CN109701455B - Isothermal and constant-flow-speed double-water-cooling horizontal reactor - Google Patents
Isothermal and constant-flow-speed double-water-cooling horizontal reactor Download PDFInfo
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- 238000001816 cooling Methods 0.000 title claims abstract description 34
- 239000003054 catalyst Substances 0.000 claims abstract description 93
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 54
- 239000000498 cooling water Substances 0.000 claims description 37
- 238000009826 distribution Methods 0.000 claims description 35
- 238000005192 partition Methods 0.000 claims description 8
- 241000251468 Actinopterygii Species 0.000 claims description 7
- 239000003795 chemical substances by application Substances 0.000 claims description 7
- 239000002826 coolant Substances 0.000 claims description 3
- 238000012544 monitoring process Methods 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 abstract description 18
- 239000012495 reaction gas Substances 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 51
- 238000012546 transfer Methods 0.000 description 15
- 238000010586 diagram Methods 0.000 description 8
- 238000000034 method Methods 0.000 description 7
- 230000008569 process Effects 0.000 description 7
- 230000000694 effects Effects 0.000 description 6
- 230000001681 protective effect Effects 0.000 description 4
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000006315 carbonylation Effects 0.000 description 1
- 238000005810 carbonylation reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000013341 scale-up Methods 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 238000013316 zoning Methods 0.000 description 1
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Abstract
The invention discloses an isothermal and constant flow rate double water-cooling horizontal reactor, which comprises a cylinder, a left end enclosure, a right end enclosure, a left end outer tube plate and a right end outer tube plate which are respectively arranged at the left end and the right end of the cylinder, a left end inner tube plate and a right end inner tube plate which are arranged in the cylinder, a catalyst frame arranged between the left end inner tube plate and the right end inner tube plate, and a sleeve-type water-cooling heat exchange tube group; the sleeve type water-cooling heat exchange tube group comprises two adjacent sleeve layers with opposite water inlet directions, each sleeve layer comprises a plurality of sleeves, each sleeve comprises an inner sleeve and an outer sleeve, one end of each outer sleeve is fixed by an inner tube plate, the other end of each outer sleeve is airtight and horizontally stretched into the catalyst bed layer, one end of each inner sleeve is fixed by an outer tube plate, and the other end of each inner sleeve horizontally stretches into the corresponding outer sleeve. The catalyst forms a rectangular catalyst bed outside the tube, and the reaction gas passes through the bed from top to bottom, so that no axial flow exists; the sleeve type water-cooling heat exchange tube groups are symmetrically arranged to traverse the catalyst bed, so that the isothermal property of the catalyst bed is achieved, and the aim of isothermal reaction of the bed is fulfilled.
Description
Technical Field
The invention belongs to the field of gas-solid phase catalytic reactors in chemical reaction engineering, relates to a low-pressure reaction device, in particular to an isothermal and constant-flow-rate double-water-cooling horizontal reactor, and particularly relates to a double-water-cooling horizontal reactor with strong heat transfer capacity, low fluid resistance and good isothermal performance.
Background
The variety of internally cooled gas-solid reactors is wide, with shell-and-tube reactors being the more common internally cooled gas-solid reactors. The shell-and-tube reactor can be divided into an axial flow reactor and a radial flow reactor according to the flow direction of the reaction gas passing through the catalyst bed layer, and the axial flow reactor can be divided into a vertical axial shell-and-tube reactor and a vertical axial cold tube reactor according to the catalyst filling mode.
The vertical axial flow shell-and-tube reactor (catalyst in tube and cooling water outside tube, as shown in figure 1) is a reactor operated by a plurality of tube reactors in parallel, and has the advantages of more cooling area, better isothermal property and equal flow velocity compared with the catalyst with the heat transfer surface reaching 100-140m 2/m3, and simpler structure. The defects are that the resistance is high, the large-scale is difficult, a plurality of single pipes are in closed operation, some single pipes are easy to overheat and fly to cause the single pipes to be damaged and stop production, as shown in figure 2, the temperature of the central point in the pipe type reactor gradually increases along with the progress of the reaction, and the temperature begins to fly to rise after reaching a certain position, and the temperature is uncontrollable.
The vertical axial cold tube reactor (the catalyst is outside the tube, and the cooling water is in the tube, as shown in figure 3) has the advantages that the catalyst bed is in open operation, even if the catalyst bed is overheated, single tube damage is not easily caused, the structure is simpler, but the heat transfer area is smaller, the heat transfer area is only 30-60m 2/m3 of the catalyst than that of the catalyst, the heat transfer capacity is insufficient, the isothermal performance is poor, and the reactor is not suitable for the working condition of strong exothermic reaction, because the catalyst is in axial flow, the resistance is large, the power consumption is high, and the catalyst is difficult to be large.
The vertical radial cold tube reactor (as shown in figure 4) has the advantages of small resistance, low power consumption and easy enlargement. The disadvantage is that the upper and lower ends of the bed layer have complex flow patterns in which radial flow and axial flow coexist simultaneously, and in the complex flow pattern region, the reaction with high requirements on isothermal property and isovelocity is not suitable.
Disclosure of Invention
The invention aims to provide an isothermal and constant-flow-rate double-water-cooling horizontal reactor.
