CN103585933A - Corrugated board type uniform-temperature hydrogenation reactor - Google Patents
Corrugated board type uniform-temperature hydrogenation reactor Download PDFInfo
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- CN103585933A CN103585933A CN201310604127.XA CN201310604127A CN103585933A CN 103585933 A CN103585933 A CN 103585933A CN 201310604127 A CN201310604127 A CN 201310604127A CN 103585933 A CN103585933 A CN 103585933A
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Abstract
A corrugated board type uniform-temperature hydrogenation reactor is characterized by comprising an annular upper header pipe (5), a catalyst bed layer (6), corrugated boards (7), a lower inlet (8), an annular lower header pipe (9), a cylinder (14) and an upper outlet (16). The corrugated board type uniform-temperature hydrogenation reactor breaks through a multi-section heat-insulation cold-shock heat-transfer structure which is used in the prior art all along, and adopts a corrugated board heat-transfer structure. The corrugated board heat-transfer structure is more beneficial to heat transfer and the mixing of gas phase, liquid phase and solid phase, and allows a reaction to occur uniformly and efficiently. Moreover, the corrugated board type uniform-temperature hydrogenation reactor overcomes the defects that the adiabatic temperature rise (Delta t=50-200 DEG C) of a traditional reactor is high and control over the reaction temperature is difficult; the temperature of the overall bed layer is regulated by the temperature, pressure and flow rate of a cold flow system in the corrugated boards, and can be effectively controlled within the range of Delta t=50 DEG C; the temperature regulation is simple and stable; the over-temperature phenomena of the reaction bed layer are completely eliminated.
Description
Technical field
The present invention relates to hydrogenation reactor technical field, especially a kind of corrugated plate dst samming hydrogenation reactor.
Background technology
Tradition hydrogenation reactor mainly contains fixed bed, thermopnore, fluid bed three major types, what wherein fixed bed reactors adopted is maximum, as shown in Figure 1, it is actually the adiabatic reactor being comprised of a plurality of beds, it is cooling that its a large amount of reaction heat is introduced Quench by cooling medium (gas or liquid) from interlayer, when removing a large amount of reaction heat, each bed temperature is controlled in certain temperature rise (as 50～100 ℃) scope.The shortcoming of this class reactor is: the temperature rise of (1) beds can not be strict controlled in the suitableeest scope, easily makes catalyst burning affect its life-span, or not at best warm area, affects quality and the output of product; (2) reaction heat is by the direct Quench of cold medium adding, so its reaction heat can not fully reclaim.
Also there is in the recent period patent to propose employing catalyst as shown in Figure 2 at tube side, water is in the shell-and-tube water-cooled reactor of shell side, solve the problem that above-mentioned hydrogenation reactor exists, but its shortcoming is: (1) apparatus with catalyst inside reaction tube quantity is many, make the gas phase of hydrogenation reactor and liquid phase evenly enter every pipe difficult, thus the efficiency of impact reaction; (2) because tube side and shell side temperature differ (especially under strong heat release condition), solve its thermal stress, at shell side, be provided with expansion joint, this not only improves equipment manufacturing cost, increases insecurity, nor is beneficial to the maximization of equipment.
Because reaction tube is smooth tube wall, will inevitably there is certain fluid " wall short-circuiting effect ", also affect the abundant catalytic chance of fluid and catalyst, this also just must affect the efficiency of catalyst reaction.
Summary of the invention
The object of the present invention is to provide a kind of corrugated plate dst samming hydrogenation reactor, to overcome above-mentioned defect, reach and improve catalyst life, raising reaction efficiency texts.
Technical scheme of the present invention is:
A kind of corrugated plate dst samming hydrogenation reactor, comprise upper header endless tube 5, beds 6, corrugated plating 7, bottom entrance 8, lower collecting box endless tube 9, cylindrical shell 14 and top outlet 16, described beds 6 is arranged in cylindrical shell 14, upper header endless tube 5 and lower collecting box endless tube 9 are arranged on respectively the upper and lower of cylindrical shell 14, between upper header endless tube 5 and lower collecting box endless tube 9, by the cooling medium interlayer being formed by some corrugated platings 7, be communicated with, in the cooling medium interlayer that corrugated plating 7 forms, cooling medium is housed, corrugated plating 7 is placed in beds 6, upper header endless tube 5 is connected with bottom entrance 8 with top outlet 16 respectively with lower collecting box endless tube 9.
