CN108261792A - Novel air dynamic formula stirs catalytic distillation device - Google Patents
Novel air dynamic formula stirs catalytic distillation device Download PDFInfo
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- CN108261792A CN108261792A CN201810009113.6A CN201810009113A CN108261792A CN 108261792 A CN108261792 A CN 108261792A CN 201810009113 A CN201810009113 A CN 201810009113A CN 108261792 A CN108261792 A CN 108261792A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/009—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
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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
- B01J8/0292—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 with stationary packing material in the bed, e.g. bricks, wire rings, baffles
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/03—Preparation of carboxylic acid esters by reacting an ester group with a hydroxy group
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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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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The present invention relates to a kind of Novel air dynamic formulas to stir catalytic distillation device, mainly solves the problems, such as that gas-liquid-solid three-phase mixing is non-uniform between column plate in catalytic rectifying tower in the prior art.The present invention stirs catalytic distillation device by using a kind of Novel air dynamic formula, every layer of column plate individually uses the air lift-type agitator of side, agitating paddle is suspended at the top of column plate using the form that top is hung, every layer of column plate arrangement riser and downspout, riser air inlet is located at the opposite side of air driven pump installation side on every layer of column plate, and connect gas distributor on riser top, gas phase from descending trays is uniformly sprayed by gas distributor in the liquid-solid mixture on column plate, downspout top cloth strainer, prevent particle or particulate catalyst from falling into descending trays, descending liquid mouth lower part is located at column plate lower part, the technical solution stretched into below adjacent lower tower plate liquid level preferably solves the above problem, available in catalytic distillation.
Description
Technical field
The present invention relates to a kind of Novel air dynamic formulas to stir catalytic distillation device.
Technical background
With the rise and development of green chemical industry, chemical process reinforcement technique increasingly attracts attention.Will chemical reaction and
Rectifying separation carries out the integrated reaction rectification technique for forming polyfunctional reactant device, be realize approach that chemical process strengthens it
One.Catalytic distillation is the heterogeneous catalytic reaction distillation technology to grow up on the basis of homogeneous reaction rectifying, which will be solid
Body catalyst is placed in tower on each layer column plate of conversion zone, and gas and liquid distinguish counter-current flow up and down, chemical reaction
It detaches with rectifying and is coupled in tower inner height, can constantly remove reaction product, reaction heat also can be as the vaporization of distillation process
Heat.Compared to the continuous stirred tank reactor of series connection, catalytic rectifying tower have Low investment, low energy consumption, high conversion, it is highly selective,
The advantages that high productive capacity, in etherificate, alkylation, ether solution, ester hydrolysis, esterification, dimerization plus the chemical industry such as hydrogen, isomerization, dehydration
It is applied in the process.For gas-liquid-solid three-phase catalytic distillation existing for solid particle or particulate catalyst, gas between each column plate
The uniform mixing that liquid consolidates three-phase is difficult point, is adapted for continuously stirring and the design of safe and reliable catalytic rectifying tower very must
It will.
203540101 U of patent CN describe a kind of catalytic rectification column member, and riser, riser are equipped in the middle part of column plate
Outer fixed calotte, calotte middle and lower part are equipped with bronchus, and each bronchus is connected with ring pipe, and are equipped with substep hole, simple in structure, urge
Agent filling is easy, but the gas phase amount and flow velocity come by descending trays are limited, it is impossible to ensure bulk catalyst and gas-liquid two
Phase is uniformly mixed, and influences catalysis reaction and mass-transfer efficiency.
Patent CN101618304A describes a kind of esterifier, by connecting rotatable gas on riser top
Distributor, on each layer column plate can carry out gas-liquid-solid three-phase continuously stirs, but be limited to the power that gas flow rate is brought, solid
Grain catalyst does not ensure that stirring is abundant on every layer of column plate, is uniformly mixed.
1015175211 A of patent CN propose the high-purity isobutene of tert-butyl alcohol dehydration system using window diversion type structured packing
Catalytic distillation is carried out, method is simple, effect is good, but catalyst change is difficult, it is desirable that catalyst has a longer life expectancy.
105561911 A of patent CN propose catalyst in a kind of efficient catalytic rectifying column and tie up filler and its preparation side
Method, catalyst packet is interior to be fitted closely equipped with solid catalyst particle, the catalyst packet chain and regular corrugation filler piece after spiraling
It is fixed-type by lock ring piece.The catalyst packet hollow structure of the patented invention increases gas-liquid mass transfer space, can effectively facilitate anti-
The progress answered, but catalyst change is difficult, and generally requiring parking could replace, more demanding to catalyst life.