The invention aims at realizing the following technical scheme:
The isothermal constant flow rate double water cooling horizontal reactor comprises a cylinder 9, a left end enclosure 1a and a right end enclosure 1b which are respectively arranged at two sides of the cylinder 9, a left end outer tube plate 3a and a right end outer tube plate 3b which are respectively arranged at the left end and the right end of the cylinder 9, a left end inner tube plate 6a and a right end inner tube plate 6b which are respectively arranged in the cylinder 9, a catalyst frame 21 which is arranged between the left end inner tube plate 6a and the right end inner tube plate 6b, and a plurality of sleeve type water cooling heat exchange tube groups; a left end pipe box is formed between the left end inner pipe plate 6a and the left end outer pipe plate 3a, and a right end pipe box is formed between the right end inner pipe plate 6b and the right end outer pipe plate 3 b; the catalyst frame 21 is filled with catalyst to form a catalyst bed, the top of the cylinder 9 is provided with a plurality of air inlets 11, the inner wall of the top of the cylinder 9 is provided with a gas distribution pipe 8, the bottom of the cylinder 9 is provided with a plurality of air outlets 18, the inner wall of the bottom of the cylinder 9 is provided with a gas collection pipe 17, and reaction gas enters the reactor from the air inlets 11, uniformly distributes through the gas distribution pipe 8, passes through the bed from top to bottom, is collected by the gas collection pipe 17 and is discharged from the gas outlets 18; the left end enclosure and the right end enclosure are respectively provided with a plurality of cooling water inlets 5, and the top and/or the bottom of the left end pipe box and the right end pipe box are respectively provided with a cooling water outlet 12; the sleeve type water-cooling heat exchange tube group comprises two adjacent sleeve layers with opposite water inlet directions, each sleeve layer comprises a plurality of sleeves, each sleeve comprises an inner sleeve and an outer sleeve, one end of each outer sleeve is fixed by a left end inner tube plate 6a or a right end inner tube plate 6b, the other end of each outer sleeve is sealed and horizontally stretched into the catalyst bed layer but is not contacted with the right end inner tube plate 6b or the left end inner tube plate 6a to leave an expansion gap, one end of each inner sleeve is fixed by a left end outer tube plate 3a or a right end outer tube plate 3b, the other end of each inner sleeve horizontally stretches into the corresponding outer sleeve, the end of each inner sleeve is not contacted with the end of each outer sleeve to leave an expansion gap, cooling water enters the inner sleeve, returns after flowing to a terminal along the inner sleeve, flows to an outer sleeve water outlet port through an annular gap between the inner sleeve and the outer sleeve, is converged in a tube box, and is discharged out of the reactor through a cooling water outlet.
The axes of the outer sleeve and the inner sleeve in the sleeve are positioned on the same horizontal line.
Preferably, a partition plate 2 is arranged in the left end socket and the right end socket along the cooling water inlet 5 respectively to divide the end socket into a plurality of water inlet distribution channels along the vertical direction so as to distribute cooling water into the inner sleeve. In specific operation, the heat is removed according to the requirement of the reaction zone to carry out zoning and control the water inlet temperature and the water inlet quantity.
The triangular pipe arrangement is realized by the staggered arrangement of the sleeves of the adjacent two layers of sleeve layers with opposite water inlet directions, namely the triangular pipe arrangement is realized by the staggered arrangement of the sleeves of the sleeve layers with opposite water inlet directions. The triangle is an equilateral triangle. The sleeves of two adjacent sleeve layers with the same water inlet direction are in a rectangular pipe distribution mode.
Preferably, one end of the outer sleeve is welded on the left inner tube plate 6a or the right inner tube plate 6b, and the outer sleeve extending into the catalyst frame 21 is supported by a plurality of support plates 10; one end of the inner sleeve is welded on the left end outer tube plate 3a or the outer end outer tube plate 3 b.
The supporting plate 10 is a rectangular plate, and the rectangular plate is provided with a hole for the outer sleeve to pass through.
Preferably, the annular gap between the inner sleeve and the outer sleeve is 2-6mm; the pipe diameter phi of the outer sleeve is 14-32mm; the outer sleeve is a reducing pipe or a pipeline with a constant diameter.
Preferably, the sleeve type water-cooling heat exchange tube group comprises a left end sleeve layer and a right end sleeve layer which are adjacent up and down; the left end sleeve layer comprises a plurality of left end sleeves, each left end sleeve comprises a left end inner sleeve 4a and a left end outer sleeve 7a, one end of each left end outer sleeve 7a is fixed by a left end inner tube plate 6a, the other end of each left end outer sleeve 7a is airtight and horizontally stretches into the catalyst bed layer, and the part of each outer sleeve stretching into the catalyst frame 21 is supported by a plurality of support plates 10; one end of the left inner sleeve 4a is fixed by a left outer tube plate 3a, the other end horizontally extends into the corresponding left outer sleeve 7a, the end part of the left inner sleeve 4a is not contacted with the end part of the left outer sleeve 7a, cooling water enters the left end socket 1a, is distributed into the inner sleeve through the partition plate 2, flows to the terminal along the inner sleeve and then turns back, flows to the outer sleeve water outlet port through an annular gap between the inner sleeve and the outer sleeve, is converged in the tube box, and is discharged out of the reactor through the cooling water outlet 5; the right-end sleeve layer comprises a plurality of right-end sleeves, each right-end sleeve comprises a right-end inner sleeve 4b and a right-end outer sleeve 7b, one end of each right-end outer sleeve 7b is fixed by a right-end inner tube plate 6b, the other end of each right-end outer sleeve is airtight and horizontally stretches into the catalyst bed layer, and the part of each outer sleeve stretching into the catalyst frame 21 is supported by a plurality of support plates 10; one end of the right inner sleeve 4b is fixed by the right outer tube plate 3b, the other end horizontally extends into the corresponding outer sleeve, and the end of the right inner sleeve 4b is not contacted with the end of the right outer sleeve 7 b.
