CN108421505B - Radial-axial combined reactor suitable for strong exothermic reaction - Google Patents
Radial-axial combined reactor suitable for strong exothermic reaction Download PDFInfo
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- CN108421505B CN108421505B CN201810493628.8A CN201810493628A CN108421505B CN 108421505 B CN108421505 B CN 108421505B CN 201810493628 A CN201810493628 A CN 201810493628A CN 108421505 B CN108421505 B CN 108421505B
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 72
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 44
- 239000003054 catalyst Substances 0.000 claims abstract description 30
- 239000007789 gas Substances 0.000 claims description 117
- 239000012495 reaction gas Substances 0.000 claims description 11
- 238000000926 separation method Methods 0.000 claims description 9
- 239000002131 composite material Substances 0.000 claims description 5
- 238000007789 sealing Methods 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 4
- 230000000149 penetrating effect Effects 0.000 claims description 2
- 230000015572 biosynthetic process Effects 0.000 abstract description 17
- 238000003786 synthesis reaction Methods 0.000 abstract description 17
- 230000000694 effects Effects 0.000 description 13
- 239000002699 waste material Substances 0.000 description 3
- 238000000034 method Methods 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0278—Feeding reactive fluids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0285—Heating or cooling the reactor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
Abstract
The invention discloses a radial-axial combined reactor suitable for strong exothermic reaction, which comprises an annular high-temperature area, a low-temperature area and a heat exchange area, wherein a plurality of first heat exchange pipes, a plurality of second heat exchange pipes and a plurality of third heat exchange pipes are respectively arranged in the high-temperature area, the low-temperature area and the heat exchange area, catalysts are filled in the shell passes of the plurality of first heat exchange pipes and the shell passes of the plurality of second heat exchange pipes, the tube pass inlets of the plurality of first heat exchange pipes are communicated with a water outlet of a circulating hot water supply mechanism, the tube pass inlets of the plurality of second heat exchange pipes and the tube pass inlets of the plurality of third heat exchange pipes are respectively communicated with the shell pass inlets of the plurality of first heat exchange pipes, the shell passes of the plurality of third heat exchange pipes and the shell passes and the middle channels of the plurality of second heat exchange pipes are sequentially communicated. The reactor has high space utilization rate, high catalyst loading rate, long residence time of the synthesis gas, various reaction temperatures and high tubular conversion rate.
Description
Technical Field
The invention relates to chemical equipment, in particular to a radial-axial combined reactor suitable for a strong exothermic reaction.
Background
The chemical reaction is typically accompanied by an endothermic or exothermic reaction. The fischer-tropsch synthesis, etc. in which synthesis gas is converted to hydrocarbons over a catalyst, is a strongly exothermic reaction. The fixed bed tube reactor has the advantages of separation of the catalyst from the product, simple catalyst regeneration flow and the like, and has wider application prospect in exothermic reaction. The shell-and-tube reactor is divided into two types, namely, the catalyst is arranged outside the heat exchange tube and inside the heat exchange tube, the catalyst is arranged inside the heat exchange tube and can be directly loaded and unloaded from the upper end enclosure and the lower end enclosure, so that the shell-and-tube reactor is more convenient, and the catalyst is arranged outside the heat exchange tube and cannot be directly loaded and unloaded from the upper end enclosure and the lower end enclosure, so that the loading and unloading of the catalyst are difficult. The synthesis gas generally flows along the axial direction or the radial direction of the bed, the radial direction flow has better heat exchange efficiency than the axial direction flow, and the residence time is long, but the existing reactor has the problem of space waste. And the exothermic reaction can improve the conversion rate by reducing the reaction temperature along with the progress of the reaction, but the existing reactor is not designed according to the temperature control of different stages of the reaction. For example, CN104368281a discloses a tubular reactor, which comprises a reactor box and a plurality of tubes arranged in the reactor box at intervals, wherein the reactor box comprises a box main body and a horizontal base fixed at the bottom of the box main body, and a reaction raw material inlet and a reaction product outlet which are communicated with the tubes are further arranged on the reactor box, wherein at least one of the tubes is obliquely arranged relative to the horizontal base. The tube array reactor cannot be designed aiming at the temperature control of different stages of the reaction, and is difficult to meet the requirement of strong exothermic reaction.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides the radial-axial composite reactor which has high space utilization rate, high catalyst loading rate, long residence time of synthesis gas, various reaction temperatures and high tube array conversion rate and is suitable for strong exothermic reaction.
