CN108421506A - A kind of energy-saving radial reactor suitable for strong exothermal reaction - Google Patents
A kind of energy-saving radial reactor suitable for strong exothermal reaction Download PDFInfo
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- CN108421506A CN108421506A CN201810494702.8A CN201810494702A CN108421506A CN 108421506 A CN108421506 A CN 108421506A CN 201810494702 A CN201810494702 A CN 201810494702A CN 108421506 A CN108421506 A CN 108421506A
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 82
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 47
- 239000003054 catalyst Substances 0.000 claims abstract description 29
- 230000008520 organization Effects 0.000 claims abstract description 17
- 239000007789 gas Substances 0.000 claims description 125
- 239000012495 reaction gas Substances 0.000 claims description 8
- 230000015572 biosynthetic process Effects 0.000 abstract description 34
- 238000003786 synthesis reaction Methods 0.000 abstract description 34
- 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
- 235000019441 ethanol Nutrition 0.000 abstract description 2
- 230000009466 transformation Effects 0.000 abstract 1
- 230000000694 effects Effects 0.000 description 10
- 238000007599 discharging Methods 0.000 description 6
- 239000004744 fabric Substances 0.000 description 5
- 230000021715 photosynthesis, light harvesting Effects 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 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
- 239000002699 waste material Substances 0.000 description 1
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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
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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
- B01J2208/00168—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
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
Energy-saving radial reactor disclosed by the invention, its reaction zone includes high-temperature region and low-temperature space, heat transfer zone is provided between high-temperature region and low-temperature space, high-temperature region, more first heat exchanger tubes are respectively arranged in low-temperature space and heat transfer zone, more second heat exchanger tubes and Duo Gen third heat exchanger tubes, catalyst is filled in the shell side of the second heat exchanger tube of shell side and Duo Gen of more first heat exchanger tubes, the tube-side inlet of more first heat exchanger tubes is communicated with the water outlet of circulating hot water organization of supply, the tube-side inlet of more second heat exchanger tubes and Duo Gen third heat exchanger tubes is communicated through first gas distributor with air inlet respectively, the outlet of the tube side of more second heat exchanger tubes and Duo Gen third heat exchanger tubes is communicated through second gas distributor with the shell side inlet of more first heat exchanger tubes respectively.Space reactor utilization rate height, catalyst charging ratio height, synthesis gas residence time length, reaction temperature diversity, the tubulation high conversion rate are suitable for the strong exothermal reactions such as F- T synthesis, transformation, methanol, ethyl alcohol.
Description
Technical field
The present invention relates to a kind of chemical industry equipments, and in particular to a kind of energy-saving radial reaction suitable for strong exothermal reaction
Device.
Background technology
Chemical reaction is generally accompanied with heat absorption or exothermic reaction.Wherein convert synthesis gas to hydrocarbon by catalyst action
Fischer-Tropsch synthesis or F-T etc. be strong exothermal reaction.Fixed-bed column reactor have catalyst detached with product, catalyst regeneration flow
The advantages that simple, has more wide application prospect in exothermic reaction.Shell-and-tube reactor divided catalyst fill heat exchanger tube it is outer and
Two kinds in heat exchanger tube, catalyst fill in heat exchanger tube can be more convenient from the direct loading and unloading of upper low head, and for catalyst
Shell-and-tube reactor outside heat exchanger tube, generally cannot be from the direct loading and unloading of upper low head, and loading and unloading is relatively difficult.Synthesis gas
Generally along the flowing of bed axial direction or Radial Flow, the more axial fluid interchange excellent in efficiency of Radial Flow, the residence time is long, but existing
With the presence of reactor space waste problem.And exothermic reaction, with the progress of reaction, conversion ratio can be improved by reducing reaction temperature, but
It is that existing reactor is not designed according to the temperature control of reaction different phase.For example, CN104368281A discloses a kind of tubulation
Formula reactor, including reactor babinet and multiple tubulations for being arranged at intervals in the reactor babinet, reactor babinet packet
Include babinet main body and the horizontal base for being fixed on the babinet bottom part body, be additionally provided on the reactor babinet with it is the multiple
The reaction raw materials import of tubulation connection and reacting product outlet, wherein at least one tubulation is relative to the horizontal base
It is obliquely installed.The shell and tube reactor can not be directed to the temperature control design of reaction different phase, it is difficult to meet the need of strong exothermal reaction
It wants.