In order to facilitate maintenance, a plurality of manholes 19 are arranged at the upper part and the lower part of the cylinder 9. And simultaneously the width of the left end pipe box and the right end pipe box is controlled to be about 1m.
Preferably, the air distribution pipe 8 is a semicircular pipe, two side arc edges of the air distribution pipe 8 are welded on the inner wall of the top of the cylinder 9, and air distribution holes are formed in the air distribution pipe 8.
Each air inlet 11 is provided with an air distribution pipe 8, and pipe orifices at two ends of the air distribution pipe 8 are closed; or all the air inlets 11 are provided with an air distribution pipe 8, and the pipe orifices at the two ends of the air distribution pipe 8 are sealed or connected with the inner pipe plates at the left end and the right end.
Preferably, the gas collecting tube 17 is a semicircular tube, two side arc edges of the gas collecting tube 17 are welded on the inner wall of the bottom of the cylinder 9, and gas collecting holes are formed in the gas collecting tube 17 to enable gas to enter the tube through the small holes, and the gas is discharged from the gas outlet after being collected.
Each air outlet 18 is provided with a gas collecting tube 17, and the tube openings at the two ends of the gas collecting tube 17 are closed; or all the air outlets 18 are provided with a gas collecting tube 17, and the tube orifices at the two ends of the gas collecting tube 17 are sealed or connected with the inner tube plates at the left end and the right end.
Preferably, the catalyst frame 21 is a cuboid catalyst frame; the top of the catalyst frame 21 is open, the bottom is provided with a fish plate and a gas collecting plate 16 from top to bottom in sequence, the catalyst frame has the functions of supporting and isolating catalysts, the front side plate and the rear side plate of the catalyst frame 21 respectively form a closed cavity with the inner wall of the cylinder 9 on the same side for cooling medium to flow, the lower part of the cylinder corresponding to the closed cavity is provided with a protective water inlet 14, and the upper part of the cylinder is provided with a protective water outlet 20. The length of the scale holes on the scale plate is 10-100mm, the width is smaller than the granularity of the catalyst, and the distance between adjacent scale holes is 25-80mm; the air collecting plate 16 is provided with vent holes, and the vent holes are matched with the fish scale plates to avoid air flow dead angles and play a role in efficient air distribution.
Further, an axial support beam 22 is provided on the inner wall of the lower portion of the cylinder 9, and the gas collecting plate 16 is supported by the support beam 22 and is not welded to the cylinder.
The front and rear side plates of the catalyst basket 21 are welded to the inner wall of the cylinder 1.
Preferably, a plurality of agent filling holes are arranged on the corresponding cylinder 9 at the top of the catalyst frame 21, and the catalyst can be filled into the catalyst frame directly through the agent filling holes without opening the cylinder; the catalyst can be replaced by arranging a plurality of catalyst discharging holes 15 on the corresponding cylinder body 9 at the bottom of the catalyst frame 21 along the axial direction, and the distance between two adjacent catalyst discharging holes 15 is about 0.7-0.8m.
The length-diameter ratio of the isothermal and equal flow rate double water-cooling horizontal reactor disclosed by the invention is L:D=1:1-1:10, the fluid resistance of the isothermal and equal flow rate double water-cooling horizontal reactor is approximately 1/10-1/2 of that of the axial flow reactor, the power consumption can be greatly saved, and the isothermal and equal flow rate double water-cooling horizontal reactor is favorable for realizing the large-scale. The length L corresponds to the distance between the left and right inner tube sheets.
Preferably, a plurality of rows of temperature measuring couple ports are respectively arranged on the left end socket and the right end socket, and a thermocouple 13 is arranged from the temperature measuring couple ports and used for monitoring the temperature of the catalyst bed. Further preferably, the distance between two upper and lower thermocouples 13 in the same column is about 250-300mm.
As shown in FIG. 8, the catalyst bed is a regular long rectangle, the catalyst is arranged outside the tube, the flow rate of the process gas is unchanged from top to bottom, the process gas completely flows at the same flow rate, no axial flow exists, and no flow state of the axial-radial mixed flow exists at any part of the bed.
