CN108261988A - A kind of gas distributor and the system comprising the gas distributor - Google Patents
A kind of gas distributor and the system comprising the gas distributor Download PDFInfo
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- CN108261988A CN108261988A CN201810293832.5A CN201810293832A CN108261988A CN 108261988 A CN108261988 A CN 108261988A CN 201810293832 A CN201810293832 A CN 201810293832A CN 108261988 A CN108261988 A CN 108261988A
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- gas distribution
- gas
- air inlet
- distribution tube
- bubble tower
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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
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1818—Feeding of the fluidising gas
- B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
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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
- B01J10/00—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor
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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
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1872—Details of the fluidised bed reactor
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- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
A kind of system the present invention relates to gas distributor and comprising the distributor.Gas distributor of the present invention includes cricoid gas distribution tube, gas distribution box in the ring of the cricoid gas distribution tube and the air inlet pipe being connect respectively with gas distribution tube and gas distribution box；The air inlet pipe is connect by least two air inlet branch roads separated with gas distribution tube and gas distribution box respectively, so as to fulfill the fixation and air inlet of gas distribution tube and gas distribution box；The surface of the gas distribution tube and gas distribution box is respectively provided with stomata.The gas distributor of the present invention is simple in structure, stable operation, and uniformly distributed performance is good.
Description
Technical field
A kind of system the present invention relates to gas distributor and comprising the gas distributor more particularly to a kind of distribution of gas
Device, the bubble tower comprising the gas distributor and system.
Background technology
Often it is related to the reaction that gas or liquid participate in the production technology of chemical field, this just needs that gas-liquid can be carried out
Two-phase or the mixing component of gas-liquid-solid three-phase mixing.Gas distributor is a kind of widely used component, is especially widely used in
In the device of heterogeneous fluidization reaction.
The gas distributor industrially used at present mainly has two type of panel-type air distributor and tubular gas distributor
For reactant is allowed to be uniformly distributed, accelerate reaction efficiency and shortens reaction time, how preferably one of type, main function is
Pressure drop and flow velocity is controlled to reach the emphasis that more preferably gas distribution is still research.
105944630 A of CN disclose a kind of gas distributor, including at least one gas distributing disc, the gas point
Cloth disk is the tray type structure assembled by several corrugated plates, and the wave rib of the corrugated plate is not set vertically, adjacent two
The inclined direction of the wave rib of a corrugated plate is opposite.The gas distributor is with Air Bubble Size is uniform, is evenly distributed and is distributed
The advantages of area is big can also promote the parameters such as composition, temperature, the flow velocity of fluid radially to reach unanimity in mass transfer apparatus, subtract
Few back-mixing.But bubble can be caused excessively intensive, bubble is easy to aggregation in uphill process and becomes larger, so as to influence mass transfer effect
Fruit.
105268396 A of CN disclose a kind of gas distributor, including air inlet, strip channel, circular passage, filtering
Net, distribution hole.The air inlet is located at gas distributor central position, is cylindrical structure, is connected with bar shaped distribution channel
Logical, the bar shaped distribution channel is horizontal column structure, and one end connects the other end with air inlet and connected with annular spread channel, institute
The annular spread channel stated is circular ring type structure, and even section is connected respectively at bar shaped distribution channel, and the filter screen is located at bar shaped
The bottom end of distribution channel and annular spread channel, circular distribution hole aperture are 6-10mm.The gas distributor can prevent gas
There is the situation in dead zone in concentration of local, greatly improves the working efficiency of gas distributor.But this distributor bubble point
Cloth excessively disperses, and causes entire tower inside gas holdup relatively low, is only suitable for the reaction of less demanding to gas holdup, has one
Fixed limitation.
Invention content
For the above-mentioned problems in the prior art, the purpose of the present invention is to provide a kind of gas distributor and comprising
The system of the gas distributor.
