surface of the external tank. 41. The method according A.25, where additionally place a layer of packed material inside this passage between the external tank and the internal tank to increase the surface area over which the processed fluid can be contacted to increase its transfer speeds. 42. The method according to paragraph 41, where at this stage of placement, a certain volume of the processed fluid is introduced into an external reservoir. 43. The method according to paragraph 41, where at this stage of placement using a layer of packing material to provide a substantially uniform temperature distribution across the passage between the external tank and the internal tank. 44. The method according A.25, where the processed fluid is used in the reactions of the fluid-fluid medium in connection with organic systems. 45. The method according A.25, where the processed fluid is used in the process of distillation or evaporation. 46. The method according A.25, where the processed fluid is superheated steam, which is cooled. 47. The method according A.25, where the processed fluid is used in reactions initiated by ultraviolet and / or microwaves. 48. The method according A.25, where the processed fluid is used in the desalination process. 49. The method according A.25, where the processed fluid is saturated with carbon dioxide and used in the process of removing carbon dioxide.

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