The technical scheme adopted for solving the technical problems is as follows: the radial and axial combined reactor suitable for strong exothermic reaction comprises a cylinder, wherein the two ends of the cylinder are respectively connected with an upper end socket and a lower end socket, an upper tube plate is arranged between the upper end socket and the cylinder, a lower tube plate is arranged between the cylinder and the lower end socket, an air inlet and an air outlet are arranged on the cylinder, a reaction zone is arranged in an inner cavity of the cylinder, the reaction zone comprises an annular high-temperature zone, a low-temperature zone and a heat exchange zone, a guide cylinder is arranged on the inner side of the cylinder, a guide cylinder is arranged on the inner side of the guide cylinder, the guide cylinder and the guide cylinder are annular, guide holes are uniformly distributed on the cylinder wall of the guide cylinder, guide holes are respectively formed in the top and the bottom of the cylinder wall of the guide cylinder, the high-temperature zone is positioned in the guide cylinder, the low temperature zone is positioned in the guide cylinder, the guide cylinder is positioned at the outer side of the guide cylinder, a first annular gap is arranged between the outer side of the guide cylinder and the inner side of the cylinder, a second annular gap is arranged between the inner side of the guide cylinder and the outer side of the guide cylinder, the heat exchange zone is positioned in the second annular gap, the inner side of the low temperature zone is provided with an intermediate channel for discharging reaction gas, the high temperature zone is internally provided with a plurality of upright first heat exchange tubes, the low temperature zone is internally provided with a plurality of upright second heat exchange tubes, the heat exchange zone is internally provided with a plurality of upright third heat exchange tubes, the upper ends and the lower ends of the plurality of first heat exchange tubes, the plurality of second heat exchange tubes and the plurality of third heat exchange tubes are respectively arranged on the upper tube plate and the lower tube plate, the shell side of the plurality of first heat exchange tubes and the shell side of the plurality of second heat exchange tubes are filled with catalysts, the tube side inlets of the plurality of first heat exchange tubes are communicated with the water outlet of the circulating hot water supply mechanism, the tube side outlets of the plurality of first heat exchange tubes are communicated with the water inlet of the circulating hot water supply mechanism, the tube side inlets of the plurality of second heat exchange tubes and the plurality of third heat exchange tubes are respectively communicated with the air inlet through a first gas distributor, the tube side outlets of the plurality of second heat exchange tubes and the plurality of third heat exchange tubes are respectively communicated with the shell side inlets of the plurality of first heat exchange tubes through a second gas distributor, the shell side of the plurality of first heat exchange tubes, the shell side of the plurality of third heat exchange tubes and the middle channel are sequentially communicated, and the middle channel is communicated with the air outlet.
When the reactor is used, fresh synthesis gas firstly enters tube passes of the second heat exchange tubes and the third heat exchange tubes through the first gas distributor, flows radially to shell passes of the first heat exchange tubes to react, flows radially to the heat exchange area, then enters a low-temperature area through the guide holes at the top of the guide cylinder, reacts axially through the shell passes of the second heat exchange tubes, and the reaction gas generated after the reaction enters the middle channel from the guide holes at the bottom of the guide cylinder, and is converged in the middle channel to be discharged out of the reactor.
The heat of the gas before entering the low temperature zone is taken away by fresh synthetic gas in a plurality of third heat exchange tubes in the heat exchange zone, the heat of the low temperature zone is taken away by fresh synthetic gas in a plurality of second heat exchange tubes, and therefore, when the reaction gas enters the reaction zone, the reaction gas firstly flows to the high temperature zone in a radial direction to react, then flows to the heat exchange zone in a radial direction to cool, enters the low temperature zone from the top of the guide cylinder, flows axially along the low temperature zone and reacts, the reaction temperature of the high temperature zone is determined by the temperature of the circulating hot water provided by the circulating hot water supply mechanism, the reaction temperature of the hot water is determined by the activity temperature of the catalyst, and the reaction temperature of the low temperature zone is determined by the temperature of the fresh synthetic gas, the activity temperature of the catalyst and the heat exchange effect of the heat exchange zone. In the reactor, the synthesis gas flows radially and then axially in the reaction zone, the reaction temperature can be effectively reduced in the reaction process, and the reactor has the advantages of high space utilization rate, high catalyst loading rate, long residence time of the synthesis gas, diversity of reaction temperature and high tubular conversion rate.
