CN209809863U - Radial tube array type adsorber - Google Patents
Radial tube array type adsorber Download PDFInfo
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- CN209809863U CN209809863U CN201920292774.4U CN201920292774U CN209809863U CN 209809863 U CN209809863 U CN 209809863U CN 201920292774 U CN201920292774 U CN 201920292774U CN 209809863 U CN209809863 U CN 209809863U
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Abstract
The utility model belongs to the adsorber field, concretely relates to radial shell and tube adsorber. The adsorber comprises: the middle shell layer comprises an inner wall, an outer wall, a plurality of adsorption tubes penetrating through the inner wall and the outer wall, and a plurality of heat exchange medium pipelines arranged at two ends of the middle shell layer and communicated with the middle shell layer; the powder collecting tank is connected with the lower end of the inner wall; a space formed by the inner wall and the powder collecting groove is used as a central flow passage; a space formed by the outer wall, the powder collecting tank and the adsorber shell is used as an outer flow passage; the outer flow channel, the central flow channel and the adsorption tube are communicated with each other to form a fluid flow channel; the intermediate shell is not in communication with the fluid flow passage. The adsorber can realize the regeneration of the adsorbent, and the regeneration mode is the combination of indirect heating and vacuum desorption.
Description
Technical Field
The utility model belongs to the adsorber field, concretely relates to can realize that adsorbent adsorbs back indirect heating and vacuum desorption and combine together regenerated radial shell and tube adsorber.
Background
Fixed bed adsorbers based on adsorption processes have found wide application in gas separations. In the adsorption process, the mixed components pass through the adsorbent bed layer, the light component gas is not or less adsorbed and penetrates through the fixed bed layer earlier, the heavy component gas is mainly adsorbed until the adsorbent is saturated, and the heavy component gas can be recovered in the regeneration process of the adsorbent, so that the separation of the light component gas and the heavy component gas is realized. Based on the process, gases with higher resource value in a plurality of industrial tail gases can be enriched and concentrated by recycling desorption gases in the regeneration process, such as a large amount of SO in the smoke of the steel furnace kiln2With NOXGases, organic gases in chemical plant exhaust gases, and the like.
Heating and evacuation are common means of adsorbent regeneration. For heating regeneration, a direct heating mode is usually adopted, namely high-temperature nitrogen or water vapor is introduced into an adsorber to heat an adsorbent bed layer, but the mode can dilute desorption gas and is not beneficial to enrichment and recovery of the desorption gas, and in addition, the problems that water-soluble organic waste gas is dissolved in water vapor condensate to form organic wastewater, new treatment and purification equipment is required and the like exist. For vacuum-pumping regeneration, a vacuum pump is used for pumping air into the closed space of the bed layer of the adsorbent to form negative pressure, so that the adsorbent can be quickly desorbed, no impurity gas is introduced, and the desorbed gas can be directly enriched and purified; however, the desorption force of the method on polar gas molecules is not enough, so that the adsorbent cannot be fully regenerated, at this time, the adsorbent is often required to be heated to a certain degree to assist regeneration, but the direct heating causes the problems of vacuum degree reduction, desorption gas dilution and the like.
The above problems all explain the importance and urgency of the regeneration stage of the adsorbent and the indirect heating mode, which not only can avoid introducing impurity gas, but also can combine the two regeneration methods of heating and vacuumizing to realize the shortening of the regeneration time of the adsorbent, the reduction of the regeneration energy consumption and the enrichment and concentration of the desorption gas.
