CN203316109U - Gas-liquid phase shell-and-tube type trickle bed solid-phase catalytic reactor - Google Patents
Gas-liquid phase shell-and-tube type trickle bed solid-phase catalytic reactor Download PDFInfo
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- CN203316109U CN203316109U CN2013203576606U CN201320357660U CN203316109U CN 203316109 U CN203316109 U CN 203316109U CN 2013203576606 U CN2013203576606 U CN 2013203576606U CN 201320357660 U CN201320357660 U CN 201320357660U CN 203316109 U CN203316109 U CN 203316109U
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Abstract
The utility model discloses a gas-liquid phase shell-and-tube type tickle bed solid- phase catalytic reactor. A bubble cap tray type distributor is arranged on the lower part of a gas-liquid distributor; an inert refractory bubble layer, a catalyst layer and a shell-and-tube type reactor are arranged underneath the bubble cap tray type distributor; the bubble cap tray tube distributor comprises a plate body and a plurality of bubble caps, wherein the plate body is matched with the periphery size of an inner cavity of each reactor barrel body; the plurality of the bubble caps are uniformly distributed on the plate body; each of the bubble cap comprises an overflow tube and a cover cap, wherein the overflow tube is fixed on the plate body; the cover cap is arranged on the overflow tube; the overflow tube is respectively communicated with the reactor barrel bodies above and below the plate body; a plurality of channels are uniformly distributed on the cover caps. The gas-liquid phase shell-and-tube type tickle bed solid-phase catalytic reactor is uniform in gas-liquid phase material flow distribution on the cross section of the reactor, stable in temperature in a catalyst bed layer, small in axial and radial temperature difference in the catalyst bed layer, accurate and flexible in reaction temperature control, and capable of recycling the reaction heat with higher potential energy; the reaction tube catalyst layer is internally free of a gas back-mixing phenomenon, so that the axial temperature of the catalyst bed layer cannot form saw-toothed considerable fluctuation.
Description
Technical field
The utility model relates to a kind of gas-liquid-phase tube shell-type trickle bed solid phase catalytic reactor, belong to the chemical process technical field, particularly belong to and take methyl alcohol, formaldehyde and series of products thereof as sub-field that raw material is produced engine replacement liquid fluid fuel, to produce diesel oil high-quality Cetane number blending composition---one of needed visual plant in the technical process of polymethoxy dialkyl ether and homologue, while also being applicable to produce fine chemical product and customization of chemicals, the process of gas and liquid phase drip (trickle) bed solid catalysis reaction for similar need.
Background technology
Traditional gas--liquid phase drip (trickle) bed solid phase catalytic reactor is all heat-insulating liquid phase drip (trickle) bed solid phase catalytic reactor for Bian, as the disclosed trickle bed reactor of China Patent No. " CN200710039089.2 ", its open day is on October 08th, 2008.Owing to generally all being attended by exothermic reaction in hydrogenation process, for guaranteeing uniformity of temperature profile in the reactor catalyst bed, mostly adopt beds is divided into to multistage, after the outlet of each beds is sent into the cold gas-liquid phase material of part (all needing to arrange the mixed distribution device) and carried out the cold shock cooling (or, intersegmental, hot reaction gas is extracted out, by the cooler outside reactor, pass into again next catalyst layer after cooling), enter again next catalyst layer, be unlikely to too high with the temperature that guarantees catalyst bed, after processing like this, although temperature can be controlled at certain limit, but fluctuation that the Temperature Distribution of beds presents regular " zigzag ", wave amplitude and the exothermic heat of reaction amount of " zigzag " fluctuation, the catalyst number of plies arranges relevant with cold shock material allocation proportion, the wave amplitude of general temperature is about 50 ℃ ~ 80 ℃.When the catalytic refining of synthetic polymethoxy dialkyl ether (DMMn) technical process, exothermic heat of reaction is large, exothermic heat of reaction is difficult to shift out in time, and the catalyst that Bian uses is more responsive to reaction temperature: reaction temperature is larger to the catalytic refining influential effect, temperature " zigzag " fluctuation when Bian uses adiabatic reactor, not only can obviously reduce the precision of catalytic refining and affect product quality but also the service life of minimizing catalyst.
