CN203227477U - Constant-temperature fixed-bed reactor for filling catalysts among heat exchange tubes - Google Patents
Constant-temperature fixed-bed reactor for filling catalysts among heat exchange tubes Download PDFInfo
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- CN203227477U CN203227477U CN 201320176372 CN201320176372U CN203227477U CN 203227477 U CN203227477 U CN 203227477U CN 201320176372 CN201320176372 CN 201320176372 CN 201320176372 U CN201320176372 U CN 201320176372U CN 203227477 U CN203227477 U CN 203227477U
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Abstract
The utility model provides a constant-temperature fixed-bed reactor for filling catalysts among heat exchange tubes. The constant-temperature fixed-bed reactor comprises a pressure-bearing shell, a plurality of heat exchange tubes and the catalysts, wherein the heat exchange tubes are arranged in the pressure-bearing shell; catalyst filling areas are formed by gaps positioned among the plurality of heat exchange tubes; an air channel is formed by the gaps positioned among the heat exchange tubes and air outlets. According to the constant-temperature fixed-bed reactor, a large quantity of the catalysts are filled among the heat exchange tubes; the heat exchange tubes can fast remove reaction heat, so that the integral bed basically achieves the temperature equalization effect, the temperature is not exceeded, and the side reaction is difficult to generate; in addition, a reaction gas can form axial and radial flows in the bed, the catalysts can be furthest utilized, and fine-granular catalysts with higher activity can be used.
Description
Technical field
The utility model relates to a kind of isothermal fixed bed reactors, relates in particular to a kind of catalyst to be loaded on isothermal fixed bed reactors between the heat exchanger tube, and this isothermal fixed reactor can be axial-radial flow reactor, pure axial flow reactor or pure radial reactor.
Background technology
Development along with Chemical Manufacture, for adapting to different heat transfer requirement and heat transfer type, the version that the various fixed bed bioreactor occurs, wherein especially to utilize the reaction mass of gaseous state, the gas solid catalytic reactor that reacts by the bed that is made of solid catalyst is most widely used in Chemical Manufacture.
Fixed bed reactors mainly are divided into heat-insulating and heat exchange type two big classes on reaction principle.
The heat-insulating fixed bed reactors are simple in structure, are widely used.But in practical operation, adiabatic reactor can not reach very high efficient, mainly contains the restriction of two aspects: the 1. restriction of chemical balance; For exothermic reaction, temperature is more high, is unfavorable for that more reaction tends to balance, and reduces temperature and then can reduce reaction rate; 2. the reaction temperature rising catalyst scope of application that made reaction bed temperature head and shoulders above can cause the active component clinkering of catalyst surface, and specific area descends significantly, active decline, and the side reaction aggravation, even cause temperature runaway, damage equipment; So for heat release type catalyst reaction device, reach darker reaction, usually adopt multistage band heat exchange type adiabatic reactor technology, flow process is tediously long, the heat-exchange network complexity, be subjected to pining down of full factory energy balance, bigger for load fluctuation and unstripped gas component variable effect, be unfavorable for device safe operation steady in a long-term.
Isothermal reactor is in time removed reaction heat by heat exchange element, keeps the basic constant temperature of bed, and its major advantage is: 1. isothermal operation makes the real reaction temperature curve near maximum reaction rate curve, improves reaction rate greatly, and reaction is tended to balance; 2. isothermal reaction provides gentle running environment to catalyst, thereby has prolonged life of catalyst; 3. the mode of utilizing water circulation byproduct steam to take away catalyst bed reaction heat is effectively through facts have proved of decades, has stronger controllability, can effectively control reaction bed temperature by regulating byproduct steam pressure; 4. isothermal reaction has effectively been stopped the generation of beds overheating problem, has avoided some to react contingent side reaction simultaneously, has improved the security of device.Along with characteristics such as device maximization, Coal Gasification Technology diversification, the use of isothermal reactor, perhaps isothermal reactor and adiabatic reactor unites the requirement that use can more adapt to some technology.