Invention content
The technical problem to be solved by the present invention is in view of the deficiencies of the prior art, provide a kind of synthesis gas in reaction zone
Interior Radial Flow and space availability ratio height, catalyst charging ratio height, synthesis gas residence time length, reaction temperature diversity, tubulation
The energy-saving radial reactor suitable for strong exothermal reaction of high conversion rate.
Technical solution is used by the present invention solves above-mentioned technical problem：It is a kind of to be suitable for the energy-saving of strong exothermal reaction
The both ends of radial reactor, including cylinder, the cylinder are connected separately with upper cover and low head, the upper cover and institute
Upper perforated plate is installed between the cylinder stated, lower perforated plate, the cylinder are installed between the cylinder and the low head
On be provided with air inlet and gas outlet, reaction zone is provided in the inner cavity of the cylinder, the reaction zone includes cricoid
High-temperature region and low-temperature space, are provided with heat transfer zone between the high-temperature region and the low-temperature space, the high-temperature region is located at institute
The outside for the heat transfer zone stated, the inside of the low-temperature space are equipped with the intermediate channel for reaction gas to be discharged, the high-temperature region
More upright first heat exchanger tubes are inside provided with, more upright second heat exchanger tubes are provided in the low-temperature space, it is described
More upright third heat exchanger tubes, more first heat exchanger tubes, more second heat exchanger tubes and Duo Gen are provided in heat transfer zone
The top and bottom of third heat exchanger tube are separately mounted on the upper perforated plate and the lower perforated plate, and described more first are changed
Catalyst is filled in the shell side of the shell side of heat pipe and more second heat exchanger tubes, more first heat exchanger tubes
Tube-side inlet is communicated with the water outlet of circulating hot water organization of supply, the outlet of the tube sides of more first heat exchanger tubes with it is described
The water inlet of circulating hot water organization of supply communicates, the tube side of more second heat exchanger tubes and the more third heat exchanger tubes
Entrance is communicated through first gas distributor with the air inlet respectively, more second heat exchanger tubes and described more
The tube side outlet of three heat exchanger tubes is communicated through second gas distributor with the shell side inlet of more first heat exchanger tubes respectively, institute
The shell side and intermediate channel of the shell side for more first heat exchanger tubes stated, the shell side of more third heat exchanger tubes, more second heat exchanger tubes
It is sequentially communicated, the intermediate channel is communicated with the gas outlet.
The reactor of the present invention is in use, fresh synthesis gas is entered by air inlet and first gas distributor simultaneously first
The shell side of the tube side of more second heat exchanger tubes and Duo Gen third heat exchanger tubes, Radial Flow at most the first heat exchanger tube of root is reacted,
Radial Flow again carries out hot friendship by the fresh synthesis gas of the low temperature flowed through in the tube side of heat transfer zone and more third heat exchanger tubes
It changes, the shell side of synthesis gas Radial Flow at most the second heat exchanger tube of root again after temperature reduces is reacted, and what is generated after reaction is anti-
Should gas go out reactor from gas outlet after intermediate channel converges.The heat in reaction process high temperature area is by circulating hot water organization of supply
It takes away, the heat of the gas before entering low-temperature space is taken away by the fresh synthesis gas in more third heat exchanger tubes in heat transfer zone,
The heat of low-temperature space is taken away by the fresh synthesis gas in more second heat exchanger tubes, it is seen then that reaction gas is when entering reaction zone, first
Radial Flow to high-temperature region is reacted, and then Radial Flow to heat transfer zone cools down, then Radial Flow to low-temperature space is reacted,
And the temperature of circulating hot water that the reaction temperature of high-temperature region is provided by circulating hot water organization of supply determines, and the temperature of hot water is by urging
The active temperature of agent determines that the reaction temperature of low-temperature space is by the temperature of the fresh synthesis gas quoted from air inlet, the work of catalyst
Warm-natured degree and the heat transfer effect of heat transfer zone determine that good energy-conserving effect can avoid unnecessary energy dissipation.The reactor of the present invention
In, synthesis gas Radial Flow in reaction zone, and reaction temperature can be effectively reduced in reaction process, there is space availability ratio
The advantages of height, catalyst charging ratio height, synthesis gas residence time length, reaction temperature diversity, tubulation high conversion rate.
Preferably, the first gas distributor and the second gas distributor be separately mounted to it is described under
On tube sheet and the upper perforated plate, the first gas distributor be located at the heat transfer zone and the low-temperature space just under
Side, the second gas distributor are located at the surface of the heat transfer zone and the low-temperature space.Low-temperature space just under
First gas distributor and second gas distributor is respectively set simultaneously in side and surface, is conducive to the gas distribution effect for improving synthesis gas
Rate, it is ensured that the conversion ratio of subsequent reactions.