Described cylindrical shell 14 tops are provided with upper entrance 1, and upper entrance 1 below is provided with disperser 2, and disperser 2 belows are provided with distribution cap 3 and gas-liquid distribution grid 4.
The described cooling medium interlayer consisting of some corrugated platings 7 is communicated with and gathers with upper header endless tube 5 and lower collecting box endless tube 9 by some short tubes 15 respectively.
Described cylindrical shell 14 bottoms are provided with bottom set cover 12, and set cover 12 belows, bottom are outlet 10.
Described cylindrical shell 14 bottoms are provided with catalyst self-unloading hole 11, and cylindrical shell 14 tops are provided with manhole 17.
Described corrugated plating 7 is arranged on cylindrical shell 14 inside by support 13.
The invention has the beneficial effects as follows:
1, corrugated plate dst samming hydrogenation reactor breakthrough of the present invention consistent multistage insulation reaction structure and the intersegmental cold shock of using in the past moves heat structure, change traditional reactor adiabatic temperature rise high (Δ t=50～200 ℃), the unmanageable shortcoming of reaction temperature, adopt corrugated plate dst samming hydrogenation reactor of the present invention, the temperature of whole bed is regulated by temperature, pressure and the flow of cold flow system makes in corrugated plating, can effectively be controlled within Δ t=50 ℃, temperature regulates steadily simple, stops the overheating problem of reaction bed completely.
2, corrugated plate dst samming hydrogenation reactor of the present invention adopts corrugated plating as cooling unit (catalyst is loaded between plate), and its advantage is:
(1) corrugated plating, due to the concavo-convex waveform on its surface, has increased the turbulent perturbation of fluid at plate surface and catalyst body, thereby has conducted heat and improve heat transfer coefficient 15～30% compared with general closed planar, has also strengthened 15～30% the heat energy power of moving.
(2) concavo-convex due to corrugated plating face, make fluid constantly expand and dwindle, constantly change the direction of fluid, thereby reduced " the wall short-circuiting effect " of fluid, increased contacting and disturbance of fluid and catalyst, improved the efficiency of reaction and the utilization rate of catalyst, this advantage is particularly favourable for gas-solid-liquid three-phase hydrogenation reaction.
(3) because the shared volume of corrugated plating is little, the reactor consisting of it increases by 10～20% than the loaded catalyst of other tubular reactors, and sheet material price is low than tubing price, after therefore multiple favorable factor stack, the cost of corrugated plate dst samming hydrogenation reactor of the present invention is low by 20～30% than the cost of other same energy yielding reaction devices.
3, adopt reactor head distribution grid 13 and distribution cap 14, effectively control gas phase and liquid phase well can be distributed to equably whole beds, make whole catalyst evenly effectively carry out hydrogenation reaction.
4, corrugated plate dst samming hydrogenation reactor of the present invention is broken through the shortcoming that a large amount of waste heats of reactor are difficult to utilization and reclaim in the past, corrugated plate dst samming hydrogenation reactor of the present invention can reclaim reaction heat and directly pay product medium-pressure or high pressure steam, pay producing steam amount according to reaction heat size, generally, at 0.5～5.0 ton of steam/ton product, greatly improved the economic benefit of operation.
Accompanying drawing explanation
Fig. 1 is the structural representation of fixed bed reactors in background technology.
Fig. 2 is the structural representation of shell-and-tube water-cooled reactor in background technology.
Fig. 3 is the structural representation of corrugated plate dst samming hydrogenation reactor of the present invention.
In Fig. 3: 1 upper entrance, 2 dispersers, 3 distribution caps, 4 gas-liquid distribution grids, 5 upper header endless tubes, 6 beds, 7 corrugated platings, 8 bottom entrances, 9 lower collecting box endless tubes, 10 outlets, 11 catalyst self-unloading holes, 12 bottom set covers, 13 supports, 14 cylindrical shells, 15 short tubes, 16 top outlets, 17 manholes.