101219950 A of patent CN give a kind of ester exchange reaction using methyl acetate and n-butanol and prepare acetic acid
The system and method for N-butyl, the catalytic rectifying tower are made of stripping section, conversion zone, rectifying section, and wherein conversion zone is by liquid collecting
Plate, riser, catalyst packet, support plate and bottom plate are formed, easy to operate, methyl acetate high conversion rate, but catalyst packet is replaced
It is difficult.
Invention content
The technical problems to be solved by the invention are gas-liquid-solids three between column plate in catalytic rectifying tower in the prior art
Non-uniform problem is mixed, a kind of new Novel air dynamic formula stirring catalytic distillation device is provided.The device is used for catalytic distillation
In, have the advantages that gas-liquid-solid three-phase mixing is non-uniform between column plate in catalytic rectifying tower.
To solve the above problems, the technical solution adopted by the present invention is as follows：A kind of Novel air dynamic formula stirring catalytic distillation dress
Put, structure of reactor therein mainly include air lift-type agitator, blade, gas distributor, downspout, gear-box, riser,
Column plate, housing, shaft, column plate, strainer, catalyst make-up mouth, catalyst outlet, light component enter anti-from reactor descending trays
Device is answered, heavy constituent enters reactor from reactor upper strata column plate, places solid particle or particulate catalyst on every layer of column plate, come
Two layers of column plate space is mutually entered by downspout from the reaction solution of upper strata column plate, the reaction gas from descending trays mutually passes through a liter gas
Pipe enters two layers of column plate space, while the liquid uniformly sprayed on the column plate in the form of bubble by gas distributor mixes admittedly
In object, the air lift-type agitator filled on the inside of column plate twice is rotated by the zone of action turn axis and blade of gear-box, solid particle
Or particulate catalyst even suspension under the action of stirrer paddle is scattered in reaction liquid phase, downspout is set in column plate opening
Strainer is put, prevents upper strata column plate catalyst granules or particle from entering descending trays, while catalyst make-up mouth is set on tower body
And catalyst outlet 13, realize the online replacement of catalyst；Wherein, adjacent two pieces of column plate spacing be H, tower internal diameter be D, H ranges
For 300~700mm, gas distributor outer tube opening diameter ranging from 2~25mm, inner tube opening diameter ranging from 1~20mm are opened
It is equidistantly uniformly distributed between hole；The ratio between the draft tube diameter c and tower internal diameter D ranging from 0.05~0.25；In riser import
The heart and column plate centre distance ranging from 0.1~0.3D；The ratio between the descending liquid pipe diameter d and tower internal diameter D ranging from 0.08~0.25；
The downspout center line is away from column plate centre distance ranging from 0.20~0.45D；The downspout must stretch into tower tray liquid level hereinafter,
Downspout height h and adjacent two pieces of column plate spacing H ranging from 0.4~0.9.
In above-mentioned technical proposal, it is preferable that gas distributor is ring type gas distributor.
In above-mentioned technical proposal, it is highly preferred that gas distributor is dicyclic gas distributor.
In above-mentioned technical proposal, it is preferable that every layer of column plate arrangement riser and downspout, riser air inlet are located at every layer
The opposite side of air driven pump installation side on column plate, and gas distributor is connected on riser top, the gas phase from descending trays is led to
It crosses in the liquid-solid mixture that gas distributor is uniformly sprayed on column plate, descending liquid mouth lower part is located at column plate lower part, stretches into adjacent lower
Below tower plate liquid level.
In above-mentioned technical proposal, it is highly preferred that the ratio between the dicyclic gas distributor outer tube diameter a and tower internal diameter D are 0.3
~0.8, the ratio between interior caliber b and tower internal diameter D are 0.2~0.7, and dicyclic gas distributor center is overlapped with column plate center.