In order to achieve the above object, the present invention uses following technical scheme：
In a first aspect, the present invention provides a kind of gas distributor, the gas distributor includes cricoid gas distribution tube,
It gas distribution box in the ring of the cricoid gas distribution tube and is distributed respectively at the gas distribution tube and gas
The air inlet pipe of box connection；
The air inlet pipe is connected by least two air inlet branch roads separated with gas distribution tube and gas distribution box respectively
It connects, so as to fulfill the fixation and air inlet of gas distribution tube and gas distribution box；
The surface of the gas distribution tube and gas distribution box is respectively provided with stomata.
As the optimal technical scheme of gas distributor of the present invention, the air inlet pipe is divided into 2N+1 air inlet branch road, N
For >=1 integer, wherein, 1 air inlet branch road is connect with gas distribution box, and remaining 2N air inlet branch road connects in pairs
To the diametrically side of gas distribution tube.
The N is >=1 integer, such as 1,2,3,4,5,6,7,8 or 10 etc..
It is highly preferred that the air inlet pipe is divided into 2N+1 air inlet branch road, N is >=2 integer, wherein, 1 air inlet branch road with
The center connection of gas distribution box, remaining 2N air inlet branch road are connected to gas distribution tube diametrically in pairs
Side, and the connector of this 2N air inlet branch road and gas distribution tube is uniformly distributed on gas distribution tube.
Preferably, the air inlet pipe is parallel with the plane where gas distribution tube and gas distribution box, and air inlet branch road is equal
It is vertical with air inlet pipe.
In the present invention, air inlet pipe and air inlet branch road are interconnected, the material and wall thickness of air inlet pipe and air inlet branch road
Control needs to ensure not only to play the role of air inlet, but also play gas distributor support fixed function with enough intensity.
As the optimal technical scheme of gas distributor of the present invention, the pipe thickness of the gas distribution tube exists
0.5cm~1cm, such as 0.5cm, 0.6cm, 0.7cm, 0.8cm, 0.9cm or 1cm.
Preferably, 1/3~1/4 of the outer annular diameter of gas distribution tube (11) described in the caliber of the gas distribution tube, example
Such as 1/3,2/7 or 1/4.
Preferably, the wall thickness of the gas distribution box is in 0.5cm~1cm, for example, 0.5cm, 0.6cm, 0.7cm, 0.8cm,
0.9cm or 1cm etc..
Preferably, the horizontal cross-section of the gas distribution box is the caliber of circle, box body vertical height and gas distribution tube
It is equal.
Preferably, the 1/2 of the outer annular diameter of a diameter of gas distribution tube in the horizontal cross-section of the gas distribution box~
1/3, such as 1/2,2/5 or 1/3 etc..
Preferably, the pipe thickness of the air inlet pipe is in 1cm~2cm, such as 1cm, 1.3cm, 1.6cm, 1.8cm or 2cm
Deng.
Preferably, the caliber of the air inlet pipe is the 1/3~1/4 of the outer annular diameter of the gas distribution tube (11), such as
1/3rd, 2/7,3/10 or 1/4 etc..
As the optimal technical scheme of gas distributor of the present invention, the surface percent opening of the gas distribution tube is
50%~80%, such as 50%, 55%, 60%, 65%, 70% or 80% etc..
Preferably, the surface percent opening of the gas distribution box be 50%~80%, such as 50%, 60%, 65%,
70%th, 75% or 80% etc..
Preferably, the air vent aperture cause not of uniform size on the gas distribution tube surface.
It is highly preferred that on the gas distribution tube, close to the gas distribution tube and the stomata at air inlet branch road connector
Aperture it is small, far from the gas distribution tube and the stomata at air inlet branch road connector aperture it is big.According to this preferred embodiment
Pore-size distribution rule carries out the design in hole, can reduce resistance to mass tranfer with equilibrium pressure drop, is conducive to raising distributor and is evenly distributed with performance.
Preferably, the air vent aperture cause not of uniform size on the gas distribution box surface.
It is highly preferred that in the gas distribution box, close to the gas distribution box and the stomata at air inlet branch road connector
Aperture it is small, far from the gas distribution box and the aperture of the stomata at air inlet branch road connector it is big.According to this preferred embodiment
Pore-size distribution rule carries out the design in hole, can reduce resistance to mass tranfer with equilibrium pressure drop.
