Contact device

FIELD: process engineering.

SUBSTANCE: invention relates to device intended for bringing in contact of gas with fluid, fluid with fluid and gas with fluid and solid. Device inner space is divided by baffles into multiple cells. Said cells make areas of counterflow contact of upward fluid flow and downward fluid flow in said device. Downward fluid flow inlet made in vertical wall of every stage acts as resistance for fluid volume formation and makes downward fluid flow locked by said baffle entering the adjacent cell of lower lateral stage. Intake port of upward fluid flow made at top side of said inlet makes upward fluid flow flowing in from lower lateral stage cells.

EFFECT: better dispersion of two-phase fluids in contact.

22 cl, 43 dwg, 3 tbl, 10 ex

 

The technical field

The present invention relates to a contactor to complete the contact gas - liquid, such as absorption, Stripping and distillation, contact, liquid - liquid, such as extraction, and contact the gas - liquid - solid substance, such as catalytic reaction liquid including solid, such as a suspension, and gas.

The level of technology

In industries such as oil refining, gas cleaning and petrochemicals, is used for many processes, such as absorption (absorption, Stripping, distillation, extraction and catalytic reaction in which the separation, purification and transformation of specific substances is carried out by, for example, the creation of the gas / liquid contact with each other or create a contact between two kinds of liquids with each other, to use the return or reception of substances or energy that is transferred between the fluid-fluid, the reaction between the substances and the like. For example, contactors, such as adsorption column, othonna column or extraction column, in which the two fluids in different phases to make contact with each other in the column to facilitate the mass transfer at the interface between fluid-fluid and distillation column, in which the temperature gradient is set in the direction of the column height, and branch and cleaning substances are carried out by using the equilibrium vapor - liquid, are equipment that are widely used in these processes.

Typically, the contactor is provided with a mechanism for increasing the efficiency of mass transfer by dispersion of the two fluid very well each other to make the contact area is larger and different types of contactors are respectively specific fluid or the applicable process. From this point of view among the main types of gas-liquid contactors, for example, (1) spray column or jet scrubber, where the liquid is fed into the column in a liquid droplet state by use of the pressure pump and the like, and liquid droplets dispersed in the gas phase bubble column, in which bubbles are dispersed in the column filled with the liquid phase, (2) Packed column, in which the fluid is forced to flow in a state of a liquid film on the surface of the Packed object, located in the column to make surface contact with the gas - liquid more, (3) disc column, which plates, forcing the liquid staying temporarily on them to flow down the column, are arranged with a given interval, and the bubbles are dispersed in the liquid phase, remaining on the plate, by means of a cap or holes provided in each plate, and so on.

Among these gas the liquid contactors types such as the spray column and bubble column, in which liquid droplets or bubbles are dispersed in the gas phase or liquid phase, respectively, have the advantage that the dispersion state of gas and liquid is good in comparison with the similar condition of the Packed column and the like, but the time period of contact of the gas - liquid is relatively short, and the number of theoretical plates in the entire column is equivalent to only one or two. Therefore, in order to obtain a high absorption efficiency or the efficiency of the distillation, for example, absorption column or organoclay column, use the special structure of the equipment, for example, making the equipment by multistage connection of multiple contactors in series, and this is a problem from the point of view of the complexity of the equipment and increase the value.

On the contrary, in the Packed column or disc column number of theoretical plates of the contactor can be designed relatively freely by increasing/decreasing the Packed height of the nozzle or the actual number of plates. However, considering the mechanism of gas-liquid contact, the contact of gas and liquid occurs mainly on the surface of the liquid film or on the surface of the bubbles in the liquid phase, and we cannot say that the fluid nah who is in good dispergirovannom condition, so that further improvement is studied. In addition, plate column, as it applies the contact mechanism in which bubbles are dispersed in the liquid phase, there is a problem of foaming, that is, the foaming of the liquid phase reduces the performance or efficiency of processing, reduces the operating range (the amount of feed gas/liquid or supplied the proportion of types of processed fluid contactor.

In patent document 1 describes a technology in which, as shown in figa, in a gas-liquid contactor 100 Poppet-type gas-liquid contact is made when the descending liquid and the ascending gas in the column is forced to flow parallel to the surface plate 101 without holes. However, the purpose of this technology is to develop a compact contactor, which can be located indoors, for example, and not to further strengthen the dispersion state of gas and liquid.

In patent document 2 describes a technique in which in a gas-liquid catalytic reaction column 110 of the Packed type, as shown in figv, by dividing the internal part of the liquid catalytic reaction column 110 on many cells 111, in which Packed hydrophobic catalyst, prevents displacement of the fluid flow through the use of gidrofobnogo the catalyst. Furthermore, it describes a technology in which, as shown in figs, by converting the surface of the wall of each cell 111 in the waveform in the direction (horizontal direction), transverse direction (vertical direction) of a liquid flow and gas flow to form a fluid flow-dependent waveform, the contact area of the fluid flow and gas flow increases. The present technology has a structure similar to the structure of one possible implementation of the present invention, described later, in the sense that the internal region of the column is divided into many cells, but the mechanism of gas-liquid contact of gas and liquid are forced to contact each other on the surface of the liquid flowing down along the wall surface of the cell 111, and says nothing about the technology of the dispersion liquid in the gas phase.

In addition, as an example of the contact liquid - liquid present inventor has developed a liquid-liquid contactor 120, in which, as shown in Fig, many plates 121 is provided in a liquid-liquid contactor 120 to cause heavy liquid (N), which flows down, and light liquid (L), which flows upward to contact with each other, and part of the plate 121 is cut off to form the flow path 123 for heavy liquid and light liquid, and is provided with a plate jumpers 122 passing vertically downward from the end portion side of the flow paths 123 each plate 121 (patent document 3). This plate jumpers 122 is provided with a hole 124, and a light liquid (L3), blocked by plate jumpers 122 and temporarily staying under the plate 121, and flows into the state jet in the horizontal direction (L1) through the opening 124 and dispersed in heavy liquid (N) by the formation of liquid droplets (L2) using the shear stress from the heavy fluid (H), the current down, whereby both liquid can effectively come into contact with each other. For this technology, the present inventor is with the development of technology, further improving the dispersion state of the heavy and light liquids in liquid-liquid contactor.

[Patent document 1]

Posted Japanese patent application No. 2002-336657: claim 1, paragraph 0010, 1

[Patent document 2]

Posted Japanese patent application No. 2000-254402: paragraphs from 0015 to 0020, 1, 4

[Patent document 3]

Posted Japanese patent application No. Hei 7-80283: paragraphs from 0017 to 0019, paragraph 0032, figure 5

Description of the invention

The present invention is made under such circumstances and its object is to provide Comtat the torus, able to force fluids of two phases in contact with each other in good dispergirovannom condition, and which can easily be made multi-stage.

According to the present invention the contactor, in which the rising fluid representing the gas is supplied from the lower part of the column, and the descending fluid constituting the liquid is supplied from the upper part of the column, and the data of the gas and liquid are subjected to countercurrent contact, includes:

providing multiple tiers of cells so that the cell upper side layer and the cell lower side layer adjacent to each other along the paths of upward flow of fluid and descending of the fluid are at different tiers, and the cell forming region countercurrent contact of the ascending fluid and downward fluid;

separation of the cells of the upper side layer and the cell lower side layer using partitions; and

the software in the partition corresponding tiers of holes entering the descending fluid in the lower part of the cell upper side of the layer, so that the descending fluid is blocked by the partition and arriving, is introduced into the cell lower side layer, and providing an inlet port of the rising fluid in the higher side than the region, which which remains downward fluid moreover, through the inlet port of the ascending fluid rising fluid medium from the cell lower side layer flows into the cell upper side of the layer.

According to another invention of the contactor, in which the rising fluid constituting the liquid is supplied from the lower part of the column, and the descending fluid constituting the liquid is supplied from the upper part of the column, and these fluids are subjected to countercurrent contact, includes:

providing multiple tiers of cells so that the cell upper side layer and the cell lower side layer adjacent to each other along the paths of upward flow of fluid and descending of the fluid are at different tiers, and the cell forming region countercurrent contact of the ascending fluid and downward fluid;

separation of the cells of the upper side layer and the cell lower side layer using partitions; and

the software in the partition corresponding tiers of holes entering the descending fluid in the lower part of the cell upper side of the layer, so that the descending fluid residing in the cell upper side of the layer, is introduced by its potential energy in the cell lower side layer, and providing an inlet port of the rising fluid in the higher the nd side, than the insertion of the descending fluid, and through the inlet port of the ascending fluid rising fluid medium from the cell lower side layer flows by its buoyancy in the cell upper side of the layer.

According to another invention of the contactor, in which the rising fluid constituting the liquid is supplied from the lower part of the column, and the descending fluid constituting the liquid is supplied from the upper part of the column, and these fluids are subjected to countercurrent contact, includes:

providing multiple tiers of cells so that the cell upper side layer and the cell lower side layer adjacent to each other along the paths of upward flow of fluid and descending of the fluid are at different tiers, and the cell forming region countercurrent contact of the ascending fluid and downward fluid;

separation of the cells of the upper side layer and the cell lower side layer using partitions; and

the software in the partition corresponding tiers of holes entering the ascending fluid in the upper part of the cell lower side layer, so that the rising fluid residing in the cell lower side layer, is introduced by its buoyancy in the cell upper side of the tier, and ensure Uchenie in the lower side, than the insertion of the ascending fluid inlet port of the descending fluid medium through which the descending fluid medium from the cell upper side layer flows through its potential energy in the cell lower side of the tier.

Each contactor described above, with the insertion of the descending fluid, can be constructed so that the cell upper side layer and the cell lower side layer are in a mutual location in which the parts thereof are stacked above and below each other, and the insertion of the descending fluid is provided in the lower side surface and/or bottom surface of the cell upper side of the layer, whereas in the contactor, with the insertion of the ascending fluid, the cell upper side layer and the cell lower side of the layer can be in the mutual arrangement in which parts thereof are stacked above and below each other, and the insertion of the ascending fluid may be provided in the upper side surface and/or a ceiling surface of the cell bottom side of the tier. Preferably, when the insertion of the descending fluid, the insertion of the ascending fluid inlet port of the ascending fluid or air supply port of the descending fluid represent the slot, passing in the transverse direction or longitudinal to the managing, or section of the numerous holes arranged in the transverse direction or the longitudinal direction.

In addition, the contactor, in which the gas is ascending the fluid and the fluid is downward fluid environment, it is possible to ensure the insertion of the descending fluid from the first valve, opening and closing, respectively, the number of descending fluid, blocked by a wall to prevent ascending the fluid flowing in the cell lower side of the layer, from passing into the cell upper side of the layer through the insertion of the descending fluid. In this case, the first valve may be provided on the side leakage of holes entering the descending fluid medium in such a way as to be closed by deflection using the first deflecting means, and may be designed to open against the deviation of the first deflecting means through pressure, that is, the hydraulic pressure of the descending fluid residing in the cell upper side of the layer.

Additionally, in the contactor, in which the gas is ascending the fluid and the fluid is a downward flowing medium, in this case, you can ensure the insertion of the descending fluid on the side surface of cells and, the first valve is configured to move up and down between a lower position, in which closed the insertion of the descending fluid, and an upper position in which it is open and can rise due to the buoyancy of the descending fluid residing in the cell upper side of the tier. Additionally, if the insertion of the descending fluid is made on the bottom surface of the cell, the first valve configured to close said hole bottom surface in the lower position. Additionally, the first valve is moved up and down due to the buoyancy of the descending fluid, may have a buoyancy compensator acting in the lateral direction in the direction of the upper layer side of the cell.

Additionally, in the contactor, in which the gas is ascending the fluid and the fluid is downward fluid environment, is possible when the supply port of the ascending fluid is provided a second valve, the opening and closing portion of the inlet port of the ascending fluid respectively to the upward pressure of the fluid flowing from the cell lower side layer of the cell upper side of the tier. In this case, you can consider the construction in which the second flap is provided on the side of the leak of pritech the second port of the ascending fluid so to be closed by deflection of the second deflector means and to open against the deviation of the second deflecting means by upward pressure of the fluid, and so forth.