Preferably, the first gas distributor is the spiral shell dish-type being made of one or more closed first square tube
The tube-side inlet of gas distributor, more second heat exchanger tubes and the more third heat exchanger tubes is respectively with described
One gas distributor communicates, and the radial direction of the first gas distributor is provided with more closed first total square tubes, institute
The air inlet stated is arranged on the low head, and the air inlet communicated with the air inlet is provided on the low head
Pipe, more first total square tubes are communicated with the first gas distributor and the air inlet pipe respectively.
Preferably, the second gas distributor is the spiral shell dish-type being made of one or more closed second square tube
The tube side outlet of gas distributor, more second heat exchanger tubes and the more third heat exchanger tubes is respectively with described the
Two gas distributors communicate, the radial direction through the second gas distributor and the high-temperature region be provided with more it is closed
Second total square tube, more second total square tubes exchange heat with the second gas distributor and described more first respectively
The shell side inlet of pipe communicates.
First gas distributor and second gas distributor are spiral shell dish configuration, and the first gas of spiral shell dish configuration is divided
Cloth device and second gas distributor can be made of one or more closed square tube, and axial dimension is small, is conducive to the sky of reactor
Between save.The lower end and upper end of more second heat exchanger tubes and Duo Gen third heat exchanger tubes are respectively along first gas distributor and the second gas
Body distributor helically arrange by type, is conducive to synthesis gas even into reactor and reaction zone.
Preferably, being equipped with the charging for the annular to the low-temperature space loading catalyst on the upper perforated plate
Cylinder, the cartridge are located at the surface of the low-temperature space, are provided on the upper perforated plate multiple along screw type arrangement
Charging hole, constituting between the second square tube of the radially adjoining of the second gas distributor has gap, to described
Screw type gap is formed on second gas distributor, the orthographic projection of multiple charging holes is fallen in the second gas point
On the screw type gap of cloth device, several charging doors, several charging doors point are installed in the upper portion side wall of the cylinder
It is not communicated with the shell side of more first heat exchanger tubes.The design of charging hole on above-mentioned cartridge combination upper perforated plate, is convenient for
The filling of catalyst feeds, and operability is strong.While by cartridge to low-temperature space loading catalyst, charging door can be passed through
It is easy to operate, quick to high-temperature region loading catalyst.
Preferably, multiple dumping pits arranged along screw type are provided on the lower perforated plate, multiple dischargings
Low-temperature space described in the face of hole, constituting between the first square tube of the radially adjoining of the first gas distributor has gap,
To be formed with screw type gap on the first gas distributor, the orthographic projection of multiple dumping pits is fallen described
On the screw type gap of first gas distributor, the discharging opposite with the low temperature zone position is installed on the lower perforated plate
Bucket, is equipped with several discharge ports on the lower sides of the cylinder, several discharge ports respectively with described more the
The shell side of one heat exchanger tube communicates.The effect of dumping pit and dump skip is to carry out discharging, discharging to the catalyst filled in low-temperature space
The effect of mouth is to carry out discharging to the catalyst filled in high-temperature region, keeps the discharging operations of low-temperature space and high-temperature region non-interference,
Ensure unloading efficiency.
Preferably, the first guide shell and the second guide shell are provided on the inside of the cylinder, first water conservancy diversion
Cylinder and second guide shell are annular, equal respectively on the barrel of first guide shell and second guide shell
Even to offer deflector hole, the intermediate channel is located at the middle part of second guide shell, first guide shell it is outer
There is first annular gap, the high-temperature region to be located between side and the inside of the cylinder in first guide shell,
The low-temperature space is located in second guide shell, and the heat transfer zone is located inside and the institute of first guide shell
Between the outside for the second guide shell stated, it is equipped on the upper perforated plate every cylinder, it is described every cylinder and first water conservancy diversion
The outer diameter of cylinder is identical, described to surround the second annular gap every cylinder, cartridge, upper cover and upper perforated plate, described more first
The tube side outlet of heat exchanger tube is communicated through second annular gap with the water inlet of the circulating hot water organization of supply, described
Every offering multiple first row stomatas on cylinder, be provided on the upper perforated plate opposite with the first annular interstitial site
Multiple second row stomatas, more second total square tubes are through multiple first row stomatas and multiple second rows
Stomata is communicated with the first annular gap.
