CN204193907U - A kind of monolith honeycomb reactor for gas-liquid-solid reaction system - Google Patents
A kind of monolith honeycomb reactor for gas-liquid-solid reaction system Download PDFInfo
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- CN204193907U CN204193907U CN201420516719.6U CN201420516719U CN204193907U CN 204193907 U CN204193907 U CN 204193907U CN 201420516719 U CN201420516719 U CN 201420516719U CN 204193907 U CN204193907 U CN 204193907U
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Abstract
A kind of upper cover of monolith honeycomb reactor has gaseous phase outlet (15) and liquid phase inlet pipe (14), liquid phase shower nozzle (2) is had in it, gripper shoe (4) is had in middle cylinder, corrugated plating distributor (5) is equipped with between gripper shoe (4), recirculated water arm (16) is had in distributor (5) bottom, the inlet side of water arm (16) is all connected with recirculated water distributing disc (17) with outlet side, and be provided with recirculated water tube connector (6) in middle cylinder outside, recirculated water distributing disc (17) water inlet or delivery port are connected with recirculated water tube connector (6), conical gaseous distributer (8) is had in low head, there is liquid phase discharge pipe (11) bottom, gas phase inlet pipe (10) is had in liquid phase discharge pipe (11), gas phase inlet pipe (10) upper end has gas phase shower nozzle (9).The utility model has that mass-transfer efficiency is high, enlarge-effect is little, all even filling of liquid distribution and more catalyst changeout advantage easily.
Description
Technical field
The utility model belongs to a kind of reactor, particularly relates to a kind of monolith honeycomb reactor for gas-liquid-solid reaction system.
Background technology
Gas-liquid-solid reaction is reaction system common in Chemical Manufacture, is often referred to catalyst in the solid phase of this system, and gas phase is reactant, and liquid phase is reactant, product or inert media.Gas-liquid-solid reaction is compared with liquid-solid two-phase reaction system with gas-solid, solution-air, there is the shortcoming transmitting the large and transmittance process complexity of resistance.Stirring-type paste state bed reactor makes catalyst remain suspended state by the mode reducing catalyst grain size and vigorous stirring, substantially increase the mass transfer between airwater mist cooling and heat transfer efficiency, this reactor also has all even advantage that can realize online more catalyst changeout of reaction temperature simultaneously, industrially achieves and applies widely.But because it is to catalyst grain size and the churned mechanically requirement of brute force, result in this reactor, to there is catalyst easy to wear, solid-liquid two-phase laminated flow difficulty and catalyst fines easily glue a series of difficult problems such as wall, considerably increase catalyst attrition, the investment of separation equipment and the expense of operation.
Monoblock type or structural catalyst have regular and uniform pore passage structure, be connected with each other by many outsides, longitudinally the parallel channels of not handicapping gear or cell form, active component is made into very thin coating structure and is carried on duct inwall.Because integral catalyzer and conventional particles shape catalyst make a big difference, make monolith honeycomb reactor in phase reaction, show the characteristic being better than traditional stirring-type paste state bed reactor, be specially: (1) bed layer pressure reduces, integer catalyzer is made up of many parallel and straight ducts, therefore it reduces 2 ~ 3 orders of magnitude with fixed bed and slurry bed system phase specific pressure drop; (2) mass-transfer efficiency is high, when selecting suitable gas-liquid two-phase flow velocity, there will be the flow pattern of approximate piston flow, increase mass transfer in catalyst duct; (3) catalyst easily separated and change, because integer catalyzer is fixed in reactor, catalyst not easily grinds and runs off, be separated and change simpler; (4) enlarge-effect is little, and unitary catalyst structure is regular, and the difference of laboratory and industrial integral reactor is just only the difference of duct quantity, is easier to amplify.Because overall catalysis technique has plurality of advantages, become one of the most potential research direction in current heterogeneous catalysis field.
