CN104096514A - Isothermal fixed bed reactor loading catalyst among heat exchange tubes - Google Patents
Isothermal fixed bed reactor loading catalyst among heat exchange tubes Download PDFInfo
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- CN104096514A CN104096514A CN201310122373.1A CN201310122373A CN104096514A CN 104096514 A CN104096514 A CN 104096514A CN 201310122373 A CN201310122373 A CN 201310122373A CN 104096514 A CN104096514 A CN 104096514A
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Abstract
The invention provides an isothermal fixed bed reactor loading a catalyst among heat exchange tubes, and the isothermal fixed bed reactor comprises a pressure-bearingg casing, the plurality of heat exchange tubes installed in the pressure-bearing casing, and the catalyst; gaps among the plurality of heat exchange tubes form a catalyst filling zone, and a gas inlet, the gaps among the plurality of heat exchange tubes and a gas outlet form a gas channel. The isothermal fixed bed reactor loads the catalyst among the plurality of heat exchange tubes, the catalyst loading quantity is large; the heat exchange tubes can quickly remove the reaction heat, the whole bed basically reaches the even temperature effect and is free of excess temperature and occurrence of side reactions, and the isothermal fixed bed reactor enables a reaction gas to axially radially flow in the bed, can maximize the use of the and can use a more active small particle catalyst.
Description
Technical field
The present invention relates to a kind of isothermal fixed bed reactors, relate in particular to and a kind of catalyst is loaded on to the isothermal fixed bed reactors between heat exchanger tube, this isothermal fixed reactor can be axial-radial flow reactor, pure axial flow reactor or pure radial reactor.
Background technology
Along with the development of Chemical Manufacture, for adapting to different heat transfer requirement and heat transfer type, there is the version of multiple fixed bed reactors, wherein, especially to utilize the reaction mass of gaseous state, the gas solid catalytic reactor reacting by the bed being made up of solid catalyst is most widely used in Chemical Manufacture.
Fixed bed reactors are mainly divided into heat-insulating and the large class of heat exchange type two reaction principle.
Heat-insulating fixed bed reactors are simple in structure, are widely used.But in practical operation, adiabatic reactor can not reach very high efficiency, mainly contains the restriction of two aspects: the 1. restriction of chemical balance; For exothermic reaction, temperature is higher, is more unfavorable for that reaction tends to balance, and reduces temperature and can reduce reaction rate; 2. reaction temperature rising makes reaction bed temperature far beyond the catalyst scope of application, can cause the active component clinkering of catalyst surface, and specific area significantly declines, active decline, and side reaction aggravation, even causes temperature runaway, damage equipment; So for heat release type catalyst reaction device, reach darker reaction, conventionally adopt multistage band heat exchange type adiabatic reactor technique, flow process is tediously long, heat-exchange network complexity, pining down of Shou Quan factory energy balance, larger for load fluctuation and unstripped gas component variable effect, be unfavorable for device safe operation steady in a long-term.
Isothermal reactor is removed reaction heat in time by heat exchange element, keeps the basic constant temperature of bed, and its major advantage is: 1. isothermal operation makes real reaction temperature curve approach maximum reaction rate curve, greatly improves reaction rate, and reaction is tended to balance; 2. isothermal reaction provides gentle running environment to catalyst, thereby has extended the life-span 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, by regulating byproduct steam pressure can effectively control reaction bed temperature; 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 features such as device maximization, Coal Gasification Technology diversification, the use of isothermal reactor, or the requirement that use can more adapt to some technique of combining of isothermal reactor and adiabatic reactor.
Isothermal reactor is divided into again axial flow reactor and radial reactor.In prior art, conventional axial isothermal reactor form is shell and tube isothermal reactor, and Catalyst packing is in heat exchanger tube, and reaction gas flows vertically in pipe, and the steam of shell-side is removed reaction heat 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 although met reversible exothermic reaction, simultaneously can also by-product middle pressure steam, but, because the restriction of reactor diameter, is subject to certain restrictions its production capacity.Radial reactor is because catalyst loading amount is large, 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 is mainly the centrifugal radial flow reactor adopting from inside to outside, although loaded catalyst is large, but the catalytic amount that Radial Flow reacting gas flows through is also little, if gas purification is bad, more easily cause catalysqt deactivation.
Summary of the invention
The object of the invention is to overcome above-mentioned deficiency, provide a kind of catalyst is loaded on to the isothermal fixed bed reactors between heat exchanger tube, can effectively keep reaction bed temperature evenly constant, maximally utilise catalyst.
