CN202700474U - Static bed axial radical reactor with calandria wall type inner and outer barrels - Google Patents

Abstract

The utility model discloses a static bed axial radical reactor with calandria wall type inner and outer barrels. The static bed axial radical reactor comprises a pressure-bearing shell body and catalyst barrel body parts installed inside the pressure-bearing shell body. The catalyst barrel body parts comprise an internals bottom support, a catalyst outer barrel, a catalyst inner barrel and catalyst top annular grids, wherein the catalyst outer barrel and the catalyst inner barrel are formed by a plurality of heat exchange tubes and a plurality of round rods, and the plurality of heat exchange tubes are arranged in a circumferential spacing mode. According to the static bed axial radical reactor with the calandria wall type inner and outer barrels, the tubes arranged closely in the circumferential direction are used to form the catalyst inner and outer barrels, and thereby opening rate is large, catalyst dead zone inside bed can be avoided and bed resistance drop is controlled by an opening cylinder which is connected with the catalyst inner barrel in a welding mode. The static bed axial radical reactor with the calandria wall type inner and outer barrels has the advantages that the static bed axial radical reactor can use a catalyst to the utmost degree and is suitable for a small particle catalyst, the inner and outer barrels are simple in structure so as to facilitate production and upsize, and reaction gas flows along the axial radical direction so that resistance is decreased.

Description

A kind of fixed bed axial-radial flow reactor with comb wall type inner/outer tube

Technical field

The utility model relates to the petrochemical technology field, relate in particular to a kind of fixed bed gas-solid catalysis device that is applicable to, be particularly related to a kind of reaction gas along the diameter of axle to skimming over catalyst, the fixed bed axial-radial flow reactor with comb wall type inner/outer tube of Catalyst packing in special inside and outside surge drum, this fixed bed axial-radial flow reactor is specially adapted to synthetic ammonia, CO conversion, hydrogen through reforming oxidized methyl alcohol, catalytic reforming, preparing phenylethylene from dehydrogenation of phenylethane etc.

Background technology

Development along with Chemical Manufacture, for adapting to different heat transfer requirement and heat transfer type, the version that multiple fixed bed reactors occur, wherein especially to utilize the reaction mass of gaseous state, the gas solid catalytic reactor that reacts by the bed that is made of solid catalyst is most widely used in Chemical Manufacture.

Fixed bed reactors mainly are divided into heat-insulating and heat exchange type two large classes on reaction principle.The heat-insulating fixed bed reactors are simple in structure, and the catalyst homogeneous reactor places in the bed, do not have exchange heat with the external world, and bed temperature is along the flow direction of material and change.The flow direction that enters bed according to process gas can be divided into fixed bed reactors axial flow, radial flow, three kinds of reaction patterns of axle radial flow.

Gas 1 in the axial flow reactor 2 flows to parallel with the axle 2a of axial flow reactor 2, as shown in Figure 1.Axial restraint bed bioreactor 2 is simple in structure, and production capacity is large.The axial restraint bed bioreactor also has larger shortcoming, and resistance drop is larger, and is all extremely unfavorable to the intensity of the activity of selective, the catalyst of reaction and life-span, equipment etc.

Gas 4 in the Radial Flow catalytic bed reactor 3 flows along radial direction on perpendicular to each cross section of Radial Flow catalytic bed reactor 3 axle 3a, as shown in Figure 2.The gas flow of Radial Flow catalytic bed reactor 3 is short, and flow velocity is low, can reduce significantly the catalytic bed pressure drop, provides condition for using catalyst particle.The design key of Radial Flow catalytic bed reactor 3 is that the appropriate design runner makes the gas flow on each cross section impartial, manufacturing to the distribution runner is had relatively high expectations, and require catalyst that higher mechanical strength is arranged, in order to avoid catalyst breakage and stop up the distribution aperture is destroyed the even distribution of fluid.