Although integral catalyzer shows the more advantage than traditional stirring-type paste state bed reactor in heterogeneous reaction, but because reactor design is not enough and the design feature of catalyst itself, it is caused still to there is following shortcoming: (1) heat-transfer effect is undesirable, duct due to integer catalyzer is relatively independent, without any effect of mass transmitting between adjacent duct, thus there is not radial heat transfer, radial heat transfer through cell walls is also very low, therefore for exothermic reaction, reaction temperature can be made to raise rapidly, the phenomenon of reacting all standing is there is for the endothermic reaction is then easier because of cooling than stirring-type paste state bed reactor, (2) liquid phase is at monolith honeycomb reactor cross-section skewness, be subject to the restriction of manufacturing process, the limited height of single integer catalyzer, for reaching required catalyst bed layer height, integer catalyzer need be carried out multiple-layer overlapped series connection, make liquid phase at two-layer integer catalyzer contact surface place skewness, (3) integer catalyzer filling and change still comparatively bother, although integer catalyzer profile and pore passage structure more regular, but due to the perfection docking in duct between layers must be ensured in Catalyst packing process, and also should control being of moderate size of gap between radial catalyst, simultaneously because its loadings is larger, the catalyst change caused due to local catalyst inactivation is bothered more.
In sum, integer catalyzer has many advantages in gas-liquid-solid reaction, but heat transfer efficiency is low, liquid is uneven and load the troublesome shortcoming of more catalyst changeout along cross-sectional distribution because the deficiency of catalyst structure feature and reactor causes it to exist.The basic reason of the problems referred to above be existing monolith honeycomb reactor with integer catalyzer unlike mating, and there is important function in the chemical process of reality, the whether reasonable of structure of reactor design not only decides catalyst performance, even can have material impact to the continuous and stable operation of producing.Therefore, for the design feature of integer catalyzer, develop that a kind of heat exchange efficiency is high, all even filling of the liquid distribution more more simple monolith honeycomb reactor of catalyst changeout, there is important theory and realistic meaning.
Summary of the invention
The purpose of this utility model is to provide a kind of monolith honeycomb reactor being applicable to airwater mist cooling system, this reactor can give play to that integer catalyzer bed pressure drop is low, mass-transfer efficiency is high, enlarge-effect little with catalyst without the need to while the advantage such as being separated, also have that heat exchange efficiency is high, all even filling of liquid distribution and a more catalyst changeout advantage easily.
In order to realize the purpose of this utility model, monolith honeycomb reactor it comprise reactor shell 1, liquid phase shower nozzle 2, gaseous distributer 8, liquid phase discharge pipe 11, liquid phase inlet pipe 14, gas phase import 10 and gaseous phase outlet 15, it is characterized in that reactor shell 1 is by upper cover, middle cylinder and low head composition, gaseous phase outlet 15 is arranged at upper cover top, upper cover is built with liquid phase shower nozzle 2, be positioned at upper cover side and have liquid phase inlet pipe 14, at least 5 layers of integer catalyzer gripper shoe 4 are had in middle cylinder, corrugated plating distributor 5 is equipped with between integer catalyzer gripper shoe 4, there is distribution hole 18 corrugated plating distributor 5 side, integer catalyzer gripper shoe 4 is equipped with integer catalyzer layer 3, parallel recirculated water arm 16 is equipped with at each corrugated plating distributor 5 lower concave surface place, the inlet side of recirculated water arm 16 is all connected with recirculated water distributing disc 17 with outlet side, and be provided with recirculated water tube connector 6 in middle cylinder outside, recirculated water distributing disc 17 water inlet or delivery port are connected with recirculated water tube connector 6, be circulating cooling water inlet 12 at middle cylinder nethermost recirculated water distributing disc 17 water inlet, middle cylinder uppermost recirculated water distributing disc 17 delivery port is circulating cooling water out 13, its concrete heat transfer process is that recirculated water enters recirculated water distributing disc 17 through circulating cooling water inlet 12 and distributes to each recirculated water arm 16, after recirculated water in recirculated water arm 16 and gas-liquid two-phase heat exchange, to be collected by recirculated water distributing disc 17 delivery port and the recirculated water arm 16 being sent to last layer through recirculated water tube connector 6 proceeds heat exchange, recirculated water through repeatedly heat exchange is finally discharged by circulating cooling water out 13 and is cooled Posterior circle and uses, built with conical gaseous distributer 8 bottom low head, there is liquid phase discharge pipe 11 low head bottom, has gas phase inlet pipe 10 in liquid phase discharge pipe 11, and gas phase inlet pipe 10 upper end has gas phase shower nozzle 9, and gas phase shower nozzle 9 is positioned at conical gaseous distributer 8.
The ratio of height to diameter of reactor middle cylinder as above is 5 ~ 20.