Existing shell-and-tube solid phase catalytic reactor, be only applicable to gas-gas phase gentle-vapor-phase material carries out the solid catalysis reaction, for example, because gas (hydrogen) is gasificated into and is easy to mixing of steam with liquid material, gas-vapour can enter the shell-and-tube solid phase catalytic reactor after mixing very equably, and be distributed to equably in every reaction tube, guaranteed that gas-vapor-phase material has satisfied reaction operational effect in the shell-and-tube solid phase catalytic reactor, numerous gas-gas phases gentle-successful operation of vapor-phase material in industrial shell-and-tube solid phase catalytic reactor obtained confirmation.But, when gas-liquid phase (reaction condition requires Wu the vaporization of Fa Full foot liquid phase material) material adopts the shell-and-tube solid phase catalytic reactor, liquid phase (drop) can't be evenly distributed to (each reaction purple has the reaction tube that several thousand external diameters are 38 ~ 45mm usually) in numerous reaction tubes as gas (or steam), and after liquid material enters in reaction tube, just can't readjust again distribution between reaction tube, cause the reaction condition of differential responses pipe not identical---the fluid flow difference, temperature and Temperature Distribution difference, reaction pressure distributes different, catalyst life shortens, catalyst layer resistance difference, cause gas flow also inhomogeneous, cause gas-liquid material general reaction weak effect, product quality is inhomogeneous, consume and rise, energy consumption rises, when serious, cause device normally to move.So, at needs, adopt in the commercial plant of gas-liquid phase trickle bed solid catalysis reaction, all adopt multistage insulation formula liquid phase drip (trickle) bed solid phase catalytic reactor.
Process for refining condition, the reaction heat of synthetic polymethoxy dialkyl ether (DMMn) technical process cause the larger and supporting catalyst performance of temperature rise to require stricter.The specification requirement that traditional heat-insulating liquid phase drip (trickle) bed solid phase catalytic reactor and existing shell-and-tube solid phase catalytic reactor all are difficult to adapt to synthetic polymethoxy dialkyl ether (DMMn) technical process.
To sum up, reaction bed temperature skewness, the temperature wave amplitude of tradition gas-liquid phase heat-insulating drip (trickle) bed solid phase catalytic reactor are large, are directed at gas-liquid phase heat-insulating drip (trickle) bed solid phase catalytic reactor scope of application and seriously are restricted.
Summary of the invention
The purpose of this utility model is to overcome the problems referred to above that existing gas-liquid phase heat-insulating trickle bed solid phase catalytic reactor exists, and a kind of gas-liquid-phase tube shell-type trickle bed solid phase catalytic reactor is provided.The utility model gas-liquid phase stream on reactor cross-section is evenly distributed, axle in steady, the beds of temperature in beds, radial direction temperature difference are little; The precise control of reaction temperature, sensitive; Can reclaim reaction heat with high bit; In reaction bed, without the gas backmixing phenomenon, the beds axial temperature can not form the zigzag fluctuation.
For achieving the above object, the technical solution adopted in the utility model is as follows:
A kind of gas-liquid-phase tube shell-type trickle bed solid phase catalytic reactor, comprise the gas-liquid distributor arranged in charging aperture, discharging opening, reactor shell and reactor shell, it is characterized in that: described gas-liquid distributor bottom is provided with bubble-cap disc type distributor, and bubble-cap disc type distributor is arranged with shell-and-tube reactor; Described bubble-cap disc type distributor comprise with the disk body of reactor cylinder intracoelomic cavity circumferential size coupling and disk body on equally distributed a plurality of bubble-caps, described bubble-cap comprises the overflow pipe be fixed on disk body and is arranged on the block on benefit stream pipe, the described overflow pipe reactor shell upper and lower with disk body respectively is communicated with, and the block surrounding is uniformly distributed a plurality of passages.