The lower surface of the cell can be tilted to the down hole input provided in a given cell, and it is applicable for the case when the descending fluid is a suspension and the like, containing the crushed material.

In addition, it is possible that is a lot of lines of cells, in which numerous cells are located in the same longitudinal line, and cells belonging to each line of cells, and cells neighboring the lines of the cells are on different tiers, and the corresponding lines of cells are placed transversely along one direction, and the corresponding cells are concentrically arranged transversely in the contactor, which has a cylindrical shape.

The contactor according to the present invention has numerous tiers of cells, forming a space countercurrent contact of the ascending fluid medium (gas or liquid) and the descending fluid medium (liquid) in each of these cells, and the descending fluid introduced from the cell upper side of the layer through hole input, and a rising fluid flowing from the cell lower side of the layer through pritech the first port, subjected to countercurrent contact, so that a good dispersion state can be obtained in each cell. As a result, in the case of gas-liquid contactor, for example, you can increase the absorption efficiency of the operation of the absorption or effectiveness of the distillation, the distillation operation.

In addition, because these areas of contact can be easily formed by only separating the inner part of the column partitions, you can easily create a stacked column, so that it becomes possible to build complex contactor at a low cost.

Brief description of drawings

Figure 1 is a longitudinal view in section, showing the structure of the entire gas-liquid contactor according to one variant of implementation of the present invention;

2 is an explanatory view showing the directions in which gas and liquid flow in a gas-liquid contactor;

figa and figv are explanatory views showing the structure of the contact area in gas-liquid contactor;

figure 4 is a perspective view showing the structure of the contact area;

figure 5 is a perspective view for explaining the action of the contact area;

6 is a longitudinal view in section for explaining the action of the contact area;

figa-7C is predstavlyaet a surface side, showing examples of modifications of the entrance/exit of a gas or liquid supplied to the contact area;

figa and figv are explanatory views showing an example of modification of the contact area;

figa-9C are explanatory views showing the second example of modification of the contact area;

figa-10C are explanatory views showing the third example of modification of the contact area;

figa and figv are explanatory views showing the fourth example of modification of the contact area;

figa and figv are a front view and a longitudinal view in section of a cell having first and second flaps;

figa and figv are explanatory views showing the action of a cell having first and second flaps;

Fig is a front view of a cell according to the first modification example of the first valve;

Fig is a longitudinal view in section of a cell according to the first modification example;

figa and 16B are explanatory views showing the action of the cell according to the first modification example;

figa and 17B are longitudinal views in the context of cells according to the second and third modification examples of the first valve;

figa and 18B are explanatory views showing steps is cheek according to the second and third examples of the modification;

Fig is a longitudinal view in section, showing an example of the application of the inner region of the gas-liquid contactor for distillation columns;

Fig is a longitudinal view in section, for explaining the action of the liquid-liquid contactor according to the second variant of implementation of the present invention;

Fig is a longitudinal view in section, showing an example of extraction columns, which used a liquid-liquid contactor according to the second variant of implementation described above;

Fig is a longitudinal view in section, showing a modification example of the second variant of implementation described above;

Fig is a longitudinal view in section, showing the structure of the distillation columns used in the experiment in the working example;

Fig is a longitudinal view in section, showing the structure of a liquid-liquid extraction columns used in the experiment of comparative example in another working example;

Fig is a longitudinal view in section, showing the structure of a liquid-liquid extraction columns used in the experiment in another working example described above;

figa-26C are explanatory views relating to the conventional technology of gas-liquid contactor; and

Fig is an explanatory view relating to the conventional technology liquid-liquid contactor.

The best option of carrying out the invention

As one possible implementation according to the present invention a gas-liquid contactor 1, carrying out gas-liquid contact, such as absorption or distillation, is taken as an example, and its structure is described using figure 1-4. Figure 1 and figure 2 are longitudinal views in section, schematically showing the entire structure of gas-liquid contactor 1 according to the present invention, while figa, figv and 4 are explanatory views of its internal structure.

Gas-liquid contactor 1, formed from a cylindrical container made, for example, stainless steel, causes the gas (bubbling fluid), ascending in this gas-liquid contactor, and the liquid (downward fluid), descending in a gas-liquid contactor to contact in countercurrent to each other. As shown in figure 1, the upper part of the column of gas-liquid contactor is provided by section 11 of the liquid supply to feed the fluid into the inner space of the gas-liquid contactor 1, and section 14 of the gas outlet in order to release the gas, whereas the lower part of the column is provided by section 12 in the start-up of fluid, in order to release the liquid, and section 13 of the gas supply to supply gas.

As shown in figure 1, in the area of gas-liquid contact between the section 11 of the liquid supply and section 13 of the gas flow in a gas-liquid contactor 1 is provided with a vertical wall 10, passing vertically in the center position of the circle formed by the inner peripheral surface of the gas-liquid contactor 1 in such a way as to divide the main body of the gas-liquid contactor 1 into two parts - left and right in figure 1.

In the left side pane of 20 gas-liquid contactor 1, separated by a vertical wall 10, provided with a lot of horizontal walls 21 with equal intervals, whereby the space of the left-side region 20 is divided into a number of regions in the longitudinal direction. On the other hand, in the right side region 30, separated by a vertical wall 10, provided with a lot of horizontal walls 31 at equal intervals on other tiers relative to the horizontal wall 21, whereby the space in the right side region 30 is divided into a number of regions in the longitudinal direction. It should be noted that the horizontal wall 31 of the right side region 30 is located at the height of the middle of the horizontal walls 21, longitudinally adjacent in the left-side region 20.

The investigator is about, when the space bounded by the two horizontal walls 21, 21 (31, 31), longitudinally adjacent to each other, the wall 15 of the column of gas-liquid contactor 1 and the vertical wall 10, is called a cell, in a gas-liquid contactor 1 is formed by two lines of cells, each of which these cells longitudinally placed on many levels, and cells belonging to one of the lines of cells that are located in other tiers relative to cells belonging to other cell lines. It should be noted that in the following description reference position 22, 32, respectively, belong to the cell of the left-side region 20 and the cell to the right-side region 30.

These cells 22, 32 are prototechno contact space gas and liquid flowing in a gas-liquid contactor 1. The respective cells 22, 32 in a gas-liquid contactor have a structure similar to each other, and further, the cell 32 shown in dotted lines in figure 1, for example, is taken as an example for explanation. Figa is a top view (visible from the surface A-a in figure 1) horizontal wall 31 of the lower side surface of the cell 32, while FIGU is a view of the surface side (visible from surface-to figa) vertical wall 10 of the cell 32. Figure 4 is a perspective view showing the internal structure of ache the key 32 gas-liquid contactor 1.

As shown in figv, in the vertical wall 10 in positions immediately below the respective horizontal walls 21, 31 are formed holes 51 for gas flow, made in the form of slits passing in a horizontal direction, while in positions directly above the corresponding horizontal walls 21, 31 in the vertical wall 10 is formed holes 52 for the flow of liquid flowing in a horizontal direction and is made of, for example, in the form of three slots. The bottom surface of the respective horizontal walls 21, 31 and the upper peripheral edge of the slit holes 51 for gas flow are common, whereas the position of the height of the bottom of the slot of the three slots constituting the hole 52 for the flow of liquid, chosen to be lower than the liquid surface of the liquid while the work of the gas-liquid contactor 1 becomes stationary, as will be shown below.

With the above structure, as shown in perspective in figure 4, for example, when the vertical wall 10 is visible from a particular cell 32, the hole 51 for gas flow and a hole 52 for fluid flow in the upper half of the sides, respectively equivalent (equal) port leakage of gas from which the gas, which is the ascending fluid medium that flows in the cell 22 diagonally in the top of the eat side layer (the previous tier) and equivalent to the inflow port of the liquid in which the liquid, which is the descending fluid medium that flows from the cell 22 in the diagonally upper side layer. Similarly, the hole 51 for gas flow and a hole 52 for the flow of liquid in the bottom half sides, respectively equivalent to the inflow port of the gas from which the gas flows from the cell 22 in a diagonally lower side layer (the next level), and the port of leakage of the liquid from which the liquid flows into the cell 22 in a diagonally lower side layer.

In other words, the port leak of fluid provided in the cell 22 in the diagonally upper side layer of the cell 32, shown in figure 4, is equivalent to the inflow port of the liquid cell 32, while the port of escaping gas, provided in the cell 22 in a diagonally lower side layer, equivalent to the inflow port of the gas cell 32. As stated above, through holes 51 for gas flow and holes 52 for the flow of liquid provided in the respective cells 22, 32, the flow path in which the gas flows upward, and a flow path in which fluid flows downward, is formed in a gas-liquid contactor 1, as shown in figure 2. It should be noted that the arrow shown in dotted lines in figure 2, indicates a period of 17 gas, while the arrow is shown as a solid line indicates a period of 16 fluid.

Here, the hole 52 to duct the fluid is formed in the form of narrow flow paths slit-like shape, as described above, resulting in that hole 52 for the flow of liquid acts as a resistance when the fluid flowing in the cell 32, flows into the cell 22 in a diagonally lower side layer, as shown in figure 4. In the space of the bottom sides in the respective cells 22, 32 become sections 53 stay, blocking and holding the fluid flowing in the cells 22, 32, with vertical walls 10, and the fluid flowing in the cells 22, 32, is directed into the cell 32, 22 of the lower side layer through the opening 52 for the flow of liquid after the formation of a volume of liquid in section 53 of the stay. Depth (depth of water) volume of the liquid residing in section 53 of stay is determined by the flow rate of the fluid supplied by the section 11 of the liquid supply, and the greater the flow, the greater the depth of the liquid, whereas the smaller the flow, the less the depth of the liquid.

On the basis of the above-described construction, the effect of gas-liquid contactor 1 according to the present variant of the implementation will be described with reference to figure 5 and 6. Figure 5 is a perspective view explaining the mechanism of gas-liquid contact of the thread 17 and gas flow 16 of the liquid in the cell 32, shown in figure 4, whereas 6 is a longitudinal view in section schematically showing the second state of the gas-liquid contact in a gas-liquid contactor 1.

The fluid injected in a gas-liquid contactor 1 through section 11 of the liquid supply, shown in figure 1, flows down the column using gravity, passing through the respective cells 22, 32, and reaches the cells 22 in the diagonally upper side layer of the cell 32, shown in figure 5. Here, as already described, the fluid injected into the cell 22 of the upper side layer, is section 53 of stay locked vertical wall 10, and forms a volume of fluid. When a given volume of liquid is formed in the partition 53 stay, the potential energy of the fluid in the bulk liquid is transformed into kinetic energy of the holes 52 for the flow of liquid and becomes a power, eject the liquid in the cell 32 of the lower side layer. As a result, if viewed from the cell 32 of the lower side layer, the fluid residing in section 53 of the stay or the cell 22 of the upper side layer, is introduced in the form of listopadova liquid flow 16 through to be a hole 52 for the flow of liquid, as shown in figure 5. How can I find such actions to be a hole 52 for the flow of liquid plays the role of hole entry, introducing the liquid is blocked by the vertical wall 10 and he that dwelleth in section 53 of stay in the cell 32 to the lower side of the tier.

On the other hand, the gas supplied in the gas-liquid contactor 1 of section and 13 gas supply, run up in gas-liquid contactor 1 under the action of pressure, compressing the gas, or power surfacing, acting on the gas, passing through the respective cells 22, 32, reaches the cell 22 in a diagonally lower side layer of the cell 32 shown in figure 5, and is sent into the cell 32 through the opening 51 to the gas flow. As already described, since the hole 51 for gas flow is formed in the form of slits, the gas becomes a leaf-fast gas stream 17 and is introduced from the hole 51 to the gas flow, when viewed from the side of the cell 32, as shown in figure 5.