Preferably, the circulating hot water organization of supply includes drum, high-temperature boiler water, institute are housed in the drum
The water outlet for the drum stated is communicated with the tube-side inlet of more first heat exchanger tubes, the pipe of more first heat exchanger tubes
Journey entrance is located at the bottom of more first heat exchanger tubes, tube side outlet and the vapour of more first heat exchanger tubes
The air inlet of packet communicates.In use, high-temperature boiler water from the second heat exchanger tube that bottom enters high-temperature region, becomes after absorbing reaction heat
Drum is returned at steam, Natural Circulation is realized by density contrast.
Compared with prior art, the invention has the advantages that：For reaction gas when entering reaction zone, Radial Flow is extremely first
High-temperature region is reacted, and then Radial Flow to heat transfer zone cools down, then Radial Flow to low-temperature space is reacted, and high-temperature region
The temperature for the circulating hot water that reaction temperature is provided by circulating hot water organization of supply determines, and the temperature of hot water is by the activity of catalyst
Temperature determines that the reaction temperature of low-temperature space by the temperature of the fresh synthesis gas quoted from air inlet, the active temperature of catalyst and is changed
The heat transfer effect of hot-zone determines that good energy-conserving effect can avoid unnecessary energy dissipation.In the reactor of the present invention, synthesis gas
The Radial Flow in reaction zone, and reaction temperature can be effectively reduced in reaction process, there is space availability ratio height, catalyst dress
The advantages of load rate height, synthesis gas residence time length, reaction temperature diversity, tubulation high conversion rate, is suitable for Fiscber-Tropscb synthesis, becomes
It changes, the strong exothermal reactions such as methanol, ethyl alcohol.
Description of the drawings
Fig. 1 is the structural schematic diagram of reactor in embodiment；
Fig. 2 is A-A sectional views in the Fig. 1 amplified after 4 times；
Fig. 3 is the partial enlarged view in the middle part of Fig. 2；
Fig. 4 is B-B sectional views in the Fig. 1 amplified after 4 times；
Fig. 5 is the partial enlarged view in the middle part of Fig. 4；
Fig. 6 is the corresponding elevational schematic of dotted line frame at C in Fig. 1.
Specific implementation mode
Below in conjunction with attached drawing embodiment, present invention is further described in detail.
The energy-saving radial reactor suitable for strong exothermal reaction of embodiment 1, as shown, including cylinder 1, cylinder 1
Both ends be connected separately with upper cover 21 and low head 22, upper perforated plate 23 is installed between upper cover 21 and cylinder 1, cylinder 1 with
Lower perforated plate 24 is installed between low head 22, air inlet 251 and gas outlet 253 are provided on cylinder 1, is set in the inner cavity of cylinder 1
It is equipped with reaction zone, reaction zone includes cricoid high-temperature region 3 and low-temperature space 4, and heat transfer zone is provided between high-temperature region 3 and low-temperature space 4
8, high-temperature region 3 is located at the outside of heat transfer zone 8, and the inside of low-temperature space 4 is equipped with the intermediate channel 42 for reaction gas to be discharged, high-temperature region
It is provided with more upright first heat exchanger tubes 31 in 3, more upright second heat exchanger tubes 41, heat transfer zone 8 are provided in low-temperature space 4
More upright third heat exchanger tubes 81 are inside provided with, more first heat exchanger tubes 31, more second heat exchanger tubes 41 and Duo Gen thirds are changed
The top and bottom of heat pipe 81 are separately mounted on upper perforated plate 23 and lower perforated plate 24, the shell side and Duo Gen of more first heat exchanger tubes 31
Catalyst is filled in the shell side of second heat exchanger tube 41, tube-side inlet and the circulating hot water of more first heat exchanger tubes 31 supply machine
The water outlet of structure 7 communicates, and the tube side outlet of more first heat exchanger tubes 31 is communicated with the water inlet of circulating hot water organization of supply 7, more
The tube-side inlet of the second heat exchanger tube of root 41 and Duo Gen thirds heat exchanger tube 81 is respectively through first gas distributor 5 and 251 phase of air inlet
Logical, the tube side outlet of more second heat exchanger tubes 41 and Duo Gen thirds heat exchanger tube 81 is respectively through second gas distributor 6 and more the
The shell side inlet of one heat exchanger tube 31 communicates, the shell side of more first heat exchanger tubes 31, the shell side of more third heat exchanger tubes 81, more
The shell side and intermediate channel 42 of two heat exchanger tubes 41 are sequentially communicated, and intermediate channel 42 is communicated with gas outlet 253.
In embodiment 1, circulating hot water organization of supply 7 includes drum 71, and high-temperature boiler water is housed in drum 71, drum 71
Water outlet is communicated with the tube-side inlet of more first heat exchanger tubes 31, and the tube-side inlet of more first heat exchanger tubes 31 is located at more first
The tube side outlet of the bottom of heat exchanger tube 31, more first heat exchanger tubes 31 is communicated with the air inlet 251 of drum 71.