Described charging aperture comprises gas feed and liquid-inlet, and the charging aperture place is provided with venturi jet mixer, diffusion type mixed distribution device or injecting type mixed distribution device.
Be fixedly installed the support fixture on described benefit stream pipe, block is fixedly connected with the support fixture.
The quantity of described bubble-cap is 3 ~ 300, and the quantity of the passage of each block surrounding is 2 ~ 20.
Described passage is circular hole passage or Channels With Grooved Parts, and is arranged on the position of block surrounding higher than the overflow pipe upper surface.
The upper perforated plate top of described shell-and-tube reactor is disposed with catalyst layer and inertia flame-proof sphere layer from bottom to top.
Employing the utility model has the advantage of:
One, the utility model is compared with liquid phase heat-insulating drip (trickle) commonly used bed solid phase catalytic reactor, have on reactor cross-section (in the numerous reaction tubes that comprise shell-and-tube reactor on cross section) gas-liquid phase stream in reactor, (comprise in reaction tube) be evenly distributed, axle in steady, the catalyst layer of temperature in catalyst layer, radial direction temperature difference be little; The precise control of reaction temperature, sensitive; Can reclaim reaction heat with high bit; In the reaction tube inner catalyst layer, without the gas backmixing phenomenon, the beds axial temperature does not form the zigzag fluctuation, the reaction tube radial temperature difference is very little, can improve utilization rate and the service life of catalyst; Not only facility compact, start-stop car facilitate, and are conducive to energy-conservation, consumption reduction.
Two, in the utility model, described charging aperture comprises gas feed and liquid-inlet, the charging aperture place is provided with venturi jet mixer, diffusion type mixed distribution device or injecting type mixed distribution device, adopt this structure, suck liquid and mix, spray with hydrogen injection, hydrogen and liquid mist are evenly distributed on the cross section of shell-and-tube reactor.
Three, the cover disc type distributor that the utility model adopts, gas-the liquid phase fluid that can guarantee and flow is uniformly distributed on the cross section of reactor, hydrogen can evenly be passed through at the passage of bubble-cap circle distribution, prevented that a large amount of hydrogen from affecting evenly dripping of liquid material by " bubble-cap " and drenching distribution.
Four, in the utility model, the upper perforated plate top of described shell-and-tube reactor is disposed with catalyst layer and inertia flame-proof sphere layer from bottom to top, this structure, not only to gas and drop, being uniformly distributed on reactor cross-section plays an important role, and carry out the part adiabatic reaction at this catalyst layer, harm and poisoning the playing an important role of part blank pipe occurs to sink to occurring at the reaction tube inner catalyst layer during to energy-saving and cost-reducing, anti-locking apparatus operation.
Five, in the utility model, bubble-cap disc type distributor is arranged with shell-and-tube reactor, Catalyst packing is in the reaction tube of shell-and-tube reactor, shell side passes into boiler feed water (or conduction oil), pass through to control the pressure of boiler water when operation, flow and temperature (or controlling temperature and the flow that conduction oil is imported and exported), evenly shift out reaction tube Inner and carry out refining reaction institute liberated heat, not only can be accurate, control delicately reaction temperature, and the axle of the interior catalyst for refining layer of reaction tube, radial temperature reaches even and stable Temperature Distribution, and (tube inner diameter stabilizes to 0.6 ~ 2 ℃ to the temperature difference, axial temperature difference stabilizes to 10 ~ 20 ℃.
The accompanying drawing explanation
Fig. 1 is the utility model structural representation
The block fit structure schematic diagram that Fig. 2 is bubble-cap disc type distributor and bubble-cap in the utility model
In figure, be labeled as: 1, gas feed, 2, the venturi jet mixer, 3, liquid-inlet, 4, gas-liquid distributor, 5, block, 6, bubble-cap disc type distributor, 7, inertia flame-proof sphere layer, 8, catalyst layer, 9, upper perforated plate, 10, reactor shell, 11, reaction tube, 12, discharging opening, 13, the boiler water import, 14, boiler water and vapor outlet port, 15, disk body, 16, overflow pipe, 17, passage, 18, support fixture, 19, isothermal reaction district catalyst for refining.
