CN108404821A - A kind of energy-saving and high efficient radial direction methanol reactor - Google Patents
A kind of energy-saving and high efficient radial direction methanol reactor Download PDFInfo
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- CN108404821A CN108404821A CN201810492978.2A CN201810492978A CN108404821A CN 108404821 A CN108404821 A CN 108404821A CN 201810492978 A CN201810492978 A CN 201810492978A CN 108404821 A CN108404821 A CN 108404821A
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 114
- 238000006243 chemical reaction Methods 0.000 claims abstract description 69
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 68
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 68
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 44
- 239000003054 catalyst Substances 0.000 claims abstract description 30
- 230000007246 mechanism Effects 0.000 claims abstract description 30
- 230000008520 organization Effects 0.000 claims abstract description 17
- 239000007789 gas Substances 0.000 claims description 187
- 239000012495 reaction gas Substances 0.000 claims description 15
- 230000003750 conditioning effect Effects 0.000 claims description 7
- 230000001351 cycling effect Effects 0.000 claims description 4
- 239000004744 fabric Substances 0.000 claims description 3
- 230000008901 benefit Effects 0.000 abstract description 4
- 230000000694 effects Effects 0.000 description 4
- 230000021715 photosynthesis, light harvesting Effects 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 210000001520 comb Anatomy 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0242—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 the fluid flow within the bed being predominantly vertical
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0285—Heating or cooling the reactor
-
- 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
- B01J8/065—Feeding reactive fluids
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/152—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
-
- 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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Fluid Mechanics (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention discloses a kind of energy-saving and high efficient radial direction methanol reactors, its reaction zone includes high-temperature region and low-temperature space, more first heat exchanger tubes are provided in high-temperature region, more second heat exchanger tubes are provided in low-temperature space, the top and bottom of the second heat exchanger tube of more first heat exchanger tubes and Duo Gen are separately mounted on upper perforated plate and lower perforated plate, 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 circulating hot water organization of supply, the tube-side inlet of more second heat exchanger tubes is communicated with synthesis gas preheating mechanism, the tube side outlet of more second heat exchanger tubes is communicated with the shell side inlet of more first heat exchanger tubes, the shell side of more first heat exchanger tubes, the shell side and intermediate channel of more second heat exchanger tubes are sequentially communicated, intermediate channel is communicated with synthesis gas preheating mechanism.The reaction utensil has the advantages that space availability ratio height, catalyst charging ratio height, synthesis gas residence time length, reaction temperature diversity, methanol conversion are high.
Description
Technical field
The present invention relates to a kind of chemical industry equipments, and in particular to a kind of energy-saving and high efficient radial direction methanol reactor.
Background technology
Reaction by carbon monoxide and hydrogen synthesizing methanol is a heat release reversible reaction, with the progress of reaction, is reduced
Reaction temperature can improve conversion ratio.Most typical methanol reactor is shell and tube reactor.Heat exchanger tube arrangement common form has
Point of 30 °, 45 °, 90 ° combs, heat exchanger tube apparatus with catalyst inside, pipe outer circulation hot water byproduct steam, synthesis gas is generally along bed
The axial flowing of layer or Radial Flow, and there is space waste in the reactor of synthesis gas Radial Flow.Also, existing reaction
Device is not designed according to the temperature control of reaction different phase.For example, methanol synthesis reactor disclosed in CN205269607U includes cylinder
The upper end of body, cylinder is equipped with upper cover, and the lower end of cylinder is equipped with lower base, upper perforated plate, lower seat are equipped between upper cover and cylinder
Lower perforated plate, the reaction tube being equipped in cylinder between upper perforated plate and lower perforated plate, upper cover and upper tube are equipped between body and cylinder
The first reaction chamber is formed between plate, is formed the second reaction chamber between upper perforated plate and lower perforated plate, is formed between lower perforated plate and lower base
Third reaction chamber, the first reaction chamber is interior to be equipped with the gas distributor being fixed on upper cover, is provided on upper cover and gas is distributed
The air inlet that device is connected, lower base is interior to be equipped with catalyst holder, is formed for flame-proof sphere between the upper end and lower perforated plate of catalyst holder
Accommodating accommodating cavity forms synthesis air cavity, is provided on lower base and is connected with accommodating cavity between the lower end and lower base of catalyst holder
Logical discharge port.In use, gas enters in reactor, initial reaction is carried out by the catalyst layer on upper perforated plate, then into
Enter in reaction tube, is further reacted with the catalyst placed in reaction tube, finally by the catalyst layer below lower perforated plate, again
It is reacted, is then come out from gas outlet by fire resisting layers of balls, leave reactor.It is different in reaction in its entire reaction process
Stage is designed without temperature control.In addition, the gas distributor of the methanol synthesis reactor includes air inlet pipe, circumferentially rotated in air inlet pipe
Be connected with several gas distribution pipes, be provided with the first blow vent on the contact surface of gas distribution pipe and air inlet pipe, the outer wall of air inlet pipe be equipped with
Corresponding second blow vent of first blow vent, and the cloth when gas distribution pipe turns to the first blow vent and the second blow vent is connected
Tracheae inner cavity is connected with air inlet pipe, and several qi-emitting holes are provided on the lower face of gas distribution pipe.The gas distributor is complicated, accounts for
With more upper cover space, also it is unfavorable for the space-saving of reactor.
