Method of removal of acid gas and device for realization of this method

FIELD: simultaneous absorption of selected components of acid gas and topping light fractions of hydrocarbons entrapped by liquid flow.

SUBSTANCE: proposed method includes delivery of gas flow and liquid flow to first mixer where they are brought in contact in direct flow and are subjected to turbulent mixing; then multi-phase flow from first mixer is directed to second mixer and after second mixer multi-phase flow is divided into gas phase and liquid phase. Second mixer has housing 102 with inlet hole 122 and outlet hole 123. Housing is provided with at least one movable control member 104 mounted hermetically; control member has central chamber for forming part of first wall connected with inlet side of housing and part of second wall connected with outlet side of housing. These parts of walls are provided with through passages 106A and 107B.

EFFECT: enhanced topping of entrapped hydrocarbons; increased absorption capacity by acid gas.

15 cl, 9 dwg, 1 tbl

 

The present invention relates to a method for simultaneous removal of acid gas components and hydrocarbons from the gas stream. In particular, the invention relates to the selective removal of H2S in excess of the CO2using Amin.

Traditionally, the components of the acid gas is removed using large absorption columns. These columns are made with the possibility of processing gas supplied at a specific flow rate and the acid gas content. However, changes in conditions of supply cause problems in the work, and the absorber must be significantly modified to achieve a satisfactory or optimal performance. Problems that require modification include, but are not limited to: increasing the volumetric flow rate of sour gas; requiring a lower concentration of acid gas in the treated gas; a lower circulation rate of the solvent to the same values purification; increasing the concentration of acid gas in the feed gas; any combination of the above. These problems with existing installations that no longer meet changing operational requirements are reduced to narrow, and their solution is to eliminate the narrowing of the installation.

Modification of existing absorption column and associated devices are expensive and on the up a lot of time, while many of the above requirements may change on a regular basis. One of the common solutions used to solve the problem of increasing performance for the removal of acid gas, is the replacement of the used solvent. However, it is not always appropriate and may enter secondary problems, such as regeneration and corrosion problems. Another solution is to replace the internal parts of the column, for example plates, disordered or structured packing. This solution has limited ability to increase the removal of acid gas only in connection with the overall size of the column.

The present invention is to provide a method for increasing the absorption capacity of the existing installation on sour gas and thereby eliminate the narrowing of the installations.

A further problem with the installations, which is related to their narrowing, is that the hydrocarbons and the carbon dioxide can be carried out and/or absorbed in the solvent acid gas (for example, Amina) and subsequently served in located downstream of the treatment units, such as block Claus for sulfur recovery. Such additional components in the feed block Claus reduce the effectiveness of the installation of desulphurization and can create additional narrowing on the more down the process. There are also additional load on the installation, including the pumping of this excess gas around the installation for regeneration of the solvent acid gas and installation for desulphurization. This may overload the existing pumps and needs to add more or replace pumps.

Thus there is a need in the way in which reduced or eliminated labarbe carbon dioxide and/or ablation of the hydrocarbons. The present invention provides such a method.

In accordance with the present invention, a method is proposed for simultaneous absorption of the selected acid gas components from a gas stream and distillate light fractions of hydrocarbons carried out in the liquid stream comprising solvent or reagent for the selected component gas in which the gas stream and the liquid stream fed to the first mixer, where they come into contact in parallel and subjected to turbulent mixing conditions; then the multiphase flow from the first mixer is passed to the second mixer, comprising a housing made with the possibility of its placement in the pipe for passing a flow of fluid passing through it, and the specified body contains the input and outlet openings respectively, a housing provided with at least one internal moving hermetically mounted regularuse the element, partially enclosing a Central chamber for the creation of the first wall connected with the side entrance of the specified body, and part of the second wall connected with the outlet side of the specified body, and these side walls provided near the through ducts, each of which has a substantially smaller cross sectional area than the cross-section flow inlet and outlet openings, respectively, and in which the braking element is made movable relative to the specified frame; and multiphase flow from the second mixer is separated into a gas phase and a liquid phase after the second mixer.

When using the method according to the present invention significantly reduce the amount of entrainment of hydrocarbon in the fluid flow can be obtained without loss of performance for absorption of acid gas. Therefore, it is possible to use half-saturated fluid flows that have gone hydrocarbons, for purification of gas streams by absorption of acid gas components. The method is also effective at removing hydrocarbons, thereby minimizing problems further downstream, where the hydrocarbons can block the installation of or create additional bottleneck.

On selection of the first mixer is a turbulent mixer with the under the tapering pipe, through which passes the gas stream, the inlet fluid located so as to form the annular space of the liquid around the inner perimeter of the tube, the sharp edge on the end of the tapered pipe and an additional section of pipe downstream after sharp edges.

Alternative first mixer may include a vessel, including the inlet to the gas inlet for fluid and an exit, and the exit leads to the passage of the Venturi tube, and a pipe extending from the outlet back up the stream, and the pipe is perforated and/or separated by a gap from the periphery of the output.

Alternative first mixer is the same as the second mixer.

Preferably, H2S was selectively absorbed better than CO2from the gas flow. More preferably, the value of H2S in the gas stream leaving the second mixer was less than 1.5 vol.%, even more preferably less than 1%vol.

Preferably the fluid flow is a stream of amine, including gone with the hydrocarbons. The choice of fluid flow (including gone with the hydrocarbon) is supplied directly to the first mixer of the Assembly of the successive elements for desulphurization of liquefied petroleum gas (LPG). Preferably the amine is chosen from the IEA, deja, DEEP, MDEA.

Preferably idku the phase is cleaned to remove any component of the absorbed gas. This cleaning can be performed by any suitable known means. The purified amine, in which now there are no sour gas components, can be recycled to the gas purification system. The mixture of sour gas from the purified amine can take place in any suitable cleaning device downstream, such as installation Claus for conversion of N2's acceptable in terms of environmental products.

Preferably, at least 70%, more preferably 80% and even more preferably 90% of the hydrocarbons in the feed liquid was distilled as light fractions in the gas stream in the mixer unit.

The present invention also relates to a device for use in the method according to the present invention. In particular, according to the present invention, a device for the simultaneous absorption of the selected acid gas components from a gas stream and distillate light fractions of hydrocarbons carried out in the liquid stream comprising solvent or reagent for the selected component gas containing the first flow mixer, in which the gas stream and the liquid stream is subjected to turbulent mixing conditions; a second flow mixer, comprising a housing made with the possibility of its placement in the pipe for the passage of the fluid flow passing through the third through it, moreover, the specified body contains the input and output apertures, respectively, the casing is provided with at least one internal moving hermetically completed the regulatory element partially enclosing a Central chamber for the creation of the first wall connected with the side of the casing inlet, and part of the second wall connected with the outlet side of the casing, and the said parts of the walls are a number of through-ducts, each of which has a substantially smaller cross sectional area than the cross-section flow inlet and outlet openings, respectively, and in which the braking element is made movable relative to the housing; and means for separating multiphase flow from the second gas mixer phase and the liquid phase.