The invention provides and a kind of catalyst is loaded on to the isothermal fixed bed reactors between heat exchanger tube, comprise pressure-bearing shell, be arranged on the multiple heat exchanger tubes in pressure-bearing shell;
On described pressure-bearing shell, be provided with gas feed, heat transferring medium outlet, gas vent, heat transferring medium import and catalyst discharge port;
Import is connected with heat transferring medium with described heat transferring medium outlet respectively at the two ends of described heat exchanger tube;
Between described multiple heat exchanger tube, exist space to form catalyst fill area, and space and gas vent between 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, described heat transferring medium import and heat transferring medium outlet lay respectively at the two ends of pressure-bearing shell.
Preferably, heat transferring medium import and gas vent are positioned at same one 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 same one 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 fixedly connected with one end of cylindrical shell, and low head is fixedly 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, being fixedly connected with mode can be welding etc.
Preferably, described isothermal fixed bed reactors also comprise catalyst inner core; Described catalyst inner core is near one 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 when use, reaction gas axially enters beds, and the gas after catalyst bed reaction is collected through catalyst inner core, finally discharges from gas vent.
Preferably, described isothermal fixed bed reactors also comprise catalyst urceolus; Between the sidewall of described catalyst urceolus and the inwall of cylindrical shell, form gap; Catalyst urceolus is open near one 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 meet again gas communication needs when keeping catalyst.
Wherein, catalyst inner core can arrange one, also can be set to multiple.
Preferably, be provided with and press layer part near a side of gas feed at catalyst fill area.
Preferably, be provided with support member at catalyst fill area away from the opposite side of gas feed.
Preferably, described support member is support inert ball; Described pressure layer part is for pressing layer inert ball.
Preferably, the two ends of described heat exchanger tube are drawn in respectively and are formed after a pipe, and import is connected with heat transferring medium with described heat transferring medium outlet respectively.
Preferably, after the two ends of described heat exchanger tube are drawn in respectively and are fixedly connected with tube sheet, form a pipe, import is connected with heat transferring medium with described heat transferring medium outlet respectively.
Further preferably, after the two ends of described heat exchanger tube are drawn in respectively and are fixedly connected with tube sheet, by bobbin carriage, import is connected with heat transferring medium with described heat transferring medium outlet respectively.
Wherein, the quantity basis process requirements of described heat exchanger tube and determining; Gap between adjacent two heat exchanger tubes is according to process requirements and catalyst particle size and determine.
Preferably, heat exchanger tube is at least divided into two parts, the two ends of every a heat exchanger tube are drawn in respectively and are formed after a pipe, and import is connected with heat transferring medium with described heat transferring medium outlet respectively.
Preferably, after the two ends of every a heat exchanger tube are drawn in respectively and are fixedly connected with tube sheet, form a pipe, import is connected with heat transferring medium with described heat transferring medium outlet respectively.
Further preferably, after the two ends of every a heat exchanger tube are drawn in respectively and are fixedly connected with tube sheet, by bobbin carriage, import is connected with heat transferring medium with described heat transferring medium outlet respectively.
Wherein, the quantity of described tube sheet should be according to the scale of equipment, heat exchanger tube quantity, and drum arranges requirement etc. and considers.
Wherein, the multiple that the quantity of tube sheet is 2, 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 moving fastening 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 moving fastening portion and attachment fastener portion lay respectively in higher level's segmentation and subordinate's segmentation, or described moving fastening portion and attachment fastener portion lay respectively in subordinate's segmentation and higher level's segmentation.Described moving fastening portion comprises spiro union portion, kink and support portion, described spiro union portion and support portion are fixed on its two ends and divide in its both sides perpendicular to described kink respectively, described spiro union portion and described attachment fastener portion are provided with the screw matching, by bolt, described spiro union portion is removably fixed to described attachment fastener portion.
Preferably, two of adjacent connection catalyst inner core subsection setups become the syndeton of concavo-convex docking.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 higher level's segmentation is established annular groove, subordinate's segmentation near one end of subordinate's segmentation and is provided with the bulge loop docking with the annular groove of higher level's segmentation near one end of higher level's segmentation; Or higher level's segmentation is established bulge loop, subordinate's segmentation near one end of subordinate's segmentation and is provided with the annular groove docking with the bulge loop of higher level's segmentation near one end of higher level's segmentation.Preferably, the subsection setup of adjacent two catalyst inner cores becomes the syndeton of latch and pin hole docking.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 higher level's segmentation is established pin hole, subordinate's segmentation near one end of subordinate's segmentation and is provided with the latch docking with the pin hole of higher level's segmentation near one end of higher level's segmentation; Or higher level's segmentation is established latch, subordinate's segmentation near one end of subordinate's segmentation and is provided with the pin hole docking with the latch of higher level's segmentation near one end of higher level's segmentation.
Preferably, in catalyst fill area, be filled with catalyst.
Preferably, described catalyst is preferably pellet type catalyst, at least one in sheet catalyst and bulk catalyst etc.
Wherein, described heat exchanger tube can be arranged by modes such as triangle, square or circular concentric.