Second aspect, the present invention provide a kind of reactor, and the reactor includes the gas distributor described in first aspect.
Reactor of the present invention can be bubble tower, fluid bed, gasification furnace or fluidized bed furnace etc., preferably bubble tower.
It is highly preferred that the present invention provides a kind of bubble tower, the bubble tower includes the gas distributor described in first aspect,
For the air inlet of the bubble tower in tower side, the air inlet is used to penetrate the air inlet pipe of the gas distributor, the gas point
Plane where cloth device and gas distribution box is parallel with horizontal plane.
The third aspect, the present invention provide a kind of system, and the system is comprising the bubble tower described in second aspect as first
Bubble tower, the system comprises：First bubble tower, the second bubble tower and heat exchanger, the top of first bubble tower are equipped with original
Material and catalyst inlet and the first circulation entrance connected with heat exchanger top exit, the lower part of first bubble tower is equipped with
The second circulation entrance connected with the second bubble tower top exit, the bottom of first bubble tower be equipped with under the second bubble tower
The product exit of portion's connection.
The bottom of second bubble tower is equipped with gas access, and the top of second bubble tower is exported equipped with overflow, institute
Overflow outlet is stated to connect with the bottom of the heat exchanger.
The bubble tower of the present invention carries out gas distribution using the gas distributor described in first aspect, is led to by constant flow
Gas can realize quiet bubbling state, and back-mixing, effectively the realization reverse concentration difference of bed raw material, effectively promotion reaction be not former for liquid phase
The conversion ratio of material.
The system of the present invention can effectively control the first bubble tower bed temperature by the control of heat exchanger exit temperature of charge
Degree, significant effect.
The system of the present invention can be used for preparing carbonic ester etc. with gas or liquid charging stock, and system operatio elasticity is big, can be
Stable operation is carried out in wider range, it is easily controllable, and also production efficiency is high, and by-product is few.
In system of the present invention, shown overflow outlet is not limited only to connect with the bottom of heat exchanger, can also draw another
Outer pipeline is connect with other storage devices or after-treatment device.
In the system of the present invention, the first bubble tower is main reaction tower, such as esterification can occur.
As the optimal technical scheme of system of the present invention, the system also includes divide with the gas-liquid of overflow outlet
From device, gas vent and liquid outlet are respectively equipped at the top and bottom of the gas-liquid separator.
Preferably, the system also includes the vacuum rectifying tower that the liquid outlet with gas-liquid separator connects, the vacuum
Raw materials recovery outlet and catalyst recycling outlet are respectively equipped at the top and bottom of rectifying column.
Preferably, inside second bubble tower demister is equipped with close to apical position.
Preferably, refer to gas velocity in quiet bubbling state, the peace and quiet bubbling state in first bubble tower and be less than
0.05m/s。
Preferably, refer to gas velocity in turbulent flow bubbling state, the turbulent flow bubbling state in second bubble tower and be higher than
0.08m/s。
In turbulent flow bubbling state in second bubble tower of the present invention, under this condition, vapor-liquid backmixing effect is good, Ke Yichong
Point utilize gas raw material (such as CO2) to (ratio of the complete raw material of unreacted in liquid product (such as ethylene carbonate) mixture
Such as EO) into line replacement, pass through gas raw material (such as CO2Gas phase) by the remaining complete raw material of unreacted (such as EO) again band
Enter the first bubble tower to be reacted, realize the cycle of the remaining complete raw material of unreacted (such as EO), be conducive to shorten material
Residence time, reduce size and the investment of equipment.
Compared with the prior art, the present invention has the advantages that：
(1) gas distributor of the invention includes gas distribution tube, gas distribution box, air inlet pipe, stomata, has annular point
Both different channels of cloth channel and discoidal gas distribution box, two channels are independent mutually and and realized by air inlet pipe solid
It is fixed；Meanwhile the aperture of the stomata at gas distribution tube, box and air inlet branch road connector is small, the separate gas distribution tube,
The aperture of box and the stomata at air inlet branch road connector is big.This structure of distributor is simple, stable operation, and uniformly distributed performance is good, gas
It is evenly distributed, gas holdup is high, applied widely.