Here, as already described, since the hole 51 to the gas flow cell 32 is secured in position directly under the hole 52 for the flow of liquid, the gas flow 17 intersects with the thread 16 of the liquid to the extension in space of the cell 32 and lowering its speed and flows in such a way that inflates the thread 16 of the liquid at the bottom. In the shear force by crossing air stream 17 acts on the thread 16 of the liquid, and the flow 16 of the liquid turns into liquid droplets and dispersed in the cell space 32, as shown in Fig.6. Thus, through that hole 52 for the flow of liquid and a hole 51 for gas flow are located above and below each other, the cell 32 functions as a space in which the thread 16 of the liquid stream 17 gas p is delaude countercurrent contact.

Further, because of the rapid gas flow 17 immediately after escaping from the hole 51 to the gas flow causes a decrease in pressure around the gas flow 17, you can also call the action fast track stream 16 fluid by pulling in the liquid passing through the holes 52 for the flow of liquid.

Mass transfer occurs between the surfaces of liquid droplets dispersed in the cell 32, and the surrounding gas, and mass transfer occurs from a gas to a liquid in the case of the absorbing column or from liquid to gas in the case organoclay columns. On the other hand, since the area of a horizontal section of the space inside the cell 32 is larger than the orifice 51 to the gas flow, the gas flow 17 flows upwards in the cell 32 with speed, gradually decreasing after the intersection with the thread 16 of the liquid. When the flow of the gas stream 17 is slowed down, the force of the gas stream 17, swelling liquid droplets, is weakened, so that the liquid droplets begin to settle down in section 53 of stay, and gas and liquid are separated. On the other hand, even in the case when the flow of the gas stream 17 reduces its speed, can be enough to separate drops of liquid in countercurrent contact in which small drops of liquid accompanied by a stream of gas by establishing a mist eliminator in the hole 51 to the gas flow.

Upon reaching th is izontally wall 31 in the upper side surface of the gas upward in the cell 32, is directed into the cell 22 in the diagonally upper side layer through the opening 51 to the gas flow provided in the vertical wall 10. On the other hand, liquid droplets, settled in section 53 of stay, merge with the amount established in section 53 of the stay, the concentration is made uniform, and then the liquid droplets are directed into the cell 22 in a diagonally lower side layer through hole 52 for the flow of liquid.

Thus, in the respective cells 22, 32 of the gas-liquid contactor 1 duplicate image operation is performed implementation of gas-liquid contact by turning the liquid into liquid droplets and dispersing them in Gaza and the operation of separating gas and liquid after the gas-liquid contact and direction in their cells 22, 32 of the side below along along the respective flow paths, through which flows the absorption or distillation between gas and liquid. When the liquid reaches the bottom of the column, the liquid ceases to communicate with the gas and is available in section 12 of the release fluid. Similarly for gas once the gas reaches the top of the column, the gas stops into contact with the liquid and is available in section 14 of the gas release.

In a gas-liquid contactor 1 according to the present variant implementation, described above, can be obtained following E. the effect. The inner region of the gas-liquid contactor 1, carrying out gas-liquid contact, divided into a number of cells 22, 32, forming a space counter-current gas / liquid contact, and the liquid residing in section 53 of the stay of the respective cells 22, 32, is introduced into the cells 22, 32 of the lower side layer through the opening 52 for the flow of liquid, which plays the role of holes in the input, or sent into the cells 22, 32 of the upper side layer under the action of the force with which the gas flows upwards in the cells 22, 32. Therefore, appropriate fluids can zabrasyvaetsya in adjacent cells 22, 32 without the use of special means of pressure application. In the respective cells 22, 32 of the thread 16 of the liquid and the flow 17 of the gas, which is introduced in the form of sheets, for example, are subjected to countercurrent contact, and the liquid droplets are dispersed in the gas phase, so there may be obtained a good dispersion state. In WATT (height equivalent to theoretical plate) becomes low, leading to improved efficiency of absorption, the efficiency of distillation or the like.

Furthermore, in addition to the fact that VAT is low, as already described, since the gas and liquid flow up/down bending their paths in the column when passing through the cells 22, 32 in a gas-liquid contactor 1 according to this the mu variant implementation, the height of the gas-liquid contactor 1 can be further made compact in comparison with ordinary disc casing and the like, in which the gas and liquid linear flow up/down, and the time of stay of the gas and the liquid in the columns are the same.

Further, since the liquid droplets formed in the respective cells 22, 32, are large compared to the drops in the spray column and the like, the separation of gas and liquid is easy, even when the fluid flow is fast, and you can do bandwidth per unit area of cross-section more or less than the diameter of the column with the same bandwidth.

Unlike column trays, in which the gas is dispersed in the liquid phase, remaining on the plate, to perform gas-liquid contact, as the cells 22, 32 according to the present variant of the implementation are not adapted to cause the gas flow to pass through the liquid phase, the occurrence of foaming (foaming liquid phase) can be avoided or limited. Due to this difference, the contact mechanism from the mechanism of the contact disc casing, the pressure loss of the gas stream becomes smaller, so that the driving force required to direct the gas in a gas-liquid contactor 1 becomes smaller, causing energy savings.

because these cells 22, 32 can be easily formed by dividing the inner area of gas-liquid contactor 1 a vertical wall 10 and horizontal walls 21, 31, can easily increase the number plates so that you may build complex gas-liquid contactor 1 lower value.

By providing openings 52 for the flow of liquid and openings 51 for gas flow in the form of slits stream 16 fluid stream 17 gas can be obtained in listopadova form the intersecting each other in the cells 22, 32, so that the large shear force is applied to the liquid gas stream 17, and the liquid stream 16 is easily dispersed with less liquid drops, ensuring a good dispersion state. It should be noted that the shape of the hole 52 for the flow of liquid, the holes 51 to the gas flow and the like are not limited to the forms shown in figv, and it is possible that, for example, a hole 52 for the flow of liquid is done by the location of numerous, shorter slots, as shown in figa, or that many holes 52 for flow of liquid from sections of round holes arranged as shown in figv. It is also possible that the hole 52 for the flow of liquid is provided in the form of a set of long slits arranged in the vertical direction, as shown in figs, and, optionally, the slot from which Erste 51 for gas flow is divided, and numerous slits are arranged in the transverse direction, for example. In addition, it is possible that many holes 51 for flow of gas from the sections of the holes are arranged in the transverse direction like a hole 52 for the flow of liquid, shown in figv, the corresponding figure is omitted.

An implementation option, explained using figure 1-6, constructed so that the inner region of the gas-liquid contactor 1 is vertically divided into two lines, and adjacent cells are on different layers, but the number of lines of cells or shape of the respective cells 22, 32 in a gas-liquid contactor 1 is not limited to this embodiment. It is possible, as shown in figa and FIGU, for example, that a circle drawn circular surface of the gas-liquid contactor 1, vertically divided into three parts, that is, three lines of cells are arranged transversely along one direction, and the cells 22, 32, 42 of the respective lines of cells are located in other tiers on tiers of neighboring cells 22, 32, 42.

In addition, the cells are not limited to cell, cross section X-Z which is rectangular, as shown in figure 1 or figa. For example, as shown in figa-9C, can be constructed so that the parts of the cells 22, 32, 42 of the upper side of the layers and cells 22, 32, 42 of the lower side of tiers stacked above and below each other is, so the volume of the section 53 of the stay becomes longer. In contrast to the above can be constructed so that the respective cells 22, 32, 42 on figa made upper side, so that an amount of section 53 of stay is less.

When constructed so that the parts of the cells 22, 32, 42 of the upper side and lower tiers of the side layers stacked above and below each other, the location of the holes 52 for the flow of liquid is not limited to a vertical wall 10, as described above, but can be constructed so that the holes 52 for the flow of liquid is provided in a horizontal walls 21, 31 of the lower sides of the surface of the cells 22, 32, as shown in figa-9C. In addition, figa-10C shows an example of a gas-liquid contactor 1 having such a structure that the inner region of the gas-liquid contactor 1 is concentrically divided in a vertical direction, and a cylindrical line cells are concentrically arranged across, and this type of gas-liquid contactor 1 is also included in the present invention. It should be noted that the numerical designation 18 of the drawings indicates the beam to maintain the cells 22, 32 of the inner side.

Then figa and figv shows an example of a gas-liquid contactor 1 used for adsorption columns or organoclay columns, in which the processed suspension, with whom containing a series of crushed solid impurity in the liquid, and for the catalytic reaction column in which the suspension containing the catalyst, and gas come into contact with each other to cause a reaction. When the suspension is treated in a gas-liquid contactor 1, there is a possibility that the shredded material in suspension settle and accumulate on the horizontal walls 21, 31, disrupting the flow of slurry flowing down the column. Therefore, in a gas-liquid contactor 1, shown in figa and FIGU, horizontal walls 21, 31 are inclined, and the inclination becomes lower in the direction of the openings 51 to the gas flow, resulting crushed material in suspension can be produced in the cells 22, 32 below along without accumulation on horizontal walls 21, 31. It should be noted that the processed objects to which you can apply such a gas-liquid contactor 1 is not limited to the suspension containing the crushed material, but gas-liquid contactor 1 can be used to contact the gas - solid material (solid), descending in a gas-liquid contactor 1, and gas, as well as to contact the liquid - solid material (solid), descending in a gas-liquid contactor 1, and liquid.

In a gas-liquid contactor 1 according to the present variant implementation, explain using Fig and 6, for example, the thread 16 of the liquid injected from the hole 52 for the flow of liquid from the volume of the liquid formed in the partition 53 and the gas flow 17, the current upward through the opening 51 to the gas flow, cross each other, so that the liquid stream 16 is inflated and shear force is applied to the thread 16 of the liquid dispersive liquid droplets in the respective cells 22, 32, whereby the good condition of the gas-liquid dispersion. Here, when the gas-liquid contactor 1 operates with low bandwidth and so on, for example, may be the case when the velocity of the gas stream 17, arising out of the hole 51 to the gas flow, slowing, weakening the power of promoting the flow 16 of the liquid, and a transverse force, leading to deterioration of the gas-liquid dispersion state.

Figure 6 shows the state when the liquid is injected from all of the slots constituting the hole 52 for the flow of liquid, but when working with low bandwidth or a similar depth of liquid in the liquid volume can sometimes be lower than the position of the slot provided in the upper side layer. In this case, the liquid is introduced from the slits provided in a higher position than the liquid volume and the cell 32 of the lower side layer and the cell 22 of the upper side layer is transferred into the state coordinadores this slot. As a result, the fraction of gas rising in the cell 22 to the lower side of the layer, can flow into the cell 22 of the upper side of the connecting layer through the slit, reducing the flow velocity of the gas stream 17 through a hole 51 for the flow of gas, and reducing gas-liquid dispersion state.

The cells 22, 32, shown in figa and FIGU, have a mechanism that prevents such deterioration of the gas-liquid dispersion state when working with low bandwidth or similar. Figa is a front view of the vertical wall 10 of the cell 22 shown in figa, for example, where the vertical wall 10 is visible from the cell 32 hand lower on the go, while FIGU is a longitudinal view in section of the cell 22 that is visible from the surface of the S1-S1'shown in figa. In the examples shown in the following figa-18V described cases, when the respective cells 22, 32 have an opening 52 for the flow of liquid, formed with three slits in General, there are two slots provided in the vertical wall 10 and one slot provided in a horizontal walls 21, 31.

In the example shown in figa and FIGU, cell 22 has a first valve that prevents the cell 22 from moving into the state with the neighboring cell 32 when the depth of liquid in the liquid volume is less than the position where provide the Jena slot openings 52 for the flow of liquid. In this example, the first valve is provided in the upper side layer openings 52 for the flow of liquid (slits)provided in the form of two layers of upper and lower slots in the vertical wall 10. The first valve has a plate 71 of the valve rectangular shape, slightly larger than the slot, for example, and the rotary shaft 711, acting horizontally to the right and to the left, is provided in the upper end part of the plate 71 of the flap.