In above-mentioned technical proposal, it is preferable that adjacent two pieces of column plate spacing be H, tower internal diameter be D, H ranging from 400~
600mm；Gas distributor outer tube opening diameter ranging from 5~20mm, inner tube opening diameter ranging from 5~15mm, between trepanning
Equidistantly it is uniformly distributed；The ratio between the draft tube diameter c and tower internal diameter D ranging from 0.1~0.15；Riser import center and column plate
Centre distance ranging from 0.1~0.2D；The ratio between the descending liquid pipe diameter d and tower internal diameter D ranging from 0.1~0.15；The descending liquid
Tube hub line-spacing column plate centre distance ranging from 0.3~0.4D；The ratio between the downspout height h and adjacent two pieces of column plate spacing H
Ranging from 0.6~0.8.
In above-mentioned technical proposal, it is preferable that agitating paddle is suspended at the top of column plate using the form that top is hung.
The Novel air dynamic formula stirring catalytic distillation device of the present invention, is characterized in that every layer of column plate individually using the pneumatic of side
Agitating paddle is suspended at the top of column plate by formula blender using the form that top is hung.Every layer of column plate arrangement riser and downspout, rise gas
Pipe air inlet is located at the opposite side of air driven pump installation side on every layer of column plate, and connects gas distributor on riser top, comes from
The gas phase of descending trays is uniformly sprayed by gas distributor in the liquid-solid mixture on column plate.Downspout top cloth strainer is prevented
Only particle or particulate catalyst fall into descending trays, and descending liquid mouth lower part is located at column plate lower part, stretches into adjacent lower tower plate liquid level
Below.Solid particle or particulate catalyst are placed on every layer of column plate, since density of solid and liquid approach, solid catalyst
Suspended dispersed, so gas-liquid-solid three-phase stirring is abundant in reaction unit, is uniformly mixed, instead in liquid phase under the action of agitating paddle
Answer excellent in efficiency.Be designed with catalyst loading and unloading mouth on every layer of column plate of conversion zone, can under the conditions of not parking more catalyst changeout.The present invention
Have many advantages, such as can to continuously stir, gas-liquid-solid three-phase is uniformly mixed, structure is safe and reliable, easy access, achieve preferable skill
Art effect.
Description of the drawings
Fig. 1 is the structure diagram of device of the present invention.
In Fig. 1,1 air lift-type agitator, 2 blade, 3 gas distributor, 4 downspout, 5 gear-box, 6 riser, 7 column plate 8
12 catalyst make-up mouth of housing 9 shaft, 10 column plate, 11 strainer, 13 catalyst outlet.
For methyl acetate and n-butanol ester-interchange method butyl acetate reactive distillation processes occur for Fig. 2.
In Fig. 2,1 catalytic rectifying tower, 2 condenser, 3 return tank, 4 reboiler, 5 reflux pump.
The present invention will be further described below by way of examples, but is not limited only to the present embodiment.
Specific embodiment
【Embodiment 1】
A kind of Novel air dynamic formula stirs catalytic distillation device, as shown in Figure 1, reactor column harden structure mainly includes：Pneumatically
Formula blender 1, blade 2, gas distributor 3, downspout 4, gear-box 5, riser 6, column plate 7, housing 8, shaft 9, column plate 10,
Strainer 11, catalyst make-up mouth 12, catalyst outlet 13.
Light component enters reactor from reactor descending trays, and heavy constituent enters reactor from reactor upper strata column plate.Often
The reaction solution of a certain amount of solid particle or particulate catalyst from upper strata column plate 7 is placed mutually by downspout 4 on layer column plate
Into two layers of column plate space.Reaction gas from 10 adjacent lower column plate of column plate mutually enters two layers of column plate space by riser 6,
And pass through gas distributor 3 and uniformly sprayed into the liquid-solid mixture of column plate 10 in the form of bubble.The pneumatic type of 10 side of column plate dress
Blender 1 is rotated by the zone of action turn axis 9 and blade 2 of gear-box 5.Solid particle or particulate catalyst are in stirrer paddle
Even suspension is scattered in reaction liquid phase under the action of 2.Wherein described 3 preferred embodiment of gas distributor is distributed for ring type gas
Device, more preferable scheme are dicyclic gas distributor, are conducive to react the homodisperse of gas phase.Downspout 4 is in column plate opening
Strainer 11 is set, prevents upper strata column plate catalyst granules or particle from entering descending trays.Catalyst is set to mend on tower body simultaneously
Fill mouth 12 and catalyst outlet 13, can under the conditions of not parking more catalyst changeout.