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, methanol
The energy-saving and high efficient radial direction methanol reactor of high conversion rate.
Technical solution is used by the present invention solves above-mentioned technical problem：A kind of energy-saving and high efficient radial direction methanol reaction
The both ends of device, including cylinder, the cylinder are connected separately with upper cover and low head, the upper cover and the cylinder
Between upper perforated plate is installed, lower perforated plate is installed, in the inner cavity of the cylinder between the cylinder and the low head
It is provided with reaction zone, the reaction zone includes cricoid high-temperature region and low-temperature space, and the high-temperature region is located at the low temperature
The outside in area, the inside of the low-temperature space are equipped with the intermediate channel for reaction gas to be discharged, are provided in the high-temperature region
More upright first heat exchanger tubes, are provided with more upright second heat exchanger tubes in the low-temperature space, described more first
The top and bottom of heat exchanger tube and more second heat exchanger tubes are separately mounted to the upper perforated plate and the lower perforated plate
On, catalyst, institute are filled in the shell side of more first heat exchanger tubes and the shell side of more second heat exchanger tubes
The tube-side inlet for more first heat exchanger tubes stated is communicated with the water outlet of circulating hot water organization of supply, described more first heat exchange
The tube side outlet of pipe is communicated with the water inlet of circulating hot water organization of supply, and the tube-side inlets of more second heat exchanger tubes is through the
One gas distributor is communicated with synthesis gas preheating mechanism, and the tube side outlet of more second heat exchanger tubes is distributed through second gas
Device is communicated with the shell side inlet of more first heat exchanger tubes, the shell side of more first heat exchanger tubes, more second change
The shell side and intermediate channel of heat pipe are sequentially communicated, and the outlet of the intermediate channel is communicated with the synthesis gas preheating mechanism,
The synthesis gas preheating mechanism is used to arrange reaction gas to the synthesis gas of reactor offer preheating is simultaneously outer.
The methanol reactor of the present invention is in use, the synthesis gas preheated through synthesis gas preheating mechanism passes through first gas first
Distributor enters the tube side of more second heat exchanger tubes, and the shell side of Radial Flow at most the first heat exchanger tube of root is reacted, then radial
The shell side for flowing to more second heat exchanger tubes is reacted, and the heat in reaction process high temperature area is by circulating hot water organization of supply band
It walks, the heat of low-temperature space is taken away by the fresh synthesis gas in more second heat exchanger tubes, and the reaction gas generated after reaction is logical in centre
Road goes out reactor and returns to synthesis gas preheating mechanism after converging.As it can be seen that reaction gas, when entering reaction zone, Radial Flow is extremely first
High-temperature region is reacted, then Radial Flow to low-temperature space is reacted, and the reaction temperature of high-temperature region supplies machine by circulating hot water
The temperature for the circulating hot water that structure provides determines, and the temperature of hot water is determined by the active temperature of catalyst, the reaction temperature of low-temperature space
The temperature of fresh synthesis gas provided by synthesis gas preheating mechanism is provided and the active temperature of catalyst determines that good energy-conserving effect can
Avoid unnecessary energy dissipation.In the methanol reactor of the present invention, synthesis gas Radial Flow in reaction zone has space profit
With the high advantage of rate height, catalyst charging ratio height, synthesis gas residence time length, reaction temperature diversity, methanol conversion.
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 is located at the underface of the low-temperature space, and described second
Gas distributor is located at the surface of the low-temperature space.In the underface of low-temperature space and surface, gas distribution is set simultaneously
Device is conducive to the gas distribution efficiency for improving synthesis gas, 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 is communicated with the first gas distributor respectively, is run through
The radial direction of the first gas distributor is provided with more closed first total square tubes, is provided with and communicates on the low head
Air inlet and air inlet pipe, the air inlet of the low head communicated with the synthesis gas preheating mechanism, described more
One total square tube is 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 is communicated with the second gas distributor respectively, is run through
The radial direction of the second gas distributor and the high-temperature region is 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 simultaneously.