The energy-saving radial reactor suitable for strong exothermal reaction of embodiment 2, as shown, including cylinder 1, cylinder 1
Both ends be connected separately with upper cover 21 and low head 22, upper perforated plate 23 is installed between upper cover 21 and cylinder 1, cylinder 1 with
Lower perforated plate 24 is installed between low head 22, air inlet 251 and gas outlet 253 are provided on cylinder 1, is set in the inner cavity of cylinder 1
It is equipped with reaction zone, reaction zone includes cricoid high-temperature region 3 and low-temperature space 4, and heat transfer zone is provided between high-temperature region 3 and low-temperature space 4
8, high-temperature region 3 is located at the outside of heat transfer zone 8, and the inside of low-temperature space 4 is equipped with the intermediate channel 42 for reaction gas to be discharged, high-temperature region
It is provided with more upright first heat exchanger tubes 31 in 3, more upright second heat exchanger tubes 41, heat transfer zone 8 are provided in low-temperature space 4
More upright third heat exchanger tubes 81 are inside provided with, more first heat exchanger tubes 31, more second heat exchanger tubes 41 and Duo Gen thirds are changed
The top and bottom of heat pipe 81 are separately mounted on upper perforated plate 23 and lower perforated plate 24, first gas distributor 5 and second gas point
Cloth device 6 is separately mounted on lower perforated plate 24 and upper perforated plate 23, first gas distributor 5 be located at heat transfer zone and low-temperature space just under
Side, second gas distributor 6 are located at the surface of heat transfer zone and low-temperature space, the shell side and Duo Gen second of more first heat exchanger tubes 31
Catalyst, tube-side inlet and the circulating hot water organization of supply 7 of more first heat exchanger tubes 31 are filled in the shell side of heat exchanger tube 41
Water outlet communicate, the tube-side inlet of more second heat exchanger tubes 41 and Duo Gen thirds heat exchanger tube 81 is respectively through first gas distributor
5 communicate with air inlet 251, and the tube side outlet of more second heat exchanger tubes 41 and Duo Gen thirds heat exchanger tube 81 is respectively through second gas point
Cloth device 6 is communicated with the shell side inlet of more first heat exchanger tubes 31, the shell side of more first heat exchanger tubes 31, more third heat exchanger tubes 81
Shell side, more second heat exchanger tubes 41 shell side and intermediate channel 42 be sequentially communicated, intermediate channel 42 is communicated with gas outlet 253.
In embodiment 2, first gas distributor 5 is to be distributed by the spiral shell dish-type gas that more closed first square tubes 51 are constituted
The tube-side inlet of device, more second heat exchanger tubes 41 and Duo Gen thirds heat exchanger tube 81 is communicated with first gas distributor 5 respectively, is run through
The radial direction of first gas distributor 5 is provided with four closed first total square tubes 52, and air inlet 251 is arranged on low head 22,
The air inlet pipe 252 communicated with air inlet 251 is provided on low head 22, four first total square tubes 52 are distributed with first gas respectively
Device 5 and air inlet pipe 252 communicate；Second gas distributor 6 is the spiral shell dish-type gas point being made of more closed second square tubes 61
The tube side outlet of cloth device, more second heat exchanger tubes 41 and Duo Gen thirds heat exchanger tube 81 is communicated with second gas distributor 6 respectively, is passed through
The radial direction for wearing second gas distributor 6 and high-temperature region 3 is provided with four closed second total square tubes 62, four second total square tubes 62
It is communicated respectively with the shell side inlet of second gas distributor 6 and the first heat exchanger tubes of Duo Gen 31.
The energy-saving radial reactor suitable for strong exothermal reaction of embodiment 3, the difference from example 2 is that, implement
In example 3, as shown, being equipped with the cartridge 26 for the annular to 4 loading catalyst of low-temperature space, cartridge on upper perforated plate 23
26 are located at the surface of low-temperature space 4, and multiple charging holes 27 arranged along screw type are provided on upper perforated plate 23, constitute second gas
There is gap, to be formed between screw type on second gas distributor 6 between second square tube 61 of the radially adjoining of distributor 6
The orthographic projection of gap 63, multiple charging holes 27 is fallen on the screw type gap 63 of second gas distributor 6, the upper portion side wall of cylinder 1
On be symmetrically installed with multiple charging doors 15, multiple charging doors 15 are communicated with the shell side of more first heat exchanger tubes 31 respectively.