By taking ester-interchange method butyl acetate reactive distillation processes occur for methyl acetate and n-butanol as an example,
Specific implementation process is as follows：As shown in Fig. 2, being equipped with 10 blocks of column plates in catalytic rectifying tower (1), filled on each layer column plate
It is filled with transesterification and dissipates heap granular pattern catalyst.N-butanol feeds (101) into the 2nd block of column plate of catalytic rectifying tower (1), methyl acetate
(102) are fed into the 10th block of column plate of catalytic rectifying tower (1).Methyl acetate and n-butanol counter current contacting, and react with dividing
From.Overhead vapours (103) main component is methyl acetate and methanol, is condensed into condenser (2), and lime set (105) enters
Return tank (3), return tank liquid phase discharging (106) to catalytic rectifying tower (1), are partly adopted by reflux pump (5) partial reflux (107)
Go out (110) into later separation workshop section, the methyl acetate after separation is recycled to catalytic rectifying tower (1) and carries out further transesterification
Reaction.Catalytic rectifying tower (1) tower reactor be equipped with reboiler provide heat source, tower reactor main component be n-butyl acetate and n-butanol, tower
Later separation and refinement are gone in kettle extraction (104), and to obtain n-butyl acetate product, while the n-butanol recycled is recycled to
Further ester exchange reaction occurs for catalytic rectifying tower (1).
Catalytic distillation device is stirred as methyl acetate and n-butanol transesterification catalysis essence using the Novel air dynamic formula of the present invention
Evaporate tower (1).
Adjacent two pieces of column plate spacing are H, and tower internal diameter is D, and H 450mm, D 200mm, the gas distributor is bicyclic
Formula gas distributor.The ratio between the dicyclic gas distributor outer tube diameter a and tower internal diameter D are 0.5, interior caliber b and tower internal diameter D it
Than being 0.4, dicyclic gas distributor center is overlapped with column plate center.Gas distributor outer tube opening diameter be 12mm, inner tube
Opening diameter is 8mm, is equidistantly uniformly distributed between trepanning.The ratio between the draft tube diameter c and tower internal diameter D be 0.1, riser into
Mouth center is 0.2D with column plate centre distance, and the ratio between the descending liquid pipe diameter d and tower internal diameter D are 0.12, the descending liquid tube hub
Line-spacing column plate centre distance is 0.4D, and the ratio between the downspout height h and adjacent two pieces of column plate spacing H are 0.7.
Tower top operation temperature is 75 DEG C, and tower top operating pressure is 0.12MPa (A).N-butanol feed (1) and methyl acetate into
Expect (2) molar ratio=2：1, mass flow is respectively：75kg/h, 38.3kg/h, reflux ratio carry out continuous experiment for 12, stablize
During operation, methyl acetate conversion per pass is up to 60%.
【Embodiment 2】
According to condition described in embodiment 1 and step, adjacent two pieces of column plate spacing are H, and tower internal diameter is D, H 300mm, D
For 200mm, the gas distributor is dicyclic gas distributor.The dicyclic gas distributor outer tube diameter a and tower internal diameter D
The ratio between for 0.3, the ratio between interior caliber b and tower internal diameter D are 0.2, and dicyclic gas distributor center is overlapped with column plate center.Gas point
Cloth device outer tube opening diameter is 2mm, and inner tube opening diameter is 1mm, is equidistantly uniformly distributed between trepanning.The draft tube diameter c
Be 0.05 with the ratio between tower internal diameter D, riser import center and column plate centre distance are 0.1D, the descending liquid pipe diameter d in tower
The ratio between diameter D be 0.08, the downspout center line away from column plate centre distance be 0.2D, the downspout height h with adjacent two pieces
The ratio between column plate spacing H is 0.4.
Tower top operation temperature is 75 DEG C, and tower top operating pressure is 0.12MPa (A).N-butanol feed (1) and methyl acetate into
Expect (2) molar ratio=2：1, mass flow is respectively：75kg/h, 38.3kg/h, reflux ratio carry out continuous experiment for 14, stablize
During operation, methyl acetate conversion per pass is up to 58.6%.