Plate 71 of the valve is located, as shown in figv, with the output side of the hole 52 for the flow of liquid (slot), when viewed from the cell 22 in which is formed the volume of liquid, that is, on the surface of the vertical wall 10 in the cell 32, the parties below on the move, which follows a stream 16 of the liquid. On the surface of the vertical wall 10 is attached host axle section 712 of the ring shape, for example, and when the above-described rotary shaft 711 penetrates into the receiving axis section 712, the plate valve is located in the state of overhangs on the rotary axis 711.

As already established, the plate 71 of the valve is formed to have a size slightly larger than the slot constituting the hole 52 for the flow of liquid, and even if the power is supplied in the direction from the cell 32 shown in figv, plate 71 of the valve is locked with the vertical wall 10 in the state covering etc the cramps. On the other hand, if the power supplied from the cell 22 shown in figv, plate 71 of the valve is rotated to the inside of the cell 32 of the lower side layer, respectively, of the applied force, so that a closed valve can be released. Here it is also possible to provide a deflecting tool, coil spring, for example, deflecting in the closing direction of the plate 71 of the valve, for example, i.e. in the direction of the compression plate 71 of the flap to the surface of the vertical wall 10, in combination with a rotary axis 721 to regulate the amount of flow of the liquid stream 16 at the time when the plate 71 of the valve starts to open.

Now will be described the structure of the second damper provided in the hole 51 to the gas flow. The second flap is similar to the above first valve plate 72 of the valve elongated rectangular shape, the rotary shaft 721 provided in the upper end part of the plate 72 of the valve and protruding horizontally right and left, and the receiving axis section 722, which penetrates the rotary shaft 721. Here, in the present example, the plate 72 of the valve of the second valve is formed so that it has a width slightly larger than the hole 51 to the gas flow, made in the form of slits, and a height approximately half the height of the hole 51 to the gas flow. Receiving the axle section is I 722 is located on the side of the cell 22, in which flows a gas stream 17, so that, for example, the location at which stretched the rotary shaft 721, is almost the middle of the height of the openings 51 to the gas flow, and the rotary shaft 721 penetrates into the receiving axis section 722, whereupon the plate 72 of the valve is located in the state of overhangs with a rotary axis 721.

In the plate 72 of the valve is set to the state when the plate 72 of the valve closes the portion of the hole 51 to the gas flow, for example the lower half of the hole 51 to the gas flow, and even if a small force, it is not sufficient for lifting plate 72 of the valve, is applied in the direction from the cell 32 shown in figv, the plate 72 of the valve barely shifted from a state of closing of the opening 51 to the gas flow. However, as soon as the force exerted in the direction from the cell 32, becomes larger, the plate 72 of the valve is rotated to the inside of the cell 22 around a rotary axis 721, so that the closed hole 51 for gas flow is gradually released. Here it is also possible to provide a deflecting tool, coil spring, for example, deflecting in the direction of the closing plate 72 of the valve, for example, i.e. in the direction of the compression plate 72 of the flap to the surface of the vertical wall 10, in combination with a rotary axis 721 to regulate the amount of flow g the gas stream 17 at the time when the plate 72 of the valve starts to open.

The first flap of the two dampers described above will be explained. As shown in figa, in the case when the capacity of gas-liquid contactor 1 is low and the liquid level (the amount of liquid descending fluid) volume of liquid formed in the partition 53 stay the respective cells 22, 32, reaches the slits of the upper side layer comprising a hole 52 for the flow of liquid, the force causing the plate 71 of the valve of the first valve to turn, no effect. Thus, the plate 71 of the valve closes the gap in the state overhangs with a rotary axis 711 and in a state where the plate 71 of the valve is pressed to the surface of the vertical wall 10 by the pressure difference between, for example, the inner part of the cell 32 of the lower side layer and the inner part of the cell 22 of the upper side layer, or between the interior of the cell 22 of the lower side layer and the inner part of the cell 32 of the upper side of the layer.

As a result, the gas ascending in the cells 32, 22 of the lower side layer, can prevent the leakage in the cells 22, 32 of the upper side of the layer through the slit, so that the flow velocity of the gas stream 17 through a hole 51 for gas flow, not slowing down. On the other hand, when the capacity of gas-liquid contactor 1 is increased and UB is the tier of liquid volume of liquid reaches the slits of the upper side layer, a force is applied, causing the plate 71 of the valve to be rotated and, as shown in figv, closed slot is freed, so that the thread 16 of the liquid may be injected according to the level of liquid (fluid) volume of liquid.

Now will be described the operation of the second valve. In the condition of low bandwidth, shown in figa, because the amount of gas rising in the respective cells 22, 32 is small, the force acting on the plate 72 of the valve is small, so that the plate 72 of the valve barely moves and leaves the closed lower half of the hole 51 to the gas flow. As a result, the orifice 51 to the gas flow becomes small, and you can limit the deceleration of the rate of flow of the gas stream 17 through a hole 51, even when the amount of gas rising in the respective cells 22, 32, small.

As shown in figv when the capacity of gas-liquid contactor 1 increases, the amount of gas rising in the respective cells 22, 32, also increases, leading to greater pressure of the gas, whereupon the plate 72 of the valve is rotated, releasing the closed hole 51 to the gas flow, so that the orifice through which the gas flow becomes larger. In the result, it is possible to form the gas on the OK 17, maintaining the necessary flow rate, without a large increase in pressure loss compared to a condition in which the open area remains small.

By providing the data to the first flap and the second flap, even in the case when the capacity of gas-liquid contactor 1 is low, you can limit the deceleration of the rate of flow of the gas stream 17 through a hole 51 for gas flow, and to maintain power, blowing a stream of 16 fluid introduced from the hole 52 for the flow of liquid, and the transverse force acting on the thread 16 of the liquid so it can be supported by good dispersion state of gas and liquid.

Here the structure of the first damper is not limited to the rotary type shown in figa and figv. For example, as shown in Fig-15, it is possible to construct the plate 73 of the valve, for example, hollow element made of stainless steel and the like, where the plate 73 of the valve moves up and down along the vertical wall 10, receiving the buoyancy of the volume of the fluid residing in the respective cells 22, 32, whereupon the hole 52 for the flow of liquid (slot) opens and closes. In the drawing reference item 732 indicates the guide element, which specifies the direction of movement of the plate 73 of the valve, whereas the reference position 731 specifies the slider, RAS is than necessary between the plate 73 of the valve and the guide element 732 and running in a guide element 732.

In the present example, the plate 73 valves are designed able to open and close two slots (hole 52 for the flow of liquid), provided in two tiers from the top and bottom slots in the vertical wall 10. In the case when low bandwidth is carried out in a gas-liquid contactor 1, as shown in figa, for example, the liquid level of the liquid is low, the plate 73 of the valve barely moves from the lower position, and the slots (hole 52 for the flow of liquid in the vertical wall 10 is in the closed state, the thread 16 of the liquid is injected only from the slot 52 for the flow of liquid)provided in the horizontal wall 21.

When the capacity of gas-liquid contactor 1 is increased and the liquid level of the liquid in section 53 of the stay begins to grow, the plate 73 of the valve receiving buoyancy from a given volume of fluid moves upward in the upper position, so that the slit (hole 52 for the flow of liquid out the bottom side of the tier of the vertical wall 10 is opened and starts the input stream of 16 fluid. When the bandwidth increases additionally, slot (hole 52 for the flow of liquid) of the upper side layer are also opened, so that the thread 16 of the liquid is injected from all of the slots, as shown in figv.

Here the design and the construction of the plate 73 of the valve, moving up and down under the action of buoyancy from the volume of the liquid is not limited to the flat shape shown in Fig-16V, but may also be provided, as shown in figa, for example, the protruding plate 74, protruding along the horizontal wall 21 in the lower end position of the plate 73a of the valve, so that the cross section of the entire plate 73a is L-shaped. In this case, as shown in figa and FIGU, slot 52 for the flow of liquid), secured in a horizontal walls 21, 31 can be opened and closed according to the level of liquid volume of liquid.

As shown in figv, you can also provide corrector 75 buoyancy acting in the transverse direction to the interior of the cell 22 of the upper side layer in a predetermined position of the height of the plate 73b of the valve, so that the cross section of the entire plate 73b has a T-shape. By providing corrector 75 buoyancy becomes possible to change the buoyancy acting on the plate 73b damper according to the level of the liquid volume of the liquid, as shown in figa and FIGU, for example. In the result, by changing the position of the height at which ensured corrector 75 buoyancy, for example, you can adjust the liquid level of the liquid in section 53 of stay at the time when the corresponding slots (hole 52 for the flow of liquid is ti) are opened and closed. It should be noted that the plate 73, 73a, 73b of the valve, moving up and down, getting the buoyancy of that volume, not limited to the design of the hollow elements may be constructed with an item, such as plastic, the density of which is less than the density of the fluid being processed in a gas-liquid contactor 1.

Different variations of the structures of the cells 22, 32, 42, described above, can be determined from a comprehensive point of view, considering, for example, the capacity of gas-liquid contactor 1, the residence time of gas or liquid in the respective cells 22, 32, 42, the efficiency of absorption or distillation, the ease of flow of the used gas or liquid, ease of maintenance or construction and the like.

In addition, the gas-liquid contactor 1 according to the present invention can also be used for the distillation column, separating or purifying a fluid, for example, as shown in Fig. Gas-liquid contactor 1, shown in Fig, is provided by section 11 of the liquid supply, a feed, for example, the pre-heated fluid in the middle tier of the gas-liquid contactor 1, and the temperature gradient is provided between the side of the top of the column and the side of the bottom of the column to reach equilibrium vapor - liquid respectively to the temperatures in the respective cells 22, 32 resulting in a lightweight component is discharged from section 14 of the gas outlet at the top of the column, and the heavy component is discharged from section 12 of the release of liquid at the bottom of the column. It should be noted that the reference position 61 on Fig indicates a condenser for condensing the gas, produced from section 14 of the gas outlet, while the reference position 62 specifies the reboiler for re-heating liquid, produced from section 12 of the release fluid.

The above-described variant implementation and examples of its modification in relation to the gas-liquid contactor 1, in which the gas and liquid come into contact with each other, but the combination of fluid, which can be dealt with by the contactor according to the present invention are not limited. As a second variant implementation of the present invention can be applied to liquid-liquid contactor 1A to perform, for example, extraction or the like using liquid-liquid contact light liquid (bubbling fluid)flowing upwards in the column, and heavy liquid (downward fluid)flowing down the column, for example.

Fig is a longitudinal view with a section schematically showing the state of the internal region of the liquid-liquid contactor 1A according to the second variant of implementation, and the same reference position, as at 6, relate to the components, the structure of which is similar components of the first version done by the means. In the present embodiment, the full structure of the liquid-liquid contactor 1A is similar to the structure of gas-liquid contactor 1, for example, shown in figure 1, except that the reference position 11 indicates the section of the filing of the heavy liquid, the reference position 12 indicates the section of production of heavy liquid, the reference position 13 indicates the section of supply light liquid and the reference position 14 indicates the section of the release of easy liquids, which are omitted. The structure of the respective cells 22, 32 is similar to the structure of the cells, shown in figure 4, and the image is omitted, but this structure differs from the structure of the cells 22, 32 according to the first variant of implementation in that the reference position 51 indicates the hole for the light liquid, and the reference position 52 indicates the hole for the heavy liquid.

In liquid-liquid contactor 1A according to the second variant implementation of the heavy liquid residing in the cells 22, 32 of the upper side tiers, is introduced by its potential energy in listopadova form in the cells 22, 32 of the lower lateral tiers through holes 52 for heavy liquid (hole type), which is provided in the form of slits. On the other hand, from the cells 22, 32 of the lower side of the tiers of the light liquid flows into the cells 22, 32 of the upper side of the tiers in the form of listopadnyh flows, Iteca upward by the buoyancy be through holes 51 for easy fluid, secured directly under the holes 52 for heavy liquid.