The tubular fixed bed adsorber is connected in parallel through a plurality of adsorption tubes, and fixed bed adsorbent is filled in the tubes for gas adsorption separation. When the adsorbent is regenerated, the heat medium is introduced into the adsorber and flows through the adsorption pipe to indirectly heat the adsorbent; after the heating is finished, the adsorption tube is indirectly cooled by introducing a cold medium, and the whole heat exchange medium is isolated from the space in the adsorption tube. In order to ensure the heat exchange efficiency, the tubular fixed bed adsorber needs a larger heat exchange area, so that for the traditional axial flow arranged adsorber, the tubular fixed bed adsorber needs a larger floor area than that of the common fixed bed adsorber. The uniformity of the tubular heat exchange relates to the desorption effect of the adsorbent, and the uniformity depends on the distribution uniformity of heat exchange media in the indirect heat exchange process to a great extent, so how to ensure the sufficient and uniform heat exchange among the tubes is a key technical problem of the tubular fixed bed adsorber. In addition, if a vacuumizing regeneration mode is combined, isolation between a heat exchange space outside the adsorption tube and a bed layer space inside the adsorption tube needs to be ensured in an indirect heating process, and the problems of material deformation, sealing failure and the like of the adsorber possibly occurring in a long-term temperature and/or pressure alternating environment are avoided.
In summary, the existing tubular fixed bed adsorbers are mainly axial adsorbers, and have the following disadvantages:
(1) the horizontal heat exchange area is large, and the occupied area is large;
(2) the problem of uneven heat exchange exists;
(3) when the method is combined with a vacuumizing regeneration mode, the problems of deformation of adsorber materials, failure of tube array tightness and the like exist;
(4) when the vacuum-pumping regeneration mode is combined, the raw material gas in the non-bed space communicated with the inner bed layer of the adsorption tube can be simultaneously pumped out, which is not beneficial to enrichment and concentration of desorption gas.
In view of the above, there is a need to provide a solution to overcome or at least mitigate at least one of the above-mentioned drawbacks of the prior art.
SUMMERY OF THE UTILITY MODEL
In order to solve the problems, the utility model provides a radial tubular adsorber; the adsorption tube in the adsorber is arranged to form an angle different from 0 with the cross section of the middle shell layer, and when the adsorber is of a vertical cylinder structure, the adsorber can fully utilize height space to reduce floor area, enhance heat exchange efficiency and uniformity and improve operation matching with a vacuumizing regeneration mode. The adsorber can realize the regeneration of the adsorbent, and the regeneration mode is the combination of indirect heating and vacuum desorption.
The utility model discloses a realize through following technical scheme:
a shell and tube adsorber, the adsorber comprising:
the two ends of the adsorber shell are respectively provided with a fluid inlet end and a fluid outlet end;
the middle shell layer is arranged inside the adsorber shell, the cross section of the middle shell layer is annular, and the middle shell layer comprises an inner wall, an outer wall, a plurality of adsorption tubes penetrating through the inner wall and the outer wall, and a plurality of heat exchange medium pipelines arranged at two ends of the middle shell layer and communicated with the middle shell layer;
a powder collection trough disposed at an end of the inner wall facing the fluid inlet end;
a space formed by the inner wall and the powder collecting groove is used as a central flow passage;
a space formed by the outer wall, the powder collecting tank and the adsorber shell is used as an outer flow passage;
the outer flow channel, the central flow channel and the adsorption tube are communicated with each other to form a fluid flow channel;
the intermediate shell is not in communication with the fluid flow passage.
Further, the adsorber also includes an internal support for stabilizing the intermediate shell; the inner support is positioned below the intermediate shell layer;
the inner support is provided with a plurality of support through holes, and the support through holes enhance the convection strength of the fluid and simultaneously slow down the flow velocity of the fluid.
Furthermore, the number of the heat exchange medium pipelines is determined according to the size of the actual absorber and the processing conditions, at least 2 heat exchange medium pipelines are arranged at any one end of the middle shell layer, and the uniformity of the heat exchange medium flowing through the middle shell layer can be improved by increasing the number of the openings, the circulation resistance of the heat exchange medium is reduced, and therefore the uniformity of heat exchange of the absorption tubes is improved.
Furthermore, 2-50 heat exchange medium pipelines are arranged at any one end of the middle shell layer.
Furthermore, the adsorber is suspended and fixed on a bearing support for bearing the weight of the adsorber.