Isothermal reactor is divided into axial flow reactor and radial reactor again.In the prior art, axial isothermal reactor form commonly used is the shell and tube isothermal reactor, and catalyst fills in the heat exchanger tube, and reaction gas flows in pipe vertically, and the steam of shell-side is removed reaction heat and byproduct steam.For example CN101249406A discloses a kind of heat insulation-cold stimulated-shell of pipe exterior cold combined gas solid phase fixed bed catalyst chamber, move hot requirement though satisfied reversible exothermic reaction, simultaneously can also the by-product middle pressure steam, but, because the restriction of reactor diameter makes its production capacity be subjected to certain restriction.Radial reactor then big owing to the catalyst useful load, flow process is short, the little preferred reactor type that becomes industrial large-sizedization of reversible exothermic reaction equipment of step-down.For example CN101254442A discloses a kind of pressurized catalysis method for exothermic reaction, it mainly is the centrifugal radial flow reactor that adopts from inside to outside, though loaded catalyst is big, but the catalytic amount that the Radial Flow reacting gas flows through is also little, if gas purification is bad, the easier catalysqt deactivation that causes.
The utility model content
The purpose of this utility model is to overcome above-mentioned deficiency, provides a kind of catalyst is loaded on isothermal fixed bed reactors between the heat exchanger tube, can effectively keep reaction bed temperature evenly constant, maximally utilises catalyst.
The utility model provides a kind of catalyst has been loaded on isothermal fixed bed reactors between the heat exchanger tube, comprises pressure-bearing shell, is installed in a plurality of heat exchanger tubes in the pressure-bearing shell;
Be provided with gas feed, heat transferring medium outlet, gas vent, heat transferring medium import and catalyst discharge port at described pressure-bearing shell;
Import is connected with heat transferring medium with described heat transferring medium outlet respectively at the two ends of described heat exchanger tube;
Exist the space to form the catalyst fill area between described a plurality of heat exchanger tube, and space and gas vent between the gas feed, heat exchanger tube form gas passage.
Preferably, described gas feed and gas vent lay respectively at the two ends of pressure-bearing shell.
Preferably, the outlet of described heat transferring medium import and heat transferring medium lays respectively at the two ends of pressure-bearing shell.
Preferably, heat transferring medium import and gas vent are positioned at the same end of pressure-bearing shell; Described gas feed and heat transferring medium outlet are positioned at the other end of pressure-bearing shell.
Preferably, described catalyst discharge port, heat transferring medium import and gas vent are positioned at the same end of pressure-bearing shell; Described gas feed and heat transferring medium outlet are positioned at the other end of pressure-bearing shell.
Wherein, described pressure-bearing shell comprises upper cover, low head, cylindrical shell; Upper cover is fixedlyed connected with an end of cylindrical shell, and low head is fixedlyed connected with the other end of cylindrical shell.
Preferably, described upper cover is provided with gas feed and heat transferring medium outlet, and described low head is provided with gas vent, heat transferring medium import and catalyst discharge port.
Wherein, fixedly connected mode can be welding etc.
Preferably, described isothermal fixed bed reactors also comprise the catalyst inner core; Described catalyst inner core is near the end sealing of gas feed, and the other end is connected with gas vent; The sidewall of catalyst inner core is provided with side opening; Described heat exchanger tube is between described catalyst inner core and pressure-bearing shell.
Described catalyst inner core can be straight tube, and during use, reaction gas axially enters beds, and the gas behind catalyst bed reaction is collected through the catalyst inner core, finally discharges from gas vent.
Preferably, described isothermal fixed bed reactors also comprise the catalyst urceolus; Form the gap between the sidewall of described catalyst urceolus and the inwall of cylindrical shell; The catalyst urceolus is open near an end of gas feed, and the other end is connected with pressure-bearing shell; The sidewall of catalyst urceolus is provided with side opening; Described catalyst urceolus is between catalyst inner core and pressure-bearing shell, and described heat exchanger tube is between described catalyst urceolus and catalyst inner core.
Wherein, the side opening of catalyst inner core and/or catalyst urceolus should be according to concrete technological requirement perforate, and technical ability can satisfy the gas communication needs again when keeping catalyst.