The specific embodiment
Below in conjunction with accompanying drawing, the invention will be further described:
As Fig. 3, a kind of corrugated plate dst samming hydrogenation reactor, comprise upper header endless tube 5, beds 6, corrugated plating 7, bottom entrance 8, lower collecting box endless tube 9, cylindrical shell 14 and top outlet 16, described beds 6 is arranged in cylindrical shell 14, upper header endless tube 5 and lower collecting box endless tube 9 are arranged on respectively the upper and lower of cylindrical shell 14, between upper header endless tube 5 and lower collecting box endless tube 9, by the cooling medium interlayer being formed by some corrugated platings 7, be communicated with, in the cooling medium interlayer that corrugated plating 7 forms, cooling medium is housed, corrugated plating 7 is placed in beds 6, upper header endless tube 5 is connected with bottom entrance 8 with top outlet 16 respectively with lower collecting box endless tube 9.
The cooling medium interlayer consisting of some corrugated platings 7 is communicated with and gathers with upper header endless tube 5 and lower collecting box endless tube 9 by some short tubes 15 respectively.
Operation principle of the present invention and the course of work are as follows:
As shown in Figure 3, corrugated plate dst samming hydrogenation reactor of the present invention, mainly by the cylindrical shell 14 of catalyst being housed and cooling medium (as water etc.) corrugated plating 7 being housed, and the parts such as gas-liquid distribution grid 4, distribution cap 3 form.In corrugated plating, be connected with cooling agent (as water), by short tube 15, be connected with lower collecting box endless tube 9 with upper header endless tube 5, form and move hot cooling system, this system is by support 13 load-bearing.Hydrogenation reaction material is entered by upper entrance 1, through disperser 2, disperse, again through being arranged on the distribution grid 4 on cylindrical shell 14 and the distribution cap 3 being fixed thereon, fluid foods is distributed in equably on whole beds 6 and carries out hydrogenation reaction from top to bottom, and then reaction mass goes out reactor by bottom set cover 12 through outlet 10.Cooling fluid is entered by bottom entrance 8, through corrugated plating, removes drum from bottom to top by top outlet 16.On reactor top, end socket place is also provided with manhole 17, and bottom is provided with catalyst self-unloading hole 11.
The corrugated plate dst samming hydrogenation reactor scope of application of the present invention is in Table 1.
Table 1: the corrugated plate dst samming hydrogenation reactor scope of application
| Reaction temperature | 100～550℃ |
| Pressure | 0.1Mpa～12.0Mpa； |
| Disposal ability | 0.5 ten thousand tons/year～1,000,000 tons/year |
| Material | Hydrogen+gas gas-phase objects, ratio is any |
| ? | Hydrogen+liquid phase thing, ratio is any |
Adopt the application example of corrugated plate dst samming hydrogenation reactor of the present invention as follows:
[application example 1]
2.5MPa, the 50% oxalate methanol solution of 180 ℃ and 3.0MPa, 250 ℃ of hydrogen (mol ratio of hydrogen and oxalate is 50) are by gas-liquid distributor, the distribution cap of corrugated plate dst samming hydrogenation reactor, make the tube side of gas-liquid homogeneous media by reactor carry out catalytic hydrogenation reaction, obtain ethylene glycol (EG) product, catalytic hydrogenation reaction heat is taken away by the steam of this reactor shell side simultaneously.180～250 ℃ of uniform-temperature reactor tube side reaction temperatures, reaction pressure 2.0MPa; The saturated boiler water pressure of shell side 1.6～2.5MPa, 205～225 ℃ of temperature, 25 ℃ of reactor mean temperature differences, byproduct steam amount 4.5t/tEG, and oxalate conversion ratio is more than 97.5%, ethylene glycol yield reaches more than 95%, thereby shows that corrugated plate dst samming hydrogenation reactor distribution performance of the present invention is good, heat-transfer capability is strong.