Further, the fluid enters from the fluid inlet end and exits from the fluid outlet end, or enters from the fluid outlet end and exits from the fluid inlet end.
Further, when the fluid enters from the fluid inlet end and exits from the fluid outlet end, the powder collecting groove can promote the diversion of the fluid to the outside of the middle shell layer, and can collect the adsorbent in the adsorption pipe carried out by the fluid.
Furthermore, the adsorber also comprises a manhole for providing maintenance personnel to maintain the inside of the adsorber and clean dust; the manhole is arranged on the adsorber shell.
Further, the included angle between the adsorption tube and the cross section of the middle shell layer is alpha, the range of alpha is 0 degrees < alpha <90 degrees, namely the adsorption tube is obliquely arranged in the middle shell layer, and the adsorption tube is obliquely arranged to bring the beneficial effects that: the adsorbent bed is tightly packed, so that the problem of fluid short circuit caused by a gap formed between the adsorbent bed and the upper pipe wall due to gravity is avoided; meanwhile, the adsorption tubes are obliquely arranged, so that the space of the intermediate shell layer can be more fully utilized, and the floor area is reduced;
the inclination angle (alpha) of the adsorption tube can be adjusted according to adsorbent materials, bed layer characteristics, intermediate shell layer space heat exchange conditions, overall occupation conditions and the like.
Further, the range of α is further 5 ° < α <75 °.
Further, all set up a plurality of adsorption tube through-holes on inner wall and the outer wall, the adsorption tube passes adsorption tube through-hole on inner wall and the outer wall, will simultaneously adsorption tube through-hole edge with the space between the adsorption tube is sealed so that middle shell with the fluid flow channel does not communicate.
Further, the manner of sealing the gap between the through hole edge of the adsorption tube and the adsorption tube includes welding and movable sealing.
Further, the movable seal includes:
the bottom support is arranged at the edge of the through hole of the adsorption tube at the fluid inlet on the adsorption tube;
the first flange is arranged at the edge of the through hole of the adsorption tube at the fluid outlet on the adsorption tube;
at least 2 sections of sliding rails arranged between the inner wall and the outer wall;
a second flange disposed outside of said fluid outlet;
the first flange plate and the second flange plate are connected through bolts, and the two flange plates mutually extrude a flange gasket to form sealing;
a movable piston cover arranged at the port of the fluid outlet; when the desorption stage is vacuumized, the adsorbent desorption fluid is pumped out from the fluid inlet, and the movable piston sealing cover covers and seals the fluid outlet under the action of gravity and/or pumping force, so that the fluid in the flow channel space at the fluid outlet is not pumped out as desorption gas;
during the adsorption phase, fluid flows in from the fluid inlet, and the movable piston cover moves outwards under the pressure of the airflow to enable the fluid to flow out from the fluid outlet.
Further, the fluid inlet is directed at the fluid inlet end and the fluid outlet is directed at the fluid outlet end.
Further, the movable piston sealing cover is a movable piston round sealing cover.
Furthermore, the bottom support is an annular surface attached with a rubber ring, and the annular surface is closely attached to the annular end surface at the bottom of the adsorption tube, so that sealing is realized.
Further, slide rail cross section structure with the laminating in the adsorption tube outside can be for the slope assembly the adsorption tube in-process passes provide the direction during the adsorption tube through-hole, it is right simultaneously the adsorption tube plays the bearing effect.
Further, the shape of the through hole of the adsorption pipe is an ellipse.
Further, the adsorber housing is of a vertical cylindrical structure.
Furthermore, the adsorption tubes are cylindrical through tubes with uniform cross sections, adsorbent fixed beds are filled in the adsorption tubes, the adsorption tubes are arranged in the middle shell layer space from top to bottom around the inner wall in a radial radioactive arrangement mode, and the adsorption tubes are parallel to each other.