Wherein, the catalyst inner core can arrange one, also can be set to a plurality of.
Preferably, the side in the close gas feed of catalyst fill area is provided with a pressure layer part.
Preferably, be provided with support member at the catalyst fill area away from the opposite side of gas feed.
Preferably, described support member is used inert ball for supporting; Described pressure layer part is for pressing layer inert ball.
Preferably, after the two ends of described heat exchanger tube were drawn in respectively and formed a pipe, import was connected with heat transferring medium with described heat transferring medium outlet respectively.
Preferably, draw in respectively with after tube sheet is fixedlyed connected at the two ends of described heat exchanger tube, forms a pipe, and import is connected with heat transferring medium with described heat transferring medium outlet respectively.
Further preferably, draw in respectively with after tube sheet is fixedlyed connected at the two ends of described heat exchanger tube, and import is connected with heat transferring medium with described heat transferring medium outlet respectively by bobbin carriage.
Wherein, the quantity of described heat exchanger tube is decided according to process requirements; Gap between adjacent two heat exchanger tubes is according to process requirements and catalyst particle size and decide.
Preferably, heat exchanger tube is divided into two parts at least, after the two ends of each part heat exchanger tube were drawn in respectively and formed a pipe, import was connected with heat transferring medium with described heat transferring medium outlet respectively.
Preferably, draw in respectively with after tube sheet is fixedlyed connected at the two ends of each part heat exchanger tube, forms a pipe, and import is connected with heat transferring medium with described heat transferring medium outlet respectively.
Further preferably, draw in respectively with after tube sheet is fixedlyed connected at the two ends of each part heat exchanger tube, and import is connected with heat transferring medium with described heat transferring medium outlet respectively by bobbin carriage.
Wherein, the quantity of described tube sheet should be according to the scale of equipment, heat exchanger tube quantity, and drum arranges and requires to wait to take all factors into consideration.
Wherein, the quantity of tube sheet is 2 multiple, is at least 2, preferably, is at least 4, preferably, is at least 6, more preferably, is at least 8.
Preferably, described catalyst inner core is segmental structure, so that maintenance or loading catalyst.
Preferably, two of adjacent connection catalyst inner core segmentations connect by fastener.Described fastener comprises movable fastener portion and attachment fastener portion.By the order away from gas feed, the segmentation of adjacent two catalyst inner cores is divided into higher level's segmentation and subordinate's segmentation, described movable fastener portion and attachment fastener portion are positioned at respectively in higher level's segmentation and the subordinate's segmentation, and perhaps described movable fastener portion and attachment fastener portion are positioned at respectively in subordinate's segmentation and the higher level's segmentation.Described movable fastener portion comprises spiro union portion, kink and support portion, described spiro union portion and support portion are fixed on its two ends perpendicular to described kink respectively and branch is in its both sides, described spiro union portion and described attachment fastener portion are provided with the screw that is complementary, by bolt, described spiro union portion is removably fixed to described attachment fastener portion.
Preferably, the syndeton of concavo-convex butt joint is arranged in two of adjacent connection catalyst inner core segmentations.For example by the order away from gas feed, the segmentation of adjacent two catalyst inner cores is divided into higher level's segmentation and subordinate's segmentation, and the end that higher level's segmentation is established annular groove, the close higher level's segmentation of subordinate's segmentation near an end of subordinate's segmentation is provided with the bulge loop that docks with the annular groove of higher level's segmentation; Perhaps an end of the close subordinate of higher level's segmentation segmentation is established bulge loop, subordinate's segmentation is provided with the annular groove that docks with the bulge loop of higher level's segmentation near an end of higher level's segmentation.Preferably, the syndeton of latch and pin hole butt joint is arranged in the segmentation of adjacent two catalyst inner cores.For example by the order away from gas feed, the segmentation of adjacent two catalyst inner cores is divided into higher level's segmentation and subordinate's segmentation, and the end that higher level's segmentation is established pin hole, the close higher level's segmentation of subordinate's segmentation near an end of subordinate's segmentation is provided with the latch that docks with the pin hole of higher level's segmentation; Perhaps an end of the close subordinate of higher level's segmentation segmentation is established latch, subordinate's segmentation is provided with the pin hole that docks with the latch of higher level's segmentation near an end of higher level's segmentation.