On selection of the first mixer is a turbulent mixer, has a section tapering pipe, through which the gas flow, the inlet fluid located so as to form the annular space of the liquid around the inner perimeter of the tube, the sharp edge on the end of the tapered pipe and an additional section of pipe downstream after sharp edges.

Alternative first mixer includes a vessel comprising a gas inlet, the inlet fluid and the exit, and the exit leads to the passage of the Venturi tube, and a pipe extending from the outlet overtower flow, the pipe is perforated and/or separated by a gap from the periphery of the outlet, or the first mixer is the same as the second mixer.

The invention may be carried into practice in various ways and some specific structural embodiment of the invention, described by way of example, to illustrate the invention with reference to the accompanying drawings, which depict:

Figure 1 - configuration process for any existing installation for removal of acid gas having a constriction;

Figure 2 - configuration of the process according to the present invention, using integration solvent;

Figa - stirrer used as the second mixer and optionally used as the first mixer in the method according to the present invention, and this view is an axial longitudinal section perpendicular to the common axis of rotation of the agitator;

Fig.3b - stirrer on figa in axial longitudinal section, but with the axis coinciding with the axis of rotation;

Figs - transverse section of the mixer on figa made through the common axis of rotation;

Figa - is a type of turbulent mixer, suitable for use as the first mixer in the method according to the present invention;

Fig.4b - is a schematic representation of the gap zhidkosti the second film on the droplet 10 a turbulent mixer on figa;

Figs - is a view of a second structural embodiment of turbulent mixer such as mixer on figa, suitable for use in the method according to the present invention;

Fig.4d - is an enlarged view of part of the entrance of fluid flow in the mixer shown in figs, encircled by a circle A;

Figa - is a view of another mixer, suitable for use as the first mixer in the method according to the present invention;

Fig.5b is a variant of the mixer shown in figa;

Figs - is a type of mixer similar to that shown in figa, but with a perforated pipe located so that all fluid which passes through the exit, made it through pipes;

Fig.5d is a variant of the mixer shown in figs;

6 is a device used to measure the simultaneous performance of the mixer unit when you remove CIS from supplied amine, and selective absorption of H2S supplied from the exhaust gas;

7 - the results of the calibration device for measuring the CIS;

Fig - hydrocarbon content in the amine stream before and after treatment in the mixer unit; and

Fig.9 - the content of H2S and CO2in the exhaust gas supplied time, after it was filed Vblock mixer.

Figure 1 shows an example of installation for removal of acid gas, which is made with narrowing. In a conventional countercurrent absorption column 1 is depleted amine solvent through the thread 3 and the feed gas stream 5. The purified gas is removed via stream 7 and, as is well known, may be subjected to further cleaning. Used amine is removed via stream 9 and serves to block 11 amine regeneration.

Depleted solvent Amin also served in the cleaning unit liquefied petroleum gas (LPG), indicated by the rectangle 20 in figure 1. Amin served through the thread 21 in a counter-current column 22, which also serves gas CIS via stream 23. The purified gas is fed into the mixer 24 via stream 25 where it is mixed with additional depleted amine supplied via stream 26, before it passes into the sump 27, where a two-phase mixture has a chance to settle. Part remote amine used can be fed back into the column 22 via stream 28, but most of it takes place in block 11 of the amine regeneration via stream 29. Used amine from the column 22 also passes directly to the block 11 regeneration via stream 30. The gas flow from the tank then passes into the coagulator 31 through stream 32. The cleaned gas is then taken through the stream 33 and may be subject to further purified or used directly if it matches. The liquid stream 34 from the coagulator 31 partially recirculates in the coagulator via stream 35 and partially sent to the block 11 regeneration via stream 36. You can see that a significant amount of amine is used once and subsequently goes directly to the regeneration unit. This creates a heavy load of liquid on the installation, which is controlled by pumps and valves (not shown).

Figure 2 shows a similar working setup, in which the unit in accordance with the present invention is added before the traditional countercurrent column 1 to clear the intake gas. Instead of threads 29, 30 and 36, passes directly to the block 11 amine regeneration, they served to additional unit 50 of the mixer through the stream 51. Some of them will still take place directly in the block 11 regeneration through the stream 52. In block 50 of the mixer also serves a portion of the used amine from the mixer 1 through the thread 53. This half-exhausted Amin from four sources served in the block 50 of the mixer, where it comes in contact with a co-current with the supplied gas 5. The block contains two mixers, the second of which is a built-in mixer, such as shown in figa, 3b and 3c. The first mixer may be any suitable mixer, and the choice may depend on variables such as available space, the flow of liquid supplies the d of gas, etc.

After the second mixer roughly two-phase mixture is separated, and the rich amine takes place in block 11 regeneration via stream 54, and the cleaned gas passes into the existing column 1 through the stream 5a. Separation in block 50 of the mixer is such that less than 1% of the liquid is entrained with the separated gas, and a small amount of gas is entrained with the separated liquid.

The cleaning unit 50 of the mixer increases the saturation Amin before his passing in block 11 of regeneration, and reduces the content of acid gas in the feed gas prior to its passage in countercurrent column 1, where it is cleared depleted amine. A new filing in the traditional column 1 can now be acid gas content, for example, only 1% compared with 2.5% in a typical flow of sour gas. This means that depleted amine is used to reduce the content of acid gas from a lower initial concentration and therefore it focuses on much more difficult to remove it. Increased saturation Amin before he goes in block 11 of regeneration means that uses a high performance amine, and therefore the costs in block 11 of regeneration is reduced, and the supply of fresh solvent in the installation as a whole is significantly reduced, for example, by 30-50%.

Submission amine of the cleaning unit of the CIS includes part unsinnig him hydrocarbons. When passing in blocks downstream, while the sour gas was separated from the amine, these hydrocarbons can significantly reduce the effectiveness of the blocks, for example, by disabling the catalyst, blocking reactors. In addition, they increase the load on the system in downstream units, such as the installation of desulphurization Claus. The block 50 of the mixer, therefore, also has the function of light distillate fractions of most or all gone hydrocarbons from the stream of liquid amine in the gas stream. This gas flow can then take place in a conventional countercurrent column, where the hydrocarbons will be held with the purified gas to the gas exit 7. Therefore, when the thread used amine takes place in block 11 of regeneration, it has a little carried away hydrocarbon, passing to the blocks downstream, or it is missing. Mixer unit preferably reduces the content of hydrocarbon in the stream of amine to at least 80%, more preferably at least 90% and most preferably at least 95%.

Because the block 20 cleaning the CIS operates at a higher pressure than the column 1 absorption of acid gas and the block 50 of the mixer will not require additional discharge, and the flow of amine from the block 20 in the advanced block 50 of the mixer can be adjusted by use of the valves is stantsionnogo control (not shown).