Furthermore, the whole adsorber is a cylindrical barrel, the adsorption pipe is a through pipe with a circular cross section, and the inner wall and the outer wall are cylindrical barrels; the adsorber can relieve the problem of stress concentration of the pipeline on the whole, and avoids the problems of material deformation, tightness failure and the like of the adsorber which may occur in the environment of long-term temperature and/or pressure alternation.
Furthermore, the adsorption tube is a cylindrical through tube with a uniform cross section, the tube diameter ranges from 0.01m to 10m, and the tube length ranges from 0.01m to 100 m.
Further, the adsorber shell also comprises a first seal head and a second seal head; the first end socket and the second end socket are respectively two ends of the absorber shell.
Furthermore, the adsorber is of a vertical cylinder structure or a horizontal cylinder structure;
when the adsorber is of a vertical cylinder structure, the adsorber can fully utilize height space to reduce floor area, enhance heat exchange efficiency and uniformity and improve operation matching of a vacuumizing regeneration mode.
The utility model discloses a shell and tube adsorber is when using:
adsorbing fluid, wherein the fluid enters from a fluid inlet end or a fluid outlet end, passes through the fluid flow channel, and is adsorbed by the adsorbent in the adsorption tube, and then the residual fluid is discharged from the fluid outlet end or the fluid inlet end;
indirectly heating desorption fluid, wherein a heat exchange medium enters the intermediate shell layer through a heat exchange medium pipeline at one end of the intermediate shell layer, and indirectly heating the adsorbent in the adsorption pipe to desorb the fluid on the adsorbent in the adsorption pipe;
when the desorption fluid is indirectly heated or is not simultaneously heated, the fluid flow channel is subjected to vacuum desorption, so that the fluid on the adsorbent in the adsorption tube is desorbed;
and cooling the adsorbent, wherein a heat exchange medium enters the intermediate shell layer through a heat exchange medium pipeline at one end of the intermediate shell layer, and the adsorbent in the adsorption pipe is indirectly cooled.
And during vacuum desorption, the fluid inlet end or the fluid outlet end is sealed, the fluid outlet end or the fluid inlet end is communicated with a vacuum pump, and the fluid flow channel is vacuumized.
Further, the heat exchange medium flows in the intermediate shell layer and exchanges heat with the outer wall, the inner wall and the outer wall of the adsorption tube; that is, besides the outer wall of the adsorption tube participating in heat exchange, the wall surfaces of the inner wall and the outer wall also participate in heat exchange, so that the heat exchange efficiency is enhanced; when the adsorbent is in a heating stage, the heat exchange medium is hot air or a hot liquid working medium; when the adsorbent is in the cooling stage, the heat exchange medium is cold air or cold liquid working medium.
Furthermore, the heat exchange efficiency of the adsorber can be adjusted by adjusting the structure parameters such as the pipe diameter, the pipe distance, the distribution rule, the inclination angle and the like of the adsorption pipes; the flowing direction of the heat medium or the inlet and the outlet on the same side can be periodically replaced by sexual intercourse to strengthen the convection of the heat transfer medium so as to improve the heat transfer convection efficiency of the heat transfer medium and the adsorption tube.
Furthermore, the vacuum desorption and the indirect heating desorption fluid are carried out simultaneously, so that the synchronous operation of the two adsorbent regeneration means of the heating and the vacuumizing of the adsorber is realized; and when the desorption of the adsorbent is finished, the vacuumizing is stopped, and the low-temperature heat exchange medium is replaced to flow through the middle shell layer to cool the adsorption tube.
Further, the fluid comprises: one of a gas and a liquid.
Further, the adsorber adsorbs one or more components of the fluid, and the adsorbed components are gases or liquids.
Further, the gas comprises: organic gases and inorganic gases.
Further, the organic gas includes formaldehyde, benzene, toluene, methane, ethane, ethylene, ethanol, acetaldehyde, acetylene, polycyclic aromatic hydrocarbon, and dioxin.
Further, the mixed inorganic gas includes sulfur dioxide, hydrogen sulfide, nitrogen dioxide, nitrogen monoxide, nitrogen oxides, carbon dioxide, carbon monoxide, water vapor, nitrogen, oxygen, argon, and chlorine.