Liquid-liquid contactor 1A shown in Fig designed so that the heavy liquid becomes dispersed phase and a light liquid becomes a continuous phase, and the velocity of light liquid increases rapidly near a hole 51 for easy fluid provided at the bottom side near the hole 52 for heavy liquid and light liquid flows into the cells 22, 32 of the upper side layer in a state where the flow rate is maximum, and then the velocity of light liquid rapidly decreases with distance from the hole 51 for easy fluid. When the heavy liquid is introduced in the form of a sheet through a set of apertures 52 for heavy liquid, provided in the longitudinal direction, flows into the region, through which the light liquid, listopadova for heavy liquid is deformed and becomes in the form of a corrugated plate, as shown in Fig, the surface area of the section of the liquid - liquid becomes more and listopadova for heavy liquid at the end is broken on numerous liquid droplets. Further, the liquid droplets formed in the hole 52 for the heavy liquid of the upper layer, flowing down and face sheet of heavy liquid formed in the hole 52 for heavy liquid nor is it tier one notch to the lowest tier, or are faced with liquid droplets, separated and formed from it, and then liquid droplets coalesce, are dispersed or dissolved. The greater the number and/or size of holes 52 for heavy liquids that are open in the respective cells 22, 32, the higher the frequency of mergers and destruction of liquid drops. As liquid droplets are formed, the surface area of the section of the liquid - liquid between the heavy liquid and the ambient light liquid becomes larger, and the liquid droplets after the formation of the repeat merger, dispersion and destruction, mass transfer proceeds, and extraction of a specific material can effectively be performed, for example. In addition, many educated liquid droplets of similar size and diameter of the droplets, and therefore small liquid droplets formed hard, so flooding hardly occurs, for example. It should be noted, of course, that variations explained using Fig-11, can also be applied to liquid-liquid contactor 1A.

On the other hand, in the extraction system having a large interfacial tension, or in the extraction system, where the heavy liquid and light liquid has a high viscosity, the diameter of the formed liquid droplets can be sometimes more, to some extent, and extraction could not be performed effectively. Then, as long as the ANO on Fig, the generator 19 ripple joins the lower section, which is a section of the bottom of the column extraction columns 1d, for example, made of a liquid-liquid contactor 1A according to the present variant implementation, or ripple generated by directing an air pulse, used in combination, resulting in forming a liquid drop is less and the extraction can be performed more efficiently. It should be noted that Fig reference position 11a indicates the section of the filing of the heavy liquid, the reference position 12A indicates the section of production of heavy liquid, the reference position 13A indicates the section of supply light liquid and the reference position 14a indicates the section of the release of light of the liquid.

On the other hand, in the case when the light liquid is the dispersed phase and a heavy liquid is a continuous phase, there is a contrast liquid-liquid contactor 1A, explained Fig, that the cell 32, shown in figure 4, is done top down, the reference position 51 in figure 4 is equivalent to the hole for heavy liquid (specified as a hole 51A for heavy liquid), and the reference position 52 is equivalent to the aperture for light liquids (specified as a hole 52a for light liquids), as in liquid-liquid contactor 1b shown in Fig.

In alkosto-liquid contactor 1b light liquid staying in the cells 22, 32 of the lower side tiers, is introduced in the form of a sheet by its buoyancy in the cells 22, 32 of the upper side of the layers through the opening 52a for light liquids (insertion), provided in the form of slits. On the other hand, from the cells 22, 32 of the upper side of the tiers of the heavy liquid flows into the cells 22, 32 of the lower side of tiers in listopadova stream, flowing down through the potential energy be through hole 51A for heavy liquids, provided directly above the hole 52a for easy fluid.

As a result, when the light liquid is introduced in the form of a sheet through the openings 52a for easy fluid rushes into the area where the heavy liquid flows in the form of a sheet in a state where the flow rate is maximum, from the hole 51A for heavy liquid, provided in the upper side relative to the hole 52a for easy fluid, listopadova for easy fluid deforms and becomes in the form of a corrugated plate, as shown in Fig, the surface of the separation liquid - liquid becomes more and listopadova for light liquid at the end is divided into numerous liquid droplets. Further, the liquid droplets formed in the hole 52a for easy fluid lower side among the holes 52a for easy fluid sequentially provided in predolin the m direction, flow up and face sheet light liquid formed in the holes 52a for easy fluid of a higher tier on the same level to the highest tier, or faced with liquid droplets, separated and formed from the given sheet of light liquid and then the liquid droplets coalesce, are dispersed or dissolved. The greater the number and/or size of holes 52a for light liquids that are open in the respective cells 22, 32, the higher the frequency of mergers and destruction of liquid drops. In the result, like the above-described liquid-liquid contactor 1A, explain using Fig, the surface area of the section of the liquid - liquid between the heavy liquid and the ambient light liquid becomes larger, and the liquid droplets after the formation of the repeat merger, dispersion and destruction, and therefore, mass transfer occurs, and not only effective extraction, but also many educated liquid droplets of the same size and diameter of the droplets, and small liquid droplets hardly formed, so that the flooding hardly occurs, for example. It should also be noted that in the liquid-liquid contactor 1b can be tilted horizontal walls 21, 31, for example, by doing the above in the direction of the hole 52a for easy fluid, to make it easier to produce a light liquid, and you can do cake 22, 32 upper side of the layers and cells 22, 32 of the lower side of tiers stacked above and below each other and to provide openings 52a for easy fluid in the horizontal walls 21, 31 of the ceiling surface. On the other hand, in the extraction system having a large interfacial tension, or in the extraction system, where the heavy liquid and light liquid has a high viscosity, the diameter of the formed liquid droplets can be sometimes more, to some extent, and extraction could not be performed effectively. Then, like the example shown in Fig, the generator 19 pulsation, for example, is attached to the lower section, which is a section of the bottom of the columns, extraction columns, made of liquid-liquid contactor 1b according to the present variant implementation, for example, or ripple generated by directing an air pulse, used in combination, resulting in forming a liquid drop is less and the extraction can be performed more efficiently.

As described above, in the second embodiment, shown in Fig and Fig, you can get heavy liquid (or light liquid), which is the dispersed phase and a light liquid or heavy liquid), which is the continuous phase, which are introduced in the form of sheets, vigorously cross each other is compared with liquid-liquid contactor 120, described in the section "prior art" using pig, and thus it is possible to increase the surface area of the section of the liquid - liquid during formation of liquid drops, increasing the frequency of mergers and destruction of the liquid droplets after the formation and increasing the rate of mass transfer, so that the extraction efficiency can be increased. In addition, because of the heavy liquid (or light liquid) is introduced in the form of a leaf as distinct from the ordinary input in the form of a liquid column, the size of the formed liquid droplets and the diameter of the droplets becomes more homogeneous, and the formation of small liquid droplets can be controlled so that the speed of flooding, for example, can be improved.

Above, the contactors 1, 1A described in the first and second variants of implementation, provides a contactor in which the inner area of the cylindrical columns are separated by partitions consisting of vertical walls 10 and horizontal walls 21, 31, 41, forming multiple cells 22, 32, 42, but the contactor included in the present invention is not limited to the contactor, in which adjacent cells 22, 32, 42 are divided by partitions, as in the above examples. For example, the present invention includes a contactor in which the cells 22, 32, 42, having a cubic shape, are formed individually, and the holes 52 for the flow of liquid and is TVersity 51 for gas flow adjacent cells 22, 32, 42 are connected to each other through pipes, respectively, at different tiers.

[Working example]

(Experiment 1)

Produced gas-liquid contactor having almost the same structure as the contactor shown in figa and 8B, and checked the condition of the gas-liquid contact.

A. Experimental method

As the main body of the gas-liquid contactor 1 used a transparent cylindrical tube made of polyvinyl chloride, which had a diameter of column 210 mm and a height of 1200 mm, and the cells 22, 32, 42 formed using partitions (vertical wall 10, the horizontal walls 21, 31), made of stainless steel (SUS304). The height of the respective cells 22, 32, 42 was 200 mm, and the inner part of the cylindrical pipe was divided so that three lines of cells from five stacked layers were located in the transverse direction. Surface sides of the respective cells 22, 32, 42 had almost the same structure as shown in figv, the height in the longitudinal direction of the slit openings 52 for the flow of liquid was 3 mm, and the height in the longitudinal direction of the slit hole 51 to the gas flow was 10 mm

In the above-described gas-liquid contactor 1 poured water from section 11 of the liquid supply and air from section 13 of the gas supply and then the water and the air was subjected to countercurrent contact is.

(Working example 1) the Air was filed with the external velocity of 0.5 m/s and the external water velocity varied as 0.5 cm/s, 1.0 cm/s and 1.5 cm/s

(Working example 2) When the external air velocity 1.0 m/s external water velocity was varied in the same way as in working example 1.

(Working example 3) When the external air speed of 1.5 m/s external water velocity was varied in the same way as in working example 1.

(Working example 4) When the external air velocity of 1.0 m/s in an aqueous solution with a low concentration (0.5% mass) ethanol, representing a foamy aqueous solution, was applied instead of water and external speed varied as 0.5 cm/s, 1.0 cm/s and 1.5 cm/s

(Working example 5) When the external air velocity 1.0 m/s a small amount of surface active agent TRITON X-100 was mixed in water (5 mg/l)to use a foamy aqueous solution instead of water, and external speed varied as 0.5 cm/s, 1.0 cm/s and 1.5 cm/s

C. Experimental results

According to the results of visual observation of gas-liquid state, it was proved that under all conditions of working example 1 to working example 3, the water turned into liquid droplets and disbelieves in the respective cells 22, 32, and then separated from the gas phase, forming a volume of liquid in section 53 of the stay. It was also proven that no foaming occurred in the work ol the least 4 and a working example 5. When the gas is dispersed in an aqueous solution of ethanol low concentrations or small quantity of an aqueous solution containing a small amount of surface-active agent, a foam layer is formed in the upper section of the liquid and foaming occurs at the gas-liquid contact plate column, creating the problem of low productivity of the method. However, when liquid droplets are dispersed in a gas, as in the present example, the foaming can be avoided, and no foam layer is not formed, that is, there can be obtained the effect that prevents the performance degradation of the way through the foam.

(Experiment 2)

Like the structure shown in Fig.9, the holes 52 for the flow of liquid provided in the vertical wall 10 and the horizontal walls 21, 31, and the hole 51 to the gas flow provided in a position directly below the hole 52 for the flow of liquid in the vertical side wall 10, and the cells 22, 32 of the two lines were made (Fig), embedded in an existing distillation column, to run the test distillation and test distillation.

A. Experimental method

The distillation column had an inner diameter of the column 198 mm and a height of 3300 mm, and the cells 22, 32 disposed in two lines and seven tiers (fourteen tiers only). Corresponding to CACI 22, 32 had a height of 400 mm, the hole for the gas flow had a height of 20 mm, and the holes 52 for the flow of liquid consisted of two rows of slits with a width of 3 mm in the horizontal wall and three rows of slits with a width of 3 mm in the vertical wall. The distillation column had the reboiler 62 in the bottom section of the column and the condenser 61 in the top of the column.

Test-first distillation was performed under full irrigation, using a mixed solution of benzene and chlorobenzene.

Then the mixture of ethylbenzene and chlorobenzene was applied to the top of the distillation column, the feed rate and temperature reboiler 62 changed, the test distillation was performed without irrigation. In both experiments the steam from the top of the column was introduced into the condenser 61, maintaining the pressure at atmospheric pressure.