Integer catalyzer gripper shoe 4 number of plies as above is 6 ~ 12 layers.
Catalyst support plate 4 as above and corrugated plating distributor 5 support by the resupinate supporting leg 7 being fixed on middle cylinder inwall, and meet and to be positioned at catalyst support plate 4 below supporting leg 7 after supporting leg 7 upwards overturns and corrugated plating distributor 5 can upwards propose.
Recirculated water distributing disc 17 water inlet as above or the form with flange between delivery port with recirculated water tube connector 6 are connected, recirculated water distributing disc 17 each points of mouths of pipe are all connected with the form of flange with between recirculated water arm 16, can realize the handling between recirculated water tube connector 6, recirculated water distributing disc 17 and recirculated water arm 16.
Gas phase shower nozzle 9 as above is upper end closed surrounding hollow outs, ensures that the gas entered from gas phase import radially sprays to surrounding.
Conical gaseous distributer 8 as above is connected with low head by four supports 22, leave the space of 3 ~ 5cm between conical gaseous distributer 8 lower limb and low head wall, ensure that the liquid phase come from top can flow into liquid phase discharge pipe 13 by space and discharge reactor.
Conical gaseous distributer 8 as above is provided with the gas-phase distribution hole 21 that aperture is 5 ~ 30mm, and its percent opening is 20% ~ 60%.
Liquid phase shower nozzle 2 as above is made up of with some spray arms 20 vertical with it a total score pipe arrangement 19, at spray arm 20 bottom opening or mounting spray head, some spray arms 20 form a circular flat structure, and the ratio of its circular flat diameter and reactor diameter is 0.4 ~ 0.7.
Catalyst support plate 4 as above is emitted by peripheral garden ring 23, vertical stiffeners 24, silk screen 25, gripper shoe hoisting ring 26 and taper and forms.
The main body of catalyst support plate 4 as above is welded with peripheral garden ring 23 by some orthogonal reinforcements 24, then silk screen 25 is fixed on reinforcement 24, be welded with a gripper shoe hoisting ring 26 at the vertical stiffeners of centre, facilitate filling and the replacing of catalyst.
Integer catalyzer layer 3 as above block-shapedly to form for fan-shaped monolith catalyst 28 by 5 ~ 20, monolith catalyst 28 can be realized to be assembled into circle by the control of fan angle, its diameter is identical with catalyst support board diameter, assembled complete after catalyst layer in the middle of have a diameter to be the hollow hole 27 of 5 ~ 20cm, this hole is filling and the replacing of conveniently catalyst on the one hand, be hoisting ring 26 slot milling in the middle of gripper shoe 4 on the other hand, but emitted by a taper after monolith catalyst 28 installs and this hole is covered sealing, prevent leakage.
Monolith honeycomb reactor disclosed in the utility model patent can be used for all use gas-liquid-solid reaction systems, as reactions such as slurry bed system methanation, hydrogenation of dinitro toluene and F-T synthesis.
The utility model compared with prior art, has substantive distinguishing features and marked improvement is:
(1) monolith honeycomb reactor is not only respectively equipped with cold paraffin hydrocarbon shower nozzle and gas phase shower nozzle and gaseous distributer in upper and lower, and be all provided with corrugated plating distributor between each catalyst layer, making gas/liquid through repeatedly distributing, avoiding the problem that there is cross-section solution-air two-phase skewness in the reaction of existing monoblock type;
(2) recirculated water arm is all provided with at the concave surface place of each corrugated plating distributor, reacted solution-air two is on good terms shift out timely or additional heat, ensure that production continuously and stable operation, avoid the problem that the heat exchange efficiency that exists in existing monolith honeycomb reactor is low.
(3) top end socket is connected with the form of flange with reactor shell, all connect with the form of flange between recirculated water arm, recirculated water distributing disc and recirculated water tube connector, and catalyst support plate and plate-type corrugated distributor are all by can resupinate supporting leg support, the filling of the installation being arranged so that integral reactor of said structure, maintenance, catalyst and change more convenient.
(4) monolithic integer catalyzer is fan-shaped, by realizing the control of fan angle being assembled into the circle (as passed through employing 6 piece 60 ° fan-shaped sliceable rounded) isometrical with gripper shoe by polylith catalyst, not only make every layer of catalyst install more convenient, and make the gap between every block catalyst more even; Be provided with hoisting ring in the middle of gripper shoe, can first in reactor outside, catalyst be loaded in gripper shoe, then lift in reactor by hoisting ring by disposable for flood catalyst, make the filling of flood catalyst and change convenient; Catalyst assembled in gripper shoe after, a hollow hole is left in centre, makes the replacing that is assembled and single catalyst of catalyst convenient.