Further, when the adsorbed component is liquid, the fluid is petroleum, coking wastewater, coal chemical wastewater or garbage penetrating fluid.
The utility model discloses following beneficial technological effect has at least:
(1) the utility model discloses an adsorber realizes going on in step of two kinds of adsorbent regeneration modes of heating and evacuation, and the guarantee desorption gas is not diluted simultaneously, does benefit to its further enrichment concentration and resourceization.
(2) The utility model discloses an when the adsorber was vertical tube structure, but the operation matching nature of adsorber high space reduction area, reinforcing heat exchange efficiency and the degree of consistency, promotion and evacuation regeneration mode can be fully utilized.
(3) The utility model discloses an adsorber heat exchange efficiency is high, and the homogeneity is strong, and desorption time is short.
(4) The utility model discloses an adsorber can be in long-term temperature and/or pressure alternation environment steady operation, and adsorber inner structure or material that avoid probably appearing warp, the seal inefficacy scheduling problem.
(5) The utility model discloses an among the adsorber, adopt the mode (being the tubulation promptly) that the adsorption tube inserted the adsorption tube through-hole, only need before inserting pack into the adsorption tube adsorbent one by one can, promptly the utility model discloses an adsorbent is convenient for assemble in the adsorber.
(6) The utility model discloses an adsorber easily realizes rapid heating up negative pressure regeneration function, and it is high to have a heat exchange efficiency, takes up an area of for a short time, length when adsorbent is regenerated, advantages such as flow field degree of consistency height.
Drawings
FIG. 1 is a schematic diagram of a longitudinal cross-sectional structure of a shell and tube adsorber in an embodiment of the invention as fluid enters from a fluid inlet port.
FIG. 2 is a schematic diagram of a longitudinal cross-sectional configuration of a shell and tube adsorber in an embodiment of the invention as fluid enters from a fluid outlet port.
Fig. 3 is a schematic diagram of a longitudinal cross-sectional structure of a shell and tube adsorber in an embodiment of the invention when fluid enters from a fluid inlet end and includes an inner support.
Fig. 4 is a schematic structural view of the embodiment of the present invention in which the through holes of the adsorption tube are disposed on the inner wall or the outer wall.
Fig. 5 is a schematic cross-sectional view of an array of sorbent tubes in an intermediate shell according to an embodiment of the present invention.
Fig. 6 is a schematic structural view of the single adsorption tube and the inner wall and the outer wall in the embodiment of the present invention during movable sealing.
Description of reference numerals: 1 is an absorber shell, 11 is a fluid inlet end, 12 is a fluid outlet end, 13 is a first seal head, and 14 is a second seal head; 2, an intermediate shell layer, 21, 22, 23, 24, 25, 26, 27, 28 and 29, wherein the intermediate shell layer is an inner wall, 22 and 23 are adsorption tubes, a bottom support, a first flange plate, a slide rail, a second flange plate, bolts and a movable piston sealing cover; 3 is a heat exchange medium pipeline; 4 is a powder collecting tank; 5 is an inner bracket; 6 is a bearing support; and 7 is a manhole.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail below with reference to the accompanying drawings of the embodiments and the specification. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
On the contrary, the invention is intended to cover alternatives, modifications, equivalents and alternatives which may be included within the spirit and scope of the invention as defined by the appended claims. Furthermore, in order to provide a better understanding of the present invention to the public, certain specific details are set forth in the following detailed description of the invention. It will be apparent to those skilled in the art that the present invention may be practiced without these specific details.