As indicated above, the block 50 of the mixer to eliminate bottlenecks in the current process or to selectively remove one or more acid gas components from a gas stream and simultaneous distillation of light fractions of hydrocarbons consists of two mixers or agitators, the second of which is shown in figa-3c. The first mixer or the mixer may be any of those shown in figure 3, 4 and 5 including a second mixer of the type shown in figure 3), although any other suitable turbulent mixers can also be used. If you want an increased gas flow, can be used one or more mixers or sequentially or in parallel with the existing column. The small size of the mixer means that they can be installed on existing sites, where there is no place for more traditional columns.

On figa depicted built-in mixer, in which case 102 stirrer placed in the pipe 101A, 101B by means of flange connections 103A, 103B. The direction of flow of fluid through a pipe indicated by the arrows F1 and F2. This mixer can be easily installed in an existing pipeline without the need for significant additional room that would be required for more traditional columns. The housing 102 has an inner wall 121, to ora depicted essentially, cylindrical, which is interrupted inlet 122 and the outlet 123. The housing includes two regulating element 104 and 105, which are coaxial and have the form (cylindrical), similar to the shape of the hull. These elements 104 and 105 can individually be rotated in the housing 102, and each includes channels 106A, 106B and 107A, 107B in their respective walls. The channels preferably have a substantially greater length than the transverse dimensions. Common axis AH of the housing 102 and regulatory elements 104 and 105 is depicted as oriented at 90° to the General flow direction, although not significantly. Generally common axis is located mainly across the direction of flow.

On the entrance side of the input channels 106A and 106B are converging orientation so that they are directed in General to the Central plot in the housing 102. This represents the ideal case. On the output side facing channels 107A and 107B substantially parallel to the respective direction to the direction of through-flow. When turning the regulating elements 104 and 105 from the position shown in the figures, the ducts through the mixer will change. As shown, the channels, coming both upstream and downstream, are aligned with each other and centered on the holes 122 and 123 so that the fluid passage is La through them with little resistance. This is a stirrer in the fully open position, where the channels form a continuous flow path without edges. Rotation of one or both of the regulatory elements can change the size and the number of channels and thereby affects the speed of the fluid, and hence the confusion. This will also result in a greater pressure drop due to higher resistance to flow.

Ducts (for example, channels 107A) can have a circular cross-section, as shown in figs, or may have an alternate configuration, such as, for example, narrow or slit-like device. Channels can also be designed so that they are more conical than cylindrical shape that can create the effect of nozzle type towards the center of the housing 102. The channels shown on figs have the correct location across the entire area of the holes 122 and 123. However, in some cases it may be preferable to a deviation from the normal distribution, in particular on the entrance side into the mixer. To increase the bandwidth of the channels, that is, to reduce the resistance to flow through the mixer housing 102 can be performed with an expanding cross-section of the flow towards one or both holes 122 and 123 with the corresponding increase in the surface of the walls of perforirovannoi the plots.

On fig.3b and 3C shows the regulatory elements 104 and 105, with coaxial spindles 114 and 115, respectively, to control the relative displacement of the elements relative to each other and the housing. Regulation of the relative provisions of the regulatory elements to control the flow through the mixer. In one extreme position, the passage through the duct is completely closed.

In addition to the channels mentioned above, regulatory elements 104 and 105 have openings 104A, 104B and 105A, and 105B, respectively, the diameter of which corresponds to the diameter of the pipe and holes 122 and 123. These holes have an axis in the main at an angle of 90° to the Central axis of the respective parts of the walls with channels. These openings 104A, 104B, 105A and 105B may be located in line with the holes 122 and 123 to create, essentially, a free and straight pipe section. Item 112 core type tube may be made so as to tightly engage with the inner side of the regulating element 104 at the outer wall 112A parts of the core. Through the detail of the core 112 passes the hole 112B, which preferably is in line with the inlet 122 and the outlet 123, and provides the same cross-section of the stream.

The location of the channels, which converge toward the Central point of the shell 02, creates a good mix for a wide range of stream structures. Any fluid components, which are located at the bottom of the flow in the pipe 101A, rise of the inclined channels in the center of the housing 102. Similarly, any gases, which are located in the upper part of the tube in the input section, are displaced in a downward direction to the Central plot. Phase therefore effectively mixed in the center of the housing 102 and then fed evenly through the parallel extending channels 107A and 107B. Therefore, there is a completely homogeneous mixture of phases in the cross-section of the pipe 101B.

On figa depicts the first constructive execution of the mixer, which may be the first of a series of agitators in block 50 of the mixer. The mixer 201 includes an input 202 of the gas stream, the input 203 of the fluid flow and the outlet 204. The gas stream is fed to the input gas flow, which leads to a convergent section 205 of the tube. Converging section 205 of the tube accelerates the gas stream when it passes through the input 203 of the fluid flow at the end of section 205 of the pipe, which has a sharp edge 206. Downstream after the sharp edges 206 area 207 of the reaction, where the gas and liquid preferably form a homogeneous mixture.

Fluid is supplied to the input 203 of the liquid, where she served adjustable manner in the inner part of the converging section 205 of the tube. The liquid present in the pipe in the form of calcev the space around the inner surface of the pipe. In the initial phase, the speed of the liquid facing the gas flow is controlled by the fluid flow, the size of the gap 208 and the size of the annular space 209. The size of the gap 208 may be changed by the movement of the blocks 210. The gap will vary depending on the liquid solvent, the properties of which vary greatly. The diameter 209 annular space fluid can be changed by changing the angle of the converging pipe or by moving the position of the annular space fluid relative to the converging end of the pipe.

The annular space fluid present on the inner surface of the pipe, stretched along the inner surface of the pipe in the form of a film 211 by the gas flow. This is best shown in fig.4b. Film 211 fluid closely sticks to the side of section 205 of the pipe until then, until it reaches the sharp edges 206. At this point, the liquid film is broken for the formation of fibers 212. The formation of fibers and their subsequent velocity vector are determined by the relative velocity between the gas and liquid phases, surface tension between gas and liquid and a sharp edge 206. In connection with conditions of extreme turbulence in the reaction zone 207 fiber 212 is further broken down into very small droplets 213, which provide a very high ratio of surface area to volume, p is the tool that making extremely efficient use of the supplied fluid. If it fits, it creates the opportunity to use much smaller volumes of fluid than is required for conventional processes of the prior art, at the same time, even through such absorption of acid gas. The formation of droplets in the reaction zone favors high Weber number (We) and, therefore, a high gas flow.

Small liquid droplets and the gas stream is intimately mixed in the zone 207 reactions and multiphase flow passes through a conical diffuser 215 (see figa), where part of the pressure that falls during acceleration of the gas flow in the converging section 205 of the pipe is restored. Multiphase flow then passes to the second mixer (as shown in figa, 3b and 3c) without separation into separate phases.