(2) it is ventilated in the first bubble tower of system of the invention comprising gas distributor of the present invention by constant flow,
It can realize quiet bubbling state, back-mixing, effective realization reverse concentration difference of bed raw material do not promote reaction raw materials effectively to liquid phase
Conversion ratio.
(3) system of the invention can be used for preparing carbonic ester etc. with gas or liquid charging stock, and system operatio elasticity is big, can
Stable operation is carried out in a wider scope, it is easily controllable, and also production efficiency is high, and by-product is few.
Description of the drawings
Fig. 1 a are the structure schematic diagram (bottom view) of gas distributor described in embodiment 1, wherein, 11：Gas distribution tube；
12：Gas distribution box；13：Air inlet pipe；14：Stomata；
Fig. 1 b are the structure schematic diagram (bottom view) of gas distributor described in embodiment 1, wherein, 11：Gas is distributed
Pipe；13：Air inlet pipe；131：Air inlet branch road；14：Stomata；
Fig. 2 is the structure schematic diagram of system described in embodiment 5, wherein, 101：First bubble tower；102：Second bubbling
Tower；201：Heat exchanger；301：Gas-liquid separator (normal pressure)；103：Vacuum rectifying tower；1：Raw material and catalyst inlet；2：First follows
Ring entrance；3：Second circulation entrance；4：Product exit；5：Gas access；6：Overflow exports；7：Gas vent；8：Liquid outlet；
9：Raw materials recovery exports；10：Catalyst recycling outlet.
Specific embodiment
Technical solution to further illustrate the present invention below with reference to the accompanying drawings and specific embodiments.
Embodiment 1
The present embodiment provides a kind of gas distributor (its structure schematic diagram is referring to Fig. 1 a and Fig. 1 b), the gas distribution
Device includes cricoid gas distribution tube 11, gas distribution box 12 in the ring of the cricoid gas distribution tube 11 and
The air inlet pipe 13 being connect respectively with gas distribution tube 11 and gas distribution box 12；
The air inlet pipe 13 by three air inlet branch roads 131 separating respectively with gas distribution tube 11 and gas distribution box 12
Connection, so as to fulfill the fixation and air inlet of gas distribution tube 11 and gas distribution box 12；
In three air inlet branch roads 131, an air inlet branch road 131 is connect with gas distribution box 12, remaining two air inlet branch
Road 131 is attached in pairs to the diametrically side of the gas distribution tube of annular；Air inlet pipe 13 and cricoid gas distribution tube 11 and
Plane where gas distribution box 12 is parallel, and air inlet branch road 131 is vertical with air inlet pipe 13；
The surface of the gas distribution tube 11 and gas distribution box 12 is respectively provided with stomata 14.
In the present embodiment, air inlet pipe 13 and air inlet branch road 131 are by overstriking, and tube wall is sufficiently thick, and material is also enough
It is solid, make support fixed function for gas distributor.
Embodiment 2
In addition to the following contents, other content is same as Example 1：
The air inlet pipe 13 by five air inlet branch roads 131 separating respectively with gas distribution tube 11 and gas distribution box 12
Connection, so as to fulfill the fixation and air inlet of gas distribution tube 11 and gas distribution box 12；
In five air inlet branch roads 131, an air inlet branch road 131 is connect with gas distribution box 12, remaining four air inlet branch
Road 131 is attached in pairs to the diametrically side of the gas distribution tube of annular, and this four air inlet branch roads 131 and gas distribution tube
11 connector is uniformly distributed on gas distribution tube；Air inlet pipe 13 and 12 institute of cricoid gas distribution tube 11 and gas distribution box
Plane it is parallel, and air inlet branch road 131 is vertical with air inlet pipe 13.