(Working example 6)

After a mixed solution of ethyl benzene and chlorobenzene (mass fraction of ethylbenzene was 0.50 mass fraction of chlorobenzene was 0,50) received at the bottom of the distillation column, part of it was sent to the reboiler 62 and output reboiler fluid is returned to the bottom of the column, the liquid temperature of the bottom of the column was increased to a predetermined temperature. Steam escaping from the top of the column was introduced into the condenser 61, and after cooling and condensation of the entire liquid distillate flowed back to the top of the column. The pressure of the condenser 61 under arrival at atmospheric pressure, and after the appropriate temperature of the liquid at the outlet of reboiler, the bottom of the column and the top of the column and the flow rate of irrigation became permanent, taking samples of the fluid, the top of the column and the liquid of the bottom of the column and analyzed using gas chromatography. The measured results for the fluid, the top of the column and the liquid of the bottom of the column after reaching the stationary state are shown in table 1.

(Working example 7)

A mixed solution of ethyl benzene and chlorobenzene (the mole fraction of benzene was 0,379 and the mole fraction of chlorobenzene was 0,621) is continuously fed into the top of organoclay columns, and the entire amount of liquid distillate produced from the top of the column and the liquid bottom was released from the bottom of the column. After reaching the stationary state taking samples of the fluid, the top of the column and the liquid of the bottom of the column and analyzed using gas chromatography. The measured results are shown in table 2.

(Working example 8)

The amount of material (the mole fraction of benzene was 0,426 and the mole fraction of chlorobenzene was 0,574), served in organoclay column, increased the number of working example 7 to about 17%, and the operation was performed in the same way, receiving the data. The measured results are shown in table 2.

Table 1
The measurement parameter, the results of operationsWorking example 6
The mass flow rateIrrigationkg/h261
TemperatureEntrance irrigation
The top of the column
The bottom of the column
The output reboiler
°C
°C
°C
°C
99,7
133,0
136,5
137,4
CompositionThe top of the column
Chlorobenzene
Ethylbenzene
The bottom of the column
Chlorobenzene
Ethylbenzene
mol. share
mol. share
mol. share
mol. share
0,655
0,345
0,456
0,544
The number of theoretical plates
The overall efficiency of the cell
-
%
6,9
49

Table 2
The measurement parameter, the results of operationsWorking example 7Working example 8
The mass flow rateIrrigation
Supply
The distillate
Bottom
kg/h
kg/h
kg/h
kg/h
0
260
253
7
0
305
238
67
TemperatureInput supply
The top of the column
The bottom of the column
The output reboiler
°C
°C
°C
°C
100,9
133,2
135,6
to 136.4
99,7
133,4
136,0
136,6
CompositionSupply
Chlorobenzene
Ethylbenzene
mol. share
mol. share
0,621
0,379
0,574
0,426
The top of the column
Chlorobenzene
Ethylbenzene
mol. share
mol. share
0,627
0,373
0,599
0,401
The bottom of the column
Chlorobenzene
Ethylbenzene
mol. share
mol. share
0,440
0,560
0,489
0,511
The number of theoretical plates
The overall efficiency of the cell
-
%
7
50
9
64

C. Experimental results

According to experimental results, shown in table 1, in the test distillation with full irrigation (working example 6) as the concentration of the low-boiling chlorobenzene (132°C) above the section of the top of the column and the concentration of the high boiling point of ethylbenzene (136,22°C) above the bottom section of the column as compared with the composition during preparation, found that fractional distillation of both components is performed in a distillation column. When the temperature of reboiler 62 is 137,4°C and the amount of irrigation from the capacitor 61 is 261 kg/h, the number of theoretical plates calculated on the basis of the respective measured compositions near the top of the column and the bottom of the column (the mole fraction (mol. share))is 6.9 plates, and the total efficiency of the cell is 49%.

In addition, according to experimental results, shown in table 2, and in the working example 7, and in the working example 8, the concentration of low-boiling chlorobenzene in the distillate from the top of the column is high, and the concentration of the high boiling point of ethylbenzene is high in the produced fluids from the bottom of the column relative to the original composition of the mixed solution, and found that the distillation of a lightweight component is the distillation column.

In the test distillation of the working example 7, when the temperature of reboiler 62 is supported to 136.4°C and the feed speed, filling organoclay column, set at 260 kg/h, the amount of distillate is 253 kg/h and the amount of the bottom liquid is 7 kg/h, and the overall efficiency of the cell is equal to 50%. In the test distillation of the working example 8, in which the bandwidth is extended when the temperature of reboiler 62 is supported 136,6°C and the feed speed, filling organoclay column, set at 305 kg/h, the amount of distillate is 238 kg/h and the amount of the bottom liquid is 67 kg/h, and the overall efficiency of the cell is equal to 64%. When the bandwidth increases and the amount of fluid residing in the respective cells, increasing, constant efficiency is improved.

(Experiment 3)

In the following comparative example and working example was running the operation liquid-liquid extraction, extragere acetic acid from an aqueous solution of acetic acid (hereinafter referred to as the original material)having a concentration of 29% of the mass. in each case, the mixed solvent (hereinafter referred to as solvent) of ethyl acetate 80% vol. + cyclohexane 20% vol.

(Comparative example 1)

As extracting apparatus used column 120, the liquid fluid is local extraction Zapadno-disc type (patent document 3), having the structure shown in Fig. Column 120 liquid-liquid extraction had an inner diameter of 208 mm, and percentage of open area route 123 liquid flow (the area of the path of liquid flow/cross-sectional area of the column) plates 121 was 32%, there was a 25 tiers of plates 121 Zapadno-disc type, having four holes 124 of the rectangles 25 mm × 20 mm as the path of liquid flow dispersed phase in the interval between the plates 100 mm

The raw material was a heavy liquid, and the solvent was a light liquid, and heavy liquid was dispersed phase, and the ratio of solvent (mass ratio of solvent/raw material) was chosen 2/1, liquid-liquid countercurrent contact is performed at a temperature of approximately 20°C at atmospheric pressure.

When the speed of supply of raw materials amounted to 218 kg/h and the solvent (the concentration of acetic acid 0%) 436 kg/h, the raffinate had current speeds of 131 kg/h and the concentration of acetic acid 2,3% of the mass. The calculation of the equilibrium liquid - liquid performed to obtain the height equivalent to a theoretical plate (hereinafter called WATT), and WATT was 0,64 m

When the supply of raw materials and the solvent was increased to 335 kg/h for raw materials and 670 kg/h for solvent, was flooding.

(Working example 9)

The experiment will is applicable, using extracting apparatus of the cellular type (liquid-liquid contactor 1C) according to a variant implementation of the present invention, which has the structure shown in Fig as extracting apparatus. The cells 22, 32, 42 three lines - twelve plates were placed in a column having an inner diameter of 208 mm, and the height of the respective cells 22, 32, 42 was 200 mm, slotted holes 52 for heavy liquid had a width of 5 mm and were arranged in two rows, and the width of the openings 51 for easy fluid was 20 mm Conditions except for the flow rates of the raw materials and solvents were the same as in comparative example 1.

When the material was 218 kg/h and the flow of solvent (the concentration of acetic acid 0%) was 436 kg/h, the raffinate had a flow rate of 132 kg/h and the concentration of acetic acid and 1.5% of the mass. The calculation of the equilibrium liquid - liquid performed to obtain WATT, and WATT was 0,54 m

When the material was 335 kg/h and the flow of solvent (the concentration of acetic acid 0%) was 670 kg/h, the raffinate had a flow rate of 205 kg/h and the concentration of acetic acid 1,2% of the mass. The calculation of the equilibrium liquid - liquid performed to obtain the height equivalent to a theoretical plate (hereinafter called WATT), and WATT was 0.49 m

When the supply of raw materials and the solvent was increased to 40 kg/h for raw materials and 900 kg/h for solvent, was the flooding.

Throughput and efficiency of extraction for comparative example 1 and the present invention is shown in table 3.

Table 3
The amount of liquid (kg/h)The efficiency of extraction
Raw materialsSolventComparative example 1Working example 9
Extracted acetic acid (%)WATT (m)Extracted acetic acid (%)WATT (m)
218436for 95.20,6496,90,54
335670**97,50,49
450900 **
*) there is flooding

According to experimental results, shown in table 3, in the case when the amount of raw materials were the same (218 kg/h for raw materials, 436 kg/h for solvent), when comparing the test results of the extraction column 120 liquid-liquid extraction Zapadno-disc type (comparative example 1) and columns 1C liquid-liquid extraction of the cellular type (working example 9) value WATCH in working example 9 was smaller than in comparative example 1, approximately 15.6%, and the efficiency of extraction was better. In addition, when the amount of water (335 kg/h for raw materials, 670 kg/h for solvent), wherein in comparative example 1, there is flooding, the extraction operation is possible without flooding in working example 9.

1. Contactor, in which the rising fluid representing the gas is supplied from the lower part of the column, and the descending fluid constituting the liquid is supplied from the upper part of the column, and the data of the gas and the dispersed phase liquid is subjected to countercurrent contact with a continuous gas phase containing:
providing multiple tiers of cells so that the cell upper side layer and the cell lower side layer, the neighbour plans to each other along the paths of upward flow of fluid and descending fluid, are on different tiers, and the cell forming region countercurrent contact of the ascending fluid and downward fluid;
separation of the cells of the upper side layer and the cell lower side layer using partitions; and
the software in the partition corresponding tiers of holes entering the descending fluid, functioning as a resistance for the formation of a volume of liquid and formed by the location of the many holes in the direction of height or by the location of many vertically elongated holes that pass in the height direction, in the transverse direction on the lower portion of the side surface of the cell upper side of the layer, so that the descending fluid is introduced from the specified volume of liquid in the cell lower side layer, and providing an inlet port of the ascending fluid is higher than the region in which arrives downward fluid and through the inlet port of the ascending fluid rising fluid from cell lower side layer flows into the cell upper side of the layer.

2. The contactor according to claim 1, in which:
the insertion of the descending fluid provided by the first valve, opening and closing in accordance with the number of descending fluid blocked by the partition, so predotvrativshie the fluid, the current in the cell lower side of the layer, from passing into the cell upper side of the layer through the insertion downward environment.

3. The contactor according to claim 2, in which:
the first flap is provided on the side leakage of holes entering the downward environment in such a way as to be closed by deflection using the first deflecting means and to open against the deviation of the first deflecting means by downward pressure of the fluid residing in the cell upper side of the layer.

4. The contactor according to claim 2, in which:
the insertion of the descending fluid medium is provided on the side surface of the cell, and the first valve is configured to move up and down between a lower position, closing the insertion of the descending fluid, and the upper position, opening the insertion of the descending fluid, and moves up from the lower position by buoyancy from the descending fluid residing in the cell upper side of the layer.

5. The contactor according to claim 4, in which:
the insertion of the descending fluid is also provided on the bottom surface of the cell, and the first valve is configured to close the holes entering the descending fluid on the bottom surface in the lower position.

6. The contactor according to claim 4, in which:
the first flap has a corre the tor buoyancy, acting in the transverse direction to the cell upper side of the layer.

7. Contactor, in which the rising fluid representing the gas is supplied from the lower part of the column, and the descending fluid constituting the liquid is supplied from the upper part of the column, and the dispersed phase liquid is subjected to countercurrent contact with a continuous gas phase containing:
providing multiple tiers of cells so that the cell upper side layer and the cell lower side layer adjacent to each other along the paths of upward flow of fluid and descending of the fluid are at different tiers, and the cell forming region countercurrent contact of the ascending fluid and downward fluid;
separation of the cells of the upper side layer and the cell lower side layer using partitions; and
the provision in the respective tiers of holes entering the descending fluid in the lower surface of the cell upper side layer, functioning as a resistance to the formation of liquid volume, so that the descending fluid is introduced from the specified volume of liquid in the cell lower side layer, and providing an inlet port of the ascending fluid is higher than the region in which dwells the descending fluid and through pritech the output port of the ascending fluid rising fluid medium from the cell lower side layer flows into the cell upper side of the layer.

8. The contactor according to claim 7, in which:
the insertion of the descending fluid is provided in the bottom surface of the cell and provided with a first valve, which is made with the capability of raising and lowering between the lower position, closing the insertion of the descending fluid, and the upper position, opening the insertion of the descending fluid, and which rises from the lower position by the force of buoyancy from the descending fluid residing in the cell upper side of the layer.