On figs depicts a second constructive performance mixer, suitable for use in the method according to the present invention as the first mixer unit 50 of the mixer. The mixer 220 contains the input 222 of the gas flow, the inlet 223 of fluid flow and exit 224. The gas stream is fed to the input of the gas flow, which leads to a convergent section 225 of the tube to accelerate the flow of gas. At the end of the converging section of the tube has a sharp edge 226, after which the downstream area 227 of the reaction, where the gas and liquid preferably form a homogeneous mixture. One difference between the mixer on figa and see what Cetelem on figs is the placement of the intake of the fluid relative to the annular space fluid. In this case, the liquid is supplied to the input 223, where it passes through the passages 223a and 223b to the tank 223c, which runs around the perimeter of the pipe. The liquid then exits through the channel 223d, which again goes around the entire perimeter of the pipe (see fig.4d) to the annular space at the inner surface of the converging section of the pipe. Because of the conditions of shear stresses and dynamic pressure transmitted by the gas to the liquid, the liquid flow still sticks to the surface of the pipe, we have not reached the sharp edge 226.

Another difference between the two mixers is the slope of the converging pipe sections 205, 225. In the mixer 220 converging section 225 of the pipe has a much steeper slope than the slope in the mixer 201, and therefore achieves a smaller cross-sectional area for the same length of pipe. The ratio of diameters between the filler neck and pipe, as well as the converging angle of the cone can be changed independently. This reduced cross-sectional area will result in greater acceleration of the gas stream when it reaches the sharp edges, but also will lead, therefore, to a greater pressure drop. Also on the choice of the angle of the converging pipe will be affected by a constant differential pressure, which can be distributed throughout the device. As indicated earlier, the gap of the liquid on the fiber and subsequently the tvii on the droplets is governed by the Weber number. It is affected by the square of relative velocity between the gas and liquid phases. Therefore, a small change in velocity of the gas stream, partially adjustable acceleration created by the angle of the converging section of the pipe, can have a significant impact on the gap of the liquid and, consequently, the efficiency of the installation.

On fig.4d depicts an enlarged cross section of a square within the circle And figs. It depicts in more detail the passage of liquid through the inlet 223 of the fluid flow. The fluid passes through the passages 223a and 223b to the camera 223c, which runs around the perimeter of the pipe. The liquid is then fed through a narrow passage 223d to the inner surface of the cone section 225 of the tube. Pass 223d shows a very narrow and may have a width of the order of only 0.2 mm. pressure Drop in the passage carefully monitored and regulated to ensure a continuous flow of fluid with homogeneous distribution around the entire perimeter of the pipe in the convergent section 225 of the tube. As indicated above, the size of the passage 223d is regulated by the movement of blocks 230 and 231. The dotted line 225a shows an alternative slope of the converging section 225 of the pipe, which gives a higher velocity of the gas phase and, therefore, improved mixing, but increases a constant differential pressure in the device. This change can be made simply by replacing one of the parts of the device to another.

After the gas and liquid were intimately mixed in the reaction zone 227 immediately downstream after sharp edges 226, may be a divergent section 228 to restore parts of the differential pressure. The length of section 228 can be changed to regulate the degree of pressure recovery. After diverging section 228 selectively has a straight pipe of considerable length to maintain the formed flow patterns and to create an area for further reactions (see figs). The length of the straight pipe is recommended to be 15 to 20 standard pipe diameters.

Typical sizes of mixers can be in the range 51-1016 mm (2-40 inch) in diameter. In particular, a device for removing impurities from natural gas may have a diameter pipes 216 (see figa)equal to 610 mm (24 inches)in diameter, with sharp edges 217, equal to 253 mm (10 inches). The initial diameter 218 diverging pipe can be 370 mm (14.5 in). As indicated above, the diameter of the sharp edges can be changed together with the slope of the converging pipe, and other diameters sharp edges, which can be used include 296 mm (11.7 in), similar to the one shown figs, and 272 mm (about 10.7 inches).

An example of another mixer that can be used as the first in a series of agitators in block 50 of the mixer depicted in figa. Turbulent mixer 300 includes a vessel 301 having a first input 302 of the fluid, the second the d input 303 of the fluid and the output 304, leading to the passage 305 of the Venturi. There is a pipe 306 (which can be made of perforated or unperforated), passing from the exit 304 back into the vessel 301. The tube 306 may be connected directly to the input 303 of the fluid.

In the first device, the mixture gas is fed into the vessel 301, and the liquid is fed into the pipe 306 to select directly, whereby gas is drawn into the Venturi by the liquid, and the two phases are mixed.

In the second device, the liquid is fed into the vessel 301, and the mixture gas is fed into the tube 306 to select directly, whereby the liquid is drawn into the Venturi gas, and the two phases are mixed.

In the third device, the liquid and gas mixture is fed into the vessel 301, and the liquid serves on the level above the level of the output 304, whereby the gas is expelled through the exit 304 through the pipe 306, thereby bringing the liquid into the Venturi so that the two phases are mixed.

The fourth option shown on fig.5b. This constructive design like the one shown on fega, but the mixer 310 is converted. It includes the vessel 311 to the input 312 of the fluid inlet 313 and gas outlet 314, leading to the passage 315 Venturi. There is a pipe 316 (which may be made of perforated or unperforated), passing from the exit 314 back to the vessel 311. Tube 316 may be connected directly to the input 31 of the gas. In this constructive fulfillment of the liquid is expelled into the tube 316, and the gas drawn into the passage 315 Venturi through the liquid, and the two phases are mixed. When the pipe 316 perforated, gas can be drawn into the pipe 316 through the perforations.

An additional example of the mixer, which can be used as the first mixer in the method according to the present invention, depicted in figs. Turbulent mixer 320 contains the vessel 321 having a first input 322 of the fluid, the second input 323 of the fluid and the output 324 leading to the passage 325 Venturi. There is a perforated pipe 326 extends from the output 324 back into the vessel 321. Perforated pipe 326 is located so that it does not have a gap at the output 324 of the vessel 321 for the passage of fluid through it. The result of this device is that all fluid out of the vessel 321 through the perforated pipe 326. Tube 326 may be connected directly to the input 323 a fluid medium.

In the first device, the mixture gas is fed into the vessel 321, and the liquid is fed into the pipe 326 choice directly, whereby gas is drawn into the Venturi by the liquid, and the two phases are mixed.

In the second device, the liquid is fed into the vessel 321, and the mixture gas is fed into the tube 326 choice directly, whereby the liquid is drawn into the Venturi gas and two phase) is raised.

In the third device, the liquid and gas mixture is fed into the vessel 321, and the liquid serves on the level above the level of the output 324, whereby the gas is expelled through the exit 324 through the pipe 326, thereby bringing the liquid into the Venturi so that the two phases are mixed.

The fourth option shown on fig.5d. This constructive design like the one shown on figs, but the mixer 330 is converted. It contains the vessel 331 to the input 332 fluid inlet 333 gas and exit 334, leading to the passage 335 Venturi. There is a perforated pipe 336 passing from the exit 334 back to the receptacle 331. As in the design implementation, shown in figs, perforated pipe 336 is located so that it does not have a gap at the exit 334 vessel 331 for the passage of the mixture of gases through it. All fluids must pass through the perforated tube 336 to the passage 335 Venturi.

