CN108421506B - Energy-saving radial reactor suitable for strong exothermic reaction - Google Patents
Energy-saving radial reactor suitable for strong exothermic reaction Download PDFInfo
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- CN108421506B CN108421506B CN201810494702.8A CN201810494702A CN108421506B CN 108421506 B CN108421506 B CN 108421506B CN 201810494702 A CN201810494702 A CN 201810494702A CN 108421506 B CN108421506 B CN 108421506B
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 84
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 38
- 239000003054 catalyst Substances 0.000 claims abstract description 31
- 239000007789 gas Substances 0.000 claims description 124
- 239000012495 reaction gas Substances 0.000 claims description 12
- 238000007599 discharging Methods 0.000 claims description 4
- 238000007789 sealing Methods 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 3
- 230000000149 penetrating effect Effects 0.000 claims description 2
- 230000015572 biosynthetic process Effects 0.000 abstract description 24
- 238000003786 synthesis reaction Methods 0.000 abstract description 24
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 abstract description 6
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 abstract description 4
- 230000000694 effects Effects 0.000 description 11
- 239000002699 waste material Substances 0.000 description 3
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000000034 method Methods 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
- B01J8/06—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 in tube reactors; the solid particles being arranged in tubes
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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
- B01J8/06—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 in tube reactors; the solid particles being arranged in tubes
- B01J8/067—Heating or cooling 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
- 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
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00194—Tubes
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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
- B01J2208/00548—Flow
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention discloses an energy-saving radial reactor, which comprises a reaction zone and a low temperature zone, wherein a heat exchange zone is arranged between the high temperature zone and the low temperature zone, 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 zone, the low temperature zone and the heat exchange zone, catalysts are filled in shell passes of the plurality of first heat exchange pipes and shell passes of the plurality of second heat exchange pipes, tube pass inlets of the plurality of first heat exchange pipes are communicated with a water outlet of a circulating hot water supply mechanism, tube pass inlets of the plurality of second heat exchange pipes and tube pass inlets of the plurality of third heat exchange pipes are respectively communicated with an air inlet through a first gas distributor, and tube pass outlets of the plurality of second heat exchange pipes and the plurality of third heat exchange pipes are respectively communicated with shell pass inlets of the plurality of first heat exchange pipes through a second gas distributor. The reactor has high space utilization rate, high catalyst loading rate, long residence time of synthesis gas, various reaction temperatures and high tubular conversion rate, and is suitable for Fischer-Tropsch synthesis, conversion, strong exothermic reactions of methanol, ethanol and the like.
Description
Technical Field
The invention relates to chemical equipment, in particular to an energy-saving radial 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
The invention aims to solve the technical problems of the prior art and provides an energy-saving radial reactor which is suitable for strong exothermic reaction and has the advantages of high space utilization rate, high catalyst loading rate, long residence time of the synthesis gas, various reaction temperatures and high tubular conversion rate, wherein the synthesis gas flows in the reaction zone in an radial manner.
The technical scheme adopted for solving the technical problems is as follows: an energy-saving radial reactor suitable for strong exothermic reaction comprises a cylinder body, wherein two ends of the cylinder body 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 body, a lower tube plate is arranged between the cylinder body and the lower end socket, an air inlet and an air outlet are arranged on the cylinder body, a reaction zone is arranged in an inner cavity of the cylinder body, the reaction zone comprises an annular high-temperature zone and a low-temperature zone, a heat exchange zone is arranged between the high-temperature zone and the low-temperature zone, the high-temperature zone is positioned at the outer side of the heat exchange zone, an intermediate channel for discharging reaction gas is arranged at the inner side of the low-temperature zone, a plurality of upright first heat exchange tubes are arranged in the high-temperature zone, a plurality of upright second heat exchange tubes are arranged in the low-temperature zone, a plurality of upright third heat exchange tubes are arranged in the heat exchange zone, the upper ends and the lower ends of the first heat exchange tubes, the second heat exchange tubes and the third heat exchange tubes are respectively arranged on the upper tube plate and the lower tube plate, the shell passes of the first heat exchange tubes and the shell passes of the second heat exchange tubes are filled with catalysts, the tube pass inlets of the first heat exchange tubes are communicated with the water outlet of the circulating hot water supply mechanism, the tube pass outlets of the first heat exchange tubes are communicated with the water inlet of the circulating hot water supply mechanism, the tube pass inlets of the second heat exchange tubes and the third heat exchange tubes are respectively communicated with the air inlet through a first gas distributor, the tube pass outlets of the second heat exchange tubes and the third heat exchange tubes are respectively communicated with the shell pass inlets of the first heat exchange tubes through a second gas distributor, the shell passes of the first heat exchange tubes, the shell passes of the third heat exchange tubes, the shell passes of the second heat exchange tubes and the middle channels are sequentially communicated, and the middle channels are communicated with the air outlets.