The specific embodiment
Embodiment 1
A kind of gas-liquid-phase tube shell-type trickle bed solid phase catalytic reactor, the gas-liquid distributor 4 that comprises charging aperture, discharging opening 12, reactor shell 10 and reactor shell 10 interior settings, described gas-liquid distributor 4 bottoms are provided with bubble-cap disc type distributor 6, bubble-cap disc type distributor 6 is arranged with shell-and-tube reactor, and shell-and-tube reactor can adopt existing shell-and-tube reactor; Described bubble-cap disc type distributor 6 comprise with the disk body 15 of reactor shell 10 inner chamber circumferential size couplings and disk body 15 on equally distributed a plurality of bubble-caps, described bubble-cap comprises the overflow pipe 16 be fixed on disk body 15 and is arranged on the block 5 on overflow pipe 16, the described overflow pipe 16 reactor cylinder intracoelomic cavity upper and lower with disk body 15 respectively is communicated with, and 5 surroundings of blocking a shot are uniformly distributed a plurality of passage 17 supplied gas and evenly pass through.
Further, preferred embodiment of the present utility model is, described charging aperture comprises gas feed 1 and liquid-inlet 3, and the charging aperture place is provided with venturi jet mixer 2, diffusion type mixed distribution device or injecting type mixed distribution device.
In the utility model, on described benefit stream pipe 16, be fixedly installed and support fixture 18, blocking a shot 5 is fixedly connected with supporting fixture 18, and as shown in the figure, blocking a shot 5 is bolted with support fixture 18.The structure of fixing block has a lot, is not limited to this.
Another preferred embodiment of the present utility model is, the quantity of described bubble-cap is 3 ~ 300, and the quantity of the passage of each 5 surrounding of blocking a shot is 2 ~ 20.
Another preferred embodiment of the present utility model is that described passage 17 can be circular hole passage or Channels With Grooved Parts, and all is arranged on the position of block 5 surroundings higher than the overflow pipe upper surface.
Another preferred embodiment of the present utility model is, upper perforated plate 9 tops of described shell-and-tube reactor are disposed with catalyst layer 8 and inertia flame-proof sphere layer 7 from bottom to top, and the inertia flame-proof sphere is radially porous ball or the medicine ball of perforate of axle.
Below the utility model is described in further details:
As the utility model is provided with venturi jet mixer 2 at gas and liquid-inlet, suck liquid and mix, spray with hydrogen injection, hydrogen and liquid mist are evenly distributed on the cross section of drip (trickle) bed shell-and-tube reactor.
The utility model adopts in venturi jet mixer 2 bottoms, be provided with the gas-liquid phase fluid equally distributed bubble-cap disc type distributor 6 on the cross section of reactor that guarantees and flow, press shell-and-tube drip (trickle) bed solid phase reactor diameter difference on bubble-cap disc type distributor 6, by the bubble-cap that is uniformly distributed requirement and arranges 3 ~ 300 or the circulation of more solution-air fluid, the cylindrical shell surrounding of the block of each bubble-cap, in higher than bubble-cap more than the height of liquid overflow pipe upper surface, evenly be provided with the circular hole passage that 2 ~ 20 supplied gas are passed through, make hydrogen evenly pass through bubble-cap disc type distributor at the passage of bubble-cap circle distribution, prevented that a large amount of hydrogen from affecting evenly dripping of liquid material by bubble-cap and drenching distribution.
Below bubble-cap disc type distributor, shell-and-tube solid phase catalytic reactor upper perforated plate top is sequentially loading catalyst layer 8 and inertia flame-proof sphere layer 7 from bottom to top.This structure, not only to gas and drop, being uniformly distributed on reactor cross-section plays an important role, and carry out the part adiabatic reaction at this catalyst layer, harm and poisoning the playing an important role of part blank pipe occurs to sink to occurring at the reaction tube inner catalyst layer during to energy-saving and cost-reducing, anti-locking apparatus operation.