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 are respectively along first gas distributor and second gas distributor helically type
Arrangement, is conducive to synthesis gas even into reactor and reaction zone.
Preferably, being equipped with the charging for the annular to the reaction zone loading catalyst on the upper perforated plate
Cylinder, the cartridge are located at the surface of the second gas distributor, are provided on the upper perforated plate multiple along spiral shell
The charging hole of rotation type arrangement, constituting between the second square tube of the radially adjoining of the second gas distributor has gap, from
And screw type gap is formed on the second gas distributor, the orthographic projection of multiple charging holes is fallen described
On the screw type gap of two gas distributors.The design of charging hole on above-mentioned cartridge combination upper perforated plate, convenient for catalyst
Filling charging, operability are strong.
Preferably, being provided with multiple dumping pits arranged along screw type on the lower perforated plate, described first is constituted
There is gap, to be formed with spiral shell on the first gas distributor between first square tube of the radially adjoining of gas distributor
The orthographic projection in rotation type gap, multiple dumping pits is fallen on the screw type gap of the first gas distributor, described
Lower perforated plate on the dump skip opposite with the first gas distributor position is installed.Above-mentioned dumping pit and dump skip are set
Meter, keeps the discharging operations of catalyst convenient, efficient.
Preferably, being provided with the guide shell of annular on the inside of the cylinder, on the barrel of the guide shell uniformly
Offer deflector hole, the intermediate channel is located at the middle part of the guide shell, the outside of the guide shell with it is described
There is first annular gap, the reaction zone is located in the guide shell, on the upper perforated plate between the inside of cylinder
It is equipped with every cylinder, it is described identical as the outer diameter of the guide shell every cylinder, it is the cartridge every cylinder, described, described
Upper cover and the 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.Guide shell can ensure that synthesis gas can be even into reaction zone, while be conducive to the modularized design of reactor.
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.
Preferably, the synthesis gas preheating mechanism includes gas-gas heat exchanger, the gas-gas heat exchanger includes first
Entrance, first outlet, second entrance and second outlet, the gas-gas heat exchanger is for preheating from the first entrance
Fresh synthesis gas, the fresh synthesis gas after preheating are communicated through first outlet with the first gas distributor, and described second
Entrance is communicated with the outlet of the intermediate channel, and the second outlet is used for outer row's reaction gas.In use, gas-gas heat exchanger
The fresh synthesis gas from first entrance is preheated, the fresh synthesis gas of preheating is sent into first gas distributor；It is generated after reaction
Reaction gas most return to gas-gas heat exchanger through second entrance afterwards, carried out after heat exchange outside through second outlet with fresh synthesis gas
Row.
Preferably, being provided with temperature conditioning unit on the synthesis gas preheating mechanism, the temperature conditioning unit includes temperature
Control valve and temperature element, the temperature control valve are mounted on the side between the first entrance and the first outlet
On the road, the temperature element is mounted on the pipeline between the first outlet and the first gas distributor, institute
The thermometer stated is electrically connected with the temperature control valve.By temperature conditioning unit, it can monitor in real time and adjust gas-gas heat exchanger
Air outlet temperature, to adjust the temperature into the synthesis gas of reactor, it is ensured that reaction effect.
Compared with prior art, the invention has the advantages that：Energy-saving and high efficient radial direction methanol reaction disclosed by the invention
During device use, reaction gas when entering reaction zone, reacted first by Radial Flow to high-temperature region, then Radial Flow is to low
Warm area 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 determines by the active temperature of catalyst, the fresh conjunction that the reaction temperature of low-temperature space is provided by synthesis gas preheating mechanism
It is determined at the temperature of gas and the active temperature of catalyst, good energy-conserving effect can avoid unnecessary energy dissipation.The first of the present invention
In alcohol reactor, there is synthesis gas Radial Flow in reaction zone high space availability ratio, catalyst charging ratio height, synthesis gas to stop
The advantage for staying time length, reaction temperature diversity, methanol conversion high.