FIG. 1 is a schematic diagram of a longitudinal cross-sectional structure of a shell and tube adsorber in an embodiment of the invention as fluid enters from a fluid inlet port. FIG. 2 is a schematic diagram of a longitudinal cross-sectional structure of a shell and tube adsorber in an embodiment of the invention as fluid enters from a fluid inlet port. Fig. 3 is a schematic diagram of a longitudinal cross-sectional structure of a shell and tube adsorber in an embodiment of the invention when fluid enters from a fluid inlet end and includes an inner support. Fig. 4 is a schematic structural view of the embodiment of the present invention in which the through holes of the adsorption tube are disposed on the inner wall or the outer wall. Fig. 5 is a schematic cross-sectional view of an array of sorbent tubes in an intermediate shell according to an embodiment of the present invention. Fig. 6 is a schematic structural view of the single adsorption tube and the inner wall and the outer wall in the embodiment of the present invention during movable sealing.
A shell and tube adsorber as shown in figure 1 comprising:
the two ends of the adsorber shell are respectively provided with a fluid inlet end and a fluid outlet end;
the middle shell layer is arranged inside the adsorber shell, the cross section of the middle shell layer is annular, and the middle shell layer comprises an inner wall, an outer wall, a plurality of adsorption tubes penetrating through the inner wall and the outer wall, and a plurality of heat exchange medium pipelines arranged at two ends of the middle shell layer and communicated with the middle shell layer;
a powder collection trough disposed at an end of the inner wall facing the fluid inlet end;
a space formed by the inner wall and the powder collecting groove is used as a central flow passage, and an adsorption fluid outlet end is arranged above the central flow passage;
a space formed by the outer wall, the powder collecting tank and the adsorber shell is used as an outer flow passage;
the outer flow channel, the central flow channel and the adsorption tube are communicated with each other to form a fluid flow channel;
the intermediate shell is not in communication with the fluid flow passage.
The intermediate shell layer is not communicated with the fluid flow channel, so that the synchronous operation of two adsorbent regeneration modes of heating and vacuumizing of the adsorber is realized, and meanwhile, the desorbed gas is not diluted, thereby being beneficial to further enrichment, concentration and resource utilization.
Referring to FIG. 3, in another alternative embodiment, the adsorber further comprises an internal support for stabilizing the intermediate shell; the inner support is positioned below the intermediate shell layer;
the inner support is provided with a plurality of support through holes, and the support through holes enhance the convection strength of the fluid and simultaneously slow down the flow velocity of the fluid.
In this embodiment, the number of the heat exchange medium pipes is determined according to the actual size of the adsorber and the processing conditions, and at least 2 heat exchange medium pipes are arranged at any end of the intermediate shell layer, so that the uniformity of the heat exchange medium flowing through the intermediate shell layer can be improved by increasing the number of the openings, the circulation resistance of the heat exchange medium is reduced, and the uniformity of heat exchange of the adsorption pipes is improved.
In another embodiment, 2-50 heat exchange medium pipelines are arranged at any one end of the intermediate shell layer.
In another embodiment, the adsorber is suspended and fixed on a load-bearing support for bearing the weight of the adsorber.
In this embodiment, fluid enters from the fluid inlet end and exits from the fluid outlet end.
In another alternative embodiment, fluid enters from the fluid outlet end and exits from the fluid inlet end.
In this embodiment, when the fluid enters from the fluid inlet end and exits from the fluid outlet end, the powder collecting groove can promote the diversion of the fluid to the outside of the middle shell layer, and can collect the adsorbent in the adsorption pipe carried out by the fluid.
Referring to fig. 1, in the present embodiment, the adsorber further includes a manhole for providing a service person to service and clean dust inside the adsorber; the manhole is arranged on the adsorber shell.
In this embodiment, an included angle between the adsorption tube and the cross section of the intermediate shell is α, where α is in a range of 0 ° < α <90 °, that is, the adsorption tube is obliquely disposed in the intermediate shell, and the adsorption tube is obliquely disposed to have the following beneficial effects: the adsorbent bed is tightly packed, so that the problem of fluid short circuit caused by a gap formed between the adsorbent bed and the upper pipe wall due to gravity is avoided; meanwhile, the adsorption tubes are obliquely arranged, so that the space of the intermediate shell layer can be more fully utilized, and the floor area is reduced;
the inclination angle (alpha) of the adsorption tube can be adjusted according to adsorbent materials, bed layer characteristics, intermediate shell layer space heat exchange conditions, overall occupation conditions and the like.