The diameter of axle 6 minutes two runners of gas in the catalytic bed reactor 5 that flows, fraction gas 6a is from bed 5a top axle to entering bed 5a, most of gas 6b flows along radial direction on each cross section of the catalytic bed reactor 5 axle 5b that flow perpendicular to the diameter of axle, as shown in Figure 3.The diameter of axle possesses all advantages of radial reactor to the catalytic bed reactor 5 that flows, and its runner has been reduced the bed top dead greatly so that the utilization rate of catalyst maximizes, give full play to catalyst activity and so that pressure drop minimize.

At present domestic fixed bed reactors research to these three kinds of patterns is very many all, and especially radially the research with axial-radial flow reactor is very popular problem.Most of Patents namely centers on realization radially or the axial-radial flow reactor internals are the exploitation of catalyst inner/outer tube, such as patent 200310109323.6 " a kind of catalytic reforming and catalytic dehydrogenation fixed bed radial reactor ", its inner/outer tube is for to beat supporting and the gas communication that small sircle hole is realized catalyst at the cylinder that rolls, and the similar industrial product also has rectangular orifice plate, bridge opening plate or Johnson Net etc.But all there is certain defective in the said goods, as makes the problems such as complexity, processing charges is high, percent opening is low, inner/outer tube intensity is low.

The utility model content

Technical problem to be solved in the utility model is for the problems referred to above, and a kind of novel fixed bed axial-radial flow reactor with comb wall type inner/outer tube is provided.It has intensity height, large, the little characteristics in catalyst dead band of simple in structure, percent opening, inner/outer tube can be installed according to specification of equipment integral body or piecemeal manufacturing, while can be with the minimise wear that produces in Catalyst packing, the infall process owing to slit between pipe/bar is axially continuously shape.

Technical problem to be solved in the utility model can be achieved through the following technical solutions:

A kind of fixed bed axial-radial flow reactor with comb wall type inner/outer tube, comprise pressure-bearing shell and be installed in the interior catalyst shell portion of described pressure-bearing shell, described catalyst shell portion comprises the internals bottom support, the catalyst urceolus, catalyst inner core and catalyst top annular grid, described internals bottom support is fixed on the bottom of described pressure-bearing shell, described catalyst urceolus and catalyst inner core are fixed on the described internals bottom support, described catalyst top annular grid is installed on described catalyst urceolus and the catalyst inner core top, catalyst is filled in by the internals bottom support, the catalyst urceolus, in the space that catalyst inner core and catalyst top annular grid surround, it is characterized in that described catalyst urceolus adopts circumferentially spaced some the first heat exchanger tubes or some the first round bars formation.

The first annular porous plate that some the first heat exchanger tubes in the described catalyst urceolus or some the first round bars adopt several axially spaced-aparts to arrange connects.

The first annular porous plate that described several axially spaced-aparts are arranged adopts first vertical connecting plate to connect.

Each first annular porous plate is formed by connecting by some blocks of the first arcuated porous plates, like this so that the catalyst urceolus can the piecemeal manufacturing.

Gap between described the first heat exchanger tube or the first round bar is according to process requirements and catalyst particle size and determine.

Described catalyst inner core by on the pipe of one section not perforate and the one section tube wall by the perforate cylinder of regular perforate and adopt the second heat exchanger tube or the second round bar that circumferentially are spaced on the described perforate cylinder outer wall to consist of, wherein said pipe is positioned at the top of catalyst inner core, the top of described perforate cylinder is connected with the bottom of pipe, the bottom of perforate cylinder is connected on the described internals bottom support, and the inner edge of described catalyst top annular grid is connected with described pipe.

The second annular porous plate that some the second heat exchanger tubes in the described catalyst inner core or some the second round bars adopt several axially spaced-aparts to arrange connects, and described perforate cylinder is connected with the described second annular porous plate.

The second annular porous plate that described several axially spaced-aparts are arranged adopts second vertical connecting plate to connect.

Gap between described the second heat exchanger tube or the second round bar is according to process requirements and catalyst particle size and determine.

Described pressure-bearing shell inwall is lined with stainless steel lining.