(5) blank of the monolith honeycomb reactor being specifically designed to integral catalyzer in prior art has not only been filled up in the proposition of this patent, overcome existing integer catalyzer Problems existing, and its range of application and extensively, substantially be applicable to the gas-liquid-solid reaction system that existing industry is all, have great importance.
Accompanying drawing explanation
Fig. 1 is the structural representation of monolith honeycomb reactor;
Fig. 2 is corrugated plating distributor A-A profile
Fig. 3 is liquid phase shower nozzle B-B top view
Fig. 4 is corrugated plating distributor and recirculated water distributing disc connection diagram
Fig. 5 is gas phase shower nozzle and supporting leg C-C top view
Fig. 6 is catalyst support plate D-D top view
Fig. 7 is catalyst shape and assembled schematic diagram
Shown in Fig. 1-7, 1 is reactor shell, 2 is liquid phase shower nozzles, 3 is integer catalyzer layers, 4 is catalyst support plates, 5 is corrugated plating distributors, 6 is recirculated water tube connectors, 7 is supporting legs, 8 is gaseous distributers, 9 is gas phase shower nozzles, 10 is gas phase imports, 11 is liquid-phase outlet pipes, 12 circulating cooling water inlets, 13 circulating cooling water outs, 14 liquid phase inlet pipes, 15 is gaseous phase outlets, 16 is recirculated water arms, 17 is recirculated water distributing discs, 18 is distribution holes, 19 is liquid phase shower nozzle total score pipe arrangements, 20 is liquid phase shower nozzle spray arms, 21 is gas-phase distribution holes, 22 is supports, 23 is peripheral annulus, 24 is vertical stiffeners, 25 is silk screens, 26 is hoisting rings, 27 is hollow holes, 28 is monolith catalysts.
Detailed description of the invention
Below by specific embodiment, the specific embodiment of the present invention is described in further detail.
Embodiment 1
Monolith honeycomb reactor it comprise reactor shell 1, liquid phase shower nozzle 2, conical gaseous distributer 8, liquid phase discharge pipe 11, liquid phase inlet pipe 14, gas phase import 10 and gaseous phase outlet 15, reactor shell 1 is by upper cover, middle cylinder and low head composition, gaseous phase outlet 15 is arranged at upper cover top, upper cover is built with liquid phase shower nozzle 2, be positioned at upper cover side and have liquid phase inlet pipe 14, 6 layers of integer catalyzer gripper shoe 4 are had in middle cylinder, corrugated plating distributor 5 is equipped with between integer catalyzer gripper shoe 4, there is distribution hole 18 corrugated plating distributor 5 side, integer catalyzer gripper shoe 4 is equipped with integer catalyzer layer 3, parallel recirculated water arm 16 is equipped with at each corrugated plating distributor 5 lower concave surface place, the inlet side of recirculated water arm 16 is all connected with recirculated water distributing disc 17 with outlet side, and be provided with recirculated water tube connector 6 in middle cylinder outside, recirculated water distributing disc 17 water inlet or delivery port are connected with recirculated water tube connector 6, be circulating cooling water inlet 12 at middle cylinder nethermost recirculated water distributing disc 17 water inlet, middle cylinder uppermost recirculated water distributing disc 17 delivery port is circulating cooling water out 13, its concrete heat transfer process is that recirculated water enters recirculated water distributing disc 17 through circulating cooling water inlet 12 and distributes to each recirculated water arm 16, after recirculated water in recirculated water arm 16 and gas-liquid two-phase heat exchange, to be collected by recirculated water distributing disc 17 delivery port and the recirculated water arm 16 being sent to last layer through recirculated water tube connector 6 proceeds heat exchange, recirculated water through repeatedly heat exchange is finally discharged by circulating cooling water out 13 and is cooled Posterior circle and uses, built with conical gaseous distributer 8 bottom low head, there is liquid phase discharge pipe 11 low head bottom, has gas phase inlet pipe 10 in liquid phase discharge pipe 11, and gas phase inlet pipe 10 upper end has gas phase shower nozzle 9, and gas phase shower nozzle 9 is positioned at conical gaseous distributer 8.