The main part of the utility model gas-liquid-phase tube shell-type drip (trickle) bed solid phase catalytic reactor is shell-and-tube reactor, and shell-and-tube reactor is connected with boiler water import 13, boiler water and vapor outlet port 14.Isothermal reaction district catalyst for refining 19 is seated in reaction tube 11, shell side passes into boiler feed water (or conduction oil), pass through to control pressure, flow and the temperature (or controlling temperature and flow that conduction oil is imported and exported) of boiler water when operation, evenly shift out reaction tube Inner and carry out refining reaction institute liberated heat, not only can control accurately, delicately reaction temperature, and in reaction tube, axle, the radial temperature of catalyst for refining layer reaches even and stable Temperature Distribution (tube inner diameter stabilizes to 0.6 ~ 2 ℃, axial temperature difference to the temperature difference and stabilizes to 10 ~ 20 ℃).
Embodiment 2
To produce the process units of 1000 tons of polymethoxy dialkyl ethers per year, the gas and liquid phase trickle bed shell-and-tube solid catalysis hydrofining reactor that supporting Bian uses, the structure of employing is as follows:
Reactor external diameter 5500-6200mm, total height are 4500-5000mm, always have that 70-90 reaction tubes, reaction tube are of a size of 40-50mm, tube length of reaction tube is to fill altogether 260-360 in 2000-2500mm, reaction tube to rise Hydrobon catalyst; Top solution-air material inlet is typical venturi jet mixer and is with the diffusion profile device, bubble-cap disc type distributor external diameter be 500-700mm, on establish 15-25 of bubble-caps, bubble-cap cap cylindrical shell external diameter be 45-55mm (bubble-cap cap cylindrical shell higher than overflow pipe upper surface 6-12mm circumference on uniform 4-8 8-15mm circular hole passages); Below bubble-cap disc type distributor, 80-100 liters, Hydrobon catalyst layer is sequentially loaded on the upper perforated plate top of shell-and-tube solid phase catalytic reactor from bottom to top, catalyst height is 260-360mm, the inertia flame-proof sphere layer of filling 5-10mm on it, floor height is 100-150mm; The distance of bubble-cap disc type distributor and inertia flame-proof sphere layer top end face is 180-220mm.
The technological condition of the utility model when operation is:
Reaction pressure is that 1.5 ~ 3.0MPa, reaction temperature are that 80 ~ 180 ℃, liquid phase enter refining material 350 ~ 500kg/h, hydrogen flowing quantity is 120 ~ 450Nm
3(hydrogen content is 98% ~ 99.9%); The control of reaction tube inner catalyst layer temperature is that Bian passes into the water yield of boiler water and the way of pressure with control valve shell-type reactor shell side.
In running, the continuous and steady operation effect: regulate and control obviously only 0.6 ~ 1.8 ℃ of good, the reaction tube inner catalyst layer radial direction temperature difference of the material refining effect of trickle bed in (temperature rises and be controlled), each reaction tube of the refining catalyst effect of carrying out adiabatic reaction that precision is high, the reactor upper perforated plate loads above of sensitive, convenient, material, axial temperature is poor is 5 ~ 10 ℃.
Operation result confirms: in trickle bed shell-and-tube solid catalysis refining reaction device, gas--the liquid material is evenly distributed; The catalyst effect of carrying out adiabatic reaction that the reactor upper perforated plate loads above is obvious; In the reaction tube of shell-and-tube solid phase catalytic reactor, reaction heat shifts out effectively also axial and radial temperature difference reliable, the reaction tube inner catalyst layer and is less than the expection level; Produce a desired effect fully.
Claims (6)
1. gas-liquid-phase tube shell-type trickle bed solid phase catalytic reactor, comprise the gas-liquid distributor (4) arranged in charging aperture, discharging opening (12), reactor shell (10) and reactor shell (10), it is characterized in that: described gas-liquid distributor (4) bottom is provided with bubble-cap disc type distributor (6), and bubble-cap disc type distributor (6) is arranged with shell-and-tube reactor; Described bubble-cap disc type distributor (6) comprises disk body (15) and the upper equally distributed a plurality of bubble-caps of disk body (15) with reactor shell (10) inner chamber circumferential size coupling, described bubble-cap comprises the overflow pipe (16) be fixed on disk body (15) and is arranged on the block (5) on benefit stream pipe (16), described overflow pipe (16) reactor shell (10) upper and lower with disk body (15) respectively is communicated with, and block (5) surrounding is uniformly distributed a plurality of passages (17).