As shown in fig. 9 or 10, the bed heat exchange partition is realized through a cooling water inlet and a water inlet distribution channel, cooling water enters the left end socket 1a, is distributed into the left end inner sleeve 4a through the partition board 2, flows to the terminal along the left end inner sleeve and then turns back, flows to the water outlet port of the left end outer sleeve 7a through the annular gap between the inner sleeve and the outer sleeve, is converged in a pipe box, and is discharged out of the reactor through the cooling water outlet 5; cooling water enters the right end enclosure 1b, is distributed into the right end inner sleeve 4b through the partition plate 2, flows to the terminal along the inner sleeve and is turned back, flows to the water outlet port of the right end outer sleeve 7b through the annular gap between the inner sleeve and the outer sleeve, is converged in the pipe box, and is discharged out of the reactor through the cooling water outlet 5; the water temperature is respectively controlled through the cooling water circulation flow to realize the control of the bed temperature, and the heat transfer capacity and the conversion rate are improved to meet the reaction requirements. Meanwhile, circulating water is introduced into the water jackets at the two sides of the catalyst basket, water bath protection is formed between the outer cylinders of the reaction zone, the heat transfer effect can be effectively realized, the cold wall effect is reduced, the temperature difference of the shell is ensured to be within 20-30 ℃, and the temperature difference stress of the shell is effectively reduced.
Compared with the existing vertical shell-and-tube reactor, the invention has the beneficial effects that:
compared with the radial flow reactor with the same low resistance, the catalyst bed in the horizontal reactor is regular long rectangular, the catalyst is arranged outside the tube, the flow rate of the process gas is unchanged from top to bottom, the process gas completely flows at the same flow rate, no axial flow exists, no flow state of the axial-radial mixed flow exists at any part of the bed, and the horizontal reactor is suitable for certain special chemical reactions with the same flow rate.
The invention adopts the integral structure, can densely arrange pipes, increase the number of the pipes, lead the specific heat transfer surface to reach 180-240m 2/m3 of catalyst, and can meet the heat transfer requirement of the strongest exothermic reaction. The sleeve type water-cooling heat exchange tube groups are symmetrically arranged to traverse the catalyst bed, so that the bed layer achieves the purpose of flow state with the same flow rate, the diameter and the number of the outer sleeves are determined by the heat transfer quantity of the reactor, the diameter and the length of the inner sleeves are determined by the isothermicity of the temperature compensation at the two ends of the catalyst bed layer, the temperature of the outer sleeves achieves the optimal temperature difference compensation, the sleeve type water-cooling heat exchange tubes are symmetrically arranged and mutually compensated, the isothermal heat transfer characteristic of the sleeve type water-cooling heat exchange tubes is achieved, the isothermal heat transfer of the catalyst in the exothermic reaction process is achieved, the isothermicity of the catalyst bed layer is achieved, and the purpose of isothermal reaction of the bed layer is achieved.
One section of the water cooling sleeve is fixed, the other end is a free end, and the temperature difference stress of each water cooling pipe can be eliminated to the maximum extent, so that the reliability of the long-period running of the reactor is improved.
The catalyst basket and the water jackets at the two sides of the catalyst basket are designed to be filled with circulating water, water bath protection is formed between the outer cylinders of the reaction zone, the temperature difference of the shell is ensured to be within 20-30 ℃ while the heat transfer effect is effectively achieved and the cold wall effect is reduced, and the temperature difference stress of the shell is effectively reduced.
The double water-cooling horizontal reactor has very low fluid resistance and has important significance for saving energy consumption, and enlarging and scale-up the reactor.
Drawings
FIG. 1 is a schematic diagram of a vertical axial flow tube reactor;
FIG. 2 is a graph showing the temperature profile of a tubular reactor;
FIG. 3 is a schematic diagram of a vertical axial flow reactor;
FIG. 4 is a schematic view of a vertical radial flow reactor;
FIG. 5 is a schematic diagram of the structure of the isothermal and constant flow rate double water-cooled horizontal reactor of the present invention;
FIG. 6 is a cross-sectional view taken along A-A of FIG. 5;
FIG. 7 is a schematic diagram of the seal head nozzle of FIG. 5;
FIG. 8 is a schematic diagram of a process gas passing through a catalyst bed of a catalytic frame of an isothermal, constant flow rate, double water cooled horizontal reactor according to the present invention;
FIG. 9 is a schematic diagram of the cooling water circulation flow of the isothermal and constant flow rate double water-cooled horizontal reactor (provided with double steam-bags) of the invention;
FIG. 10 is a schematic diagram of the cooling water circulation flow of the isothermal and constant flow rate double water-cooled horizontal reactor (single steam drum);
FIG. 11 is a schematic diagram showing a cooling water circulation flow in example 1.
In the figure, 1 a-left end enclosure, 1 b-right end enclosure, 2-water inlet baffle, 3 a-left end outer tube plate, 3 b-right end outer tube plate, 4 a-left end inner tube, 4 b-right end inner tube, 5-cooling water inlet, 6 a-left end inner tube plate, 6 b-right end inner tube plate, 7 a-left end outer tube, 7 b-right end outer tube, 8-gas distribution tube, 9-cylinder, 10-support plate, 11-gas inlet, 12-cooling water outlet, 13-thermocouple, 14-protection water inlet, 15-discharge port, 16-gas collecting plate, 17-gas collecting tube, 18-gas outlet, 19-manhole, 20-protection water outlet, 21-catalyst frame and 22-support beam.