Preferably, the first gas distributor and the second gas distributor are respectively arranged on the lower tube plate and the upper tube plate, the first gas distributor is positioned right below the heat exchange area and the low temperature area, and the second gas distributor is positioned right above the heat exchange area and the low temperature area. And the first gas distributor and the second gas distributor are respectively arranged under and over the low-temperature region, so that the gas distribution efficiency of the synthesis gas is improved, and the conversion rate of subsequent reactions is ensured.
Preferably, the first gas distributor is a spiral disc type gas distributor formed by one or more closed first side pipes, the pipe side inlets of the second heat exchange pipes and the third heat exchange pipes are respectively communicated with the first gas distributor, a plurality of closed first side pipes penetrate through the first gas distributor in the radial direction, the gas inlet is arranged on the lower sealing head, the gas inlet pipe communicated with the gas inlet is arranged on the lower sealing head, and the first side pipes are respectively communicated with the first gas distributor and the gas inlet pipe.
Preferably, the second gas distributor is a spiral disc type gas distributor formed by one or more closed second square tubes, tube side outlets of the second heat exchange tubes and the third heat exchange tubes are respectively communicated with the second gas distributor, a plurality of closed second total square tubes penetrate through the second gas distributor and the high-temperature area in the radial direction, and the second total square tubes are simultaneously communicated with shell side inlets of the second gas distributor and the first heat exchange tubes.
The first gas distributor and the second gas distributor are of spiral disc type structures, and the first gas distributor and the second gas distributor of the spiral disc type structures can be formed by one or more closed square tubes, so that the axial size is small, and the space saving of the reactor is facilitated. The lower ends and the upper ends of the second heat exchange tubes and the third heat exchange tubes are respectively spirally distributed along the first gas distributor and the second gas distributor, so that the synthesis gas can uniformly enter the reactor and the reaction zone.
Preferably, the upper tube plate is provided with an annular charging barrel for charging the catalyst to the low temperature area, the charging barrel is positioned right above the low temperature area, the upper tube plate is provided with a plurality of charging holes which are arranged along a spiral shape, gaps are arranged between radially adjacent second square tubes forming the second gas distributor, therefore, the second gas distributor is provided with a spiral gap, orthographic projections of the charging holes fall on the spiral gap of the second gas distributor, and the side wall of the upper part of the barrel is provided with a plurality of charging holes which are respectively communicated with shell passes of the first heat exchange tubes. The charging barrel is combined with the design of the charging hole on the upper tube plate, so that the catalyst is convenient to charge and feed, and the operability is high. The catalyst is filled into the low-temperature area through the charging barrel, and meanwhile, the catalyst can be filled into the high-temperature area through the charging port, so that the operation is convenient and quick.
Preferably, the lower tube plate is provided with a plurality of discharge holes which are arranged along a spiral shape, the discharge holes are opposite to the low-temperature area, gaps are formed between the radially adjacent first side tubes forming the first gas distributor, so that spiral gaps are formed on the first gas distributor, orthographic projections of the discharge holes fall on the spiral gaps of the first gas distributor, the lower tube plate is provided with a discharge hopper which is opposite to the low-temperature area in position, and the side wall of the lower part of the cylinder is provided with a plurality of discharge openings which are respectively communicated with shell passes of the first heat exchange tubes. The effect of discharge opening and discharge hopper is to the catalyst of filling in the low temperature district to be unloaded, and the effect of discharge opening is to the catalyst of filling in the high temperature district to be unloaded, makes the operation of unloading of low temperature district and high temperature district mutually noninterfere, ensures the efficiency of unloading.
Preferably, the upper tube plate is provided with a separation tube, the outer diameter of the separation tube is the same as that of the guide tube, the separation tube, the charging tube, the upper end socket and the upper tube plate enclose a third annular gap, tube side outlets of the plurality of first heat exchange tubes are communicated with a water inlet of the circulating hot water supply mechanism through the third annular gap, the separation tube is provided with a plurality of first exhaust holes, the upper tube plate is provided with a plurality of second exhaust holes opposite to the first annular gap in position, and the plurality of second total square tubes are communicated with the first annular gap through the plurality of first exhaust holes and the plurality of second exhaust holes.