Described pressure-bearing shell comprises upper and lower end socket, cylindrical shell, bearing; Wherein upper cover is connected with the welded top of cylindrical shell, offers manhole and thermocouple patchhole at upper cover, and thermocouple is inserted in the pressure cylinder by described thermocouple patchhole and passes described catalyst top annular grid and is inserted in the catalyst; Described low head is connected with the bottom welding of cylindrical shell, offers process gas import, process gas outlet and discharge port at low head, is inserted with the process gas outlet in the described process gas outlet, and described process gas outlet is connected with described catalyst inner core bottom; Be inserted with discharge duct in the described discharge port, the top of described discharge duct is connected with described internals bottom support; Form a process gas rising passway between the inwall of described cylindrical shell and the described catalyst urceolus, described upper cover inside is provided with the process gas chamber of turning back, and the described process gas chamber of turning back is communicated with described process gas rising passway; Described bearing is fixed on the middle and lower part of described cylinder body outer wall.

Owing to adopted technical scheme as above, of the present utility modelly utilize circumferential compact arranged pipe to form the catalyst inner/outer tube, have larger percent opening, avoid bed inner catalyst dead band, bed resistance falls by the perforate cylinder control that is welded in the catalyst inner core.Adopt this reactor to have following characteristics: can utilize to greatest extent catalyst, and be applicable to catalyst particle; Inner/outer drum structure is simple, is convenient to make and maximize; Reaction gas is along the diameter of axle to flowing, and resistance drop is little.

Description of drawings

Fig. 1 is the structural representation of existing axial flow reactor.

Fig. 2 is the structural representation of existing Radial Flow catalytic bed reactor.

Fig. 3 is the structural representation of the existing diameter of axle to the catalytic bed reactor that flows.

Fig. 4 is that the utility model is with the fixed bed axial-radial flow reactor structural representation of comb wall type inner/outer tube.

Fig. 5 is the structural representation of the utility model catalyst urceolus.

Fig. 6 is the assembling schematic diagram of heat exchanger tube and arcuated porous plate in the utility model catalyst urceolus.

Fig. 7 is the A-A cutaway view of Fig. 6.

Fig. 8 is the assembling of the integral body between heat exchanger tube and annular porous plate schematic diagram in the utility model catalyst urceolus.

Fig. 9 is the welding schematic diagram between heat exchanger tube and the annular porous plate in the utility model catalyst urceolus.

The specific embodiment

Further describe the utility model below in conjunction with the drawings and specific embodiments.

Referring to Fig. 4, the fixed bed axial-radial flow reactor with comb wall type inner/outer tube that provides among the figure comprises pressure-bearing shell 100 and the catalyst shell portion that is installed in the pressure-bearing shell 100.

Pressure-bearing shell 100 comprises upper cover 110, low head 120, cylindrical shell 130, bearing 140; The material of upper cover 110, low head 120, cylindrical shell 130, bearing 140 should comprehensively be chosen according to technological temperature, pressure, dielectric property etc.When this fixed bed axial-radial flow reactor with comb wall type inner/outer tube was applied to the Coal Chemical Industry sulfur resistant conversion process, the inwall of upper cover 110, low head 120, cylindrical shell 130 was lined with stainless steel lining.

Upper cover 110 is connected with the welded top of cylindrical shell 130, offer manhole 111 and thermocouple patchhole 112 at upper cover 110, thermocouple 150 is inserted in the pressure cylinder 100 and is passed catalyst top annular grid 210 by thermocouple patchhole 112 and is inserted in the catalyst 220.

Low head 120 is connected with the bottom welding of cylindrical shell 130, offer process gas import 121, process gas outlet 122 and discharge port 123 at low head 120, be inserted with process gas outlet 160 in the process gas outlet 122, process gas outlet 160 is connected with catalyst inner core 230 bottoms; Be inserted with discharge duct 170 in the discharge port 123, the top of discharge duct 170 is connected with internals bottom support 250.

Form a process gas rising passway 300 between the inwall of cylindrical shell 130 and the catalyst urceolus 240, upper cover 110 inside are provided with the process gas chamber 310 of turning back, and the process gas chamber 310 of turning back is communicated with 300 with the process gas rising passway.