Detailed Description
The technical scheme of the invention is further described through the specific embodiments. The parameters of the embodiments are merely preferred embodiments of the present invention, and are not intended to limit the invention, but all modifications, equivalents, improvements, etc. within the spirit and principles of the invention are included in the scope of the invention.
Example 1
As shown in fig. 5 to 7, the isothermal and constant flow rate double water-cooling horizontal reactor comprises a cylinder 9, a left end enclosure 1a and a right end enclosure 1b which are respectively arranged at two sides of the cylinder 9, a left end outer tube plate 3a and a right end outer tube plate 3b which are respectively arranged at the left end and the right end of the cylinder 9, a left end inner tube plate 6a and a right end inner tube plate 6b which are respectively arranged in the cylinder 9, a catalyst frame 21 arranged between the left end inner tube plate 6a and the right end inner tube plate 6b, a plurality of sleeve-type water-cooling heat exchange tube groups and a plurality of manholes 19 which are arranged at the upper part and the lower part of the cylinder 9; a left end pipe box is formed between the left end inner pipe plate 6a and the left end outer pipe plate, a right end pipe box is formed between the right end inner pipe plate 6b and the right end outer pipe plate 3b, and the width of the left end pipe box and the width of the right end pipe box are about 1m; the catalyst frame 21 is filled with catalyst to form a catalyst bed, the top of the cylinder 9 is provided with a plurality of air inlets 11, the inner wall of the top of the cylinder 9 is provided with a gas distribution pipe 8, the bottom of the cylinder 9 is provided with a plurality of air outlets 18, the inner wall of the bottom of the cylinder 9 is provided with a gas collection pipe 17, and reaction gas enters the reactor from the air inlets 11, uniformly distributes through the gas distribution pipe 8, passes through the bed from top to bottom, is collected by the gas collection pipe 17 and is discharged from the gas outlets 18; the left end enclosure and the right end enclosure are respectively provided with a plurality of cooling water inlets 5, and the top parts of the left end pipe box and the right end pipe box are respectively provided with a cooling water outlet 12; the sleeve type water-cooling heat exchange tube group comprises two adjacent sleeve layers with opposite water inlet directions, namely a left sleeve layer and a right sleeve layer, the left sleeve layer comprises a plurality of left sleeves, the left sleeve comprises a left inner sleeve 4a and a left outer sleeve 7a, one end of the left outer sleeve 7a is fixed by a left inner tube plate 6a, the other end of the left outer sleeve 7a is airtight and horizontally stretches into the catalyst bed layer but does not contact with a right inner tube plate 6b to leave an expansion gap, and the part of the outer sleeve stretching into the catalyst frame 21 is supported by a plurality of support plates 10; one end of the left inner sleeve 4a is fixed by the left outer tube plate 3a, the other end horizontally extends into the corresponding left outer sleeve 7a to enable the axes of the outer sleeve and the inner sleeve to be positioned on the same horizontal line, and the end part of the left inner sleeve 4a is not contacted with the end part of the left outer sleeve 7 a; the right-end sleeve layer comprises a plurality of right-end sleeves, each right-end sleeve comprises a right-end inner sleeve 4b and a right-end outer sleeve 7b, one end of each right-end outer sleeve 7b is fixed by a right-end inner tube plate 6b, the other end of each right-end outer sleeve is airtight and horizontally stretches into the catalyst bed layer, and the part of each outer sleeve stretching into the catalyst frame 21 is supported by a plurality of support plates 10; one end of the right inner sleeve 4b is fixed by the right outer tube plate 3b, the other end horizontally extends into the corresponding outer sleeve, and the end of the right inner sleeve 4b is not contacted with the end of the right outer sleeve 7 b. And a baffle plate 2 is arranged in the left end socket and the right end socket along the cooling water inlet 5 respectively, and the end sockets are separated into water inlet distribution channels by the baffle plate 2 to distribute cooling water into the inner sleeve.
The sleeves of two adjacent sleeve layers with opposite water inlet directions are staggered to realize equilateral triangle pipe distribution, and the pipe spacing is 23mm; the sleeves of two adjacent sleeve layers with the same water inlet direction are in a rectangular pipe distribution mode.
The annular gap between the inner sleeve and the outer sleeve is 4mm.
The supporting plate 10 is a rectangular plate and is provided with holes corresponding to the pipe diameters of the outer sleeves, and the outer sleeves penetrate through the holes of the supporting plate.
The gas distribution pipe 8 is a semicircular pipe, two side arc edges of the gas distribution pipe 8 are welded on the inner wall of the top of the cylinder 9, and gas distribution holes are formed in the gas distribution pipe 8. All air inlets 11 are provided with an air distribution pipe 8, and pipe orifices at two ends of the air distribution pipe 8 are sealed or connected with inner pipe plates at the left end and the right end.
The gas collecting tube 17 is a semicircular tube, two side arc edges of the gas collecting tube 17 are welded on the inner wall of the bottom of the cylinder 9, the gas collecting tube 17 is provided with gas collecting holes so that gas enters the tube through small holes, and the gas is discharged from the gas outlet after being collected. All the air outlets 18 are provided with a gas collecting tube 17, and the tube openings at the two ends of the gas collecting tube 17 are sealed or connected with the inner tube plates at the left end and the right end.