Preferably, the circulating hot water supply mechanism comprises a steam drum, high-temperature boiler water is filled in the steam drum, a water outlet of the steam drum is communicated with tube side inlets of the first heat exchange tubes, the tube side inlets of the first heat exchange tubes are positioned at the bottoms of the first heat exchange tubes, and tube side outlets of the first heat exchange tubes are communicated with an air inlet of the steam drum. When the boiler is used, high-temperature boiler water enters the second heat exchange tube of the high-temperature zone from the bottom, and after the reaction heat is absorbed, the water turns into steam to return to the steam drum, and natural circulation is realized by density difference.
Compared with the prior art, the invention has the following advantages: when the reaction gas enters the reaction zone, the reaction gas firstly flows to the high-temperature zone in the radial direction, then flows to the heat exchange zone in the radial direction for cooling, then enters the low-temperature zone from the top of the guide cylinder, flows axially along the low-temperature zone for reaction, the reaction temperature of the high-temperature zone is determined by the temperature of circulating hot water provided by the circulating hot water supply mechanism, the temperature of the hot water is determined by the activity temperature of the catalyst, and the reaction temperature of the low-temperature zone is determined by the temperature of fresh synthetic gas, the activity temperature of the catalyst and the heat exchange effect of the heat exchange zone, so that the energy-saving effect is good, and unnecessary energy waste can be avoided. In the reactor, the synthesis gas flows radially and then axially in the reaction zone, the reaction temperature can be effectively reduced in the reaction process, and the reactor has the advantages of high space utilization rate, high catalyst loading rate, long residence time of the synthesis gas, diversity of reaction temperature and high tubular conversion rate.
Drawings
FIG. 1 is a schematic view of the structure of a reactor in the examples;
FIG. 2 is a cross-sectional view A-A of FIG. 1, at 4-fold magnification;
FIG. 3 is an enlarged view of a portion of the middle of FIG. 2;
FIG. 4 is a cross-sectional view taken at 4-fold magnification of B-B in FIG. 1;
FIG. 5 is an enlarged view of a portion of the middle of FIG. 4;
fig. 6 is a schematic longitudinal section corresponding to the dashed box at C in fig. 1.
Detailed Description
The invention is described in further detail below with reference to the embodiments of the drawings.
The radial-axial combined reactor suitable for strong exothermic reaction of embodiment 1 is shown in the figure, which comprises a cylinder 1, wherein the two ends of the cylinder 1 are respectively connected with an upper seal head 21 and a lower seal head 22, an upper tube plate 23 is arranged between the upper seal head 21 and the cylinder 1, a lower tube plate 24 is arranged between the cylinder 1 and the lower seal head 22, an air inlet 251 and an air outlet 253 are arranged on the cylinder 1, a reaction zone is arranged in the inner cavity of the cylinder 1, the reaction zone comprises an annular high-temperature zone 3, a low-temperature zone 4 and a heat exchange zone 8, a guide cylinder 11 is arranged on the inner side of the cylinder 1, a guide cylinder 12 is arranged on the inner side of the guide cylinder 11, the guide cylinder 11 and the guide cylinder 12 are annular, guide holes (not shown in the figure) are uniformly distributed on the cylinder wall of the guide cylinder 11, guide holes (not shown in the figure) are respectively arranged at the top and the bottom of the cylinder wall of the guide cylinder 12, the high-temperature zone 3 is positioned in the guide cylinder 11, the low-temperature zone 4 is positioned in the guide cylinder 12, the guide cylinder 11 is positioned at the outer side of the guide cylinder 12, a first annular gap 14 is arranged between the outer side of the guide cylinder 11 and the inner side of the cylinder body 1, a second annular gap 15 is arranged between the inner side of the guide cylinder 11 and the outer side of the guide cylinder 12, the heat exchange area 8 is positioned in the second annular gap 15, an intermediate channel 42 for discharging reaction gas is arranged at the inner side of the low temperature area 4, a plurality of upright first heat exchange pipes 31 are arranged in the high temperature area 3, a plurality of upright second heat exchange pipes 41 are arranged in the low temperature area 4, a plurality of upright third heat exchange pipes 81 are arranged in the heat exchange area 8, the upper ends and the lower ends of the plurality of first heat exchange pipes 31, the plurality of second heat exchange pipes 41 and the plurality of third heat exchange pipes 81 are respectively arranged on the upper tube plate 23 and the lower tube plate 24, the shell side of the plurality of first heat exchange pipes 31 and the shell side of the plurality of second heat exchange pipes 41 are filled with catalysts, the tube side inlets of the plurality of first heat exchange tubes 31 are communicated with the water outlet of the circulating hot water supply mechanism 7, the tube side outlets of the plurality of first heat exchange tubes 31 are communicated with the water inlet of the circulating hot water supply mechanism 7, the tube side inlets of the plurality of second heat exchange tubes 41 and the plurality of third heat exchange tubes 81 are respectively communicated with the air inlet 251 through the first gas distributor 5, the tube side outlets of the plurality of second heat exchange tubes 41 and the plurality of third heat exchange tubes 81 are respectively communicated with the shell side inlets of the plurality of first heat exchange tubes 31 through the second gas distributor 6, the shell side of the plurality of first heat exchange tubes 31, the shell side of the plurality of third heat exchange tubes 81, the shell side of the plurality of second heat exchange tubes 41 and the middle channel 42 are sequentially communicated, and the middle channel 42 is communicated with the air outlet 253.