[application example 2]
2.5MPa, the 50% oxalate methanol solution of 180 ℃ and 3.0MPa, 225 ℃ of hydrogen (mol ratio of hydrogen and oxalate is 100) are by gas-liquid distributor, the distribution cap of samming hydrogenation reactor, make the tube side of gas-liquid homogeneous media by reactor carry out catalytic hydrogenation reaction, obtain ethylene glycol (EG) product, catalytic hydrogenation reaction heat is taken away by the steam of this reactor shell side simultaneously.180～240 ℃ of uniform-temperature reactor tube side reaction temperatures, reaction pressure 2.0MPa; The saturated boiler water pressure of shell side 1.6～2.5MPa, 205～225 ℃ of temperature, 20 ℃ of reactor mean temperature differences, byproduct steam amount 4.0t/tEG, and oxalate conversion ratio is more than 98.5%, ethylene glycol yield reaches more than 96%, thereby shows that corrugated plate dst samming hydrogenation reactor distribution performance of the present invention is good, heat-transfer capability is strong.
[application example 3]
4.5MPa, the 60% oxalate methanol solution of 160 ℃ and 5.0MPa, 250 ℃ of hydrogen (mol ratio of hydrogen and oxalate is 50) are by gas-liquid distributor, the distribution cap of samming hydrogenation reactor, make the tube side of gas-liquid homogeneous media by reactor carry out catalytic hydrogenation reaction, obtain ethylene glycol (EG) product, catalytic hydrogenation reaction heat is taken away by the steam of this reactor shell side simultaneously.180～240 ℃ of uniform-temperature reactor tube side reaction temperatures, reaction pressure 4.0MPa; The saturated boiler water pressure of shell side 1.6～2.0MPa, 205～215 ℃ of temperature, 25 ℃ of reactor mean temperature differences, byproduct steam amount 4.2t/tEG, and oxalate conversion ratio is more than 98.0%, ethylene glycol yield reaches more than 95%, thereby shows that corrugated plate dst samming hydrogenation reactor distribution performance of the present invention is good, heat-transfer capability is strong.
[application example 4]
4.5MPa, the 60% oxalate methanol solution of 160 ℃ and 5.0MPa, 225 ℃ of hydrogen (mol ratio of hydrogen and oxalate is 100) are by gas-liquid distributor, the distribution cap of samming hydrogenation reactor, make the tube side of gas-liquid homogeneous media by reactor carry out catalytic hydrogenation reaction, obtain ethylene glycol (EG) product, catalytic hydrogenation reaction heat is taken away by the steam of this reactor shell side simultaneously.180～240 ℃ of uniform-temperature reactor tube side reaction temperatures, reaction pressure 4.0MPa; The saturated boiler water pressure of shell side 1.6～2.0MPa, 205～215 ℃ of temperature, 20 ℃ of reactor mean temperature differences, byproduct steam amount 4.0t/tEG, and oxalate conversion ratio is more than 98.5%, ethylene glycol yield reaches more than 95.5%, thereby shows that corrugated plate dst samming hydrogenation reactor distribution performance of the present invention is good, heat-transfer capability is strong.
Embodiment recited above is described the preferred embodiment of the present invention; not the spirit and scope of the present invention are limited; do not departing under design concept prerequisite of the present invention; various modification and improvement that in this area, common engineers and technicians make technical scheme of the present invention; all should fall into protection scope of the present invention, the technology contents that the present invention asks for protection is all documented in claims.
Claims (6)
1. a corrugated plate dst samming hydrogenation reactor, it is characterized in that comprising upper header endless tube (5), beds (6), corrugated plating (7), bottom entrance (8), lower collecting box endless tube (9), cylindrical shell (14) and top outlet (16), described beds (6) is arranged in cylindrical shell (14), upper header endless tube (5) and lower collecting box endless tube (9) are arranged on respectively the upper and lower of cylindrical shell (14), between upper header endless tube (5) and lower collecting box endless tube (9), by the cooling medium interlayer being formed by some corrugated platings (7), be communicated with, corrugated plating (7) is placed in beds (6), upper header endless tube (5) is connected with bottom entrance (8) with top outlet (16) respectively with lower collecting box endless tube (9).