Description of the drawings
Fig. 1 is the structural schematic diagram of energy-saving and high efficient radial direction methanol 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 and high efficient radial direction methanol reactor of embodiment 1, including cylinder 1, the both ends of cylinder 1 are connected separately with envelope
First 21 and low head 22, upper perforated plate 23 is installed between upper cover 21 and cylinder 1, is equipped with down between cylinder 1 and low head 22
Tube sheet 24 is provided with reaction zone in the inner cavity of cylinder 1, and reaction zone includes cricoid high-temperature region 3 and low-temperature space 4, and high-temperature region 3 is located at
The outside of low-temperature space 4, the inside of low-temperature space 4 are equipped with the intermediate channel 42 for reaction gas to be discharged, are provided in high-temperature region 3 upright
More first heat exchanger tubes 31, be provided with more upright second heat exchanger tubes 41 in low-temperature space 4, more first heat exchanger tubes 31 and more
The top and bottom of the second heat exchanger tube of root 41 are separately mounted on upper perforated plate 23 and lower perforated plate 24, the shell of more first heat exchanger tubes 31
Catalyst, the tube-side inlet and cycling hot of more first heat exchanger tubes 31 are filled in the shell side of journey and the second heat exchanger tubes of Duo Gen 41
The water outlet of water organization of supply 7 communicates, the water inlet of the tube side outlet and circulating hot water organization of supply 7 of more first heat exchanger tubes 31
It communicates, the tube-side inlet of more second heat exchanger tubes 41 is communicated through first gas distributor 5 with synthesis gas preheating mechanism 8, more
The tube side outlet of two heat exchanger tubes 41 is communicated through second gas distributor 6 with the shell side inlet of more first heat exchanger tubes 31, more the
The shell side of one heat exchanger tube 31, the shell side of more second heat exchanger tubes 41 and intermediate channel 42 are sequentially communicated, the outlet of intermediate channel 42
It is communicated with synthesis gas preheating mechanism 8, the synthesis gas that synthesis gas preheating mechanism 8 is used to preheat to reactor offer simultaneously react by outer arrange
Gas.
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 of drum 71.
The energy-saving and high efficient radial direction methanol reactor of embodiment 2, including cylinder 1, the both ends of cylinder 1 are connected separately with envelope
First 21 and low head 22, upper perforated plate 23 is installed between upper cover 21 and cylinder 1, is equipped with down between cylinder 1 and low head 22
Tube sheet 24 is provided with reaction zone in the inner cavity of cylinder 1, and reaction zone includes cricoid high-temperature region 3 and low-temperature space 4, and high-temperature region 3 is located at
The outside of low-temperature space 4, the inside of low-temperature space 4 are equipped with the intermediate channel 42 for reaction gas to be discharged, are provided in high-temperature region 3 upright
More first heat exchanger tubes 31, be provided with more upright second heat exchanger tubes 41 in low-temperature space 4, more first heat exchanger tubes 31 and more
The top and bottom of the second heat exchanger tube of root 41 are separately mounted on upper perforated plate 23 and lower perforated plate 24, the shell of more first heat exchanger tubes 31
Catalyst, the tube-side inlet and cycling hot of more first heat exchanger tubes 31 are filled in the shell side of journey and the second heat exchanger tubes of Duo Gen 41
The water outlet of water organization of supply 7 communicates, and the tube-side inlet of more second heat exchanger tubes 41 is pre- through first gas distributor 5 and synthesis gas
Heat engine structure 8 communicates, and the tube side of more second heat exchanger tubes 41 exports the shell through second gas distributor 6 Yu more first heat exchanger tubes 31
Journey entrance communicates, and first gas distributor 5 and second gas distributor 6 are separately mounted on lower perforated plate 24 and upper perforated plate 23, the
One gas distributor 5 is located at the underface of low-temperature space 4, and second gas distributor 6 is located at the surface of low-temperature space 4, more first
The shell side of heat exchanger tube 31, the shell side of more second heat exchanger tubes 41 and intermediate channel 42 are sequentially communicated, the outlet of intermediate channel 42 with
Synthesis gas preheating mechanism 8 communicates, and synthesis gas preheating mechanism 8 is used to arrange reaction gas to the synthesis gas of reactor offer preheating is simultaneously outer.
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 is communicated with first gas distributor 5 respectively, through first gas distributor 5
Radial direction is provided with four closed first total square tubes 52, and the air inlet 251 communicated and air inlet pipe 252 are provided on low head 22,
The air inlet 251 of low head 22 is communicated with synthesis gas preheating mechanism 8, four first total square tubes 52 respectively with first gas distributor
5 and air inlet pipe 252 communicate；Second gas distributor 6 is to be distributed by the spiral shell dish-type gas that more closed second square tubes 61 are constituted
The tube side outlet of device, more second heat exchanger tubes 41 is communicated with second gas distributor 6 respectively, runs through 6 He of second gas distributor
The radial direction of high-temperature region 3 is provided with four closed second total square tubes 62, and four second total square tubes 62 are distributed with second gas simultaneously
The shell side inlet of device 6 and the first heat exchanger tubes of Duo Gen 31 communicates.