In embodiment 1, the circulating hot water supply mechanism 7 includes a steam drum 71, high temperature boiler water is contained in the steam drum 71, the water outlet of the steam drum 71 is communicated with the tube side inlets of the plurality of first heat exchange tubes 31, the tube side inlets of the plurality of first heat exchange tubes 31 are positioned at the bottoms of the plurality of first heat exchange tubes 31, and the tube side outlets of the plurality of first heat exchange tubes 31 are communicated with the air inlet of the steam drum 71.
The radial-axial combined reactor suitable for strong exothermic reaction of embodiment 2 is shown in the figure, which comprises a cylinder 1, wherein the two ends of the cylinder 1 are respectively connected with an upper seal head 21 and a lower seal head 22, an upper tube plate 23 is arranged between the upper seal head 21 and the cylinder 1, a lower tube plate 24 is arranged between the cylinder 1 and the lower seal head 22, an air inlet 251 and an air outlet 253 are arranged on the cylinder 1, a reaction zone is arranged in the inner cavity of the cylinder 1, the reaction zone comprises an annular high-temperature zone 3, a low-temperature zone 4 and a heat exchange zone 8, a guide cylinder 11 is arranged on the inner side of the cylinder 1, a guide cylinder 12 is arranged on the inner side of the guide cylinder 11, the guide cylinder 11 and the guide cylinder 12 are annular, guide holes (not shown in the figure) are uniformly distributed on the cylinder wall of the guide cylinder 11, the guide holes are respectively arranged at the top and the bottom of the cylinder wall of the guide cylinder 12, the high-temperature zone 3 is positioned in the guide cylinder 11, the low-temperature zone 4 is positioned in the guide cylinder 12, the guide cylinder 11 is positioned at the outer side of the guide cylinder 12, a first annular gap 14 is arranged between the outer side of the guide cylinder 11 and the inner side of the cylinder body 1, a second annular gap 15 is arranged between the inner side of the guide cylinder 11 and the outer side of the guide cylinder 12, the heat exchange area 8 is positioned in the second annular gap 15, an intermediate channel 42 for discharging reaction gas is arranged at the inner side of the low temperature area 4, a plurality of upright first heat exchange pipes 31 are arranged in the high temperature area 3, a plurality of upright second heat exchange pipes 41 are arranged in the low temperature area 4, a plurality of upright third heat exchange pipes 81 are arranged in the heat exchange area 8, the upper ends and the lower ends of the plurality of first heat exchange pipes 31, the plurality of second heat exchange pipes 41 and the plurality of third heat exchange pipes 81 are respectively arranged on the upper tube plate 23 and the lower tube plate 24, the shell side of the plurality of first heat exchange pipes 31 and the shell side of the plurality of second heat exchange pipes 41 are filled with catalysts, the tube side inlets of the plurality of first heat exchange tubes 31 are communicated with the water outlet of the circulating hot water supply mechanism 7, the tube side inlets of the plurality of second heat exchange tubes 41 and the plurality of third heat exchange tubes 81 are respectively communicated with the air inlet 251 through the first gas distributor 5, the first gas distributor 5 is positioned right below the heat exchange area 8 and the low temperature area 4, the tube side outlets of the plurality of second heat exchange tubes 41 and the plurality of third heat exchange tubes 81 are respectively communicated with the shell side inlets of the plurality of first heat exchange tubes 31 through the second gas distributor 6, the second gas distributor 6 is positioned right above the heat exchange area 8 and the low temperature area 4, the first gas distributor 5 and the second gas distributor 6 are respectively arranged on the lower tube plate 24 and the upper tube plate 23, the shell side of the plurality of first heat exchange tubes 31, the shell side of the plurality of third heat exchange tubes 81, the shell side of the plurality of second heat exchange tubes 41 and the middle channel 42 are sequentially communicated, and the middle channel 42 is communicated with the air outlet 253.