2. a kind of corrugated plate dst samming hydrogenation reactor according to claim 1, it is characterized in that described cylindrical shell (14) top is provided with upper entrance (1), upper entrance (1) below is provided with disperser (2), and disperser (2) below is provided with distribution cap (3) and gas-liquid distribution grid (4).
3. a kind of corrugated plate dst samming hydrogenation reactor according to claim 1, is characterized in that the described cooling medium interlayer consisting of some corrugated platings (7) is communicated with and gathers with upper header endless tube (5) and lower collecting box endless tube (9) by some short tubes (15) respectively.
4. a kind of corrugated plate dst samming hydrogenation reactor according to claim 1, is characterized in that described cylindrical shell (14) bottom is provided with bottom set cover (12), and bottom set cover (12) below is outlet (10).
5. a kind of corrugated plate dst samming hydrogenation reactor according to claim 1, is characterized in that described cylindrical shell (14) bottom is provided with catalyst self-unloading hole (11), and cylindrical shell (14) top is provided with manhole (17).
6. a kind of corrugated plate dst samming hydrogenation reactor according to claim 1, is characterized in that described corrugated plating (7) is arranged on cylindrical shell (14) inside by support (13).
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104841339A (en) * | 2015-04-16 | 2015-08-19 | 中国五环工程有限公司 | Novel hydrogenation reactor for synthesis gas-to-ethylene glycol process |
| CN105032305A (en) * | 2015-08-27 | 2015-11-11 | 德艾柯工程技术（上海）有限公司 | Novel radial plate type reactor |
| CN106955645A (en) * | 2015-12-17 | 2017-07-18 | 乔治·克劳德方法的研究开发空气股份有限公司 | Reactor for performing heat release or the endothermic reaction |
| CN114307908A (en) * | 2022-01-19 | 2022-04-12 | 华中科技大学 | Device and method for synthesizing liquid fuel through carbon dioxide multi-field concerted catalytic hydrogenation |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101993349A (en) * | 2009-08-31 | 2011-03-30 | 中国石油化工股份有限公司 | Method for producing glycol by using oxalic ester |
| CN203648501U (en) * | 2013-11-25 | 2014-06-18 | 南京国昌化工科技有限公司 | Corrugated plate type uniform-temperature hydrogenation reactor |
-
2013
- 2013-11-25 CN CN201310604127.XA patent/CN103585933B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101993349A (en) * | 2009-08-31 | 2011-03-30 | 中国石油化工股份有限公司 | Method for producing glycol by using oxalic ester |
| CN203648501U (en) * | 2013-11-25 | 2014-06-18 | 南京国昌化工科技有限公司 | Corrugated plate type uniform-temperature hydrogenation reactor |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104841339A (en) * | 2015-04-16 | 2015-08-19 | 中国五环工程有限公司 | Novel hydrogenation reactor for synthesis gas-to-ethylene glycol process |
| CN105032305A (en) * | 2015-08-27 | 2015-11-11 | 德艾柯工程技术（上海）有限公司 | Novel radial plate type reactor |
| CN106955645A (en) * | 2015-12-17 | 2017-07-18 | 乔治·克劳德方法的研究开发空气股份有限公司 | Reactor for performing heat release or the endothermic reaction |
| CN114307908A (en) * | 2022-01-19 | 2022-04-12 | 华中科技大学 | Device and method for synthesizing liquid fuel through carbon dioxide multi-field concerted catalytic hydrogenation |
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| CN103585933B (en) | 2016-03-09 |
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Address after: 211500 No. 186, Shidai Avenue, Liuhe Economic Development Zone, Nanjing City, Jiangsu Province Patentee after: Nanjing Goodchina Chemical Technologies Co., Ltd. Address before: 210044, No. 355, Ning six road, Liuhe Industrial Development Zone, Nanjing District, Jiangsu, Nanjing Patentee before: Nanjing Goodchina Chemical Technologies Co., Ltd. |
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