Wherein the ratio of height to diameter of reactor middle cylinder is 5.
Catalyst support plate 4 and corrugated plating distributor 5 support by the resupinate supporting leg 7 being fixed on middle cylinder inwall, and meet and to be positioned at catalyst support plate 4 below supporting leg 7 after supporting leg 7 upwards overturns and corrugated plating distributor 5 can upwards propose.
Recirculated water distributing disc 17 water inlet or the form with flange between delivery port with recirculated water tube connector 6 are connected, recirculated water distributing disc 17 each points of mouths of pipe are all connected with the form of flange with between recirculated water arm 16, can realize the handling between recirculated water tube connector 6, recirculated water distributing disc 17 and recirculated water arm 16.
Gas phase shower nozzle 9 is upper end closed surrounding hollow outs, ensures that the gas entered from gas phase import radially sprays to surrounding.
Conical gaseous distributer 8 is connected with low head by four supports 22, leaves the space of 3cm between conical gaseous distributer 8 lower limb and low head wall, ensures that the liquid phase come from top can flow into liquid phase discharge pipe 13 by space and discharge reactor.Conical gaseous distributer 8 is provided with the gas-phase distribution hole 21 that aperture is 5mm, and its percent opening is 20%.
Liquid phase shower nozzle 2 is made up of with some spray arms 20 vertical with it a total score pipe arrangement 19, at spray arm 20 bottom opening or mounting spray head, some spray arms 20 form a circular flat structure, and the ratio of its circular flat diameter and reactor diameter is 0.4.
Integer catalyzer layer 3 is made up of the fan-shaped catalyst 28 of monolithic of 5 pieces 72 °, its diameter is identical with catalyst support board diameter, assembled complete after catalyst layer in the middle of have a diameter to be the hollow hole 27 of 5cm, this hole is filling and the replacing of conveniently catalyst on the one hand, be hoisting ring 26 slot milling in the middle of gripper shoe 4 on the other hand, but emitted by a taper after monolith catalyst 28 installs and this hole is covered sealing, prevent leakage.
The monolith honeycomb reactor of the present embodiment is used for slurry bed system methanation reaction, reactions steps and condition as follows:
Integer catalyzer is loaded in integral reactor, hydrogen and nitrogen pass into respectively in reactor bottom pipeline autoreactor, and the volumetric concentration of hydrogen is 5%, after reactor being risen to 500 DEG C, normal pressure reduces to integer catalyzer, and reducing gases air speed is 6000L/ (hkg); After reduction terminates, the paraffin hydrocarbon in medium reservoirs is sent into monolith honeycomb reactor through pipeline from top, then switches to volume to consist of H reducing gases
265.5%, CO 20.5%, CO
21%, CH
412%, N
21% synthesis gas, 450 DEG C, carry out methanation reaction under the condition of 6MPa and 8000L/ (hKg), must H be consisted of from top
21.83%, CO0.02%, CO
20.03%, CH
42.8%, N
2the gas product of 2.82%.
Embodiment 2
Integer catalyzer gripper shoe 4 has 8 layers, the ratio of height to diameter of reactor middle cylinder is 10, leave the space of 4cm between conical gaseous distributer 8 lower limb and low head wall, conical gaseous distributer 8 is provided with the gas-phase distribution hole 21 that aperture is 10mm, and its percent opening is 30%.The ratio that spray arm 20 forms circular flat diameter and reactor diameter is 0.5, monolithic integer catalyzer 28 is 60 ° fan-shaped, by 6 pieces of catalyst be assembled into circular assembled complete after catalyst layer in the middle of have a diameter to be the hollow hole 27 of 10cm, all the other are with embodiment 1.
Embodiment 3
Integer catalyzer gripper shoe 4 has 10 layers, the ratio of height to diameter of reactor middle cylinder is 15, leave the space of 5cm between conical gaseous distributer 8 lower limb and low head wall, conical gaseous distributer 8 is provided with the gas-phase distribution hole 21 that aperture is 15mm, and its percent opening is 40%.The ratio that spray arm 20 forms circular flat diameter and reactor diameter is 0.6, monolithic integer catalyzer 28 is 40 ° fan-shaped, by 9 pieces of catalyst be assembled into circular assembled complete after catalyst layer in the middle of have a diameter to be the hollow hole 27 of 15cm, all the other are with embodiment 1.