In this constructive fulfillment of the liquid is expelled into the tube 336, and the gas drawn into the passage 335 Venturi through the liquid, and the two phases are mixed. Because the pipe 336 perforated, gas can be drawn into the pipe 336 through the perforations.

As indicated above, it is difficult to modernize many of filing in existing columns, and in many cases there is not enough space to accommodate additional columns. By imposing unit 50 through conduit mixture is an indicator of the possible pre-cleaned is fed into the absorber gas using half depleted amine from a variety of sources. Therefore, the flow of the injected gas (e.g., natural gas) pre-cleared in block 50 flow mixer integrated flow Amin. This means that the gas included in the existing counterflow column 1, has a significantly reduced content of acid gas, which is then cleared depleted amine. Excessive saturation of the amine by means of the recirculation means that the number of the desired depleted amine is reduced up to 50% and, consequently, reduces the circulation of liquid in the installation.

As mentioned above, the mixers of the present invention have a significant advantage in selective removal of H2S from the gas stream and simultaneous instantaneous evaporation is carried out of the liquid hydrocarbons from the solvent. This is particularly useful in situations, where N2S is removed from liquefied petroleum gas (LPG), for example, in the extractors. When using traditional columns hydrocarbons are carried away with the liquid solvent, thereby reducing the efficiency of amines, and the degree of absorption of H2S is reduced accordingly. Also CIS, instantly evaporated into the regenerator, is the capacity of the processing equipment downstream, such as installation Claus (blocks processing of sulfur). By using the method according to the present invention and submitting it together with the solvent from the extractor is, that is, introducing an additional flow faucets in front of the existing columns, a large percentage of N2S can be removed before the traditional column and gone hydrocarbons substantially removed. The effectiveness of traditional columns therefore increases, and the amine circulation rate in the column is reduced, thereby reducing the load on the whole installation.

The amine molecules used in these installations are found, both polar and nonpolar parts, so the molecules will penetrate in phase liquid hydrocarbons and aqueous phase. For the mixture of the hydrocarbon-amines prediction characteristics instantaneous evaporation of the CIS is not possible without experimental data obtained with the participation of fluid.

The components of the liquid C3+ Amina from the CIS unit with sequential elements are not in balance with the components C3+ in the gas supplied to clean. The main components of the gas are C1, C2, and H2and the feed gas is initially low content of components C3+.

Because the block 50 of the mixer of the present invention is characterized by a very high area of the boundary surface of the gas-liquid (per unit length) and corresponding high rates of mass transfer, it is assumed that the multi-phase installation should be close to equal is the dynamic equilibrium much faster than matching vessel for flash evaporation. One reason for this is the high driving force transmitted liquefied CIS exposed to the gas phase. Another reason is that the volume of liquefied CIS exposed to the gas phase through the continuous redistribution of liquefied CIS dispersed in Amina. Impact and redistribution are amplified due to the high velocity of the ablation fluid and deposition associated with the flow of the gas-droplets and mixing gas-liquid in block 50 of the mixer. The result of the quantity of liquid hydrocarbons is significantly reduced towards the end of the block 50 of the mixer.

It is assumed that the vessel for flash evaporation include the following assumptions:

(i) light hydrocarbons (C1, C2) and hydrogen are absorbed or taken away as a gas and will be easily separated from the amine in the vessel for flash evaporation due to the shift of equilibrium (e.g., pressure) and the favorable conditions for gravity separation of gas bubbles in liquid;

(ii) a liquid C3+ should be subjected to the atmosphere at a sufficiently low partial pressure of C3+ to evaporation. This process is slow, and the mass transfer depends on the area of the boundary surface of the gas-liquid and residence time. So abrazandolos, the rate of evaporation C3+ in the vessel is low.

In the end, the mass flow of C3+ with the amine is a function of the initial stream of C3+ with amine (before interaction with the contacting gas); the area of the boundary surface of the gas-liquid residence time in the mixer unit; and the concentration of gaseous C3+ in a mixture of gases.

Mixer unit according to the present invention contributes to a significant decrease in the flow of C3+ in the vessel for flash evaporation. The integration flow amine reduces the circulation rate and, consequently, increases the residence time in the vessel for flash evaporation.

Figure 6 depicts the device used to test the simultaneous operation of the mixer unit of the present invention to remove CIS from filing amine by flash evaporation in a continuing process of interaction between the gas and the liquid and selective removal of H2S from the exhaust gas refinery using half depleted amine of the extractor CIS. CIS is fed through the flow 420 in the extractor 421 CIS together with depleted amine through the stream 422. The product from the top of the pass in an additional mixer 423, which adds additional depleted Amin. Multiphase fluid passes into the sump 424, where half depleted amine can be fed back to extra the tor 421 CIS. Gaseous product passes from the tank into the coagulator 425 from which to extract a greater amount of half-depleted amine. A significant part of this half-depleted amine acts as a feeding unit 430 of the mixer through the stream 426. In block 430 mixer half depleted amine reacts with the exhaust gas refinery stream 427), producing a purified gas flows 428 and saturated amine, which will take place in block 429 regeneration.

To measure the amount of CIS, remote from the stream amine fed to the mixer should be determined by the initial content of the CIS amine stream. Fluid samples approximately 0.5 DM3so take away from the flow of amine in the expanding piston cylinder in the process. CIS evaporates from the sample Amin in pre vakuumirovaniya receiver gas through the repeated execution of the following sequence: vacuuming, shaking and deposition of selected liquids up until gas no longer instantly evaporate. Volume instantly evaporated gas collected in the receiver for the samples measured, and the composition of the mixture gas mixture determined using gas chromatography.

This method of analysis was evaluated by sampling a known volume of pure restored amine and mixtures vos is adjusted amine and CIS. The method was further evaluated by repeating tests. As can be seen from the results shown in Fig.7, the uncertainty in the analysis of liquids is of the order ±10%, which is considered acceptable. The results of some of the tests are shown in table 1 below.

Table 1
Concentrations of sour gas (vol %)Remote sour gas (%)Hydrocarbons that are removed from the amine (%)
H2S inputH2's outputCO2inputCO2outputH2SCO2
2,780,581,551,4679681
2,720,611,611,4978790

As can be seen from the above results, approximately 90% of hydrocarbons, gone with the amine, and 78% H2S sour gas can be removed simultaneously in the mixer unit according to the present invention. In addition, the joint absorption of CO2is only 7%. Data for the second set of results is in table 1 are shown in the graphs on Fig and 9.

The present invention therefore provides an effective solution to the problem of hydrocarbons is carried out in the liquid supplied Amina, and also provides an efficient way of selective absorption of H2S from a gas stream is preferable to CO2at the same time producing a light distillate fractions greater part, if not all gone hydrocarbons in the stream of recirculating integrated Amin.