When the reactor is used, fresh synthetic gas firstly enters the tube passes of the second heat exchange tubes and the third heat exchange tubes through the air inlet and the first gas distributor, flows radially to the shell passes of the first heat exchange tubes to react, flows radially, exchanges heat with low-temperature fresh synthetic gas flowing in the tube passes of the third heat exchange tubes through the heat exchange areas, flows radially to the shell passes of the second heat exchange tubes to react, and the reaction gas generated after the reaction is converged in the middle channel and then exits the reactor from the air outlet. 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 pipes 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 pipes, and therefore, when the reaction gas enters the reaction zone, the reaction gas firstly flows to the high temperature zone radially to react, then flows to the heat exchange zone radially to cool, then flows to the low temperature zone radially to react, 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 temperature of the hot water is determined by the activity temperature of a catalyst, and the reaction temperature of the low temperature zone is determined by the temperature of the fresh synthetic gas introduced from the gas inlet, the activity temperature of the catalyst and the heat exchange effect of the heat exchange zone. In the reactor, the synthesis gas flows radially 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, reaction temperature diversity 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 respectively 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 inner side of the cylinder is provided with a first guide cylinder and a second guide cylinder, the first guide cylinder and the second guide cylinder are annular, guide holes are uniformly formed in the cylinder walls of the first guide cylinder and the second guide cylinder respectively, the middle channel is located in the middle of the second guide cylinder, a first annular gap is formed between the outer side of the first guide cylinder and the inner side of the cylinder, the high-temperature area is located in the first guide cylinder, the low-temperature area is located in the second guide cylinder, the heat exchange area is located between the inner side of the first guide cylinder and the outer side of the second guide cylinder, the upper tube plate is provided with a baffle cylinder with the same outer diameter as the first guide cylinder, the baffle cylinder, the charging cylinder, the upper end enclosure and the upper tube plate form a second annular gap, the plurality of first heat exchange tube outlets are communicated with the plurality of air exhaust holes through the second annular gaps of the second heat exchange tube, the plurality of air exhaust holes are formed in the plurality of annular gaps of the first tube plates and the second tube plate, and the plurality of air exhaust holes are communicated with the plurality of air exhaust holes through the second annular gaps of the first tube.
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 a radial direction, then flows to the heat exchange zone in a radial direction for cooling, then flows to the low-temperature zone in a radial direction 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 active temperature of the catalyst, and the reaction temperature of the low-temperature zone is determined by the temperature of fresh synthesis gas introduced from the air inlet, the active 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 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, multiple reaction temperatures and high tubular conversion rate, and is suitable for strong exothermic reactions such as Fischer-Tropsch synthesis, conversion, methanol, ethanol and the like.
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 energy-saving radial 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 and a low-temperature zone 4, a heat exchange zone 8 is arranged between the high-temperature zone 3 and the low-temperature zone 4, the high-temperature zone 3 is positioned at the outer side of the heat exchange zone 8, an intermediate channel 42 for discharging reaction gas is arranged at the inner side of the low-temperature zone 4, a plurality of first heat exchange tubes 31 are arranged vertically in the high-temperature zone 3, a plurality of second heat exchange tubes 41 are arranged vertically in the low-temperature zone 4, a plurality of third heat exchange tubes 81 are arranged vertically in the heat exchange zone 8, the upper ends and the lower ends of the plurality of first heat exchange tubes 31, the plurality of second heat exchange tubes 41 and the plurality of third heat exchange tubes 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 tubes 31 and the shell side of the plurality of second heat exchange tubes 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 third heat exchange tubes 81, the shell side of the plurality of second heat exchange tubes 41 is sequentially communicated with the intermediate passage 42, and the intermediate passage 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 251 of the steam drum 71.