Embodiment 4
Integer catalyzer gripper shoe 4 has 11 layers, the ratio of height to diameter of reactor middle cylinder is 15, leave the space of 4cm between conical gaseous distributer 8 lower limb and low head wall, conical gaseous distributer 8 is provided with the gas-phase distribution hole 21 that aperture is 20mm, and its percent opening is 50%.The ratio that spray arm 20 forms circular flat diameter and reactor diameter is 0.6, monolithic integer catalyzer 28 is 30 ° fan-shaped, by 12 pieces of catalyst be assembled into circular assembled complete after catalyst layer in the middle of have a diameter to be the hollow hole 27 of 15cm, all the other are with embodiment 1.
Embodiment 5
Integer catalyzer gripper shoe 4 has 12 layers, the ratio of height to diameter of reactor middle cylinder is 20, leave the space of 4cm between conical gaseous distributer 8 lower limb and low head wall, conical gaseous distributer 8 is provided with the gas-phase distribution hole 21 that aperture is 30mm, and its percent opening is 60%.The ratio that spray arm 20 forms circular flat diameter and reactor diameter is 0.7, monolithic integer catalyzer 28 is 18 ° fan-shaped, by 20 pieces of catalyst be assembled into circular assembled complete after catalyst layer in the middle of have a diameter to be the hollow hole 27 of 20cm, all the other are with embodiment 1.
Claims (12)
1. the monolith honeycomb reactor for gas-liquid-solid reaction system, it comprises reactor shell (1), liquid phase shower nozzle (2), gaseous distributer (8), liquid phase discharge pipe (11), liquid phase inlet pipe (14), gas phase import (10) and gaseous phase outlet (15), it is characterized in that reactor shell (1) is by upper cover, middle cylinder and low head composition, gaseous phase outlet (15) is arranged at upper cover top, upper cover is built with liquid phase shower nozzle (2), be positioned at upper cover side and have liquid phase inlet pipe (14), at least 4 layers of integer catalyzer gripper shoe (4) are had in middle cylinder, corrugated plating distributor (5) is equipped with between integer catalyzer gripper shoe (4), there is distribution hole (18) corrugated plating distributor (5) side, integer catalyzer gripper shoe (4) is equipped with integer catalyzer layer (3), parallel recirculated water arm (16) is equipped with at each corrugated plating distributor (5) lower concave surface place, the inlet side of recirculated water arm (16) is all connected with recirculated water distributing disc (17) with outlet side, and be provided with recirculated water tube connector (6) in middle cylinder outside, recirculated water distributing disc (17) water inlet or delivery port are connected with recirculated water tube connector (6), be circulating cooling water inlet (12) at middle cylinder nethermost recirculated water distributing disc (17) water inlet, middle cylinder uppermost recirculated water distributing disc (17) delivery port is circulating cooling water out (13), built with conical gaseous distributer (8) bottom low head, there is liquid phase discharge pipe (11) low head bottom, gas phase inlet pipe (10) is had in liquid phase discharge pipe (11), gas phase inlet pipe (10) upper end has gas phase shower nozzle (9), gas phase shower nozzle (9) is positioned at conical gaseous distributer (8).
2. a kind of monolith honeycomb reactor for gas-liquid-solid reaction system as claimed in claim 1, is characterized in that the ratio of height to diameter of described middle cylinder is 5 ~ 20.
3. a kind of monolith honeycomb reactor for gas-liquid-solid reaction system as claimed in claim 1, is characterized in that described integer catalyzer gripper shoe (4) number of plies is 6 ~ 12 layers.
4. a kind of monolith honeycomb reactor for gas-liquid-solid reaction system as claimed in claim 1, it is characterized in that described catalyst support plate (4) and corrugated plating distributor (5) support by the resupinate supporting leg (7) being fixed on middle cylinder inwall, and meet and to be positioned at catalyst support plate (4) below supporting leg (7) after supporting leg (7) upwards overturns and corrugated plating distributor (5) can upwards propose.
5. a kind of monolith honeycomb reactor for gas-liquid-solid reaction system as claimed in claim 1, it is characterized in that described recirculated water distributing disc (17) water inlet or be connected with the form of flange between delivery port with recirculated water tube connector (6), recirculated water distributing disc (17) each point of mouth of pipe is all connected with the form of flange with between recirculated water arm (16).