1. Method for the simultaneous absorption of the selected acid gas components from a gas stream and distillate light fractions of hydrocarbons carried out in the liquid stream comprising solvent or reagent for the selected component gas in which the gas stream and the liquid stream fed to the first mixer, where they come into contact in parallel and subjected to turbulent mixing conditions, the multiphase flow from the first mixer is passed to the second mixer, comprising a housing made with the possibility of its placement in the pipe for the passage of the fluid flow through it, and the specified body contains the input and output apertures, respectively, the case is equipped, at least one internal moving hermetically established by the regulating element partially enclosing a Central chamber for the creation of the first wall connected with the side of the casing inlet, and part of the second wall, the connection is Noah and outlet side of the housing, moreover, these side walls provided near the through ducts, each of which has a substantially smaller cross sectional area than the cross-section of the duct inlet and outlet openings, respectively, and in which the braking element is made movable relative to the housing, and the multiphase flow from the second mixer is separated into a gas phase and a liquid phase after the second mixer.

2. The method according to claim 1, wherein using the first mixer, which represents the turbulent mixer, has a section tapering pipe, through which the gas flow, the inlet fluid located so as to form the annular space of the liquid around the inner perimeter of the tube, the sharp edge on the end of the tapered pipe and an additional section of pipe downstream after sharp edges.

3. The method according to claim 1, wherein using the first mixer containing vessel comprising a gas inlet, the inlet fluid and the exit, and the exit leads to the passage of the Venturi tube, and a pipe extending from the outlet back up the stream, and the pipe is perforated and/or separated by a gap from the periphery of the output.

4. The method according to claim 1, wherein using the first mixer, which is the same as the second mixer.

5. The method according to any of the preceding paragraphs, in which H2S is selectively absorbed Ave is doctitle, than CO2.

6. The method according to claim 5, in which the value of H2S in the stream leaving gas is less than 1.5 vol.%, preferably less than 1%vol.

7. The method according to claim 1, in which the fluid flow is a stream of amine, including gone with the hydrocarbons.

8. The method according to claim 7, in which the liquid stream is fed directly to the first mixer of the Assembly of the successive elements for desulphurization of liquefied petroleum gas (LPG).

9. The method according to claim 7, in which the amine is chosen from the IEA, deja, DEEP, MDEA.

10. The method according to claim 1, in which the liquid phase is subsequently cleaned to remove any component of the absorbed gas.

11. The method according to claim 1, in which 70%, preferably 80% and more preferably 90% of the hydrocarbons in the feed liquid is distilled over as light fractions in the gas stream.

12. Device for the simultaneous absorption of the selected acid gas components from a gas stream and distillate light fractions of hydrocarbons carried out in the liquid stream comprising solvent or reagent for the selected component gas containing the first flow mixer, where the gas stream and the liquid stream is subjected to turbulent mixing conditions, the second flow mixer, comprising a housing made with the possibility of its placement in the pipe for the passage of the fluid flow through it, and the body contains the entrance of the OE and the output apertures, accordingly, the housing is equipped with at least one internal moving hermetically established by the regulating element partially surrounding a Central chamber for the creation of the first wall connected with the side of the casing inlet, and part of the second wall connected with the outlet side of the casing, and the said parts of the walls are a number of through-ducts, each of which has a substantially smaller cross sectional area than the cross-section flow inlet and outlet openings, respectively, and in which the braking element is made movable relative to the specified enclosure, and means for separating multiphase flow from the second mixer in the gas phase and the liquid phase.

13. The device according to item 12, in which the first mixer is a turbulent mixer, has a section tapering pipe, through which the gas flow, the inlet for the liquid located so as to form the annular space of the liquid around the inner perimeter of the tube, the sharp edge on the end of the tapered pipe and an additional section of pipe downstream after sharp edges.

14. The device according to item 12, in which the first mixer includes a vessel comprising a gas inlet, the inlet fluid and the exit, and the exit leads to the passage of the Venturi tube, and a pipe extending from the outlet back up popochku, the pipe is perforated and/or separated by a gap from the periphery of the output.

15. The device according to item 12, in which the first mixer is the same as the second mixer.



 

Same patents:

FIELD: oil-refining industry; devices for a dispersion and agitation of liquid mediums.

SUBSTANCE: the invention is pertaining to the field of oil-refining industry, in particular, to devices for a dispersion and agitation of liquid mediums and may be used for homogenization of the heavy oil fuels. The device contains a body, in which the ultrasonic emitters with crescent-shaped are mounted. The disperser is made with the tangential holes and has a mounted inside conical splitter with a screw groove. Due to the certain cross-section of the tangential holes inside them there is a cavitation. Then in the turbulence chamber a cavitational-turbulent-ultrasonic treatment of a liquid takes place. The technical result consists in production of high-dispersive and homogeneous multi-component mixtures.

EFFECT: the invention ensures production of high-dispersive and homogeneous multi-component mixtures.

3 dwg

Mixer // 2261755

FIELD: mixing reagents or dispersed air with water.

SUBSTANCE: proposed mixer is made in form of diaphragm with central hole which is mounted on pipe. Said diaphragm has inner and outer radial slots which divide diaphragm into equal number of inner and outer sectors. Angle between adjacent inner and outer slots is determined by formula which ensures smooth process of mixing over entire cross section of pipe. Guides of outer and inner sectors are made in form of helical lines of opposite twisting.

EFFECT: reduced usage of metal; avoidance of losses of pressure at high intensity of mixing.

1 dwg

FIELD: mechanical engineering; power engineering; transportation industry; domestic equipment and other industries.

SUBSTANCE: the invention is pertaining to the fields of mechanical engineering, power engineering, transportation industry, domestic equipment and other fields, where processes of mixing of different liquids and gases take place, and also, in particular, to creation of low- emission combustion chambers (CC) of the stationary gas-turbine plants (GTP) with a preliminary preparation of a mixture of a liquid or gaseous fuels and air. According to the offered method the liquid and the gas are preliminary mixed, then a stream of the formed two-phase mixture pass through a penetrable element (PE) with a set value of porosity, where the basic mixing of components takes place with formation of a homogeneous mixture and its speeding up in the nozzle. The liquid is sprayed by its feeding either through a centrifugal or an air-operated injectors or through a perforated element and (or) an additional PE with the given values of porosity and dispersity installed at the end of the corresponding trunks of the liquid feeding. At that the liquid is fed under pressure, at which the dripping mode of its outflow from the additional PE is realized. A field of the centrifugal force is influenced on the two-phase mixture stream. For this purpose a special device - a turbulent mixing chamber representing a cap-shape hollow body of rotation is used. At that the side walls of the camber are in part or completely formed by PE. The field is formed by rotation of the two-phase mixture stream along the lateral surface of the turbulent mixing chamber with the help of an inlet axial - vane swirler or at the expense of one-, two- or multi-channel tangential feeding of the stream to this surface. In the capacity of a nozzle they use an outlet axial - vane swirler and (or) an axisymmetric profiled converging nozzle. Realization of the given method allows to produce the low- emission combustion chambers (CC) of the gas-turbine installations (GTI), household, office and industrial mixers with a multiple (in 5-7 times) saving of the sweet water and safe heaters of water with the help of the heated air, etc.