The energy-saving radial 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 and a low-temperature zone 4, a heat exchange zone 8 is arranged between the high-temperature zone 3 and the low-temperature zone 4, the high-temperature zone 3 is positioned at the outer side of the heat exchange zone 8, an intermediate channel 42 for discharging reaction gas is arranged at the inner side of the low-temperature zone 4, a plurality of first heat exchange tubes 31 are arranged vertically in the high-temperature zone 3, a plurality of second heat exchange tubes 41 are arranged vertically in the low-temperature zone 4, a plurality of third heat exchange tubes 81 are arranged vertically in the heat exchange zone 8, the upper ends and the lower ends of the plurality of first heat exchange tubes 31, the plurality of second heat exchange tubes 41 and the plurality of third heat exchange tubes 81 are respectively arranged on the upper tube plate 23 and the lower tube plate 24, 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 first gas distributor 5 is positioned right below the heat exchange region and the low temperature region, the second gas distributor 6 is positioned right above the heat exchange region and the low temperature region, the shell side of the plurality of first heat exchange tubes 31 and the shell side of the plurality of second heat exchange tubes 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 through the first gas distributor 251 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 sides of the plurality of first heat exchange tubes 31, the shell sides of the plurality of third heat exchange tubes 81, the shell sides of the plurality of second heat exchange tubes 41 and the intermediate channel 42 are sequentially communicated, and the intermediate channel 42 is communicated with the gas 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 respectively communicated with shell side inlets of the second gas distributor 6 and the first heat exchange tubes 31.
The energy-saving radial 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, 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 15 are symmetrically installed on the upper side wall of the cylinder 1, and the plurality of charging holes 15 are respectively communicated with the shell side of the plurality of first heat exchange tubes 31.
The energy-saving radial reactor for strong exothermic reaction of embodiment 4 is different from embodiment 3 in that in embodiment 4, as shown in the drawing, a plurality of discharge holes 28 are arranged on the lower tube plate 24 along a spiral shape, the plurality of discharge holes 28 are opposite to the low temperature region 4, a gap is formed between radially adjacent first side tubes 51 forming the first gas distributor 5, thus 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 region 4 is installed on the lower tube plate 24, a plurality of discharge openings 16 are symmetrically installed on the lower side wall of the cylinder 1, and the plurality of discharge openings 16 are respectively communicated with shell passes of a plurality of first heat exchange tubes 31.
The energy-saving radial reactor suitable for strong heat release reaction of embodiment 5 is different from embodiment 4 in that, in embodiment 5, as shown in the drawing, the inner side of the cylinder 1 is provided with a first guide cylinder 10 and a second guide cylinder 11, the first guide cylinder 10 and the second guide cylinder 11 are both annular, the cylinder walls of the first guide cylinder 10 and the second guide cylinder 11 are respectively and uniformly provided with a flow guide hole (not shown in the drawing), the middle channel 42 is positioned in the middle of the second guide cylinder 11, a first annular gap 12 is arranged between the outer side of the first guide cylinder 10 and the inner side of the cylinder 1, the high temperature zone 3 is positioned in the first guide cylinder 10, the low temperature zone 4 is positioned in the second guide cylinder 11, the heat exchange zone 8 is positioned between the inner side of the first guide cylinder 10 and the outer side of the second guide cylinder 11, the upper tube plate 23 is provided with a baffle cylinder 13 with the same outer diameter as the first guide cylinder 10, the baffle cylinder 13, the charging cylinder 26, the upper end enclosure 21 and the upper tube plate 23 are respectively and uniformly provided with a second annular gap 14, the tube outlets of the plurality of first heat exchange tubes 31 are respectively provided with a plurality of annular gaps 14 through the second annular gaps 14 and a plurality of air exhaust holes 29 which are respectively and are arranged in the opposite positions of the second annular gaps 29 and the second tube plates and the second annular gap 14 are respectively provided with a plurality of air exhaust holes 29.