Wherein, on described pressure-bearing shell, can also be provided with other the auxiliary mouth of pipe of necessity, 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, in the time that isothermal fixed bed reactors of the present invention are applied to Coal Chemical Industry sulfur resistant conversion process, the inwall of upper cover, low head and cylindrical shell is lined with stainless steel lining.
Provided by the invention catalyst is loaded on to the isothermal fixed bed reactors between heat exchanger tube, by Catalyst packing, between heat exchanger tube, loaded catalyst is large; Heat exchanger tube can be removed reaction heat rapidly, and whole bed reaches even temperature effect substantially, and not overtemperature is difficult for occurring side reaction.And the present invention can make reaction gas be axle radial flow in bed, can utilize to greatest extent catalyst, and can use active higher catalyst particle.
Brief description of the drawings
Fig. 1 is the structural representation of isothermal fixed bed reactors described in embodiment 1;
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 isothermal fixed bed reactors described in embodiment 2.
Detailed description of the invention
With reference to the accompanying drawings, in conjunction with specific embodiments the present invention is further described, to understand better the present invention.
Embodiment 1
With reference to Fig. 1,2 and 3, a kind of catalyst is loaded on to the isothermal fixed bed reactors between heat exchanger tube, be axial-radial flow reactor, comprise pressure-bearing shell, be arranged on heat exchanger tube 1 and catalyst cylindrical shell in 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 on upper cover 2; Low head 3 is connected with the bottom welding of cylindrical shell 4, offers gas vent 31, heat transferring medium import 32 and catalyst discharge port 33 on low head 3.
Heat exchanger tube 1 two is drawn in and is welded in respectively on tube sheet 5, communicates respectively with upper tube box 61 and lower tube box 62, and upper tube box 61 is connected with heat transferring medium outlet 22, and lower tube box 62 is connected with heat transferring medium import 32;
Catalyst cylindrical shell comprises catalyst urceolus 7 and catalyst inner core 8; Between the inwall of the sidewall of catalyst urceolus 7 and cylindrical shell 4, form annular space 71; The open-top of catalyst urceolus 7, bottom is connected with pressure-bearing shell; Catalyst inner core 8 top seals, are connected with gas vent 31; On the sidewall of catalyst urceolus 7 and catalyst inner core 8, need to be provided with side opening according to technique.
Heat exchanger tube 1 is between catalyst urceolus 7 and catalyst inner core 8, and catalyst is filled between heat exchanger tube 1.Below the bottom of catalyst, be provided with support inert ball 91, be provided with and press a layer inert ball 92 on the top of catalyst, catalyst is filled in and supports in the space surrounding by inert ball 91, catalyst urceolus 7, catalyst inner core 8 and pressure layer inert ball 92.
Wherein, after catalyst filling, between catalyst, appoint and have space, the space between gas feed, catalyst and gas vent form gas passage.
When use, reaction gas enters in pressure-bearing shell from gas feed, the annular space forming 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, after catalyst bed reaction, gas is collected through catalyst inner core, finally discharges from gas vent.Wherein, beds by catalyst urceolus, catalyst inner core, heat exchanger tube, fill in catalyst between heat exchanger tube and support by inert ball and press layer inert ball etc. to form, be the core of whole reactor.Boiler feedwater by heat transferring medium import in lower tube box enters heat exchanger tube, after absorption reaction heat, transform to saturated vapor, discharge from the heat transferring medium outlet at top through the upper tube box on top.
Embodiment 2
With reference to Fig. 4, a kind of catalyst is loaded on to the isothermal fixed bed reactors between heat exchanger tube, be axial flow reactor, comprise pressure-bearing shell, be arranged on heat exchanger tube 1 and catalyst cylindrical shell in 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 on upper cover 2; Low head 3 is connected with the bottom welding of cylindrical shell 4, offers gas vent 31, heat transferring medium import 32 and catalyst discharge port 33 on low head 3.
Heat exchanger tube 1 two is drawn in and is welded in respectively on tube sheet 5, communicates respectively with upper tube box 61 and lower tube box 62, and upper tube box 61 is connected with heat transferring medium outlet 22, and lower tube box 62 is connected with heat transferring medium import 32.
Catalyst cylindrical shell comprises catalyst inner core 8, and wherein, pressure-bearing shell directly forms the catalyst urceolus of catalyst cylindrical shell; Catalyst inner core 8 top seals, are connected with gas vent 31; On the sidewall of catalyst inner core 8, need to be provided with side opening according to technique.
Heat exchanger tube 1 is between pressure-bearing shell and catalyst inner core 8, and catalyst is filled between heat exchanger tube 1.Below the bottom of catalyst, be provided with support inert ball 91, be provided with and press a layer inert ball 92 on the top of catalyst, catalyst is filled in and supports in the space surrounding by inert ball 91, pressure-bearing shell, catalyst inner core 8 and pressure layer inert ball 92.