EFFECT: the invention allows to produce the low- emission combustion chambers of the gas-turbine installations, household, office and industrial mixers with a multiple (in 5-7 times) saving of the sweet water as well as the safe heaters of water.

3 cl, 2 dwg

FIELD: medical engineering.

SUBSTANCE: device has high pressure pump with homogenizing head unit attached to pressure collector. The head unit has casing with saddle, valve, pressure unit rod and outlet tube mounted thereon. The homogenizing head unit has two additional homogenization stages being pressure chambers having inlet openings arranged as circle. The first stage pressure chamber and inlet openings of both stages are enclosed in the rod and the second stage chamber is in the outlet tube. The valve is designed as ball. The head unit body is divided into two compartments with cross partition. The rod is designed as cylindrical cup having inlet openings in lateral wall. Rod neck member is engageable with the valve and bottom end part with the pressure unit. The first stage openings make communication between the first casing compartment and the internal cavity of the rod. The second stage openings make communication between the internal cavity of the rod and the second casing compartment being outlet tube cavity. Inlet openings of the second stage are arranged at least in two rows so that each opening group axes belonging to the same radial plane intersect at the same point belonging to the second compartment cavity. Intersection points of all opening groups belong to the plane arranged in perpendicular to the rod axis and are equidistant from it.

EFFECT: enhanced effectiveness of both low-viscous and highly viscous liquids homogenization.

2 cl, 1 dwg

The invention relates to a method for producing Homo - and copolymers of ethylene in a tubular reactor

Generator // 2227063
The invention relates to a technology for obtaining a stable foam, designed to control downhole pressures under conditions of abnormally low formation pressure,

The invention relates to a method of foaming of the liquid and gaseous phases, by the way circulate foam, and also to the purification method of installation due to the circulation in her foam

The invention relates to equipment for processing of polymeric materials and can be used for continuous mixing istropolitana fluids in the lines of the granulation and anticorrosive coatings

The invention relates to a device integrated chemical processing, suited for use with high-speed chemical reactions, which can be embedded in a broader integrated block structure of multiple chemical treatment or in an integral system

FIELD: chemical industry; petrochemical industry; other industries; spraying heat-mass exchange apparatuses.

SUBSTANCE: the invention is pertaining to the engineering realization of the heat-mass exchange processes, which take place in the gas-liquid system, such as absorption, chilling, dust-trapping, aeration, and may find application in the chemical industry and its adjacent industries. The body of the apparatus is divided by the partition into the contact and separating zones. Inside the contact zone there are the sprayers and the contact components. The apparatus is supplied with the drum installed in the contact zone with the possibility of rotation. On the drum there are fixed with the possibility of rotation the Т-shaped contact components. The T-shaped contact components are formed by the solid and mesh-type plates. The invention allows to reduce the aerodynamic drag of the apparatus, and also to improve the gas injection into the contact zone of the apparatus, that increases efficiency of the heat-mass exchange process.

EFFECT: the invention ensures the reduced aerodynamic drag of the apparatus, the improvement of the gas injection into the contact zone of the apparatus and the increased efficiency of the heat- mass exchange process.

3 dwg

FIELD: natural gas industry; oil-refining industry; chemical industry; devices for realization of the mass-exchange processes in the gas(vapor)-liquid systems.

SUBSTANCE: the invention is pertaining to the devices for realization of the mass-exchange processes in the gas (vapor)-liquid systems, in particular, to the absorption and to the rectifying columns and may be used in the natural gas industry, il-refining industry, chemical industry. The regular overflow head contains the packed solids made out of the punching-drawn perforated sheets. The punching-drawn perforated sheets are made rectangular and bent along the longitudinal axis of the symmetry in the form of the small corners with the apex angle making from 110° up to 130°. The small corners are arranged with their peaks upward and laid in the staggered order one over another in the horizontal rows in the framework with formation of the packed-column block module. The small corners shelves edges of the above located row are connected with the apexes of the corners of the below row. In the shelves of the small corners and along the corners shelves edges there are the perforated section-shaped holes arranged uniformly in the staggered order along the whole area of the corners shelves. Above the holes there are the salient cone-shaped visors and their peaks on each of the corners shelves are facing the same direction in parallel to the corner shelf bent line. The mass-exchange column contains the packing block modules mounted one above another in the central part of the body. In the body the horizontal segment-shaped baffle plate are mounted. At that the baffle plates are arranged along the corners of packing modules on the opposite sides of the framework with formation of the zigzag-shaped channel of the multipath crisscross stream of the vapor. As the result of it the invention allows to increase effectiveness and productivity for the gas (vapor) in the mass-exchange column in conditions of the low loading by the liquid, to expand the range of the stable operation of the column as a whole.

EFFECT: the invention ensures the increased effectiveness and productivity for the gas (vapor) in the mass-exchange column in conditions of the low loading by the liquid and to expand the range of the stable operation of the column as a whole.

4 cl, 5 dwg

FIELD: chemical industry; designs of the bubble-type reactors for production of 1.2-dichloroethane.

SUBSTANCE: the invention is pertaining to the design of the bubble-type reactors for production of 1.2-dichloroethane by the method of the liquid-phase chlorination of ethylene with the reaction heat removal at boiling of the working medium. As the contact device the reactor uses two layers of the metallic nozzle. The liquid 1.2-dichloroethane is fed from above to the nozzle, into the space between the layers of the nozzle feed the gaseous chlorine with nitrogen, and under the lower layer of the nozzle feed the gaseous ethylene with nitrogen, that allows to reduce the diameter of the reactor in 1.5-2 times due to the increased effectiveness of stirring and formation of the developed contact surface of the phases. At that the heat of the reaction is removed by evaporation of 1.2-dichloroethane in nitrogen. At that the temperature of the liquid is maintained below the boiling temperature. The technical result of the invention is the increased selectivity of the process, reduction of the outlet of the by-products (the highest ethane chlorides) and the decreased overall dimensions of the reactor.

EFFECT: the invention ensures the increased selectivity of the process, reduction of the outlet of the by-products (the highest ethane chlorides) and the decreased overall dimensions of the reactor.

1 ex, 4 dwg

FIELD: chemical industry; metallurgy industry; methods of the wet ash-trapping with the help of Venturi tube.