Bearing 140 is fixed on the middle and lower part of cylindrical shell 130 outer walls, in order to support whole pressure-bearing shell 100.

The catalyst shell portion comprises internals bottom support 250, catalyst urceolus 240, catalyst inner core 230 and catalyst top annular grid 210, internals bottom support 250 is fixed on the low head 120, catalyst urceolus 240 and catalyst inner core 230 are fixed on the internals bottom support 250, catalyst top annular grid 210 is installed on catalyst urceolus 240 and the catalyst inner core top 230, and catalyst 220 is filled in the space that is surrounded by internals bottom support 250, catalyst urceolus 240, catalyst inner core 230 and catalyst top annular grid 210.

Referring to Fig. 5, catalyst urceolus 240 adopts circumferentially spaced some heat exchanger tubes 241 formations, and can certainly adopting circumferentially, spaced some round bars consist of.Form certain gap between adjacent heat exchanger tube 241 or round bar, both kept catalyst not reveal the while also as the gas communication passage, the diameter of heat exchanger tube 241 or round bar and the gap of arrangement are determined according to process requirements and catalyst particle size.

The annular porous plate 242 that these heat exchanger tubes 241 can adopt several axially spaced-aparts to arrange connects (referring to Fig. 7).And adopt vertical connecting plate 243 to connect between the annular porous plate 242 that several axially spaced-aparts are arranged.

The material multiselect stainless steel of heat exchanger tube 241, annular porous plate 242 and vertical connecting plate 243.

For easy for installation, each annular porous plate 242 is formed by connecting by some arcuated porous plate 242a, and (referring to Fig. 6) like this catalyst urceolus 240 can the piecemeal manufacturing, in pressure-bearing shell 100 interior welding assembly units.

Again referring to Fig. 4, catalyst inner core 230 by on the pipe 231 of one section not perforate and the one section tube wall by the perforate cylinder 232 of regular perforate and adopt the heat exchanger tube 233 that circumferentially is spaced on perforate cylinder 232 outer walls to consist of, heat exchanger tube 233 also can adopt round bar to substitute certainly.

Pipe 231 is positioned at the top of catalyst inner core 230, and the top of perforate cylinder 232 is connected with the bottom of pipe 231, and the bottom of perforate cylinder 232 is connected on the internals bottom support 250, and the inner edge of catalyst top annular grid 210 is connected with pipe 231.The resistance of whole reactor is by 232 controls of perforate cylinder, and its percent opening should consider that suitable resistance is to guarantee that air-flow is even in the bed.Material is stainless steel.

Referring to Fig. 8 and Fig. 9, the annular porous plate 234 that the some heat exchanger tubes 233 in the catalyst inner core adopt several axially spaced-aparts to arrange connects, and perforate cylinder 232 is connected with annular porous plate 234.And the annular porous plate 234 that several axially spaced-aparts are arranged adopts vertical connecting plate 235 to connect.

Whole catalyst inner core 230 is whole preparation, lifting.The material multiselect stainless steel of its each part.233 of adjacent heat exchanger tubes form certain gap, have both kept catalyst not reveal the while also as the gas communication passage, and the diameter of heat exchanger tube 233 and the gap of arrangement are determined according to process requirements and catalyst particle size.

Operation principle of the present utility model is identical to the operation principle of the catalytic bed reactor that flows with the previously described diameter of axle, and reaction gas diameter of axle in bed utilizes catalyst to greatest extent to flowing.The main feature of this reactor has larger percent opening for utilizing circumferential compact arranged heat exchanger tube to form the catalyst inner/outer tube, avoids bed inner catalyst dead band, and bed resistance falls by perforate cylinder 232 controls that are welded in the catalyst inner core.

Claims (11)

1. fixed bed axial-radial flow reactor with comb wall type inner/outer tube, comprise pressure-bearing shell and be installed in the interior catalyst shell portion of described pressure-bearing shell, described catalyst shell portion comprises the internals bottom support, the catalyst urceolus, catalyst inner core and catalyst top annular grid, described internals bottom support is fixed on the bottom of described pressure-bearing shell, described catalyst urceolus and catalyst inner core are fixed on the described internals bottom support, described catalyst top annular grid is installed on described catalyst urceolus and the catalyst inner core top, catalyst is filled in by the internals bottom support, the catalyst urceolus, in the space that catalyst inner core and catalyst top annular grid surround, it is characterized in that described catalyst urceolus adopts circumferentially spaced some the first heat exchanger tubes or some the first round bars formation.