9. The contactor according to claim 1 or 7, in which:
inlet port of the ascending fluid provided by the second valve, the opening and closing portion of the inlet port of the rising fluid in accordance with the upward pressure of the fluid flowing from the cell lower side layer of the cell upper side of the layer.

10. The contactor according to claim 9, in which:
a second valve provided on the side of the flow inlet port of the ascending fluid medium in such a way as to be closed by deflection of the second deflector means and to open against the deviation of the second deflecting means by upward pressure of the fluid.

11. Contactor, in which the rising fluid constituting the liquid is supplied from the lower part of the column, and the descending fluid, not only the maintenance of a liquid, is supplied from the upper part of the column, and the dispersed phase of the downward flow is subjected to countercurrent contact with the continuous phase of the upward stream containing:
providing multiple tiers of cells so that the cell upper side layer and the cell lower side layer adjacent to each other along the paths of upward flow of fluid and descending of the fluid are at different tiers, and the cell forming region countercurrent contact of the ascending fluid and downward fluid;
separation of the cells of the upper side layer and the cell lower side layer using partitions; and
the software in the partition corresponding tiers of holes entering the descending fluid, functioning as a resistance for the formation of the descending volume of fluid, and formed by the location of the many holes in the direction of height or by the location of many vertically elongated holes that pass in the height direction, in the transverse direction on the lower portion of the side surface of the cell upper side of the layer, so that the descending fluid is injected by means of its potential energy from the specified volume of fluid in the cell lower side layer, and providing an inlet port of the ascending fluid is higher than the hole is brought to enter the descending fluid, moreover, through the inlet port of the ascending fluid rising fluid medium from the cell lower side layer flows due to its buoyancy in the cell upper side of the layer.

12. The contactor according to claim 1 or 11, in which:
cell upper side layer and the cell lower side layer are in a mutual location in which the parts thereof are stacked above and below each other, and
the insertion of the descending fluid is provided in the lower portion of the side surface and the bottom surface of the cell upper side of the layer.

13. The contactor according to claim 1, 7 or 11, in which:
holes enter the descending fluid are slits passing in the transverse direction or longitudinal direction, or sections of the holes.

14. The contactor according to claim 1, 7 or 11, in which:
inlet port of the ascending fluid is a slot passing in the transverse direction or longitudinal direction, or a section of multiple holes arranged in the transverse direction or the longitudinal direction.

15. The contactor according to claim 1, 7 or 11, in which:
the lower surface of the cell is inclined to fall to the hole of the input provided in the cell.

16. Contactor, in which the rising fluid constituting the liquid is supplied from the lower part of the column, and the descending fluid representing W is dcost, is supplied from the upper part of the column, and the dispersed phase of the upward stream is subjected to countercurrent contact with the continuous phase of the downward stream containing:
providing multiple tiers of cells so that the cell upper side layer and the cell lower side layer adjacent to each other along the paths of upward flow of fluid and descending of the fluid are at different tiers, and the cell forming region countercurrent contact of the ascending fluid and downward fluid;
separation of the cells of the upper side layer and the cell lower side layer using partitions; and
the software in the partition corresponding tiers of holes entering the ascending fluid, functioning as a resistance for the education of the rising volume of fluid and formed by the location of the many holes in the direction of height or by the location of many vertically elongated holes that pass in the height direction, in the transverse direction on the upper portion of the side surface of the cell lower side layer, so that the rising fluid is introduced through its buoyancy from the specified volume of fluid in the cell upper side layer, and providing an inlet port of the descending fluid is lower than the hole BBO is and ascending fluid, through which the descending fluid medium from the cell upper side layer flows due to its potential energy in the cell lower side of the tier.

17. Contactor according to clause 16, in which:
cell upper side layer and the cell lower side layer are in a mutual location in which the parts thereof are stacked above and below each other, and
the insertion of the ascending fluid is provided in the upper portion of the side surface and the ceiling surface of the cell upper side of the layer.

18. Contactor according to clause 16, in which:
holes enter the ascending fluid predstavljaet a slot passing in the transverse direction or longitudinal direction, or sections of the holes.

19. Contactor according to clause 16, in which:
inlet port of the descending fluid is a slot passing in the transverse direction or longitudinal direction, or a section of multiple holes arranged in the transverse direction or the longitudinal direction.

20. The contactor according to claim 1, 7, 11 or 16, in which:
there are many lines of cells in which multiple cells are arranged in a line longitudinally, and the cell belonging to each line of the cell and the neighboring cell line cells are on different tiers.

21. The contactor according to claim 20, in which:
the corresponding lines of cells placed transversely along one what about the directions.

22. The contactor according to claim 20, in which:
this contactor has a cylindrical shape, and the corresponding cells are concentrically arranged transversely.



 

Same patents:

FIELD: chemistry.

SUBSTANCE: in the method of neutralising acidic impurities during synthesis of acrylates, the neutralising agent used is ammonia solution with concentration of not less than 0.01% in amount which ensures pH of the mixture of 5.5-6.7, said mixture being formed after mixing the neutralising agent with raw acrylate. Said method involves preparation of a neutralising agent, mixing the prepared neutralising agent and raw acrylate followed by phase separation of the mixture into a top organic layer of raw acrylate and a bottom aqueous layer of spent neutralising agent. Copper sulphate is also added to the ammonia solution in amount of 0.6-0.12 wt %. When preparing the neutralising agent, the solution is mixed through circulation thereof. Ammonia solution concentration of 1-2% if optimum for industrial engineering. The apparatus has containers connected by pipes for preparing aqueous solution for the neutralising agent, a circulation pump, an overhead tank, a pump, a mixer, a phase separator, as well as an overhead tank for raw acrylate connected with the pump. The apparatus also has a container for ammonia solution and an additional pump fitted at the inlet of the container for preparing ammonia solution, and a pH metre fitted at the outlet of the mixer, where the mixer is in form of a turbulator. The turbulator is a metal pipe into which a disc with holes is fitted perpendicular the longitudinal axis, said disc being made from fluoroplastic or steel.

EFFECT: obtaining a high-purity end product, characterised by low content of acidic impurities, achieved owing to use of structural components and process operations which enable addition of a neutralising agent according to a defined scheme.

5 cl, 2 dwg, 1 tbl, 12 ex

FIELD: process engineering.

SUBSTANCE: invention relates to continuous gas-fluid reactions in high-pressure tubular reactor. Proposed method comprises feeding, at least, one fluid reagent by gas reagent flow feeder 2, and, not obligatorily, by feeder 3. Note here that, at least, one initial flow is fed at supercritical pressure. It comprises also heating, at least, one said flow by heater 4 connected with feeder and combining said flows in jet mixer 5. Obtained gas-fluid mix reacts in direct-flow tubular reactor in, in fact, adiabatic conditions. Reaction mix flow is throttle via reducing device 7 into evaporating separator 8 at lower pressure with stripping gas flow comprising, mainly, low-boiling components from top part of evaporating separator 8, and liquid flow comprising, mainly, high-boiling components from bottom part of said evaporating separator 8. Note here that said flows are heated to temperature that allows interaction reaction in supercritical fluid. Aforesaid flows are combined in jet mixer 5 with gas-fluid mix rate of 10-350 m/s. Note here that time whereat combination occurs makes less than 1 second. Obtained gas-fluid mix interacts in direct-flow tubular reactor 6 that drastically reduces liner rate of said gas-fluid mix to 0.01-10 m/s. Note also that time whereat said interaction occurs makes less than 600 seconds.

EFFECT: higher reaction rate and target product yield.

25 cl, 3 ex, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention can be used in the paint and varnish industry. Before feeding liquid components into reactor 1, the explosive medium vacuum pumping system is switched on and when the required degree of vacuum is attained, a shut-off apparatus, which is in form of a shut-off valve 4, is opened. Liquid components are loaded into the reactor 1 from the storage 9 of liquid material through process pipes 2. After loading the required amount of components into the reactor 1, the shut-off valve is closed, sealing the reactor 1.

EFFECT: invention increases cost effectiveness of fire- and environmental safety of the process of producing alkyd varnish.

23 cl, 1 dwg

FIELD: transport, construction.

SUBSTANCE: proposed method is implemented by applying anti-black ice agent comprising, wt %, i.e. calcium chloride of 20 to 30 (on the dry road surface), corrosion inhibitor solution (on the dry road surface) of 1 to 2. Note that the aforesaid agent comprises also, wt %, the following components, i.e. carbamide of 21.5 to 23.0, diazotising salt of 45.78 to 51.85, sodium hexametaphosphate of 0.65 to 0.82, levenol "Ц-201" of 13.0 to 15.2, tetranilum 511K of 13.0 to 15.2 and water making the rest. The proposed method of preparing the liquid anti-black ice agent comprises force-feeding the corrosion inhibitor solution into the mixer at a pressure 1.8 to 2.2 times higher than that of feeding the calcium chloride solution. The resultant reagent is pumped over into storage tank. The process line to produce liquid anti-black ice agent comprises vessels to prepare, store and discharge water solutions of calcium chloride along with the corrosion inhibitor, the said vessels communicating via pipelines with the reagent tank.

EFFECT: expanded temperature range of reagent applications not affecting environments, nor road surface and reducing metal corrosion, easier road surface cleaning.

4 cl, 2 tbl, 1 dwg

Reactor // 2323773

FIELD: production methods; chemical engineering.

SUBSTANCE: reactor includes body, as minimum one nozzle for input the reagents, then one pair (as minimum) of nozzles and pipe lines for input the reagent mixture with two sections of mixture circulation, the internal tube devices of the steam separation with mixers, connected with nozzles for input the reagent mixture, the nozzle and the pipe line for emergency layout of gas phase to the "plug". Every nozzle and pipe line for output the reagent mixture and final product from reactor by free plum are provided with intermediate tank, the way that the lower part of the tank is connected with nozzle, and the upper with pipe line. The movement "▵" between the axis of the nozzle and the pipe line, defined the height of the tank, should be more then critical height of filler generating "Нcr" of free plum.

EFFECT: reactor let to dispose the scrap; to increase the output of the final product with quality speciation and increase the safety of the process.

5 cl, 3 dwg

FIELD: petrochemical industry; integral reactors and the methods of realization of exothermal and endothermic reactions.

SUBSTANCE: the invention is pertaining to the integral reactors of combustion (IRC), intended for realization of the exothermal and endothermic reactions. The IRC contains the exothermal reaction chamber (12) with the catalytic agents of the exothermic reaction (14,16), the endothermic reaction chamber (15) with the catalytic agent of the endothermic reaction (17), the open channels (18,19) for free flow of the of the medium stream through the chamber and the heat-conducting partition separating the chambers. It is preferable, that the exothermal or endothermic chambers would have the width (the minimum size in a direction perpendicular to the stream) - 2 mm or less. The invention also describes the separate models of the reactors and the methods of realization of the reactions in them. The invention ensures the safe work with the fuel, realization of the vapor reforming during the short time of the contact, the increased productivity per the unit of the volume of the reactor, extinguishing/inhibition of the gaseous-phase reactions.

EFFECT: The invention ensures the safe work with the fuel, realization of the vapor reforming during the short time of the contact, the increased productivity per the unit of the volume of the reactor, extinguishing/inhibition of the gaseous-phase reactions.

12 cl, 9 tbl, 27 dwg

Tower reactor // 2275236

FIELD: chemical or physical processes.

SUBSTANCE: tower reactor comprises reaction zones for simultaneous esterification and/or ester interchange and preliminary condensation. The top one third part of the tower reactor is made of hydrocyclone (2) with suspended heat exchanger (5) and has inlet (3) for paste, suspension and/or liquid raw mixture. The part of the tower reactor that underlies hydrocyclone (2) is made of cascade (7) with downflow. Cascade (7) is connected with the bottom part of the tower reactor through the pipeline. The bottom part is made of one-step or multi-step zone (9) with falling film with zone (8) of preliminary pressure drop.