Wherein, after catalyst filling, between catalyst, appoint and have space, the space between gas feed, catalyst and gas vent form gas passage.
When use, reaction gas enters in pressure-bearing shell from gas feed, through overvoltage layer inert ball, axially enters beds, and the gas after catalyst bed reaction is collected through catalyst inner core, finally discharges from gas vent.Wherein, beds by pressure-bearing shell, catalyst inner core, heat exchanger tube, fill in 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 by heat transferring medium import in lower tube box enters heat exchanger tube, after absorption reaction heat, transform to saturated vapor, discharge from the heat transferring medium outlet at top through the upper tube box on top.
Above specific embodiments of the invention be have been described in detail, but it is just as example, the present invention is not restricted to specific embodiment described above.To those skilled in the art, any equivalent modifications that the present invention is carried out and alternative also all among category of the present invention.Therefore, equalization conversion and the amendment done without departing from the spirit and scope of the invention, all should contain within the scope of the invention.
Claims (10)
1. catalyst is loaded on to the isothermal fixed bed reactors between heat exchanger tube, it is characterized in that, comprise pressure-bearing shell, be arranged on the multiple heat exchanger tubes in pressure-bearing shell;
On described pressure-bearing shell, be provided with gas feed, heat transferring medium outlet, gas vent, heat transferring medium import and catalyst discharge port;
Import is connected with heat transferring medium with described heat transferring medium outlet respectively at the two ends of described heat exchanger tube;
Between described multiple heat exchanger tube, exist space to form catalyst fill area, and space and gas vent between 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 same one 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 catalyst inner core; Described catalyst inner core is near one 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 catalyst urceolus; Between the sidewall of described catalyst urceolus and the inwall of cylindrical shell, form gap; Catalyst urceolus is open near one 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 the isothermal fixed bed reactors described in claim 1,2,3 or 4, it is characterized in that, be provided with and press layer part near a side of gas feed at catalyst fill area, opposite side is provided with support member.
6. isothermal axle radial fixed-bed reactor according to claim 5, is characterized in that, described pressure layer part is for pressing layer inert ball; Described support member is support inert ball.
7. according to the isothermal fixed bed reactors described in claim 1,2,3 or 4, it is characterized in that, after the two ends of described heat exchanger tube are drawn in respectively and are fixedly connected with tube sheet, form 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, after the two ends of described heat exchanger tube are drawn in respectively and are fixedly connected with tube sheet, by bobbin carriage, import is connected with heat transferring medium with described heat transferring medium outlet respectively.
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, in catalyst fill area, are filled with catalyst.
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| CN104689767A (en) * | 2015-03-26 | 2015-06-10 | 南通华兴石油仪器有限公司 | Catalytic reaction vessel |
| CN105797650A (en) * | 2016-05-24 | 2016-07-27 | 华烁科技股份有限公司 | Fixed-bed catalytic temperature-control reactor with headers |
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| CN115414872A (en) * | 2022-08-11 | 2022-12-02 | 安徽润衍科技有限公司 | Tubular isothermal reactor and process for producing 1,2-pentanediol from 1, 2-cyclopentane oxide |
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| CN105797650A (en) * | 2016-05-24 | 2016-07-27 | 华烁科技股份有限公司 | Fixed-bed catalytic temperature-control reactor with headers |
| CN105833802A (en) * | 2016-05-27 | 2016-08-10 | 成都赛普瑞兴科技有限公司 | Steam rising type catalyst bed reactor |
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| CN108421505A (en) * | 2018-05-22 | 2018-08-21 | 中石化宁波工程有限公司 | A kind of radial-axial combined reactor suitable for strong exothermal reaction |
| CN108421505B (en) * | 2018-05-22 | 2024-04-12 | 中石化宁波工程有限公司 | Radial-axial combined reactor suitable for strong exothermic reaction |
| CN108993370A (en) * | 2018-10-18 | 2018-12-14 | 辽宁石油化工大学 | A kind of spiral coil isothermal reactor and its application method |
| CN108993370B (en) * | 2018-10-18 | 2021-01-12 | 辽宁石油化工大学 | Spiral coil isothermal reactor and use method thereof |
| WO2022062129A1 (en) * | 2020-09-28 | 2022-03-31 | 江苏永大化工机械有限公司 | Multi-pass radial reactor |
| CN115414872A (en) * | 2022-08-11 | 2022-12-02 | 安徽润衍科技有限公司 | Tubular isothermal reactor and process for producing 1,2-pentanediol from 1, 2-cyclopentane oxide |
| CN115414872B (en) * | 2022-08-11 | 2023-11-03 | 安徽润衍科技有限公司 | Tubular isothermal reactor and method for producing 1,2-pentanediol from 1, 2-epoxypentane |
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