The catalyst frame 21 is a cuboid catalyst frame; the upper part of the catalyst frame 21 is provided with an opening, the bottom is sequentially provided with a louver and a gas collecting plate 16 from top to bottom, the length of the louver holes on the louver is 10-100mm, the width is smaller than the granularity of the catalyst, the distance between every two adjacent louver holes is 25-80mm, the gas collecting plate 16 is provided with vent holes, and the gas collecting plate 16 is supported by a supporting beam 22 in the axial direction of the inner wall of the lower part of the cylinder 9; the front and rear side plates of the catalyst basket 21 are welded on the inner wall of the cylinder 9 respectively, and a closed cavity is formed on the inner wall of the cylinder 9 on the same side for cooling medium to flow, a protective water inlet 14 is arranged at the lower part of the cylinder 9 corresponding to the closed cavity, and a protective water outlet 20 is arranged at the upper part. The cylinder 9 corresponding to the top of the catalyst frame 21 is provided with a plurality of agent loading holes, the cylinder 9 corresponding to the bottom of the catalyst frame 21 is provided with a plurality of agent unloading holes 15 along the axial direction, and the distance between two adjacent agent unloading holes 15 is about 0.8m.
The left end socket and the right end socket are respectively provided with a plurality of rows of temperature measuring thermocouple ports, the distance between the upper and lower adjacent thermocouples 13 in the same row is about 250-300mm, and the thermocouples 13 are arranged from the temperature measuring thermocouple ports and used for monitoring the temperature of the catalyst bed.
As shown in FIG. 8, the catalyst bed is a regular long rectangle, the catalyst is arranged outside the tube, the flow rate of the process gas is unchanged from top to bottom, the process gas completely flows at the same flow rate, no axial flow exists, and no flow state of the axial-radial mixed flow exists at any part of the bed.
The diameter of the cylinder 9 in this embodiment is 3400mm; the length of the outer sleeve is 11000mm, the length-diameter ratio of the reactor is 3.2, the outer sleeve is 7a and 7b with the specification phi of 19mm, the inner sleeve is 4a and 4b with the specification phi of 8mm, the number of heat exchange tubes is 8500, the specific cooling surface of the catalyst is 200m 2/m3, the water inlet areas at the a and b ends are respectively 3 areas, the cooling water is circulated to form a single steam drum, the flow chart is shown in figure 11, bed heat exchange areas are realized through a cooling water inlet and a water inlet distribution channel, cooling water enters the left end enclosure 1a, is distributed into the left end inner sleeve 4a through a partition board 2, flows back after flowing to the terminal along the left end inner sleeve, flows to the water outlet port of the left end outer sleeve 7a through an annular gap between the inner sleeve and the outer sleeve, is converged in a tube box, and is discharged out of the reactor through the cooling water outlet 5; cooling water enters the right end enclosure 1b, is distributed into the right end inner sleeve 4b through the partition plate 2, flows to the terminal along the inner sleeve and is turned back, flows to the water outlet port of the right end outer sleeve 7b through the annular gap between the inner sleeve and the outer sleeve, is converged in the pipe box, and is discharged out of the reactor through the cooling water outlet 5; the water temperature is respectively controlled through the cooling water circulation flow to realize the control of the bed temperature, and the heat transfer capacity and the conversion rate are improved to meet the reaction requirements. Meanwhile, circulating water is introduced into the water jackets at the two sides of the catalyst basket, water bath protection is formed between the outer cylinders of the reaction zone, the heat transfer effect can be effectively realized, the cold wall effect is reduced, the temperature difference of the shell is ensured to be within 20-30 ℃, and the temperature difference stress of the shell is effectively reduced.
The results of the comparison of the isothermal and equal-flow-rate double-water-cooled horizontal reactor of the present example as a reactor for the carbonylation of ethylene glycol with an annual production of 7 ten thousand tons with a vertical shell-and-tube reactor of the same scale are shown in Table 1.
TABLE 1
Note that: "x 2" is two vertical shell-and-tube reactors.
Example 2
On the basis of the isothermal and constant flow rate double water-cooled horizontal reactor in the embodiment 1, cooling water outlets 12 are respectively arranged at the bottoms of the left end pipe box and the right end pipe box.