In embodiment 2, the first gas distributor 5 is a spiral disc type gas distributor formed by a plurality of closed first square tubes 51, tube side inlets of the plurality of second heat exchange tubes 41 and the plurality of third heat exchange tubes 81 are respectively communicated with the first gas distributor 5, four closed first square tubes 52 are radially arranged to penetrate through the first gas distributor 5, the gas inlet 251 is arranged on the lower seal head 22, the gas inlet 252 communicated with the gas inlet 251 is arranged on the lower seal head 22, and the four first square tubes 52 are respectively communicated with the first gas distributor 5 and the gas inlet 252; the second gas distributor 6 is a spiral disc type gas distributor formed by a plurality of closed second square tubes 61, tube side outlets of the second heat exchange tubes 41 and the third heat exchange tubes 81 are respectively communicated with the second gas distributor 6, four closed second total square tubes 62 are radially arranged penetrating through the second gas distributor 6 and the high-temperature zone 3, and the four second total square tubes 62 are simultaneously communicated with shell side inlets of the second gas distributor 6 and the first heat exchange tubes 31.
The radial-axial combined reactor for strong exothermic reaction of embodiment 3 is different from embodiment 2 in that, in embodiment 3, as shown in the drawing, an annular charging cylinder 26 for charging the catalyst to the low temperature zone 4 is installed on the upper tube plate 23, the charging cylinder 26 is located right above the low temperature zone 4, a plurality of charging holes 27 arranged along a spiral are provided on the upper tube plate 23, a gap is provided between radially adjacent second square tubes 61 constituting the second gas distributor 6, thus a spiral gap 63 is formed on the second gas distributor 6, the orthographic projection of the plurality of charging holes 27 falls on the spiral gap 63 of the second gas distributor 6, a plurality of charging holes 16 are symmetrically installed on the upper side wall of the cylinder 1, and the plurality of charging holes 16 are respectively communicated with the shell passes of the plurality of first heat exchange tubes 31.
The difference between the radial-axial combined reactor for strong exothermic reaction of embodiment 4 and embodiment 3 is that in embodiment 4, as shown in the drawing, a plurality of discharge holes 28 are arranged on the lower tube plate 24 and are opposite to the low temperature zone 4, and gaps are formed between the radially adjacent first side tubes 51 forming the first gas distributor 5, so that a spiral gap 53 is formed on the first gas distributor 5, the orthographic projection of the plurality of discharge holes 28 falls on the spiral gap 53 of the first gas distributor 5, a discharge hopper 20 opposite to the low temperature zone 4 is installed on the lower tube plate 24, a plurality of discharge openings 17 are symmetrically installed on the lower side wall of the cylinder 1, and the plurality of discharge openings 17 are respectively communicated with shell passes of the plurality of first heat exchange tubes 31.
The difference between the radial-axial combined reactor suitable for strong exothermic reaction of embodiment 5 and embodiment 4 is that in embodiment 5, as shown in the drawing, a baffle cylinder 13 is installed on the cylinder upper tube plate 23, the outer diameter of the baffle cylinder 13 is the same as that of the guide cylinder 11, a third annular gap 18 is enclosed by the baffle cylinder 13, the charging cylinder 26, the upper end enclosure 21 and the upper tube plate 23, tube side outlets of a plurality of first heat exchange tubes 31 are communicated with water inlets of the circulating hot water supply mechanism 7 through the third annular gap 18, a plurality of first exhaust holes (not shown in the drawing) are formed on the baffle cylinder 13, a plurality of second exhaust holes 29 opposite to the first annular gap 14 are formed on the upper tube plate 23, and four second total square tubes 62 are communicated with the first annular gap 14 through the plurality of first exhaust holes and the plurality of second exhaust holes 29.