The energy-saving radial reactor suitable for strong exothermal reaction of embodiment 4, difference lies in implement with embodiment 3
In example 4, as shown, being provided with multiple dumping pits 28 arranged along screw type on lower perforated plate 24,28 face of multiple dumping pits is low
Warm area 4, constituting between the first square tube 51 of the radially adjoining of first gas distributor 5 has gap, to which first gas is distributed
Screw type gap 53 is formed on device 5, the orthographic projection of multiple dumping pits 28 is fallen in the screw type gap 53 of first gas distributor 5
On, the dump skip 20 opposite with 4 position of low-temperature space is installed on lower perforated plate 24, is symmetrically installed on the lower sides of cylinder 1 more
A discharge port 16, multiple discharge ports 16 are communicated with the shell side of more first heat exchanger tubes 31 respectively.
The energy-saving radial reactor suitable for strong exothermal reaction of embodiment 5, difference lies in implement with embodiment 4
In example 5, as shown, the inside of cylinder 1 is provided with the first guide shell 10 and the second guide shell 11, the first guide shell 10 and second
Guide shell 11 is annular, and deflector hole is uniformly provided with respectively on the barrel of the first guide shell 10 and the second guide shell 11（In figure
It is not shown）, intermediate channel 42 is located at the middle part of the second guide shell 11, between the outside and the inside of cylinder 1 of the first guide shell 10
With first annular gap 12, high-temperature region 3 is located in the first guide shell 10, and low-temperature space 4 is located in the second guide shell 11, heat transfer zone
8 are located between the inside and the outside of the second guide shell 11 of the first guide shell 10, are equipped on upper perforated plate 23 every cylinder 13, every cylinder 13
It is identical as the outer diameter of the first guide shell 10, surround the second annular gap every cylinder 13, cartridge 26, upper cover 21 and upper perforated plate 23
14, the tube side outlet of more first heat exchanger tubes 31 is communicated through the second annular gap 14 with the water inlet of circulating hot water organization of supply 7,
Every offering multiple first row stomatas on cylinder 13（It is not shown in figure）, it is provided with and 14 position of first annular gap on upper perforated plate 23
Opposite multiple second row stomatas 29, four second total square tubes 62 are through multiple first row stomatas and multiple second row stomatas 29 and
One annular gap 12 communicates.
The above-mentioned energy-saving radial reactor suitable for strong exothermal reaction is in use, fresh synthesis gas passes through air inlet first
251 and first gas distributor 5 simultaneously enter more second heat exchanger tubes 41 and Duo Gen thirds heat exchanger tube 81 tube side, Radial Flow
The shell side of at most the first heat exchanger tube of root 31 is reacted, then Radial Flow, by the pipe of heat transfer zone 8 and more third heat exchanger tubes 81
The fresh synthesis gas of the low temperature flowed through in journey carries out heat exchange, and Radial Flow at most root second changes the synthesis gas after temperature reduction again
The shell side of heat pipe 41 is reacted, and the reaction gas generated after reaction goes out reactor after intermediate channel 42 converges from gas outlet 253.
The heat in reaction process high temperature area 3 is taken away by circulating hot water organization of supply 7, and the heat of the gas before entering low-temperature space is changed
The fresh synthesis gas in more third heat exchanger tubes 81 in hot-zone 8 is taken away, and the heat of low-temperature space 4 is by more second heat exchanger tubes 41
Fresh synthesis gas take away, it is seen then that reaction gas enter reaction zone when, Radial Flow to high-temperature region 3 is reacted first, then
Radial Flow to heat transfer zone 8 cools down, then Radial Flow to low-temperature space 4 is reacted, and the reaction temperature of high-temperature region 3 is by cycling hot
The temperature for the circulating hot water that water organization of supply 7 provides determines, and the temperature of hot water is determined by the active temperature of catalyst, low-temperature space
4 reaction temperature by the temperature of the fresh synthesis gas quoted from air inlet 251, the active temperature of catalyst and heat transfer zone 8 heat exchange
Effect determines that good energy-conserving effect can avoid unnecessary energy dissipation.In the reactor, synthesis gas radial flow in reaction zone
It is dynamic, and reaction temperature can be effectively reduced in reaction process, there is high space availability ratio, catalyst charging ratio height, synthesis gas to stop
The advantages of staying time length, reaction temperature diversity, tubulation high conversion rate.