2. the fixed bed axial-radial flow reactor with comb wall type inner/outer tube as claimed in claim 1 is characterized in that, the first annular porous plate that some the first heat exchanger tubes in the described catalyst urceolus or some the first round bars adopt several axially spaced-aparts to arrange connects.

3. the fixed bed axial-radial flow reactor with comb wall type inner/outer tube as claimed in claim 2 is characterized in that, the first annular porous plate that described several axially spaced-aparts are arranged adopts first vertical connecting plate to connect.

4. as claimed in claim 2 or claim 3 with the fixed bed axial-radial flow reactor of comb wall type inner/outer tube, it is characterized in that each first annular porous plate is formed by connecting by some blocks of the first arcuated porous plates, like this so that the catalyst urceolus can the piecemeal manufacturing.

5. the fixed bed axial-radial flow reactor with comb wall type inner/outer tube as claimed in claim 1 is characterized in that, the gap between described the first heat exchanger tube or the first round bar is according to process requirements and catalyst particle size and determine.

6. the fixed bed axial-radial flow reactor with comb wall type inner/outer tube as claimed in claim 1, it is characterized in that, described catalyst inner core by on the pipe of one section not perforate and the one section tube wall by the perforate cylinder of regular perforate and adopt the second heat exchanger tube or the second round bar that circumferentially are spaced on the described perforate cylinder outer wall to consist of, wherein said pipe is positioned at the top of catalyst inner core, the top of described perforate cylinder is connected with the bottom of pipe, the bottom of perforate cylinder is connected on the described internals bottom support, and the inner edge of described catalyst top annular grid is connected with described pipe.

7. the fixed bed axial-radial flow reactor with comb wall type inner/outer tube as claimed in claim 6, it is characterized in that, the second annular porous plate that some the second heat exchanger tubes in the described catalyst inner core or some the second round bars adopt several axially spaced-aparts to arrange connects, and described perforate cylinder is connected with the described second annular porous plate.

8. the fixed bed axial-radial flow reactor with comb wall type inner/outer tube as claimed in claim 7 is characterized in that, the second annular porous plate that described several axially spaced-aparts are arranged adopts second vertical connecting plate to connect.

9. the fixed bed axial-radial flow reactor with comb wall type inner/outer tube as claimed in claim 6 is characterized in that, the gap between described the second heat exchanger tube or the second round bar is according to process requirements and catalyst particle size and determine.

10. the fixed bed axial-radial flow reactor with comb wall type inner/outer tube as claimed in claim 1 is characterized in that, described pressure-bearing shell inwall is lined with stainless steel lining.

11. the fixed bed axial-radial flow reactor with comb wall type inner/outer tube as claimed in claim 1 is characterized in that described pressure-bearing shell comprises upper and lower end socket, cylindrical shell, bearing; Wherein upper cover is connected with the welded top of cylindrical shell, offers manhole and thermocouple patchhole at upper cover, and thermocouple is inserted in the pressure cylinder by described thermocouple patchhole and passes described catalyst top annular grid and is inserted in the catalyst; Described low head is connected with the bottom welding of cylindrical shell, offers process gas import, process gas outlet and discharge port at low head, is inserted with the process gas outlet in the described process gas outlet, and described process gas outlet is connected with described catalyst inner core bottom; Be inserted with discharge duct in the described discharge port, the top of described discharge duct is connected with described internals bottom support; Form a process gas rising passway between the inwall of described cylindrical shell and the described catalyst urceolus, described upper cover inside is provided with the process gas chamber of turning back, and the described process gas chamber of turning back is communicated with described process gas rising passway; Described bearing is fixed on the middle and lower part of described cylinder body outer wall.

Images