2. gas according to claim 1-liquid-phase tube shell-type trickle bed solid phase catalytic reactor, it is characterized in that: described charging aperture comprises gas feed (1) and liquid-inlet (3), and the charging aperture place is provided with venturi jet mixer (2), diffusion type mixed distribution device or injecting type mixed distribution device.
3. gas according to claim 1 and 2-liquid-phase tube shell-type trickle bed solid phase catalytic reactor is characterized in that: be fixedly installed on described overflow pipe (16) and support fixture (18), block (5) is fixedly connected with support fixture (18).
4. gas according to claim 3-liquid-phase tube shell-type trickle bed solid phase catalytic reactor, it is characterized in that: the quantity of described bubble-cap is 3 ~ 300, the quantity of the passage (17) of each block surrounding is 2 ~ 20.
5. according to claim 1,2 or 4 described gas-liquid-phase tube shell-type trickle bed solid phase catalytic reactor, it is characterized in that: described passage (17) is circular hole passage or Channels With Grooved Parts, and is arranged on the position of block (5) surrounding higher than overflow pipe (16) upper surface.
6. gas according to claim 5-liquid-phase tube shell-type trickle bed solid phase catalytic reactor, it is characterized in that: the upper perforated plate of described shell-and-tube reactor (9) top is disposed with catalyst layer (8) and inertia flame-proof sphere layer (7) from bottom to top.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013203576606U CN203316109U (en) | 2013-06-21 | 2013-06-21 | Gas-liquid phase shell-and-tube type trickle bed solid-phase catalytic reactor |
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| CN2013203576606U CN203316109U (en) | 2013-06-21 | 2013-06-21 | Gas-liquid phase shell-and-tube type trickle bed solid-phase catalytic reactor |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105582854A (en) * | 2014-10-21 | 2016-05-18 | 中国石油化工股份有限公司 | Fixed bed hydrogenation reactor and application method thereof |
| CN106732209A (en) * | 2017-01-24 | 2017-05-31 | 江苏德邦工程有限公司 | A kind of new boiling type isothermal reactor and isothermal control technique |
| CN107921392A (en) * | 2015-08-28 | 2018-04-17 | Lg化学株式会社 | Distributor and the downflow system catalytic reactor comprising the distributor |
-
2013
- 2013-06-21 CN CN2013203576606U patent/CN203316109U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105582854A (en) * | 2014-10-21 | 2016-05-18 | 中国石油化工股份有限公司 | Fixed bed hydrogenation reactor and application method thereof |
| CN105582854B (en) * | 2014-10-21 | 2018-11-30 | 中国石油化工股份有限公司 | A kind of fixed bed hydrogenation reactor and application method |
| CN107921392A (en) * | 2015-08-28 | 2018-04-17 | Lg化学株式会社 | Distributor and the downflow system catalytic reactor comprising the distributor |
| CN106732209A (en) * | 2017-01-24 | 2017-05-31 | 江苏德邦工程有限公司 | A kind of new boiling type isothermal reactor and isothermal control technique |
| CN106732209B (en) * | 2017-01-24 | 2023-01-20 | 江苏德邦工程有限公司 | Boiling type isothermal reactor and isothermal control process |
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Address after: 1606, B, building 19, building 1, No. 100176, Ronghua Road, Beijing economic and Technological Development Zone, Beijing, China Patentee after: Beijing Dongfang Hongsheng New Energy Application Technology Research Institute Co.,Ltd. Address before: 11 Yangzhou, Jiangsu Yangtze River Road, No. 225009, world building, floor, floor, room 438 Patentee before: Beijing Dongfang Hongsheng New Energy Application Technology Research Institute Co.,Ltd. |
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Granted publication date: 20131204 |
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