In embodiment 2, synthesis gas preheating mechanism 8 include gas-gas heat exchanger 81, gas-gas heat exchanger 81 include first entrance 82,
First outlet 83, second entrance 84 and second outlet 85, gas-gas heat exchanger 81 is for preheating the fresh conjunction from first entrance 82
At gas, the fresh synthesis gas after preheating is communicated through first outlet 83 with first gas distributor 5, second entrance 84 and intermediate channel
42 outlet communicates, and second outlet 85 is used for outer row's reaction gas.
The energy-saving and high efficient radial direction methanol reactor of embodiment 3, the difference from example 2 is that, in embodiment 3, upper tube
Cartridge 26 for from the annular to reaction zone loading catalyst is installed, cartridge 26 is located at second gas distributor on plate 23
6 surface is provided with multiple charging holes 27 arranged along screw type on upper perforated plate 23, constitutes the diameter of second gas distributor 6
To having gap between the second adjacent square tube 61, to be formed with screw type gap 63, multiple dresses on second gas distributor 6
The orthographic projection in material hole 27 is fallen on the screw type gap 63 of second gas distributor 6.
The energy-saving and high efficient radial direction methanol reactor of embodiment 4, with embodiment 3 difference lies in, in embodiment 4, down tube
It is provided with multiple dumping pits 28 arranged along screw type on plate 24, constitutes the first party of the radially adjoining of first gas distributor 5
There is gap, to be formed with screw type gap 53, the orthographic projection of multiple dumping pits 28 on first gas distributor 5 between pipe 51
It falls on the screw type gap 53 of first gas distributor 5, is equipped on lower perforated plate 24 opposite with 5 position of first gas distributor
Dump skip 20.
The energy-saving and high efficient radial direction methanol reactor of embodiment 5, with embodiment 4 difference lies in, in embodiment 5, cylinder 1
Inside be provided with the guide shell 11 of annular, be uniformly provided with deflector hole on the barrel of guide shell 11（It is not shown in figure）, intermediate
Channel 42 is located at the middle part of guide shell 11, has first annular gap 12 between the outside and the inside of cylinder 1 of guide shell 11, instead
Answer area to be located in guide shell 11, be equipped on upper perforated plate 23 every cylinder 13, it is identical as the outer diameter of guide shell 11 every cylinder 13, every cylinder 13,
Cartridge 26, upper cover 21 and upper perforated plate 23 surround the second annular gap 14, and the tube side outlets of more first heat exchanger tubes 31 is through the
Second ring gap 14 is communicated with the water inlet of circulating hot water organization of supply 7, every offering multiple first row stomatas on cylinder 13（In figure
It is not shown）, the multiple second row stomatas 29 opposite with 14 position of first annular gap are provided on upper perforated plate 23, four second total
Square tube 62 is communicated through multiple first row stomatas and multiple second row stomatas 29 with first annular gap 12.
The energy-saving and high efficient radial direction methanol reactor of embodiment 6, difference lies in embodiment 6, synthesize with embodiment 5
Temperature conditioning unit is provided on gas preheating mechanism 8, temperature conditioning unit includes temperature control valve 86 and temperature element 87, temperature control valve 86
In bypass between first entrance 82 and first outlet 83, temperature element 87 is mounted on first outlet 83 and first gas
On pipeline between distributor 5, thermometer is electrically connected with temperature control valve 86.
Above-mentioned energy-saving and high efficient radial direction methanol reactor in use, through synthesis gas preheating mechanism 8 preheat synthesis gas first
Enter the tube side of more second heat exchanger tubes 41, the shell of Radial Flow at most the first heat exchanger tube of root 31 by first gas distributor 5
Cheng Jinhang reacts, then the shell side of Radial Flow at most the second heat exchanger tube of root 41 is reacted, the heat in reaction process high temperature area 3
It is taken away by circulating hot water organization of supply 7, the heat of low-temperature space is taken away by the fresh synthesis gas in more second heat exchanger tubes 41, reaction
The reaction gas generated afterwards, which goes out reactor after intermediate channel 42 converges and returns to synthesis gas preheating mechanism 8, carries out outer arrange.As it can be seen that anti-
Should gas enter reaction zone when, Radial Flow to high-temperature region 3 is reacted first, then Radial Flow to low-temperature space 4 is reacted,
And the temperature of circulating hot water that the reaction temperature of high-temperature region 3 is provided by circulating hot water organization of supply 7 determines, and the temperature of hot water by
The active temperature of catalyst determines, the temperature for the fresh synthesis gas that the reaction temperature of low-temperature space 4 is provided by synthesis gas preheating mechanism 8
And the active temperature of catalyst determines, good energy-conserving effect can avoid unnecessary energy dissipation.