Claims (7)
1. The isothermal constant flow rate double water cooling horizontal reactor is characterized by comprising a cylinder, a left end socket and a right end socket which are respectively arranged at two sides of the cylinder, a left end outer tube plate and a right end outer tube plate which are respectively arranged at the left end and the right end of the cylinder, a left end inner tube plate and a right end inner tube plate which are respectively arranged in the cylinder, a catalyst frame arranged between the left end inner tube plate and the right end inner tube plate, and a plurality of sleeve type water cooling heat exchange tube groups; a left end pipe box is formed between the left end inner pipe plate and the left end outer pipe plate, and a right end pipe box is formed between the right end inner pipe plate and the right end outer pipe plate; filling a catalyst into the catalyst frame to form a catalyst bed, wherein the catalyst frame is a cuboid catalyst frame; the top of the catalyst frame is open, the bottom of the catalyst frame is sequentially provided with a fish scale plate and a gas collecting plate from top to bottom, the length of fish scale holes on the fish scale plate is 10-100mm, the width of the fish scale holes is smaller than the granularity of the catalyst, and the distance between adjacent fish scale holes is 25-80mm; the gas collecting plate is provided with vent holes; the front side plate and the rear side plate of the catalyst basket respectively form a closed cavity with the inner wall of the cylinder body on the same side for cooling medium to flow, the lower part of the cylinder body corresponding to the closed cavity is provided with a protection water inlet, and the upper part of the cylinder body is provided with a protection water outlet; the cylinder top is provided with a plurality of air inlets, an air distribution pipe is arranged along the inner wall of the cylinder top, the air distribution pipe is a semicircular pipe, the two side arc edges of the air distribution pipe are welded on the inner wall of the cylinder top, and the air distribution pipe is provided with air distribution holes; the bottom of the cylinder body is provided with a plurality of air outlets, and a gas collecting pipe is arranged along the inner wall of the bottom of the cylinder body; the left end enclosure and the right end enclosure are respectively provided with a plurality of cooling water inlets, and the top and/or the bottom of the left end pipe box and the right end pipe box are respectively provided with a cooling water outlet; the sleeve type water-cooling heat exchange tube group comprises a left end sleeve layer and a right end sleeve layer which are vertically adjacent, the left end sleeve layer comprises a plurality of left end inner sleeves and left end outer sleeves, one end of each left end outer sleeve is fixed by a left end inner tube plate, the other end of each left end outer sleeve is airtight and horizontally stretched into the catalyst bed layer, one end of each left end inner sleeve is fixed by a left end outer tube plate, the other end of each left end inner sleeve horizontally stretches into the corresponding left end outer sleeve, and the end part of each left end inner sleeve is not contacted with the end part of each left end outer sleeve; the right end sleeve layer comprises a plurality of right end inner sleeves and right end outer sleeves, one end of each right end outer sleeve is fixed by a right end inner tube plate, the other end of each right end outer sleeve is airtight and horizontally stretched into the catalyst bed layer, one end of each right end inner sleeve is fixed by a right end outer tube plate, the other end of each right end inner sleeve horizontally stretches into the corresponding outer sleeve, and the end of each right end inner sleeve is not contacted with the end of each right end outer sleeve; the sleeves of two adjacent sleeve layers with opposite water inlet directions are staggered to form a triangular pipe distribution mode; the sleeves of two adjacent sleeve layers with the same water inlet direction are in a rectangular pipe distribution mode.
2. The isothermal and constant flow rate double water cooled horizontal reactor according to claim 1, wherein the portion of the outer sleeve extending into the catalyst frame is supported by a plurality of support plates.
3. The isothermal and constant flow rate double water cooling horizontal reactor according to claim 1, wherein the annular gap between the inner and outer sleeves is 2-6mm; the pipe diameter of the outer sleeve is 14-32mm.
4. The isothermal and equal flow rate double water cooled horizontal reactor according to claim 1, wherein a partition plate is disposed along the cooling water inlet in each of the left and right seal heads, and the seal heads are divided into a plurality of water inlet distribution channels in the vertical direction to distribute cooling water into the inner sleeve.
5. The isothermal and constant flow rate double water cooling horizontal reactor according to claim 1, wherein a plurality of manholes are arranged at the upper part and the lower part of the cylinder; the left end socket and the right end socket are respectively provided with a plurality of rows of temperature measuring thermocouple ports, and thermocouples are arranged from the temperature measuring thermocouple ports and used for monitoring the temperature of the catalyst bed.
6. The isothermal and constant flow rate double water cooling horizontal reactor according to claim 1, wherein the gas collecting tube is a semicircle tube, the two side arc edges of the gas collecting tube are welded on the inner wall of the bottom of the cylinder, and the gas collecting tube is provided with a gas collecting hole.
7. The isothermal and equal flow rate double water cooling horizontal reactor according to claim 1, wherein a plurality of agent loading holes are axially arranged on the corresponding cylinder body at the top of the catalyst frame, and a plurality of agent unloading holes are axially arranged on the corresponding cylinder body at the bottom of the catalyst frame.