6. a kind of monolith honeycomb reactor for gas-liquid-solid reaction system as claimed in claim 1, is characterized in that described gas phase shower nozzle (9) is upper end closed surrounding hollow out.
7. a kind of monolith honeycomb reactor for gas-liquid-solid reaction system as claimed in claim 1, it is characterized in that described gaseous distributer (8) is connected with low head by four supports (22), between gaseous distributer (8) lower limb and low head wall, leave the space of 3 ~ 5cm.
8. a kind of monolith honeycomb reactor for gas-liquid-solid reaction system as claimed in claim 1, it is characterized in that described gaseous distributer (8) is provided with the gas-phase distribution hole (21) that aperture is 5 ~ 30mm, its percent opening is 20% ~ 60%.
9. a kind of monolith honeycomb reactor for gas-liquid-solid reaction system as claimed in claim 1, it is characterized in that described liquid phase shower nozzle (2) is made up of with some spray arms (20) vertical with it a total score pipe arrangement (19), at spray arm (20) bottom opening or mounting spray head, some spray arm (20) compositions circular flat structure, the ratio of its circular flat diameter and reactor diameter is 0.4 ~ 0.7.
10. a kind of monolith honeycomb reactor as claimed in claim 1, is characterized in that described catalyst support plate (4) is emitted by peripheral annulus (23), vertical stiffeners (24), silk screen (25), gripper shoe hoisting ring (26) and taper and forms.
11. a kind of monolith honeycomb reactors for gas-liquid-solid reaction system as claimed in claim 11, it is characterized in that described some orthogonal reinforcement (24) welds with peripheral garden ring (23), then silk screen (25) is fixed on vertical stiffeners (24), is welded with a gripper shoe hoisting ring (26) at the vertical stiffeners (24) of centre.
12. a kind of monolith honeycomb reactors for gas-liquid-solid reaction system as claimed in claim 1, it is characterized in that described integer catalyzer layer (3) block-shapedly to form for fan-shaped monolith catalyst (28) by 5 ~ 20, monolith catalyst (28) is assembled into circle, its diameter is identical with catalyst support board diameter, assembled complete after integer catalyzer layer (3) in the middle of have a diameter to be the hollow hole (27) of 5 ~ 20cm.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104164265A (en) * | 2014-09-10 | 2014-11-26 | 赛鼎工程有限公司 | Technique and device for performing slurry reactor methanation by utilizing monolithic catalyst |
| CN109685117A (en) * | 2018-12-04 | 2019-04-26 | 浙江大学 | The image measuring method of flow parameter in a kind of gas liquid particle three phase system |
| CN112403431A (en) * | 2020-10-27 | 2021-02-26 | 中国科学院过程工程研究所 | Wave-shaped supporting plate, tower equipment and application |
| CN113385109A (en) * | 2021-06-24 | 2021-09-14 | 江苏万盛大伟化学有限公司 | Device and method for coproducing pentamethyl diethylenetriamine and trimethyl hydroxyethyl ethylenediamine |
-
2014
- 2014-09-10 CN CN201420516719.6U patent/CN204193907U/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104164265A (en) * | 2014-09-10 | 2014-11-26 | 赛鼎工程有限公司 | Technique and device for performing slurry reactor methanation by utilizing monolithic catalyst |
| CN109685117A (en) * | 2018-12-04 | 2019-04-26 | 浙江大学 | The image measuring method of flow parameter in a kind of gas liquid particle three phase system |
| CN109685117B (en) * | 2018-12-04 | 2020-09-11 | 浙江大学 | Image measuring method for flow parameters in gas-liquid-solid three-phase system |
| CN112403431A (en) * | 2020-10-27 | 2021-02-26 | 中国科学院过程工程研究所 | Wave-shaped supporting plate, tower equipment and application |
| CN113385109A (en) * | 2021-06-24 | 2021-09-14 | 江苏万盛大伟化学有限公司 | Device and method for coproducing pentamethyl diethylenetriamine and trimethyl hydroxyethyl ethylenediamine |
| CN113385109B (en) * | 2021-06-24 | 2023-04-28 | 江苏万盛大伟化学有限公司 | Device and method for coproducing pentamethyldiethylenetriamine and trimethylhydroxyethyl ethylenediamine |
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