When the radial-axial combined reactor suitable for strong exothermic reaction is used, fresh synthesis gas firstly enters the tube passes of the second heat exchange tubes 41 and the third heat exchange tubes 81 through the air inlet 251 and the first gas distributor 5, flows radially to the shell passes of the first heat exchange tubes 31 to react, flows radially to the heat exchange area 8, then enters the low-temperature area 4 through the guide holes at the top of the guide cylinder 12, reacts axially through the shell passes of the second heat exchange tubes 41, and the reaction gas generated after the reaction enters the middle channel 42 from the guide holes at the bottom of the guide cylinder 12, and then exits the reactor from the air outlet 253 after the middle channel 42 is converged. The heat of the high temperature area 3 is taken away by the circulating hot water supply mechanism 7 in the process, the heat of the gas before entering the low temperature area 4 is taken away by the fresh synthetic gas in the plurality of third heat exchange tubes 81 in the heat exchange area 8, the heat of the low temperature area 4 is taken away by the fresh synthetic gas in the plurality of second heat exchange tubes 41, the reaction gas firstly flows to the high temperature area 3 radially to react and then flows to the heat exchange area 8 radially to cool, then enters the low temperature area 4 from the top of the guide cylinder 12, flows axially along the low temperature area 4 and reacts, the reaction temperature of the high temperature area 3 is determined by the temperature of the circulating hot water provided by the circulating hot water supply mechanism 7, the reaction temperature of the hot water is determined by the activity temperature of the catalyst, the reaction temperature of the low temperature area 4 is determined by the temperature of the fresh synthetic gas led from the air inlet 251, the activity temperature of the catalyst and the heat exchange effect of the heat exchange area 8, the energy saving effect is good, and unnecessary energy waste can be avoided.
Taking the radial-axial combined reactor suitable for strong exothermic reaction of example 6 as an example, the working procedure is: in use, fresh synthesis gas is fed into the first gas distributor 5 via inlet 251; after entering the first gas distributor 5, fresh synthesis gas enters the tube passes of the plurality of second heat exchange tubes 41 in the low temperature region 4 and the tube passes of the plurality of third heat exchange tubes 81 in the heat exchange region 8 through the four first total square tubes 52, flows into the four second total square tubes 62 from the tube pass outlets of the second heat exchange tubes 41, enters the second annular gap 15 through the four second total square tubes 62, then enters the first annular gap 14, radially flows into the shell passes of the plurality of first heat exchange tubes 31 in the high temperature region 3 through the guide cylinder 11, reacts in the shell passes of the plurality of first heat exchange tubes 31, high-temperature boiler water enters the second heat exchange tubes 41 in the high temperature region 3 from the bottom in the reaction process, absorbs reaction heat and then becomes steam to return to the steam drum 71, natural circulation is realized by density difference, cooled synthesis gas flows out of the guide cylinder 11 radially into the heat exchange region 8, flows into the low-temperature synthesis gas flowing through the tube passes through the guide cylinder 12 from the top of the guide cylinder 12, flows into the guide cylinder 42 from the low temperature region 42 through the guide hole 4, and then flows out of the guide cylinder 42 from the middle channel 42 in the reaction channel 42.
Claims (5)
1. The utility model provides a radial axial combined type reactor suitable for strong exothermic reaction, includes the barrel, the both ends of barrel be connected with upper cover and low head respectively, the upper cover with the barrel between install the upper tube sheet, the barrel with the low head between install the low tube sheet, the barrel on be provided with air inlet and gas outlet, the inner chamber of barrel in be provided with reaction zone, its characterized in that: the reaction zone comprises an annular high-temperature zone, a low-temperature zone and a heat exchange zone, a guide cylinder is arranged on the inner side of the cylinder body, a guide cylinder is arranged on the inner side of the guide cylinder, the guide cylinder and the guide cylinder are annular, guide holes are uniformly distributed on the cylinder wall of the guide cylinder, guide holes are respectively formed in the top and the bottom of the cylinder wall of the guide cylinder, the high-temperature zone is positioned in the guide cylinder, the low-temperature zone is positioned in the guide cylinder, the guide cylinder is positioned on the outer side of the guide cylinder, a first annular gap is formed between the outer side of the guide cylinder and the inner side of the cylinder body, a second annular gap is formed between the inner side of the guide cylinder and the outer side of the guide cylinder, the heat exchange zone is positioned in the second annular gap, an intermediate channel for discharging reaction gas is arranged on the inner side of the low-temperature zone, the high temperature area is internally provided with a plurality of upright first heat exchange tubes, the low temperature area is internally provided with a plurality of upright second heat exchange tubes, the heat exchange area is internally provided with a plurality of upright third heat exchange tubes, the upper ends and the lower ends of the plurality of first heat exchange tubes, the plurality of second heat exchange tubes and the plurality of third heat exchange