When the energy-saving radial reactor suitable for strong exothermic reaction is used, fresh synthesis gas firstly enters the tube passes of the plurality of second heat exchange tubes 41 and the plurality of third heat exchange tubes 81 through the air inlet 251 and the first gas distributor 5 at the same time, flows radially to the shell passes of the plurality of first heat exchange tubes 31 for reaction, flows radially again, exchanges heat with low-temperature fresh synthesis gas flowing through the tube passes of the plurality of third heat exchange tubes 81 through the heat exchange region 8, flows radially to the shell passes of the plurality of second heat exchange tubes 41 for reaction, and the reaction gas generated after the reaction is converged in the middle channel 42 and then exits the reactor from the air outlet 253. In the reaction process, the heat of the high-temperature area 3 is taken away by the circulating hot water supply mechanism 7, the heat of the gas before entering the low-temperature area 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, and as the reaction gas enters the reaction area, the reaction gas firstly flows to the high-temperature area 3 to react, then flows to the heat exchange area 8 to cool, flows to the low-temperature area 4 to react, 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, and 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, so that the energy saving effect is good and unnecessary energy waste can be avoided. In the reactor, the synthesis gas flows radially 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.
Taking the energy-saving radial reactor suitable for strong exothermic reaction of example 6 as an example, the working process is as follows: in use, fresh synthesis gas is fed into the first gas distributor 5 via inlet 251; after fresh synthesis gas enters the first gas distributor 5, the 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 14 through the four second total square tubes 62, then enters the first annular gap 12, then radially flows into the shell passes of the plurality of first heat exchange tubes 31 in the high temperature region 3 through the first guide cylinder 10, 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 the reaction heat and then becomes steam to return to the steam drum 71, naturally circulates through the density difference, the cooled synthesis gas radially flows into the heat exchange region 8 from the high temperature region 3, radially flows into the low temperature fresh synthesis gas flowing through the tube passes in the tube passes of the plurality of third heat exchange tubes 81, radially flows into the shell passes through the second guide cylinder 11, then flows into the shell passes through the second guide cylinder 11 to the middle channel 42 from the inner side of the second guide cylinder 42, finally flows out of the middle channel 11 from the second guide cylinder 11, and finally flows into the shell pass 11 from the middle channel 42.
Claims (5)
1. The utility model provides an energy-saving radial 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 a ring-shaped high-temperature zone and a low-temperature zone, a heat exchange zone is arranged between the high-temperature zone and the low-temperature zone, the high-temperature zone is positioned at the outer side of the heat exchange zone, the inner side of the low-temperature zone is provided with a middle channel for discharging reaction gas, a plurality of vertical first heat exchange tubes are arranged in the high-temperature zone, a plurality of vertical second heat exchange tubes are arranged in the low-temperature zone, a plurality of vertical third heat exchange tubes are arranged in the heat exchange zone, 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 pass of the plurality of first heat exchange tubes and the shell pass 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, and the shell side of the plurality of first heat exchange tubes, the shell side of the plurality of third heat exchange tubes, the shell side of the plurality of second heat exchange tubes and the middle channel are sequentially communicated with the air 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 respectively communicated with shell pass inlets of the second gas distributor and the first heat exchange tubes.