Embodiment 3
In addition to the following contents, other content is same as Example 1：
On the gas distribution tube 11, close to the gas distribution tube 11 and the stomata 14 at 131 connector of air inlet branch road
Aperture it is small, far from the gas distribution tube 11 and the stomata 14 at 131 connector of air inlet branch road aperture it is big；
Preferably, in the gas distribution box 12, at the gas distribution box 12 and 131 connector of air inlet branch road
The aperture of stomata 14 is small, big far from the gas distribution box 12 and 14 aperture of stomata at 131 connector of air inlet branch road.
Embodiment 4
The present embodiment provides a kind of bubble tower, the bubble tower includes gas distributor described in embodiment 1, the bubbling
For the air inlet of tower in tower side, the air inlet is used to penetrate the air inlet pipe 13 of the gas distributor, the gas distribution tube and
Plane where gas distribution box 12 is parallel with horizontal plane.
Comprising gas distributor described in embodiment 1 in the bubble tower of the present embodiment, quiet bubbling state, liquid can be realized
Mutually not back-mixing effectively realizes the reverse concentration difference of bed raw material, effectively promotes the conversion ratio of reaction raw materials.
Embodiment 5
The present embodiment provides a kind of system (its structure schematic diagram is referring to Fig. 2), the system is included described in embodiment 4
Bubble tower as the first bubble tower, the system comprises：First bubble tower 101, the second bubble tower 102 and heat exchanger 201, it is described
The top of first bubble tower 101 is equipped with raw material and catalyst inlet 1 and the first circulation connected with 201 top exit of heat exchanger
Entrance 2, the lower part of first bubble tower 101 are equipped with the second circulation entrance 3 connected with 102 top exit of the second bubble tower,
The bottom of first bubble tower 101 is equipped with the product exit 4 connected with 102 lower part of the second bubble tower；
The bottom of second bubble tower 102 is equipped with gas access 5, and the top of second bubble tower 102 is equipped with overflow
Outlet 6, the overflow outlet 6 are connected with the bottom of the heat exchanger 201；
The system also includes with 6 gas-liquid separators 301 that connects of overflow outlet, 301 top of gas-liquid separator with
Bottom is respectively equipped with gas vent 7 and liquid outlet 8；
The system also includes the vacuum rectifying tower 301 that the liquid outlet 8 with gas-liquid separator 301 connects, the vacuum
The top and bottom of rectifying column 103 are respectively equipped with raw materials recovery outlet 9 and catalyst recycling outlet 10；
Second bubble tower, 102 inside is equipped with demister close to apical position.
The system of the present embodiment can be used for preparing carbonic ester etc. with gas or liquid charging stock, and system operatio elasticity is big, can
Stable operation is carried out in a wider scope, it is easily controllable, and also production efficiency is high, and by-product is few.
Applicant states that the present invention illustrates the method detailed of the present invention, but not office of the invention by above-described embodiment
It is limited to above-mentioned method detailed, that is, does not mean that the present invention has to rely on above-mentioned method detailed and could implement.Technical field
Technical staff it will be clearly understood that any improvement in the present invention, equivalence replacement and auxiliary element to each raw material of product of the present invention
Addition, selection of concrete mode etc., all fall within protection scope of the present invention and the open scope.
Claims (10)
1. a kind of gas distributor, which is characterized in that the gas distributor includes cricoid gas distribution tube (11), positioned at institute
It states the gas distribution box (12) in the ring of cricoid gas distribution tube (11) and divides respectively with gas distribution tube (11) and gas
The air inlet pipe (13) of cloth box (12) connection；
The air inlet pipe (13) is divided by least two air inlet branch roads (131) separated with gas distribution tube (11) and gas respectively
Cloth box (12) connects, so as to fulfill the fixation and air inlet of gas distribution tube (11) and gas distribution box (12)；
The surface of the gas distribution tube (11) and gas distribution box (12) is respectively provided with stomata (14).