SUBSTANCE: the invention is pertaining to the method of the wet ash-trapping with the help of the Venturi tube intended for trapping of the fly ash from the flue gases of the boilers burning the solid fuel, and also may be used for trapping of the cement kiln dust in production of the cement and for the dust trapping in the metallurgical, chemical and other industries, where the ash-and-dust catchers use the Venturi tubes. The purpose of the invention is to increase the degree of trapping of the fly ash from the flue gases of the boilers with the Venturi tubes and burning the solid fuels as well as the reduction of the specific consumptions of the water and steam to increase the boilers efficiency by sprinkling of the Venturi tube with the flue gases transiting in it, the acoustic injector giving more thin and uniform atomization of the water at the decreased consumption both of the water and the steam of the sprinkler, where the acoustic field is characterized by the strictly determined frequency, intensity and the variable acoustic pressure and the steam is in the narrow temperature interval. The flue gases passing in the Venturi tube are sprinkled by the acoustic injector using the steam with the temperature of 250-350°С and forming in the volume of the tube the acoustic field, which is characterized by the frequency of 20-22, 36-38 or 44-48 kHz, the variable sound pressure of no less than 140 dB and the acoustic field intensity of no less than 0.5 W/cm2. The offered method, unlike the methods applied now, allows to act on the flue gases transiting in the Venturi tube simultaneously by several methods of deposition of the ash: - the acoustic method (coagulation - under action of the oscillations of the certain frequency, intensity and the variable sound pressure); humidification of the ash particles of ash in the steam-water aerosphere of the very finely sprinkled water with the full spectrum of the drops dimensions for all the sizes of the ash particles). This considerably increases the degree of trapping of the fly ash from the flue gases of the boilers at the simultaneous reduction of the specific consumptions of the water and steam and increases the efficiency of the boilers.

EFFECT: the invention ensures the increased degree of trapping of the fly ash from the flue gases of the boilers at the simultaneous reduction of the specific consumptions of the water and steam and the increased efficiency of the boilers using the solid fuel.

2 dwg, 1 tbl

FIELD: chemical engineering.

SUBSTANCE: invention relates to design of fill0in heads for mass transfer apparatuses and it car be used in heat-mass transfer processes in liquid-vapor(gas) systems, for instance at rectification, absorption, desorption, distillation a dn other processes. Proposed head member for mass transfer apparatuses has cut elements curved to circle of side surface. According to invention, head member is made in form of parallel cylinders formed by cut elements arranged in rod height, curved to circle in turn, inside and outside. Cylinders are connected by bridges and are arranged relative to each other so that their diametral planes from side surface of regular polygonal prism.

EFFECT: increased efficiency of heat-mass transfer by increasing surface of phase contact owing to reduction of drop formation and uniform distribution of phase surface in volume of heat-mass transfer apparatus.

3 dwg

FIELD: chemical industry; other industries; production of the heads for the heat-mass-exchanging apparatuses.

SUBSTANCE: the invention is pertaining to the devices of heat-mass-exchanging apparatuses with the fluidized three-phase layer and may be used in chemical industry and other industries at purification of the gas bursts of the harmful gaseous components. The head for the heat-mass-exchanging apparatuses is made in the form of the torus produced out of the cylindrical component made out of the synthetic filaments by its twisting from one or two ends. The cylinder is made out of the longitudinal filaments fasten among themselves in the staggered order with formation of the longitudinal cells. At that the diameter of the head exceeds its height in 1.25-1.33 times, and the ratio of the cell height to the diameter of the head makes 0.25-0.3. At utilization of the head the gas-liquid layer is uniformly distributed in the operation volume of the apparatus, that predetermines the stable hydrodynamic situation. At that the mass exchanging process is intensified due to the highly developed surface and the strong turbulization of the gas-liquid layer.

EFFECT: the invention ensures the gas-liquid layer uniform distribution in the operation volume of the apparatus, the stable hydrodynamic situation, intensification of the mass-exchange process.

4 dwg

FIELD: wet dust collection; chemical, textile, food-processing and light industries.

SUBSTANCE: proposed hydrodynamic dust collector has housing with inlet and outlet branch pipes, reservoir filled with liquid and provided with level indicator, phase mixer consisting of inclined blades with partitions and two layers of twin concave plates which are symmetrical relative to axis of apparatus, one central plate and sludge removal unit. Vibrator located in upper layers of liquid is secured to housing by means of elastic perforated membrane; ratio of width "a" of inclined blades to width "b" of first pair of concave plates is equal to a/b=4.0-4.5; ratio of width "b" of first pair of concave plates to width "c" of second pair of concave plates is within optimal range of b/c=1.25-1.5. Vibrator is made in form of section inscribed in sizes or liquid reservoir.

EFFECT: enhanced efficiency and reliability of dust collection process.

2 cl, 1 dwg

FIELD: absorption, desorption, dust and gas separation, drying, mixing and cooling gases.

SUBSTANCE: proposed apparatus has housing, cover, bottom, phase supply and discharge branch pipes, vortex contact device consisting of upper base, tangential plates, plate and separator, liquid distributors equipped with injectors and mounted on upper base of contact device. Horizontal disk-type partitions are mounted in height of tangential plates of vortex contact device. Horizontal disk-type partitions and upper base of vortex contact device are provided with circular slots in area of attachment of tangential plates. Circular shoulders are made on external and internal shears of disk-type partitions and on external shear of upper base of vortex contact device. Separator is made in form of truncated taper ferrule; diameter of lower shear of this ferrule is equal to 0.75-0.9 of inner diameter of vortex contact device. Number of vortex contact devices ranges from 1 to 3. Distance between upper base of vortex contact device and lower shear of separator is equal to 0.3-1.0 of inner diameter of vortex contact device.

EFFECT: enhanced efficiency of heat and mass exchange of vortex apparatus at high loads in gas and liquid phases.

3 cl, 5 dwg

FIELD: separation.

SUBSTANCE: conical ejecting scrubber comprises housing with branch pipes for dusted and cleaned gas, nozzle spraying device, bearing and arresting plates, nozzle interposed between the plates, and device for discharging slime. The bearing plates are flexible, and the nozzle is mounted above the bottom bearing plate and is made of flexible materials in the form of polyethylene balls. The bottom bearing plate is provided with vibrator. The nozzle can be made of hollow balls, whose spherical surfaces are provided with screw groove, or toroidal rings.

EFFECT: enhanced efficiency and reliability and reduced metal consumption for manufacturing.

7 cl, 4 dwg

FIELD: separation.

SUBSTANCE: conical scrubber comprises housing with branch pipes for dusted and cleaned gas, nozzle spraying device, bearing and arresting plates, nozzle interposed between the plates, spray trap, and device for discharging slime. The bearing plates are flexible, the nozzle mounted above the bottom bearing plate is made of a flexible material, and the bottom bearing plate is provided with the vibrator. The nozzle can be made of polyethylene balls or hollow balls whose spherical surface is provided with the screw groove.

EFFECT: enhanced efficiency and reliability and reduced metal consumption for manufacturing.

7 cl, 4 dwg

FIELD: cleaning gas mixtures from CO2 by multi-stage absorption method; chemical and oil-and-gas industries.

SUBSTANCE: proposed method includes absorption of CO2 from gas mixture by means of water in four absorbers (3,4,5 and 6) interconnected in succession. Water is fed to absorbers in parallel by means of one pump (7). Gas mixture to be cleaned contains 60-70 mass-% of CO2. Diameters of absorbers are decreased successively in such way that velocity of gas mixture in absorbers is within limits ensuring required final concentration of CO2 in cleaned mixture and height of absorbers is approximately equal.

EFFECT: high degree of cleaning gas mixture.

1 dwg

Up!