2. An energy efficient radial 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. An energy efficient radial reactor suitable for use in a strongly exothermic reaction according to claim 2, characterized in that: 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. An energy efficient radial reactor suitable for use in a strongly exothermic reaction according to claim 2, characterized in that: the inner side of the cylinder is provided with a first guide cylinder and a second guide cylinder, the first guide cylinder and the second guide cylinder are annular, guide holes are respectively and uniformly formed in the cylinder walls of the first guide cylinder and the second guide cylinder, the middle channel is positioned in the middle of the second guide cylinder, a first annular gap is formed between the outer side of the first guide cylinder and the inner side of the cylinder, the high-temperature area is positioned in the first guide cylinder, the low-temperature area is positioned in the second guide cylinder, the heat exchange area is positioned between the inner side of the first guide cylinder and the outer side of the second guide cylinder, the upper tube plate is provided with a separation cylinder, the outer diameters of the separation cylinder and the first guide cylinder are the same, the middle channel is positioned in the middle of the second guide cylinder, the upper end socket and the upper tube plate, the plurality of first heat exchange tube outlets are positioned in the first annular gap, the plurality of first heat exchange tube outlets are communicated with the plurality of second air exhaust holes of the first heat exchange tube and the plurality of air exhaust holes of the second heat exchange tube are arranged in the second annular gap, and the plurality of air exhaust holes are communicated with the plurality of air exhaust holes of the first heat exchange tube and the second heat exchange tube are arranged in the air exchange tube.
5. An energy efficient radial 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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| CN110790226A (en) * | 2019-10-24 | 2020-02-14 | 中石化宁波工程有限公司 | Double-system conversion furnace |
| CN110902650A (en) * | 2019-10-24 | 2020-03-24 | 中石化宁波工程有限公司 | Double-steam-drum double-isothermal conversion furnace |
| CN111115574B (en) * | 2019-10-24 | 2023-05-05 | 中石化宁波工程有限公司 | CO conversion process for CO-producing synthetic gas and hydrogen and isothermal conversion furnace |
| CN110790227B (en) * | 2019-10-24 | 2023-03-24 | 中石化宁波工程有限公司 | Isothermal transformation hydrogen production method and isothermal transformation furnace matched with coal water slurry gasification device |
| CN110790225A (en) * | 2019-10-24 | 2020-02-14 | 中石化宁波工程有限公司 | Isothermal converter with double cooling systems |
| CN110790223B (en) * | 2019-10-24 | 2023-03-14 | 中石化宁波工程有限公司 | Transformation hydrogen production method matched with coal water slurry gasification device and isothermal transformation furnace |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1308561A (en) * | 1998-07-09 | 2001-08-15 | 华盛顿集团国际公司 | Radial flow reactor |
| CN101301597A (en) * | 2007-05-11 | 2008-11-12 | 曼德韦有限公司 | Cooling pipe reactor |
| CN101703910A (en) * | 2009-08-20 | 2010-05-12 | 上海国际化建工程咨询公司 | Built-in cold wall type shift reactor for heat exchanger and direction connection structure for shift reactor and downstream heat exchanging equipment |
| CN105457563A (en) * | 2014-09-09 | 2016-04-06 | 航天长征化学工程股份有限公司 | Isothermal shift reactor with built-in tube bundle |
| CN208711670U (en) * | 2018-05-22 | 2019-04-09 | 中石化宁波工程有限公司 | A kind of energy-saving radial reactor suitable for strong exothermal reaction |
-
2018
- 2018-05-22 CN CN201810494702.8A patent/CN108421506B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1308561A (en) * | 1998-07-09 | 2001-08-15 | 华盛顿集团国际公司 | Radial flow reactor |
| US6620386B1 (en) * | 1998-07-09 | 2003-09-16 | Stone & Webster, Inc. | Radial flow reactor |
| CN101301597A (en) * | 2007-05-11 | 2008-11-12 | 曼德韦有限公司 | Cooling pipe reactor |
| CN101703910A (en) * | 2009-08-20 | 2010-05-12 | 上海国际化建工程咨询公司 | Built-in cold wall type shift reactor for heat exchanger and direction connection structure for shift reactor and downstream heat exchanging equipment |
| CN105457563A (en) * | 2014-09-09 | 2016-04-06 | 航天长征化学工程股份有限公司 | Isothermal shift reactor with built-in tube bundle |
| CN208711670U (en) * | 2018-05-22 | 2019-04-09 | 中石化宁波工程有限公司 | A kind of energy-saving radial reactor suitable for strong exothermal reaction |
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