By taking the energy-saving radial reactor suitable for strong exothermal reaction of embodiment 6 as an example, the course of work is：It uses
When, fresh synthesis gas is sent into first gas distributor 5 through air inlet 251；After fresh synthesis gas enters first gas distributor 5,
Through four first total square tubes 52 simultaneously into more in the tube side of more second heat exchanger tubes 41 in low-temperature space 4 and heat transfer zone 8
The tube side of root third heat exchanger tube 81, then exported from the tube side of the second heat exchanger tube 41 and flow into four second total square tubes 62, through four pieces the
Two total square tubes 62 enter the second annular gap 14, subsequently into first annular gap 12, after through 10 radial flow of the first guide shell
The shell side for entering more first heat exchanger tubes 31 in high-temperature region 3, is reacted in the shell side of more first heat exchanger tubes 31, was reacted
Journey high temperature boiler water becomes steam and returns to drum from the second heat exchanger tube 41 that bottom enters high-temperature region 3 after absorbing reaction heat
71, Natural Circulation is realized by density contrast, the synthesis gas after cooling from 3 radial inflow heat transfer zone 8 of high-temperature region, changes again with more thirds
The fresh synthesis gas of the low temperature flowed through in the tube side of heat pipe 81 carries out heat exchange, temperature reduce after synthesis gas Radial Flow again,
Low-temperature space 4 is entered to through the second guide shell 11, is reacted in the shell side of more second heat exchanger tubes 41, finally from the second water conservancy diversion
11 inside of cylinder flows into intermediate channel 42, goes out reactor from gas outlet 253 after intermediate channel 42 converges.
Claims (8)
1. a kind of energy-saving radial reactor suitable for strong exothermal reaction, including cylinder, the both ends of the cylinder connect respectively
Be connected to upper cover and low head, upper perforated plate be installed between the upper cover and the cylinder, the cylinder with it is described
Low head between lower perforated plate is installed, air inlet and gas outlet are provided on the cylinder, in the inner cavity of the cylinder
It is provided with reaction zone, it is characterised in that：The reaction zone includes cricoid high-temperature region and low-temperature space, the high-temperature region and institute
Heat transfer zone is provided between the low-temperature space stated, the high-temperature region is located at the outside of the heat transfer zone, the low-temperature space
Inside is equipped with the intermediate channel for reaction gas to be discharged, and more upright first heat exchanger tubes, institute are provided in the high-temperature region
It is provided with more upright second heat exchanger tubes in the low-temperature space stated, upright more thirds heat exchange is provided in the heat transfer zone
Pipe, the top and bottom of more first heat exchanger tubes, more second heat exchanger tubes and Duo Gen third heat exchanger tubes are separately mounted to
On the upper perforated plate and the lower perforated plate, the shell side of more first heat exchanger tubes and more second heat exchanger tubes
Shell side in be filled with catalyst, the water outlet of the tube-side inlet and circulating hot water organization of supply of more first heat exchanger tubes
Mouth communicates, and the tube side outlet of more first heat exchanger tubes is communicated with the water inlet of the circulating hot water organization of supply, institute
The tube-side inlet of more second heat exchanger tubes and the more third heat exchanger tubes stated respectively through first gas distributor with it is described
Air inlet communicate, the tube sides of more second heat exchanger tubes and the more third heat exchanger tubes exports respectively through the second gas
Body distributor is communicated with the shell side inlet of more first heat exchanger tubes, the shell side of more first heat exchanger tubes, more
The shell side of third heat exchanger tube, the shell side of more second heat exchanger tubes and intermediate channel are sequentially communicated, the intermediate channel with it is described
Gas outlet communicate.
2. according to a kind of energy-saving radial reactor suitable for strong exothermal reaction of claim 1, it is characterised in that：Described
One gas distributor and the second gas distributor are separately mounted on the lower perforated plate and the upper perforated plate, described
First gas distributor be located at the underface of the heat transfer zone and the low-temperature space, the second gas distributor position
Surface in the heat transfer zone and the low-temperature space.
3. according to a kind of energy-saving radial reactor suitable for strong exothermal reaction of claim 2, it is characterised in that：Described
One gas distributor is the spiral shell dish-type gas distributor being made of one or more closed first square tube, described more second
The tube-side inlet of heat exchanger tube and the more third heat exchanger tubes is communicated with the first gas distributor respectively, through described
The radial direction of first gas distributor be provided with more closed first total square tubes, the air inlet is arranged in the lower envelope
On head, the air inlet pipe communicated with the air inlet, more first total square tube difference are provided on the low head
It is communicated with the first gas distributor and the air inlet pipe.