By taking the energy-saving and high efficient radial direction methanol reactor of embodiment 6 as an example, a diameter of 4m of cylinder 1, tangential length is
8m, the course of work are：In use, gas-gas heat exchanger 81 preheats the fresh conjunction that the temperature from first entrance 82 is 40~60 DEG C
At gas, the fresh synthesis gas that the temperature of preheating is 120~140 DEG C is sent into first gas distributor 5 through air inlet 251；It is fresh
After synthesis gas enters first gas distributor 5, enter more second heat exchanger tubes 41 in low-temperature space 4 through four first total square tubes 52
Tube side, then four second total square tubes 62 are flowed into from the tube side outlet of more second heat exchanger tubes 41, through four second total square tubes 62
Into the second annular gap 14, subsequently into first annular gap 12, after through more in 11 radial inflow high-temperature region 3 of guide shell
The shell side of the first heat exchanger tube of root 31 is reacted, reaction process with the catalyst filled in the shell side of more first heat exchanger tubes 31
High temperature boiler water becomes steam and returns to drum 71 from the second heat exchanger tube 41 that bottom enters high-temperature region 3 after absorbing reaction heat
（Drum coolant-temperature gage is 212~250 DEG C）, Natural Circulation is realized by density contrast, the synthesis gas after cooling is again from 3 radial flow of high-temperature region
The shell side for entering more second heat exchanger tubes 41 in low-temperature space 4, is reacted in the shell side of more second heat exchanger tubes 41, reaction
The heat in low-temperature space 4 is taken away by the fresh synthesis gas in more second heat exchanger tubes 41 simultaneously, the gas after reaction（Temperature 230
~210 DEG C）Intermediate channel 42 finally is flowed into from 11 inside of guide shell, reactor is gone out after intermediate channel 42 converges and is entered through second
Mouthfuls 84 return to gas-gas heat exchanger 81, are carried out after heat exchange through second outlet 85 with fresh synthesis gas（Gas temperature is at this time
150~130 DEG C）Outer row.Different according to different catalysts and catalyst useful load, which produces methanol per year up to 55
~70 ten thousand tons/8000 hours, the mole fraction for exporting methanol can be 0.13~0.16.
Claims (10)
1. a kind of energy-saving and high efficient radial direction methanol reactor, including cylinder, the both ends of the cylinder are connected separately with upper cover
And low head, upper perforated plate is installed between the upper cover and the cylinder, the cylinder and the low head it
Between lower perforated plate is installed, be provided with reaction zone in the inner cavity of the cylinder, it is characterised in that：The reaction zone includes ring-type
High-temperature region and low-temperature space, the high-temperature region be located at the outside of the low-temperature space, the inside of the low-temperature space, which is equipped with, to be used
It is provided with more upright first heat exchanger tubes, the low-temperature space in the intermediate channel of discharge reaction gas, in the high-temperature region
Inside it is provided with more upright second heat exchanger tubes, the upper end of more first heat exchanger tubes and more second heat exchanger tubes
It is separately mounted to lower end on the upper perforated plate and the lower perforated plate, the shell side of more first heat exchanger tubes and described
More second heat exchanger tubes shell side in be filled with catalyst, the tube-side inlet and cycling hot of more first heat exchanger tubes
The water outlet of water organization of supply communicates, and the outlet of the tube sides of more first heat exchanger tubes enters water with circulating hot water organization of supply
Mouth communicates, and the tube-side inlet of more second heat exchanger tubes is communicated through first gas distributor with synthesis gas preheating mechanism, institute
The tube side for more second heat exchanger tubes stated exports the shell side inlet through second gas distributor Yu more first heat exchanger tubes
It communicates, the shell side of more first heat exchanger tubes, the shell side of more second heat exchanger tubes and intermediate channel are sequentially communicated, described
The outlet of intermediate channel is communicated with the synthesis gas preheating mechanism, and the synthesis gas preheating mechanism is used to provide to reactor
The synthesis gas of preheating and outer row's reaction gas.