In one embodiment, said a further ranges from 5 ° < a <75 °.
Referring to fig. 4, in this embodiment, a plurality of adsorption tube through holes are disposed on the inner wall and the outer wall, the adsorption tubes pass through the adsorption tube through holes on the inner wall and the outer wall, and gaps between edges of the adsorption tube through holes and the adsorption tubes are sealed so that the intermediate shell is not communicated with the fluid flow channel.
Referring to fig. 6, in the present embodiment, the manner of sealing the gap between the through-hole edge of the adsorption tube and the adsorption tube includes welding and movable sealing.
In this embodiment, the movable sealing step includes:
welding a bottom support on the edge of the through hole of the adsorption tube at the fluid inlet on the adsorption tube;
welding a first flange plate at the edge of a through hole of the adsorption tube at the fluid outlet on the adsorption tube;
at least 2 sections of sliding rails are welded between the inner wall and the outer wall of the part, located inside the middle shell layer, of the adsorption pipe;
welding a second flange plate at the outer side of the fluid outlet;
the first flange plate and the second flange plate are connected through bolts, and the two flange plates mutually extrude a flange gasket to form sealing;
a movable piston sealing cover is arranged at the port of the fluid outlet; when the desorption stage is vacuumized, the adsorbent desorption fluid is pumped out from the fluid inlet, and the movable piston sealing cover covers and seals the fluid outlet under the action of gravity and/or pumping force, so that the fluid in the flow channel space at the fluid outlet is not pumped out as desorption gas;
during the adsorption phase, fluid flows in from the fluid inlet, and the movable piston cover moves outwards under the pressure of the airflow to enable the fluid to flow out from the fluid outlet.
In this or other embodiments, the fluid inlet is directed toward the fluid inlet end and the fluid outlet is directed toward the fluid outlet end.
In this embodiment, the movable piston cover is a movable piston circular cover.
In this embodiment, the collet is the toroidal surface that pastes the rubber circle, the toroidal surface closely pastes with the adsorption tube bottom annular end face closely and closely and realizes sealedly.
In this embodiment, slide rail cross section structure with the laminating in the adsorption tube outside can be for the slope assembly the adsorption tube in-process passes provide the direction during the adsorption tube through-hole, it is right simultaneously the adsorption tube plays the bearing effect.
In this embodiment, the through hole of the adsorption tube is elliptical; the size of the through hole of the adsorption tube is matched with the size of the cross section of the adsorption tube.
It will be appreciated that in other embodiments, the through hole of the adsorption pipe is circular, and the size of the through hole of the adsorption pipe is matched with the size of the cross section of the adsorption pipe.
In this embodiment, the adsorber housing is of a vertical cylindrical configuration.
Referring to fig. 5, in this embodiment, the adsorption tubes are cylindrical through tubes with uniform cross-section, adsorbent fixed beds are filled in the adsorption tubes, a plurality of adsorption tubes are radially arranged around the inner wall from top to bottom in the intermediate shell space, and the adsorption tubes are parallel to each other.
In this embodiment, the adsorption tube is a cylindrical through tube with a uniform cross section, the tube diameter is 10m, and the tube length range is 0.01 m.
In another embodiment, the diameter of the adsorption tube is 0.01mm, and the length of the tube is 100 m.
In another embodiment, the diameter of the adsorption tube is 3m, and the length of the adsorption tube is 40 m.
In another embodiment, the diameter of the adsorption tube is 8m, and the length of the adsorption tube is 70 m.
In other embodiments, the diameter of the adsorption tube ranges from 2m to 9m, and the length of the adsorption tube ranges from 2m to 90 m.