【Embodiment 3】
According to condition described in embodiment 1 and step, adjacent two pieces of column plate spacing are H, and tower internal diameter is D, H 400mm, D
For 200mm, the gas distributor is dicyclic gas distributor.The dicyclic gas distributor outer tube diameter a and tower internal diameter D
The ratio between for 0.5, the ratio between interior caliber b and tower internal diameter D are 0.4, and dicyclic gas distributor center is overlapped with column plate center.Gas point
Cloth device outer tube opening diameter is 10mm, and inner tube opening diameter is 8mm, is equidistantly uniformly distributed between trepanning.The draft tube diameter c
It is 0.1 with the ratio between tower internal diameter D, riser import center is 0.2D, the descending liquid pipe diameter d and tower internal diameter with column plate centre distance
The ratio between D is 0.25, and the downspout center line is 0.45D, the downspout height h and adjacent two pieces of towers away from column plate centre distance
The ratio between plate spacing H is 0.7.
Tower top operation temperature is 75 DEG C, and tower top operating pressure is 0.12MPa (A).N-butanol feed (1) and methyl acetate into
Expect (2) molar ratio=2：1, mass flow is respectively：75kg/h, 38.3kg/h, reflux ratio carry out continuous experiment for 12, stablize
During operation, methyl acetate conversion per pass is up to 59.5%.
【Embodiment 4】
According to condition described in embodiment 1 and step, adjacent two pieces of column plate spacing are H, and tower internal diameter is D, H 500mm, D
For 200mm, the gas distributor is dicyclic gas distributor.The dicyclic gas distributor outer tube diameter a and tower internal diameter D
The ratio between for 0.5, the ratio between interior caliber b and tower internal diameter D are 0.4, and dicyclic gas distributor center is overlapped with column plate center.Gas point
Cloth device outer tube opening diameter is 15mm, and inner tube opening diameter is 10mm, is equidistantly uniformly distributed between trepanning.The draft tube diameter
The ratio between c and tower internal diameter D are 0.15, and riser import center is 0.15D, the descending liquid pipe diameter d and tower with column plate centre distance
The ratio between internal diameter D be 0.1, the downspout center line away from column plate centre distance be 0.3D, the downspout height h with adjacent two pieces
The ratio between column plate spacing H is 0.7.
Tower top operation temperature is 75 DEG C, and tower top operating pressure is 0.12MPa (A).N-butanol feed (1) and methyl acetate into
Expect (2) molar ratio=2：1, mass flow is respectively：75kg/h, 38.3kg/h, reflux ratio carry out continuous experiment for 12, stablize
During operation, methyl acetate conversion per pass is up to 59.5%.
【Embodiment 5】
According to condition described in embodiment 1 and step, adjacent two pieces of column plate spacing are H, and tower internal diameter is D, H 600mm, D
For 200mm, the gas distributor is dicyclic gas distributor.The dicyclic gas distributor outer tube diameter a and tower internal diameter D
The ratio between for 0.7, the ratio between interior caliber b and tower internal diameter D are 0.6, and dicyclic gas distributor center is overlapped with column plate center.Gas point
Cloth device outer tube opening diameter is 15mm, and inner tube opening diameter is 10mm, is equidistantly uniformly distributed between trepanning.The draft tube diameter
The ratio between c and tower internal diameter D are 0.2, and riser import center and column plate centre distance are 0.3D, the descending liquid pipe diameter d in tower
The ratio between diameter D is 0.1, and the downspout center line is 0.4D, the downspout height h and adjacent two pieces of towers away from column plate centre distance
The ratio between plate spacing H is 0.9.
Tower top operation temperature is 75 DEG C, and tower top operating pressure is 0.12MPa (A).N-butanol feed (1) and methyl acetate into
Expect (2) molar ratio=2：1, mass flow is respectively：75kg/h, 38.3kg/h, reflux ratio carry out continuous experiment for 12, stablize
During operation, methyl acetate conversion per pass is up to 61.0%.
【Embodiment 6】
According to condition described in embodiment 1 and step, adjacent two pieces of column plate spacing are H, and tower internal diameter is D, H 700mm, D
For 200mm, the gas distributor is dicyclic gas distributor.The dicyclic gas distributor outer tube diameter a and tower internal diameter D
The ratio between for 0.8, the ratio between interior caliber b and tower internal diameter D are 0.7, and dicyclic gas distributor center is overlapped with column plate center.Gas point
Cloth device outer tube opening diameter is 25mm, and inner tube opening diameter is 20mm, is equidistantly uniformly distributed between trepanning.The draft tube diameter
The ratio between c and tower internal diameter D are 0.25, and riser import center and column plate centre distance are 0.2D, the descending liquid pipe diameter d in tower
The ratio between diameter D be 0.1, the downspout center line away from column plate centre distance be 0.45D, the downspout height h with adjacent two pieces
The ratio between column plate spacing H is 0.9.