EFFECT: enhanced efficiency.

25 cl, 7 dwg, 1 ex

FIELD: polymer production.

SUBSTANCE: process comprises feeding halogenating agent into continuous stream of elastomer solution, mixing the two components, which, after interaction, produce halogenated elastomer. The latter is neutralized by means of a neutralization medium and at least once washed with a washing medium. Neutralization and washing are carried out in reactor provided with static and dynamic means creating turbulent motion including inversion effect and consecutive withdrawal of excess of halogenating agent and settling separation of washing and neutralization media from halogenated elastomer. Process is carried out in installation comprising halogenation, washing, and neutralization reactors.

EFFECT: intensified all process stages, reduced equipment dimensions, and enabled continuous process resulting in production of homogeneous high-quality product.

19 cl, 5 dwg, 1 tbl, 8 ex

FIELD: chemical industry; conducting reactions with use of peroxide, such as hydrogen peroxide for reduction of chlorine contained in liquid effluent.

SUBSTANCE: proposed device has at least static mixer communicated with at least one feed pipe line for delivery of liquid medium to it, cyclone-type reactor connected with said static mixer and equipped with exhaust pipe for removal of formed gas and units for removal of liquid medium.

EFFECT: absolute safety; enhanced kinetics; enhanced efficiency; increased productivity.

26 cl, 1 dwg, 1 ex

The invention relates to the technology of organic synthesis

FIELD: chemistry.

SUBSTANCE: invention relates to the implementation of the chemical processes flowing in the gas-liquid medium, in particular to the construction of the gas-liquid reactor with ascendant unit-directional motion of the phases and can be applied to namely the industrial manufacturing of carbamid; the gas-liquid reactor contains the vertical housing with the reagents induct and reaction products educt junction pipes; at the bottom part of the housing there is a mixer including a coaxial tube and a cyclone chamber having a tangential induct junction pipe connected to a first reagent induct junction pipe and an axial educt junction pipe located sidewise the reactor floor; the coaxial tube is inserted into the cylindrical housing of the cyclone chamber; the upper end of the coaxial tube is connected to the second reagent induct junction pipe; the axial educt junction pipe of the mixer is furnished with the diffuser, the lower part of the reactor contains the shield located closely to the reactor floor opposite the educt junction pipe of the mixer; in the second variant the mixer includes at least two connected in series coaxial cyclone chambers having the tangential educt junction pipes connected to the reagents induct junction pipes and axial educt junction pipes located sidewise the reactor floor.

EFFECT: increase of the dispersion intensification of the interacting phases and evenness of the reagents allocation in the produced two-phases flow; the additional effect associated with the availability of the shield lies in the prevention of the reactor material tear and wear.

10 cl, 3 dwg

FIELD: chemical hardware.

SUBSTANCE: group of inventions refers to hardware of chemical processes running in the gas-liquid medium, namely to gas-liquid reactors with ascendant one-way flow of phases. It can be, particularly, used for industrial production of carbamide. Gas-liquid reactor consists of vertical body with reagent inlet and reaction product outlet nozzles and mixer situated in the lower part of the body. Mixer is connected to the inlet reagent nozzles and has axial outlet upward nozzle with diffuser. Both variants of reactor have cylinder shell concentric to its body comprising mixer. Its diameter is within (0.6-0.9)D where D is the internal diameter of the body. In the first variant the mixer includes annular tube an at least one swirlchamber with tangent inlet nozzle connected to the inlet nozzle of first reagent. Annular tube is inserted into the cylinder body of swirlchamber and connected to the inlet nozzle of second reagent. In the second variant the mixer includes at least two series-connected coaxial swirlchambers which have tangent inlet nozzle connected to the reagent inlet nozzles and axial upward outlet nozzles.

EFFECT: increase of interacting phases dispersion intensivty and homonenious distribution of reagents in the two-phase flow.

13 cl, 3 dwg

FIELD: chemistry.

SUBSTANCE: device 100 has a liquid reservoir 104, a feed pump 102, a coupling element 120 with two inlets and one outlet, a reactor unit and a pressure regulator, connected into a flow channel. The device 100 also has an ozone source 110 and a distribution valve 112 which allows passage of the gas stream in one direction only and is installed between the ozone source and one of the inlets of the coupling element 120. The feed pump 102 of the device 100 is a liquid pump which generates constant flow rate. The reservoir 104 contains at least one substance in form of a solution which must undergo ozonolysis. The reactor unit consists of a first and a second reactor zone. The outlet of the first reactor zone on the flow path is connected to the inlet of the second reactor zone. There is also a device for possible feed of additives into the flow channel between the reactor zones. The ozone source 110 generates ozone in situ via electrolysis. The common inner volume measured along the flow path from the feed pump 102 to the pressure regulator 160 is not greater than 50 cm3.

EFFECT: device is safe, cheap and provides high output of the reaction product.

24 cl, 2 tbl, 5 dwg, 2 ex

FIELD: process engineering.

SUBSTANCE: invention relates to heat and mass exchange processed in gas-fluid mixes and in systems prone to solid precipitate formation. Proposed device comprise casing, silicon organic fluid and ammonia feed branch pipes and reaction product discharge branch pipes. Said casing is made up of two chambers arranged one above the other. One chamber makes cylindrical settler while another one makes cylindrical collector interconnected by hollow tube. Inside said tube and collector, circulation tube is arranged secured to casing wall to receive ammonium gas. Settler top part wherein neutralised fluid is clarified accommodates separator tube to neutralised ammonium chloride fed into collector.

EFFECT: higher efficiency, yield and quality, and simplified design.

1 dwg

FIELD: chemistry.

SUBSTANCE: present invention relates to a carrier with a catalytic coating, production method thereof, use thereof in processes with heterogeneous catalysts, as well as a reactor containing the said catalyst layer. Described is a carrier with a catalytic coating, having at least one porous and cavity-containing catalyst layer, where the cavity consists of random voids with size greater than 5 mcm in at least two dimensions or with cross-sectional area of at least 10 mcm2. Described is a method of producing the said carrier, comprising a) preparing a carrier substrate, b) if needed, depositing an adhesion improving layer, c) spraying a suspension with at least 30% content of solid substance containing a catalytically active substance with average diameter of at least 5 mcm and/or precursor thereof and, if needed, an additional component of a catalytically active layer, and d) if needed, repeating step c) once or more. Described is a rector with a surface intended for coating, having at least one carrier with a catalytic coating described above. Described is use of the carrier in a method for catalytic oxidation of aliphatic compounds, in a method for oxidation of xylene and/or naphthalene to phthalic acid, in a method for oxidative coupling of acetic acid and ethane to form vinyl acetate using oxygen, in a method for catalytic hydrogenation of organic compounds and in a method for converting synthetic gas.

EFFECT: catalytic coatings are characterised by high adhesion strength of layers, having stability, negligible tolerance on layer thickness and mass-transfer resistance and can be universally used in multiple catalyst systems.

51 cl, 3 ex, 5 dwg

FIELD: chemistry.

SUBSTANCE: invention can be used in chemical industry to prepare a composition of polycarboxylic acids. A bubble column reactor 600 has an external reaction vessel and an internal structure 602 which lies at least partly inside the external reaction vessel. The reaction zone lies inside the external reaction vessel and outside the internal structure 602. The rest zone lies inside the internal structure 602. The rest zone includes at least one section lying from the reaction at a distance equal to approximately 0.2 m or a multiple of the maximum horizontal diametre of the external reaction vessel with a factor of 0.05.

EFFECT: invention simplifies gas-phase oxidation reactions.

40 cl, 4 tbl, 31 dwg

FIELD: process engineering.

SUBSTANCE: invention relates to continuous gas-fluid reactions in high-pressure tubular reactor. Proposed method comprises feeding, at least, one fluid reagent by gas reagent flow feeder 2, and, not obligatorily, by feeder 3. Note here that, at least, one initial flow is fed at supercritical pressure. It comprises also heating, at least, one said flow by heater 4 connected with feeder and combining said flows in jet mixer 5. Obtained gas-fluid mix reacts in direct-flow tubular reactor in, in fact, adiabatic conditions. Reaction mix flow is throttle via reducing device 7 into evaporating separator 8 at lower pressure with stripping gas flow comprising, mainly, low-boiling components from top part of evaporating separator 8, and liquid flow comprising, mainly, high-boiling components from bottom part of said evaporating separator 8. Note here that said flows are heated to temperature that allows interaction reaction in supercritical fluid. Aforesaid flows are combined in jet mixer 5 with gas-fluid mix rate of 10-350 m/s. Note here that time whereat combination occurs makes less than 1 second. Obtained gas-fluid mix interacts in direct-flow tubular reactor 6 that drastically reduces liner rate of said gas-fluid mix to 0.01-10 m/s. Note also that time whereat said interaction occurs makes less than 600 seconds.

EFFECT: higher reaction rate and target product yield.

25 cl, 3 ex, 1 dwg

FIELD: process engineering.

SUBSTANCE: invention relates to chemical industry. Proposed reactor comprises column reactor 1, bubble-type plate 2 to divide reactor column into top and bottom reaction chambers 3 and 4. Top reaction chamber comprises bottom two-phase section 5 and top gas-phase section 6. Detector of level 2 in two-phase section 5 incorporates emitter 11 and electromagnetic radiation detector 12 arranged outside column reactor 1. Signals detected by detector 12 are transmitted to control unit 13 that controls valve 14 arranged in fluid product discharge line 10.

EFFECT: possibility to measure fluid level in two-phase reactor.

10 cl, 1 dwg

FIELD: machine building.

SUBSTANCE: bubble reactor consists of column reactor with bubble plate dividing column reactor into upper reaction compartment and lower compartment. Also, washing medium is supplied into the lower compartment along a supplying pipeline and is withdrawn from it via a drain line correspondingly.

EFFECT: control over drop condensation on bubble plate in bubble column reactor.

6 cl, 1 dwg

FIELD: process engineering.

SUBSTANCE: invention can be used in production of polycondensation products in polymerisation reactor running on the principle of gravity feed and intended for polymerisation in polymer melt. Assembly 10 comprises first stationary line 24 made up of one or several support film structures 38, 40, 42, 44 and one or more stationary film generators 32, 34, 36 to separate and direct polymer melt onto support film structures. First part 74 of polymer melt is directed by gravity on the first side 76 of each support film structure, while second part 78 of polymer melt flows does on second side 80 of each support polymer structure. Proposed method of increasing polymer melt polymerisation comprises: a) introducing polymer melt into assembly 10, b) affecting produced polymer melt free surface by atmosphere, and c) removing polymer melt from assembly 10, polymer melt removed having higher degree of polymerisation compared with that of the melt introduced into assembly 10.

EFFECT: higher degree of polymerisation.

29 cl, 20 dwg

FIELD: process engineering.

SUBSTANCE: heat exchanger relates to desorption of gases from fluids with the help and other inert gas and abruption of definite gases by fluid from gas flow in mutual contact. Proposed heat exchange comprises horizontal casing 1 with bottoms 1a and 1b, fluid feed and discharge branch pipes 2 and 3, respectively. Gas distribution manifold 6 is arranged coaxially inside said casing and provided with branch pipe 7 to feed desorbing or absorbing gas provided with bubbling orifices 8 and inclined baffles 0 arranged above said orifices. Casing bottom 1b has fluid discharge hole 1c arranged on the side of fluid feed branch pipe to define minimum fluid working level. Hydraulic gate 4 is arranged behind said branch pipe and has adjusted height sill 4b to adjust fluid level in aforesaid case while branch pipe 3 to discharge processed fluid us connected to hydraulic gate. Flute 10 to collect and discharge fluid is arranged above aforesaid gas distribution manifold 6.

EFFECT: higher quality of desorption, simplified design, reduced metal consumption.

4 cl, 5 dwg

Up!