4. according to a kind of energy-saving radial reactor suitable for strong exothermal reaction of claim 2, it is characterised in that：Described
Two gas distributors are the spiral shell dish-type gas distributor being made of one or more closed second square tube, described more second
The outlet of the tube side of heat exchanger tube and the more third heat exchanger tubes is communicated with the second gas distributor respectively, through described
Second gas distributor and the radial direction of the high-temperature region be provided with more closed second total square tubes, described more second
Total square tube is communicated with the shell side inlet of the second gas distributor and more first heat exchanger tubes respectively.
5. according to a kind of energy-saving radial reactor suitable for strong exothermal reaction of claim 4, it is characterised in that：Described is upper
Cartridge for from the annular to the low-temperature space loading catalyst is installed, the cartridge is located at described on tube sheet
The surface of low-temperature space is provided with multiple charging holes arranged along screw type on the upper perforated plate, constitutes second gas
There is gap, to be formed with spiral on the second gas distributor between second square tube of the radially adjoining of body distributor
The orthographic projection in type gap, multiple charging holes is fallen on the screw type gap of the second gas distributor, described
Several charging doors are installed in the upper portion side wall of cylinder, several charging doors respectively with more first heat exchanger tubes
Shell side communicates.
6. according to a kind of energy-saving radial reactor suitable for strong exothermal reaction of claim 5, it is characterised in that：Under described
Multiple dumping pits arranged along screw type are provided on tube sheet, the low-temperature space described in multiple dumping pit faces constitutes institute
There is gap, on the first gas distributor between first square tube of the radially adjoining for the first gas distributor stated
It is formed with screw type gap, the orthographic projection of multiple dumping pits is fallen in the screw type gap of the first gas distributor
On, the dump skip opposite with the low temperature zone position be installed, on the lower sides of the cylinder on the lower perforated plate
Several discharge ports are installed, several discharge ports are communicated with the shell side of more first heat exchanger tubes respectively.
7. according to a kind of energy-saving radial reactor suitable for strong exothermal reaction of claim 5, it is characterised in that：The cylinder
The first guide shell and the second guide shell are provided on the inside of body, first guide shell and second guide shell are ring
It is uniformly provided with deflector hole, the centre respectively on the barrel of shape, first guide shell and second guide shell
Channel is located at the middle part of second guide shell, has between the outside and the inside of the cylinder of first guide shell
There are first annular gap, the high-temperature region to be located in first guide shell, the low-temperature space is located at described second
In guide shell, the heat transfer zone is located between the inside and the outside of second guide shell of first guide shell,
It is equipped on the upper perforated plate every cylinder, it is described identical as the outer diameter of the first guide shell every cylinder, it is described every cylinder, dress
Barrel, upper cover and upper perforated plate surround the second annular gap, and the tube side outlets of more first heat exchanger tubes is through described the
Second ring gap is communicated with the water inlet of the circulating hot water organization of supply, described every offering multiple first exhausts on cylinder
Hole is provided with the multiple second row stomatas opposite with the first annular interstitial site on the upper perforated plate, and described is more
Second total square tube of root is through multiple first row stomatas and multiple second row stomatas and the first annular gap
It communicates.
8. according to a kind of energy-saving radial reactor suitable for strong exothermal reaction of claim 1, it is characterised in that：Described follows
Ring hot-water supply structure includes drum, and high-temperature boiler water is housed in the drum, the water outlet of the drum with it is described
The tube-side inlet of more first heat exchanger tubes communicates, and the tube-side inlet of more first heat exchanger tubes is located at described more first
The tube side outlet of the bottom of heat exchanger tube, more first heat exchanger tubes is communicated with the air inlet of the drum.
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| CN201810494702.8A CN108421506B (en) | 2018-05-22 | 2018-05-22 | Energy-saving radial reactor suitable for strong exothermic reaction |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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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 |
| CN110790223A (en) * | 2019-10-24 | 2020-02-14 | 中石化宁波工程有限公司 | Transformation hydrogen production method and isothermal transformation furnace matched with coal water slurry gasification device |
| CN110790227A (en) * | 2019-10-24 | 2020-02-14 | 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 |
| 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 |
| CN111115574A (en) * | 2019-10-24 | 2020-05-08 | 中石化宁波工程有限公司 | CO conversion process for coproducing synthesis gas and hydrogen and isothermal converter |
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| CN111115574A (en) * | 2019-10-24 | 2020-05-08 | 中石化宁波工程有限公司 | CO conversion process for coproducing synthesis gas and hydrogen and isothermal converter |
| 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 |
| 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 |
| 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 |
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| CN108421506B (en) | 2023-11-28 |
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