Tower top operation temperature is 75 DEG C, and tower top operating pressure is 0.12MPa (A).N-butanol feed (1) and methyl acetate into
Expect (2) molar ratio=2：1, mass flow is respectively：75kg/h, 38.3kg/h, reflux ratio carry out continuous experiment for 12, stablize
During operation, methyl acetate conversion per pass is up to 59.0%.
Comparative example
Methyl acetate and n-butanol enter at the top and bottom of catalytic reaction zone respectively in patent CN101219950A
In catalytic rectifying tower, the two molar ratio be 1, reaction temperature be 60 DEG C, with reflux ratio 15 it is stable after, methyl acetate conversion ratio
It is 58.4%.Catalytic rectifying tower catalyst is positioned in the form of catalyst packet in reaction liquid phase, difficulty is replaced, to the catalyst longevity
Life requirement is high, and attainable methyl acetate conversion per pass is less than the embodiment of invention.
Obviously, device using the present invention, every layer of column plate individually use the air lift-type agitator of side, the shape hung using top
Agitating paddle is suspended at the top of column plate by formula.Every layer of column plate arrangement riser and downspout, riser air inlet are located at every layer of column plate
The opposite side of upper air driven pump installation side, and gas distributor is connected on riser top, the gas phase from descending trays passes through gas
Body distributor is uniformly sprayed into the liquid-solid mixture on column plate.Downspout top cloth strainer, prevents particle or particulate catalyst
Descending trays are fallen into, descending liquid mouth lower part is located at column plate lower part, stretches into below adjacent lower tower plate liquid level.Solid particle or particle type
Catalyst is placed on every layer of column plate, and since density of solid and liquid approach, solid catalyst suspends under the action of agitating paddle
It is scattered in liquid phase, so gas-liquid-solid three-phase stirring is abundant in reaction unit, is uniformly mixed, reaction efficiency is good.Every layer of conversion zone
Catalyst loading and unloading mouth is designed on column plate, can under the conditions of not parking more catalyst changeout.The present invention have can continuously stir, gas-liquid
The advantages that Gu three-phase is uniformly mixed, structure is safe and reliable, easy access, achieves preferable technique effect.
Claims (7)
1. a kind of Novel air dynamic formula stirs catalytic distillation device, structure of reactor therein mainly includes air lift-type agitator, paddle
Leaf, gas distributor, downspout, gear-box, riser, column plate, housing, shaft, column plate, strainer, catalyst make-up mouth, catalysis
Agent exports, and light component enters reactor from reactor descending trays, and heavy constituent enters reactor from reactor upper strata column plate, every layer
Solid particle or particulate catalyst are placed on column plate, the reaction solution from upper strata column plate mutually enters two layers of column plate by downspout
Space, the reaction gas from descending trays mutually enter two layers of column plate space, while by gas distributor with gas by riser
The form of bubble is uniformly sprayed into the liquid-solid mixture on the column plate, and the air lift-type agitator filled on the inside of column plate twice passes through gear
Zone of action turn axis and the blade rotation of case, solid particle or the particulate catalyst even suspension point under the action of stirrer paddle
It dissipates in reacting in liquid phase, downspout sets strainer in column plate opening, prevents under upper strata column plate catalyst granules or particle entrance
Layer column plate, while catalyst make-up mouth and catalyst outlet 13 are set on tower body, realize the online replacement of catalyst；Wherein,
Adjacent two pieces of column plate spacing be H, tower internal diameter be D, H ranging from 300~700mm, gas distributor outer tube opening diameter ranging from 2
~25mm, inner tube opening diameter ranging from 1~20mm, is equidistantly uniformly distributed between trepanning；The draft tube diameter c and tower internal diameter
The ratio between D ranging from 0.05~0.25；Riser import center and column plate centre distance ranging from 0.1~0.3D；The downspout
The ratio between diameter d and tower internal diameter D ranging from 0.08~0.25；The downspout center line away from column plate centre distance ranging from 0.20~
0.45D；The downspout must stretch into tower tray liquid level hereinafter, the ratio between downspout height h and adjacent two pieces of column plate spacing H ranging from
0.4~0.9.
2. Novel air dynamic formula stirring catalytic distillation device according to claim 1, it is characterised in that gas distributor is ring type
Gas distributor.