2. a kind of energy-saving and high efficient radial direction methanol reactor according to claim 1, it is characterised in that：First gas
Body distributor and the second gas distributor are separately mounted on the lower perforated plate and the upper perforated plate, and described the
One gas distributor is located at the underface of the low-temperature space, and the second gas distributor is being located at the low-temperature space just
Top.
3. a kind of energy-saving and high efficient radial direction methanol reactor according to claim 2, it is characterised in that：First gas
Body distributor is the spiral shell dish-type gas distributor being made of one or more closed first square tube, described more second heat exchange
The tube-side inlet of pipe is communicated with the first gas distributor respectively, through the radial setting of the first gas distributor
There are more closed first total square tubes, the air inlet communicated and air inlet pipe, the low head are provided on the low head
Air inlet communicated with the synthesis gas preheating mechanism, more first total square tubes respectively with the first gas point
Cloth device and the air inlet pipe communicate.
4. a kind of energy-saving and high efficient radial direction methanol reactor according to claim 2, it is characterised in that：Second gas
Body distributor is the spiral shell dish-type gas distributor being made of one or more closed second square tube, described more second heat exchange
The tube side outlet of pipe is communicated with the second gas distributor respectively, runs through the second gas distributor and the height
The radial direction of warm area is provided with more closed second total square tubes, more second total square tubes simultaneously with the second gas
The shell side inlet of distributor and more first heat exchanger tubes communicates.
5. a kind of energy-saving and high efficient radial direction methanol reactor according to claim 4, it is characterised in that：The upper perforated plate
On be equipped with for the reaction zone loading catalyst annular cartridge, the cartridge be located at described second
The surface of gas distributor is provided with multiple charging holes arranged along screw type on the upper perforated plate, constitutes described the
There is gap, to be formed on the second gas distributor between second square tube of the radially adjoining of two gas distributors
The orthographic projection in screw type gap, multiple charging holes is fallen on the screw type gap of the second gas distributor.
6. a kind of energy-saving and high efficient radial direction methanol reactor according to claim 5, it is characterised in that：The lower perforated plate
On be provided with multiple dumping pits arranged along screw type, constitute the first square tube of the radially adjoining of the first gas distributor
Between there is gap, to be formed with screw type gap on the first gas distributor, multiple dumping pits are just
Projection is fallen on the screw type gap of the first gas distributor, is equipped on the lower perforated plate and first gas
The opposite dump skip in body distributor position.
7. a kind of energy-saving and high efficient radial direction methanol reactor according to claim 5, it is characterised in that：The cylinder
Inside is provided with the guide shell of annular, and deflector hole, the intermediate channel position are uniformly provided on the barrel of the guide shell
Between the middle part of the guide shell, the outside of the guide shell and the inside of the cylinder have it is first annular between
Gap, the reaction zone are located in the guide shell, are equipped on the upper perforated plate every cylinder, described every cylinder and described
The outer diameter of guide shell is identical, and the cartridge every cylinder, described, the upper cover and the upper perforated plate surround the second ring
The tube side outlet in shape gap, more first heat exchanger tubes is supplied through second annular gap and the circulating hot water
The water inlet of mechanism communicates, described every offering multiple first row stomatas on cylinder, be provided on the upper perforated plate with it is described
The opposite multiple second row stomatas of first annular interstitial site, more second total square tubes are through multiple first rows
Stomata and multiple second row stomatas are communicated with the first annular gap.
8. a kind of energy-saving and high efficient radial direction methanol reactor according to claim 1, it is characterised in that：The cycling hot
Water organization of supply includes drum, and high-temperature boiler water is housed in the drum, the water outlet of the drum with described more
The tube-side inlet of first heat exchanger tube communicates, and the tube-side inlet of more first heat exchanger tubes is located at more first heat exchange
The tube side outlet of the bottom of pipe, more first heat exchanger tubes is communicated with the air inlet of the drum.
9. a kind of energy-saving and high efficient radial direction methanol reactor according to claim 1, it is characterised in that：The synthesis gas
Preheating mechanism includes gas-gas heat exchanger, and the gas-gas heat exchanger includes that first entrance, first outlet, second entrance and second go out
Mouthful, the gas-gas heat exchanger is for preheating the fresh synthesis gas from the first entrance, the fresh synthesis gas after preheating
It is communicated with the first gas distributor through first outlet, the outlet phase of the second entrance and the intermediate channel
Logical, the second outlet is used for outer row's reaction gas.