Preferably, in the catalyst fill area, be filled with catalyst.
Preferably, described catalyst is preferably pellet type catalyst, at least a in sheet catalyst and the bulk catalyst etc.
Wherein, described heat exchanger tube can be arranged by modes such as triangle, square or circular concentric.
Wherein, can also be provided with other the auxiliary mouth of pipe of necessity on the described pressure-bearing shell, as thermocouple port etc.
Wherein, the material of upper cover, low head and cylindrical shell is comprehensively chosen according to technological temperature, pressure, dielectric property etc.For example, when isothermal fixed bed reactors described in the utility model were applied to the Coal Chemical Industry sulfur resistant conversion process, the inwall of upper cover, low head and cylindrical shell was lined with stainless steel lining.
The utility model provides is loaded on catalyst isothermal fixed bed reactors between the heat exchanger tube, and catalyst is filled between heat exchanger tube, and loaded catalyst is big; Heat exchanger tube can be removed reaction heat rapidly, and whole bed reaches equal temp effect substantially, and overtemperature is not difficult for taking place side reaction.And the utility model can make reaction gas be a radial flow in bed, can utilize catalyst to greatest extent, and can use active higher catalyst particle.
Description of drawings
Fig. 1 is the structural representation of embodiment 1 described isothermal fixed bed reactors;
Fig. 2 is the A-A sectional view of Fig. 1;
Fig. 3 is the B-B sectional view of Fig. 1;
Fig. 4 is the structural representation of embodiment 2 described isothermal fixed bed reactors.
The specific embodiment
With reference to the accompanying drawings, the utility model is further described in conjunction with specific embodiments, to understand the utility model better.
With reference to Fig. 1,2 and 3, a kind of catalyst is loaded on isothermal fixed bed reactors between the heat exchanger tube, be axial-radial flow reactor, comprise pressure-bearing shell, be installed in heat exchanger tube 1 and catalyst cylindrical shell in the pressure-bearing shell.
Pressure-bearing shell comprises upper cover 2, low head 3, cylindrical shell 4; Upper cover 2 is connected with the welded top of cylindrical shell 4, offers gas feed 21 and heat transferring medium outlet 22 at upper cover 2; Low head 3 is welded to connect with the bottom of cylindrical shell 4, offers gas vent 31, heat transferring medium import 32 and catalyst discharge port 33 at low head 3.
The catalyst cylindrical shell comprises catalyst urceolus 7 and catalyst inner core 8; Form annular space 71 between the inwall of the sidewall of catalyst urceolus 7 and cylindrical shell 4; The open-top of catalyst urceolus 7, the bottom is connected with pressure-bearing shell; Catalyst inner core 8 top seals are connected with gas vent 31; Be provided with side opening according to arts demand on the sidewall of catalyst urceolus 7 and catalyst inner core 8.
Wherein, behind the catalyst filling, appoint between the catalyst and have the space, the space between gas feed, the catalyst and gas vent form gas passage.
During use, reaction gas enters in the pressure-bearing shell from gas feed, the annular space that forms along the inwall of catalyst urceolus and pressure-bearing shell radially enters beds, partial reaction gas is by pressing layer inert ball simultaneously, from the top axle of catalyst urceolus to entering beds, behind catalyst bed reaction, gas is collected through the catalyst inner core, finally discharges from gas vent.Wherein, beds by catalyst urceolus, catalyst inner core, heat exchanger tube, fill in the catalyst between heat exchanger tube and support with inert ball and press layer inert ball etc. to form, be the core of whole reactor.Boiler feedwater then by the heat transferring medium import in lower tube box enters heat exchanger tube, transform to give saturated vapor after the absorption reaction heat, discharge from the heat transferring medium outlet at top through the upper tube box on top.
With reference to Fig. 4, a kind of catalyst is loaded on isothermal fixed bed reactors between the heat exchanger tube, be axial flow reactor, comprise pressure-bearing shell, be installed in heat exchanger tube 1 and catalyst cylindrical shell in the pressure-bearing shell.