2. gas distributor according to claim 1, which is characterized in that the air inlet pipe (13) is divided into 2N+1 air inlet branch
Road (131), N are >=1 integer, wherein, 1 air inlet branch road (131) connect with gas distribution box (12), remaining 2N air inlet
Branch (131) is connected to the diametrically side of gas distribution tube (11) in pairs；
Preferably, the air inlet pipe (13) is divided into 2N+1 air inlet branch road (131), and N is >=2 integer, wherein, 1 air inlet branch
Road (131) is connect with the center of gas distribution box (12), and remaining 2N air inlet branch road (131) is connected to gas in pairs
The diametrically side of distributor pipe (11), and this 2N air inlet branch road (131) and the connector of gas distribution tube (11) divide in gas
Stringing is uniformly distributed on (11).
3. gas distributor according to claim 1 or 2, which is characterized in that the air inlet pipe (13) and gas distribution tube
(11) it is parallel with the plane where gas distribution box (12), and air inlet branch road (131) is vertical with air inlet pipe (13)；
Preferably, the pipe thickness of the gas distribution tube (11) is in 0.5cm~1cm；
Preferably, the caliber of the gas distribution tube (11) is the 1/3~1/4 of the outer annular diameter of the gas distribution tube (11)；
Preferably, the wall thickness of the gas distribution box (12) is in 0.5cm~1cm；
Preferably, the horizontal cross-section of the gas distribution box (12) is circle, box body vertical height and the gas distribution tube
(11) caliber is equal；
Preferably, the 1/2 of the outer annular diameter of a diameter of gas distribution tube (11) in the horizontal cross-section of the gas distribution box~
1/3；
Preferably, the pipe thickness of the air inlet pipe (13) is in 1cm~2cm；
Preferably, the caliber of the air inlet pipe (13) is the 1/3~1/4 of the outer annular diameter of the gas distribution tube (11).
4. according to claim 1-3 any one of them gas distributors, which is characterized in that the table of the gas distribution tube (11)
Face percent opening is 50%~80%；
Preferably, the surface percent opening of the gas distribution box (12) is 50%~80%.
5. according to claim 1-4 any one of them gas distributors, which is characterized in that gas distribution tube (11) surface
Stomata (14) pore size it is inconsistent；
Preferably, on the gas distribution tube (11), at the gas distribution tube (11) and air inlet branch road (131) connector
Stomata (14) aperture it is small, far from the stomata (14) at the gas distribution tube (11) and air inlet branch road (131) connector
Aperture is big；
Preferably, the air vent aperture cause not of uniform size on gas distribution box (12) surface；
Preferably, on the gas distribution box (12), at the gas distribution box (12) and air inlet branch road (131) connector
Stomata (14) aperture it is small, far from stomata (14) hole at the gas distribution box (12) and air inlet branch road (131) connector
Diameter is big.
6. a kind of reactor, which is characterized in that the reactor includes claim 1-5 any one of them gas distributors；
Preferably, the reactor includes any one in bubble tower, fluid bed, gasification furnace or fluidized bed furnace, preferably bubbling
Tower；
Preferably, the bubble tower includes claim 1-5 any one of them gas distributors, the air inlet of the bubble tower
In tower side, the air inlet is used to penetrate the air inlet pipe (13) of the gas distributor, the gas distribution tube and gas distribution
Plane where box (12) is parallel with horizontal plane.
7. a kind of system, which is characterized in that the system is comprising the bubble tower described in claim 6 as the first bubble tower, institute
The system of stating includes：First bubble tower (101), the second bubble tower (102) and heat exchanger (201), first bubble tower (101)
Top is equipped with raw material and catalyst inlet (1) and the first circulation entrance (2) connected with heat exchanger (201) top exit, institute
The lower part for stating the first bubble tower (101) is equipped with the second circulation entrance (3) connected with the second bubble tower (102) top exit, institute
The bottom for stating the first bubble tower (101) is equipped with the product exit (4) connected with the second bubble tower (102) lower part；
The bottom of second bubble tower (102) is equipped with gas access (5), and the top of second bubble tower (102), which is equipped with, overflows
Outflux (6), the overflow outlet (6) connect with the bottom of the heat exchanger (201).