10. a kind of energy-saving and high efficient radial direction methanol reactor according to claim 9, it is characterised in that：The synthesis
Temperature conditioning unit is provided on gas preheating mechanism, the temperature conditioning unit includes temperature control valve and temperature element, the temperature
Control valve is mounted in the bypass between the first entrance and the first outlet, and the temperature element is mounted on institute
On pipeline between the first outlet stated and the first gas distributor, the thermometer and the temperature control valve
Electrical connection.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109054908A (en) * | 2018-09-30 | 2018-12-21 | 中石化宁波工程有限公司 | A kind of isothermal conversion process of mating coal gasification |
| CN109173937A (en) * | 2018-09-30 | 2019-01-11 | 中石化宁波工程有限公司 | Temperature-changeable methanol synthesis reaction system |
| CN109173938A (en) * | 2018-09-30 | 2019-01-11 | 中石化宁波工程有限公司 | A kind of temperature-changeable methanol-fueled CLC water-cooled reactor |
| CN109173939A (en) * | 2018-09-30 | 2019-01-11 | 中石化宁波工程有限公司 | A kind of water cooling methanol synthesis reactor |
| CN109225074A (en) * | 2018-09-30 | 2019-01-18 | 中石化宁波工程有限公司 | A kind of temperature-changeable isothermal shift-converter |
| CN109261082A (en) * | 2018-09-30 | 2019-01-25 | 中石化宁波工程有限公司 | Isothermal shift-converter |
| CN109261081A (en) * | 2018-09-30 | 2019-01-25 | 中石化宁波工程有限公司 | A kind of temperature-changeable isothermal shift-converter |
| CN109395670A (en) * | 2018-09-30 | 2019-03-01 | 中石化宁波工程有限公司 | The temperature shift reactions device such as alternating temperature |
Citations (4)
| 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 |
| 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 |
| CN107382665A (en) * | 2017-07-13 | 2017-11-24 | 南京国昌化工科技有限公司 | The technique and device of a kind of methanol-fueled CLC |
| CN208389982U (en) * | 2018-05-22 | 2019-01-18 | 中石化宁波工程有限公司 | A kind of energy-saving and high efficient radial direction methanol reactor |
-
2018
- 2018-05-22 CN CN201810492978.2A patent/CN108404821B/en active Active
Patent Citations (4)
| 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 |
| 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 |
| CN107382665A (en) * | 2017-07-13 | 2017-11-24 | 南京国昌化工科技有限公司 | The technique and device of a kind of methanol-fueled CLC |
| CN208389982U (en) * | 2018-05-22 | 2019-01-18 | 中石化宁波工程有限公司 | A kind of energy-saving and high efficient radial direction methanol reactor |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109054908A (en) * | 2018-09-30 | 2018-12-21 | 中石化宁波工程有限公司 | A kind of isothermal conversion process of mating coal gasification |
| CN109173937A (en) * | 2018-09-30 | 2019-01-11 | 中石化宁波工程有限公司 | Temperature-changeable methanol synthesis reaction system |
| CN109173938A (en) * | 2018-09-30 | 2019-01-11 | 中石化宁波工程有限公司 | A kind of temperature-changeable methanol-fueled CLC water-cooled reactor |
| CN109173939A (en) * | 2018-09-30 | 2019-01-11 | 中石化宁波工程有限公司 | A kind of water cooling methanol synthesis reactor |
| CN109225074A (en) * | 2018-09-30 | 2019-01-18 | 中石化宁波工程有限公司 | A kind of temperature-changeable isothermal shift-converter |
| CN109261082A (en) * | 2018-09-30 | 2019-01-25 | 中石化宁波工程有限公司 | Isothermal shift-converter |
| CN109261081A (en) * | 2018-09-30 | 2019-01-25 | 中石化宁波工程有限公司 | A kind of temperature-changeable isothermal shift-converter |
| CN109395670A (en) * | 2018-09-30 | 2019-03-01 | 中石化宁波工程有限公司 | The temperature shift reactions device such as alternating temperature |
| CN109173937B (en) * | 2018-09-30 | 2021-06-11 | 中石化宁波工程有限公司 | Temperature-variable methanol synthesis reaction system |
| CN109225074B (en) * | 2018-09-30 | 2022-04-05 | 中石化宁波工程有限公司 | Temperature-variable isothermal shift reactor |
| CN109173939B (en) * | 2018-09-30 | 2022-04-08 | 中石化宁波工程有限公司 | Water-cooling methanol synthesis reactor |
| CN109261081B (en) * | 2018-09-30 | 2022-04-08 | 中石化宁波工程有限公司 | Temperature-variable isothermal shift reactor |
| CN109395670B (en) * | 2018-09-30 | 2022-04-12 | 中石化宁波工程有限公司 | Temperature-changing isothermal transformation reaction device |
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