In this embodiment, the whole adsorber is a cylindrical cylinder, the adsorption tube is a circular cross-section through tube, and the inner wall and the outer wall are cylindrical cylinders; the adsorber can relieve the problem of stress concentration of the pipeline on the whole, and avoids the problems of material deformation, tightness failure and the like of the adsorber which may occur in the environment of long-term temperature and/or pressure alternation.
In another embodiment, the adsorber housing comprises a first head and a second head; the first end socket and the second end socket are respectively two ends of the absorber shell.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit it; although the present application has been described in detail with reference to the foregoing embodiments, it should be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; such modifications and substitutions do not depart from the spirit and scope of the present invention in its corresponding aspects.
Claims (8)
1. A shell and tube adsorber, comprising:
the two ends of the adsorber shell are respectively provided with a fluid inlet end and a fluid outlet end;
the middle shell layer is arranged inside the adsorber shell, the cross section of the middle shell layer is annular, and the middle shell layer comprises an inner wall, an outer wall, a plurality of adsorption tubes penetrating through the inner wall and the outer wall, and a plurality of heat exchange medium pipelines arranged at two ends of the middle shell layer and communicated with the middle shell layer;
a powder collection trough disposed at an end of the inner wall facing the fluid inlet end.
2. The shell and tube adsorber of claim 1 further comprising an internal support for stabilizing the intermediate shell; the inner support is positioned below the intermediate shell layer;
the inner support is provided with a plurality of support through holes for enhancing the convection strength of the fluid and slowing down the flow velocity of the fluid.
3. The shell and tube adsorber of claim 1 wherein the adsorption tubes are at an angle α to the cross-section of the intermediate shell, α being in the range 0 ° < α <90 °.
4. The shell and tube adsorber of claim 1 wherein the inner wall and the outer wall each have a plurality of adsorber tube openings therethrough;
the adsorption tube passes through the through holes of the adsorption tube on the inner wall and the outer wall, and simultaneously the edges of the through holes of the adsorption tube are sealed with the gaps between the adsorption tubes.
5. The shell and tube adsorber of claim 4 wherein the void seal is a weld or a moving seal.
6. The shell and tube adsorber of claim 5, wherein the movable seal comprises:
the bottom support is arranged at the edge of the through hole of the adsorption tube at the fluid inlet on the adsorption tube;
the first flange is arranged at the edge of the through hole of the adsorption tube at the fluid outlet on the adsorption tube;
at least 2 sections of sliding rails arranged between the inner wall and the outer wall;
a second flange disposed outside of said fluid outlet;
the first flange plate and the second flange plate are connected through bolts, and the two flange plates mutually extrude a flange gasket to form sealing;
and the movable piston cover is arranged at the port of the fluid outlet.
7. The tubular adsorber of claim 1, wherein the adsorption tubes are cylindrical tubes of equal cross-section, the tube diameter ranges from 0.01m to 10m, and the tube length ranges from 0.01m to 100 m.
8. The shell and tube adsorber of claim 1 further comprising a manhole for service personnel to service the adsorber interior and clean dust; the manhole is arranged on the adsorber shell.
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| CN201920292774.4U CN209809863U (en) | 2019-03-08 | 2019-03-08 | Radial tube array type adsorber |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109876593A (en) * | 2019-03-08 | 2019-06-14 | 北京科技大学 | A kind of method of radial alignment tubular adsorber and its adsorption-desorption |
| CN113069873A (en) * | 2021-03-05 | 2021-07-06 | 广钢气体(广州)有限公司 | Automatic adsorbent filling device for air separation radial flow adsorber |
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2019
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109876593A (en) * | 2019-03-08 | 2019-06-14 | 北京科技大学 | A kind of method of radial alignment tubular adsorber and its adsorption-desorption |
| CN109876593B (en) * | 2019-03-08 | 2024-01-26 | 北京科技大学 | Radial tube type adsorber and adsorption and desorption method thereof |
| CN113069873A (en) * | 2021-03-05 | 2021-07-06 | 广钢气体(广州)有限公司 | Automatic adsorbent filling device for air separation radial flow adsorber |
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