tubes are respectively arranged on the upper tube plate and the lower tube plate, the shell side of the plurality of first heat exchange tubes and the shell side of the plurality of second heat exchange tubes are filled with catalysts, the tube side inlets of the plurality of first heat exchange tubes are communicated with the water outlet of the circulating hot water supply mechanism, the tube side outlets of the plurality of first heat exchange tubes are communicated with the water inlet of the circulating hot water supply mechanism through a first gas distributor respectively, the tube side outlets of the second heat exchange tubes and the third heat exchange tubes are respectively communicated with the shell side inlets of the first heat exchange tubes through a second gas distributor, the shell sides of the first heat exchange tubes, the third heat exchange tubes, the second heat exchange tubes and the middle channels are sequentially communicated, and the middle channels are communicated with the gas outlet; the first gas distributor and the second gas distributor are respectively arranged on the lower tube plate and the upper tube plate, the first gas distributor is positioned right below the heat exchange area and the low temperature area, and the second gas distributor is positioned right above the heat exchange area and the low temperature area; the first gas distributor is a spiral disc type gas distributor formed by one or more closed first square pipes, tube pass inlets of the second heat exchange pipes and the third heat exchange pipes are respectively communicated with the first gas distributor, a plurality of closed first square pipes are radially arranged penetrating through the first gas distributor, the gas inlet is arranged on the lower sealing head, an air inlet pipe communicated with the gas inlet is arranged on the lower sealing head, and the first square pipes are respectively communicated with the first gas distributor and the air inlet pipe; the second gas distributor is a spiral disc type gas distributor formed by one or more closed second square tubes, tube pass outlets of the second heat exchange tubes and the third heat exchange tubes are respectively communicated with the second gas distributor, a plurality of closed second total square tubes penetrate through the second gas distributor and the high-temperature area in the radial direction, and the second total square tubes are simultaneously communicated with shell pass inlets of the second gas distributor and the first heat exchange tubes.
2. A radial-axial composite reactor suitable for use in a strongly exothermic reaction according to claim 1, wherein: the upper tube plate is provided with an annular charging barrel for filling the catalyst into the low-temperature area, the charging barrel is positioned right above the low-temperature area, the upper tube plate is provided with a plurality of charging holes which are arranged along a spiral shape, gaps are arranged between radially adjacent second square tubes forming the second gas distributor, thereby the second gas distributor is provided with a spiral gap, orthographic projections of the charging holes fall on the spiral gap of the second gas distributor, the side wall of the upper part of the barrel is provided with a plurality of charging holes, and the charging holes are respectively communicated with shell passes of the plurality of first heat exchange tubes.
3. A radial-axial composite reactor suitable for use in a strongly exothermic reaction according to claim 2, wherein: the lower tube plate is provided with a plurality of discharge holes which are arranged along a spiral shape, the discharge holes are opposite to the low-temperature area, gaps are formed between the radially adjacent first side tubes forming the first gas distributor, so that the spiral gaps are formed on the first gas distributor, orthographic projections of the discharge holes fall on the spiral gaps of the first gas distributor, the lower tube plate is provided with discharge hoppers which are opposite to the low-temperature area in position, the side wall of the lower part of the cylinder is provided with a plurality of discharge openings, and the discharge openings are respectively communicated with shell passes of the first heat exchange tubes.
4. A radial-axial composite reactor suitable for use in a strongly exothermic reaction according to claim 2, wherein: the upper tube plate is provided with a separation tube, the outer diameter of the separation tube is the same as that of the guide tube, the separation tube, the charging tube, the upper sealing head and the upper tube plate enclose a third annular gap, tube side outlets of the plurality of first heat exchange tubes are communicated with a water inlet of the circulating hot water supply mechanism through the third annular gap, the separation tube is provided with a plurality of first exhaust holes, the upper tube plate is provided with a plurality of second exhaust holes opposite to the first annular gap in position, and the plurality of second total square tubes are communicated with the first annular gap through the plurality of first exhaust holes and the plurality of second exhaust holes.
5. A radial-axial composite reactor suitable for use in a strongly exothermic reaction according to claim 1, wherein: the circulating hot water supply mechanism comprises a steam drum, high-temperature boiler water is filled in the steam drum, a water outlet of the steam drum is communicated with tube side inlets of the first heat exchange tubes, the tube side inlets of the first heat exchange tubes are positioned at the bottoms of the first heat exchange tubes, and tube side outlets of the first heat exchange tubes are communicated with an air inlet of the steam drum.
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