Pressure-bearing shell comprises upper cover 2, low head 3, cylindrical shell 4; Upper cover 2 is connected with the welded top of cylindrical shell 4, offers gas feed 21 and heat transferring medium outlet 22 at upper cover 2; Low head 3 is welded to connect with the bottom of cylindrical shell 4, offers gas vent 31, heat transferring medium import 32 and catalyst discharge port 33 at low head 3.
The catalyst cylindrical shell comprises catalyst inner core 8, and wherein, pressure-bearing shell directly constitutes the catalyst urceolus of catalyst cylindrical shell; Catalyst inner core 8 top seals are connected with gas vent 31; Be provided with side opening according to arts demand on the sidewall of catalyst inner core 8.
Wherein, behind the catalyst filling, appoint between the catalyst and have the space, the space between gas feed, the catalyst and gas vent form gas passage.
During use, reaction gas enters in the pressure-bearing shell from gas feed, through overvoltage layer inert ball, axially enters beds, and the gas behind catalyst bed reaction is collected through the catalyst inner core, finally discharges from gas vent.Wherein, beds by pressure-bearing shell, catalyst inner core, heat exchanger tube, fill in the catalyst between heat exchanger tube and support with inert ball and top and press layer inert ball etc. to form, be the core of whole reactor.Boiler feedwater then by the heat transferring medium import in lower tube box enters heat exchanger tube, transform to give saturated vapor after the absorption reaction heat, discharge from the heat transferring medium outlet at top through the upper tube box on top.
More than specific embodiment of the utility model is described in detail, but it is just as example, the utility model is not restricted to specific embodiment described above.To those skilled in the art, any equivalent modifications that the utility model is carried out and substituting also all among category of the present utility model.Therefore, not breaking away from impartial conversion and the modification of doing under the spirit and scope of the present utility model, all should be encompassed in the scope of the present utility model.
Claims (10)
1. one kind is loaded on isothermal fixed bed reactors between the heat exchanger tube with catalyst, it is characterized in that, comprises pressure-bearing shell, is installed in a plurality of heat exchanger tubes in the pressure-bearing shell;
Be provided with gas feed, heat transferring medium outlet, gas vent, heat transferring medium import and catalyst discharge port at described pressure-bearing shell;
Import is connected with heat transferring medium with described heat transferring medium outlet respectively at the two ends of described heat exchanger tube;
Exist the space to form the catalyst fill area between described a plurality of heat exchanger tube, and space and gas vent between the gas feed, heat exchanger tube form gas passage.
2. isothermal fixed bed reactors according to claim 1 is characterized in that, described heat transferring medium import and gas vent are positioned at the same end of pressure-bearing shell; Described gas feed and heat transferring medium outlet are positioned at the other end of pressure-bearing shell.
3. isothermal fixed bed reactors according to claim 1 is characterized in that, also comprise the catalyst inner core; Described catalyst inner core is near the end sealing of gas feed, and the other end is connected with gas vent; The sidewall of catalyst inner core is provided with side opening; Described heat exchanger tube is between described catalyst inner core and pressure-bearing shell.
4. isothermal fixed bed reactors according to claim 3 is characterized in that, also comprise the catalyst urceolus; Form the gap between the sidewall of described catalyst urceolus and the inwall of cylindrical shell; The catalyst urceolus is open near an end of gas feed, and the other end is connected with pressure-bearing shell; The sidewall of catalyst urceolus is provided with side opening; Described catalyst urceolus is between catalyst inner core and pressure-bearing shell, and described heat exchanger tube is between described catalyst urceolus and catalyst inner core.
5. according to claim 1,2,3 or 4 described isothermal fixed bed reactors, it is characterized in that be provided with near a side of gas feed at the catalyst fill area and press a layer part, opposite side is provided with support member.
6. the isothermal diameter of axle according to claim 5 is characterized in that to fixed bed reactors, and described pressure layer part is for pressing layer inert ball; Described support member is used inert ball for supporting.