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Citations (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB471424A (en) * | 1935-03-04 | 1937-09-03 | Houdry Process Corp | Converters and their assembly |
| US3711253A (en) * | 1970-01-16 | 1973-01-16 | Fischer Apparate Rohr | Apparatus for synthesis of formaldehyde |
| US4305910A (en) * | 1979-02-28 | 1981-12-15 | Mitsui Engineering And Shipbuilding Co., Ltd. | Catalytic reaction for reduction of nitrogen oxide |
| DE3310772A1 (en) * | 1983-03-24 | 1984-09-27 | Interatom Internationale Atomreaktorbau Gmbh, 5060 Bergisch Gladbach | Methanol synthesis reactor with low-boiling coolant |
| CN1181452A (en) * | 1996-10-15 | 1998-05-13 | 康宁股份有限公司 | Method of making catalytic converter for use in internal combustion engine |
| CN2328420Y (en) * | 1998-03-09 | 1999-07-14 | 中国成达化学工程公司 | Horizontal reaction synthesizing tower |
| EP1060788A1 (en) * | 1999-06-15 | 2000-12-20 | Methanol Casale S.A. | Isothermal catalytic reactor for exothermic or endothermic heterogeneous reactions |
| DE10047693A1 (en) * | 2000-09-25 | 2002-04-11 | Basf Ag | Process for lengthening the service life of catalysts comprises using a charge of inert material in the contact tubes, the tubular base and between the base and gas inlet and outlet |
| CN1788835A (en) * | 2004-12-14 | 2006-06-21 | 杭州林达化工技术工程有限公司 | Transverse pipe type heat transfer reaction unit |
| CN1856358A (en) * | 2003-07-24 | 2006-11-01 | 巴斯福股份公司 | Preparation of (meth)acrolein and/or (meth)acrylic acid by heterogeneously catalyzed partial oxidation of C3 and/or C4 precursor compounds in a reactor having thermoplate modules |
| CN201253566Y (en) * | 2008-09-16 | 2009-06-10 | 庞玉学 | Heat exchange type reborner |
| CN202570111U (en) * | 2012-03-30 | 2012-12-05 | 池州东升药业有限公司 | Formaldehyde catalyst basket with jacket |
| JP2012236161A (en) * | 2011-05-12 | 2012-12-06 | Mitsubishi Rayon Co Ltd | Fixed-bed multitubular reactor and production method for the fixed-bed multitubular reactor |
| CN102836676A (en) * | 2012-09-28 | 2012-12-26 | 神华集团有限责任公司 | Gas-solid phase catalytic reactor |
| CN103585932A (en) * | 2013-10-30 | 2014-02-19 | 浙江大学 | Bionic fixed bed reactor with distributed feeding and discharging network channels |
| CN204952858U (en) * | 2015-08-06 | 2016-01-13 | 天津大学 | Self -balancing heat pipe formula isothermal reactor |
| CN209612901U (en) * | 2019-02-25 | 2019-11-12 | 南京国昌化工科技有限公司 | A kind of double water cooling horizontal reactors of isothermal uniform flow |
-
2019
- 2019-02-25 CN CN201910137982.1A patent/CN109701455B/en active Active
Patent Citations (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB471424A (en) * | 1935-03-04 | 1937-09-03 | Houdry Process Corp | Converters and their assembly |
| US3711253A (en) * | 1970-01-16 | 1973-01-16 | Fischer Apparate Rohr | Apparatus for synthesis of formaldehyde |
| US4305910A (en) * | 1979-02-28 | 1981-12-15 | Mitsui Engineering And Shipbuilding Co., Ltd. | Catalytic reaction for reduction of nitrogen oxide |
| DE3310772A1 (en) * | 1983-03-24 | 1984-09-27 | Interatom Internationale Atomreaktorbau Gmbh, 5060 Bergisch Gladbach | Methanol synthesis reactor with low-boiling coolant |
| CN1181452A (en) * | 1996-10-15 | 1998-05-13 | 康宁股份有限公司 | Method of making catalytic converter for use in internal combustion engine |
| CN2328420Y (en) * | 1998-03-09 | 1999-07-14 | 中国成达化学工程公司 | Horizontal reaction synthesizing tower |
| EP1060788A1 (en) * | 1999-06-15 | 2000-12-20 | Methanol Casale S.A. | Isothermal catalytic reactor for exothermic or endothermic heterogeneous reactions |
| DE10047693A1 (en) * | 2000-09-25 | 2002-04-11 | Basf Ag | Process for lengthening the service life of catalysts comprises using a charge of inert material in the contact tubes, the tubular base and between the base and gas inlet and outlet |
| CN1856358A (en) * | 2003-07-24 | 2006-11-01 | 巴斯福股份公司 | Preparation of (meth)acrolein and/or (meth)acrylic acid by heterogeneously catalyzed partial oxidation of C3 and/or C4 precursor compounds in a reactor having thermoplate modules |
| CN1788835A (en) * | 2004-12-14 | 2006-06-21 | 杭州林达化工技术工程有限公司 | Transverse pipe type heat transfer reaction unit |
| CN201253566Y (en) * | 2008-09-16 | 2009-06-10 | 庞玉学 | Heat exchange type reborner |
| JP2012236161A (en) * | 2011-05-12 | 2012-12-06 | Mitsubishi Rayon Co Ltd | Fixed-bed multitubular reactor and production method for the fixed-bed multitubular reactor |
| CN202570111U (en) * | 2012-03-30 | 2012-12-05 | 池州东升药业有限公司 | Formaldehyde catalyst basket with jacket |
| CN102836676A (en) * | 2012-09-28 | 2012-12-26 | 神华集团有限责任公司 | Gas-solid phase catalytic reactor |
| CN103585932A (en) * | 2013-10-30 | 2014-02-19 | 浙江大学 | Bionic fixed bed reactor with distributed feeding and discharging network channels |
| CN204952858U (en) * | 2015-08-06 | 2016-01-13 | 天津大学 | Self -balancing heat pipe formula isothermal reactor |
| CN209612901U (en) * | 2019-02-25 | 2019-11-12 | 南京国昌化工科技有限公司 | A kind of double water cooling horizontal reactors of isothermal uniform flow |
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