3. Novel air dynamic formula stirring catalytic distillation device according to claim 2, it is characterised in that gas distributor is bicyclic
Formula gas distributor.
4. Novel air dynamic formula stirring catalytic distillation device according to claim 1, it is characterised in that every layer of column plate arrangement rises gas
Pipe and downspout, riser air inlet is located at the opposite side of air driven pump installation side on every layer of column plate, and is connected on riser top
Gas distributor, the gas phase from descending trays are uniformly sprayed by gas distributor in the liquid-solid mixture on column plate, descending liquid
Mouth lower part is located at column plate lower part, stretches into below adjacent lower tower plate liquid level.
5. Novel air dynamic formula stirring catalytic distillation device according to claim 3, it is characterised in that the dicyclic gas point
The ratio between cloth device outer tube diameter a and tower internal diameter D are 0.3~0.8, and the ratio between interior caliber b and tower internal diameter D are 0.2~0.7, dicyclic gas
Distributor center is overlapped with column plate center.
6. Novel air dynamic formula stirring catalytic distillation device according to claim 1, it is characterised in that adjacent two pieces of column plate spacing
For H, tower internal diameter is D, H ranging from 400~600mm；Gas distributor outer tube opening diameter ranging from 5~20mm, inner tube trepanning
Diameter range is 5~15mm, is equidistantly uniformly distributed between trepanning；The ratio between the draft tube diameter c and tower internal diameter D ranging from 0.1
~0.15；Riser import center and column plate centre distance ranging from 0.1~0.2D；The descending liquid pipe diameter d and tower internal diameter D it
Than ranging from 0.1~0.15；The downspout center line is away from column plate centre distance ranging from 0.3~0.4D；The downspout is high
Spend the ratio between h and adjacent two pieces of column plate spacing H ranging from 0.6~0.8.
7. Novel air dynamic formula stirring catalytic distillation device according to claim 1, it is characterised in that will in the form of top is hung
Agitating paddle is suspended at the top of column plate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810009113.6A CN108261792B (en) | 2018-01-04 | 2018-01-04 | Novel pneumatic stirring catalytic rectification device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109651081A (en) * | 2019-01-14 | 2019-04-19 | 河北科技大学 | A kind of reactive distillation method and device thereof of preparing cyclohexanol by cyclohexene hydration reaction |
| CN116020153A (en) * | 2023-02-20 | 2023-04-28 | 安徽瑞柏新材料有限公司 | Rectifying device with heat recycling function for methyl acetate production |
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| CN1075662A (en) * | 1993-02-17 | 1993-09-01 | 中国石油化工总公司 | Multistage suspension reaction fractionating tower |
| CN203540101U (en) * | 2013-10-23 | 2014-04-16 | 中国石油化工股份有限公司 | Catalytic rectifying tower component |
| CN203890273U (en) * | 2014-06-23 | 2014-10-22 | 杭州百事特实业有限公司 | Pilot test reaction device suitable for preparing higher methyl acrylate |
| CN104971667A (en) * | 2014-04-01 | 2015-10-14 | 清华大学 | Fluidized bed equipment and method for preparing poly-methoxy-dimethyl ether from dimethoxymethane and paraformaldehyde |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1075662A (en) * | 1993-02-17 | 1993-09-01 | 中国石油化工总公司 | Multistage suspension reaction fractionating tower |
| CN203540101U (en) * | 2013-10-23 | 2014-04-16 | 中国石油化工股份有限公司 | Catalytic rectifying tower component |
| CN104971667A (en) * | 2014-04-01 | 2015-10-14 | 清华大学 | Fluidized bed equipment and method for preparing poly-methoxy-dimethyl ether from dimethoxymethane and paraformaldehyde |
| CN203890273U (en) * | 2014-06-23 | 2014-10-22 | 杭州百事特实业有限公司 | Pilot test reaction device suitable for preparing higher methyl acrylate |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109651081A (en) * | 2019-01-14 | 2019-04-19 | 河北科技大学 | A kind of reactive distillation method and device thereof of preparing cyclohexanol by cyclohexene hydration reaction |
| CN116020153A (en) * | 2023-02-20 | 2023-04-28 | 安徽瑞柏新材料有限公司 | Rectifying device with heat recycling function for methyl acetate production |
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| CN108261792B (en) | 2020-08-11 |
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