7. according to claim 1,2,3 or 4 described isothermal fixed bed reactors, it is characterized in that draw in respectively with after tube sheet is fixedlyed connected at the two ends of described heat exchanger tube, forms a pipe, import is connected with heat transferring medium with described heat transferring medium outlet respectively.
8. isothermal fixed bed reactors according to claim 7 is characterized in that, draw in respectively with after tube sheet is fixedlyed connected at the two ends of described heat exchanger tube, and import is connected with heat transferring medium with described heat transferring medium outlet respectively by bobbin carriage.
9. isothermal fixed bed reactors according to claim 3 is characterized in that, described catalyst inner core is segmental structure.
10. isothermal fixed bed reactors according to claim 1 is characterized in that, are filled with catalyst in the catalyst fill area.
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| Application Number | Priority Date | Filing Date | Title |
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| CN 201320176372 CN203227477U (en) | 2013-04-09 | 2013-04-09 | Constant-temperature fixed-bed reactor for filling catalysts among heat exchange tubes |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104096514A (en) * | 2013-04-09 | 2014-10-15 | 上海国际化建工程咨询公司 | Isothermal fixed bed reactor loading catalyst among heat exchange tubes |
| CN104923130A (en) * | 2014-03-21 | 2015-09-23 | 中石化洛阳工程有限公司 | Radial fixed bed reactor and application thereof in preparing hydrocarbon from oxygenated compounds |
| CN105399604A (en) * | 2015-10-12 | 2016-03-16 | 上海国际化建工程咨询公司 | Energy-efficient super-large scale methanol-synthesizing method with production of steam of different grades and apparatus thereof |
| CN105457563A (en) * | 2014-09-09 | 2016-04-06 | 航天长征化学工程股份有限公司 | Isothermal shift reactor with built-in tube bundle |
| CN105561889A (en) * | 2014-10-23 | 2016-05-11 | 新煤化工设计院（上海）有限公司 | Radial flow by-product steam isothermal shift converter |
| CN105582855A (en) * | 2014-10-23 | 2016-05-18 | 新煤化工设计院（上海）有限公司 | Radial-flow uniform-temperature methanation furnace with byproduct steam |
| CN109603689A (en) * | 2018-12-26 | 2019-04-12 | 湖南安淳高新技术有限公司 | Axial-radial flow reactor |
-
2013
- 2013-04-09 CN CN 201320176372 patent/CN203227477U/en not_active Expired - Fee Related
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104096514A (en) * | 2013-04-09 | 2014-10-15 | 上海国际化建工程咨询公司 | Isothermal fixed bed reactor loading catalyst among heat exchange tubes |
| CN104096514B (en) * | 2013-04-09 | 2018-01-30 | 上海国际化建工程咨询公司 | A kind of isothermal fixed bed reactors that catalyst is loaded between heat exchanger tube |
| CN104923130A (en) * | 2014-03-21 | 2015-09-23 | 中石化洛阳工程有限公司 | Radial fixed bed reactor and application thereof in preparing hydrocarbon from oxygenated compounds |
| CN105457563A (en) * | 2014-09-09 | 2016-04-06 | 航天长征化学工程股份有限公司 | Isothermal shift reactor with built-in tube bundle |
| CN105561889A (en) * | 2014-10-23 | 2016-05-11 | 新煤化工设计院（上海）有限公司 | Radial flow by-product steam isothermal shift converter |
| CN105582855A (en) * | 2014-10-23 | 2016-05-18 | 新煤化工设计院（上海）有限公司 | Radial-flow uniform-temperature methanation furnace with byproduct steam |
| CN105399604A (en) * | 2015-10-12 | 2016-03-16 | 上海国际化建工程咨询公司 | Energy-efficient super-large scale methanol-synthesizing method with production of steam of different grades and apparatus thereof |
| CN109603689A (en) * | 2018-12-26 | 2019-04-12 | 湖南安淳高新技术有限公司 | Axial-radial flow reactor |
| CN109603689B (en) * | 2018-12-26 | 2021-08-31 | 湖南安淳高新技术有限公司 | Axial radial reactor |
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| C14 | Grant of patent or utility model | ||
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| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20131009 Termination date: 20180409 |