8. system according to claim 7, which is characterized in that the system also includes the gas for (6) are exported with overflow connecting
Liquid/gas separator (301), gas-liquid separator (301) top and bottom are respectively equipped with gas vent (7) and liquid outlet (8).
9. system according to claim 7 or 8, which is characterized in that the system also includes with gas-liquid separator (301)
The vacuum rectifying tower (103) of liquid outlet (8) connection, is respectively equipped with raw material at the top and bottom of the vacuum rectifying tower (103)
Recycling outlet (9) and catalyst recycling outlet (10).
10. according to claim 7-9 any one of them systems, which is characterized in that second bubble tower (102) is internal close
Apical position is equipped with demister；
Preferably, in quiet bubbling state in first bubble tower (101)；
Preferably, it is in turbulent flow bubbling state in second bubble tower (102).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810293832.5A CN108261988B (en) | 2018-03-30 | 2018-03-30 | Gas distributor and system comprising same |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810293832.5A CN108261988B (en) | 2018-03-30 | 2018-03-30 | Gas distributor and system comprising same |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108261988A true CN108261988A (en) | 2018-07-10 |
| CN108261988B CN108261988B (en) | 2021-06-04 |
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ID=62778236
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|---|---|---|---|
| CN201810293832.5A Active CN108261988B (en) | 2018-03-30 | 2018-03-30 | Gas distributor and system comprising same |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5781693A (en) * | 1996-07-24 | 1998-07-14 | Applied Materials, Inc. | Gas introduction showerhead for an RTP chamber with upper and lower transparent plates and gas flow therebetween |
| CN2604434Y (en) * | 2003-01-30 | 2004-02-25 | 西南化工研究设计院 | Bubble tower converter for technology of methyl alcohol low pressure liquid phase carbonyl synthesizing acetic acid |
| CN2635202Y (en) * | 2003-07-21 | 2004-08-25 | 房双宽 | Gas-liquid reaction pot |
| CN101885678A (en) * | 2010-07-05 | 2010-11-17 | 兖矿国泰化工有限公司 | Reaction equipment for synthesizing ethylic acid by low-pressure methanol carbonylation of methanol |
| CN103060018A (en) * | 2011-10-21 | 2013-04-24 | 神华集团有限责任公司 | Gas distributor for coal gas high-efficiency washing and cleaning technique, secondary coal gas washing tower, coal gas cleaning device and application thereof |
| CN204952862U (en) * | 2015-08-21 | 2016-01-13 | 中石化宁波工程有限公司 | Thick liquid attitude bed reactor feed distribution ware |
| CN106478585A (en) * | 2015-08-28 | 2017-03-08 | 中国石油化工股份有限公司 | The control method of ethylene carbonate building-up process |
-
2018
- 2018-03-30 CN CN201810293832.5A patent/CN108261988B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5781693A (en) * | 1996-07-24 | 1998-07-14 | Applied Materials, Inc. | Gas introduction showerhead for an RTP chamber with upper and lower transparent plates and gas flow therebetween |
| CN2604434Y (en) * | 2003-01-30 | 2004-02-25 | 西南化工研究设计院 | Bubble tower converter for technology of methyl alcohol low pressure liquid phase carbonyl synthesizing acetic acid |
| CN2635202Y (en) * | 2003-07-21 | 2004-08-25 | 房双宽 | Gas-liquid reaction pot |
| CN101885678A (en) * | 2010-07-05 | 2010-11-17 | 兖矿国泰化工有限公司 | Reaction equipment for synthesizing ethylic acid by low-pressure methanol carbonylation of methanol |
| CN103060018A (en) * | 2011-10-21 | 2013-04-24 | 神华集团有限责任公司 | Gas distributor for coal gas high-efficiency washing and cleaning technique, secondary coal gas washing tower, coal gas cleaning device and application thereof |
| CN204952862U (en) * | 2015-08-21 | 2016-01-13 | 中石化宁波工程有限公司 | Thick liquid attitude bed reactor feed distribution ware |
| CN106478585A (en) * | 2015-08-28 | 2017-03-08 | 中国石油化工股份有限公司 | The control method of ethylene carbonate building-up process |
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