CN106475017B - Heterophase reactor for ethylene carbonate Lipase absobed - Google Patents
Heterophase reactor for ethylene carbonate Lipase absobed Download PDFInfo
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- CN106475017B CN106475017B CN201510540715.0A CN201510540715A CN106475017B CN 106475017 B CN106475017 B CN 106475017B CN 201510540715 A CN201510540715 A CN 201510540715A CN 106475017 B CN106475017 B CN 106475017B
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Abstract
The present invention relates to a kind of gas -liquid -solid three -phase reactors for ethylene oxide and carbon dioxide synthesizing ethylene carbonate, from bottom to top include liquid outlet opening, liquid hydraulic barrier, gas feed mouth, gas feed distributor, supporting screening plate under catalyst, lower part porcelain layers of balls, catalyst layer, top porcelain layers of balls, supporting screening plate, liquid inlet opening, liquid feed distributor and gas discharge mouth on catalyst.Gas and liquid feedstock pass through gas distributor respectively and liquid distribution trough is radially uniform into catalyst bed, catalyst bed is fixed in reactor by upper and lower part porcelain ball and upper and lower supporting screening plate, multiple groups hydraulic barrier is arranged in reactor lower part, and overflow weir is arranged in two sides.Being unevenly distributed in the abundant progress and product liquid for be unfavorable for reaction present invention mainly solves gas, liquid charging has the problems such as gas entrainment, can be used in the industrial production of ethylene oxide and carbon dioxide synthesizing ethylene carbonate.
Description
Technical field
The present invention relates to a kind of gas -liquid -solid three -phase reactors for ethylene carbonate Lipase absobed, are more specifically one kind
The liquid-solid phase reactor of gas-of ethylene carbonate synthesis process is generated by ethylene oxide and carbon dioxide catalysis.
Background technique
Ethylene carbonate (EC) is a kind of excellent polar high-boiling solvent and important organic synthesis raw material.20th century are later half
Phase, various countries researcher have carried out numerous research, many new synthetic methods and new catalyst quilt to the synthesis of carbonic ester
It was found that.EC traditional production method is phosgenation, but its there are process flows it is long, yield is low, at high cost the disadvantages of, and phosgene
Toxicity is big, seriously polluted, has substantially stopped using in developed country.With CO2It is that raw material direct esterification prepares carbonic acid with EO
Vinyl acetate is a kind of efficient, green, environmentally friendly synthesis new intermediate ester method, and provides a chemical utilization two
The new way for aoxidizing carbon resource, can receive apparent economic benefit and social benefit, by various countries' most attention, be suitble to extensive
Industrialized production.
CN1421431A discloses ethylene glycol and urea in the presence of solid base catalyst, in the item for depressurizing or rousing nitrogen
Reaction generates ethylene carbonate under part, though technique selectivity is high, reaction condition is mild, it is with ethylene glycol and urea for original
Material, other than obtaining reaction product ethylene carbonate, while can also generate ammonia, and meeting environment pollutes, and improve environmental protection
Cost.
CN85100162A discloses a kind of process for synthesising vinylcarbonate by complex catalyst, to the high pressure for having electromagnetic agitation
Catalyst and ethylene oxide are added in kettle, is passed through CO2To 6atm, heated in bath of draining the oil, pressure first rises and reduces afterwards in kettle, reduces
Then continue to be passed through CO afterwards2, it is maintained at pressure in the range of 20-25atm, is reacted when confirming that pressure no longer reduces in kettle
It accuses and completes, after logical cooling water is cooled to room temperature, take out white solid in kettle, 99.9% yield can be obtained (to ethylene oxide)
Ethylene carbonate.Pressure autoclave type reactor reaction process used in the technique is not easy to control, is unfavorable for industrial application.
Summary of the invention
To be solved by this invention is following problem existing in the prior art: (1) gas, liquid charging, which is unevenly distributed, leads
It causes the presence of short circuit, channeling in reactor, reduces the utilization efficiency of catalyst, it is unfavorable to reaction process；(2) liquid produces
There are Vapor Entrainments in object, easily damage to upstream device after outflow reactor, such as the cavitation of pump, and the present invention proposes
A kind of new gas -liquid -solid three -phase reactor for ethylene carbonate Lipase absobed, the reactor is for ethylene carbonate Lipase absobed
When, have many advantages, such as that catalyst utilization is high, gas, liquid charging is evenly distributed, is suitable for heavy industrialization and applies.
In order to solve the above technical problems, the present invention is as follows using technical solution: a kind of for ethylene carbonate Lipase absobed
Gas -liquid -solid three -phase reactor includes liquid outlet opening (4), liquid hydraulic barrier (8), gas feed mouth (2), gas from bottom to top
Supporting screening plate (6) under body import distributor (10), catalyst, lower part porcelain layers of balls (9), catalyst layer (7), top porcelain layers of balls (9),
Supporting screening plate (6), liquid inlet opening (1), liquid-inlet distributor (5) and gas discharge mouth (3) on catalyst.Liquid feedstock
Mouth (1) is connected with liquid-inlet distributor (5), is located at the top of catalyst layer (7)；Gas feed mouth (2) and gas feed
Distributor (10) is connected, and is located at the lower part of catalyst layer (7).Gas discharge mouth (3) is located at liquid outlet opening (4)
The top and bottom of reactor.Wherein, gas feed distributor (10) and liquid-inlet distributor (5) include general pipeline and branch pipe,
The aperture short tube that at least 1 row is had on the aperture or branch pipe of at least 1 row is provided on branch pipe；Liquid hydraulic barrier (8) includes radial
Baffle and overflow weir positioned at side.
In above-mentioned technical proposal, it is preferable that catalyst bed (7) is at least 1 layer, when catalyst bed (7) are more than 1 layer
When, gas distributor (4) are installed in the space between catalyst bed.Liquid-inlet distributor (5) and gas feed distributor
(10) each branch pipe and general pipeline circular pipe more electedly, are distributed in cross, are spaced between each branch pipe in intersection distribution
Equal angular installation.Aperture or aperture short tube are 1 row on the branch pipe of liquid-inlet distributor (5) and gas feed distributor (10)
When, along reactor axial aperture or mounting opening short tube；When aperture or aperture short tube are 2 rows or more on branch pipe, every rows of openings
Angle between direction is identical.Percent opening is 5-50% on the branch pipe of gas feed distributor (10), if percent opening is below 5%
Or 50% or more, it will appear plunger area or uneven Bubble Region in reactor, the air pocket of generation rises rapidly, seriously affects
Alternate contact effect.
In above-mentioned technical proposal, it is preferable that the number of reactor lower part liquid phase hydraulic barrier (8) is 0-100, more preferably
Range is 3-50, and the residence time needed for the setting of hydraulic barrier number is separated according to gas phase in product liquid determines, such as gas phase point
From of less demanding, it can be not provided with hydraulic barrier, every piece of baffle plate is equidistant or Unequal distance is arranged in reactor, is in shell
90 ° of angles.
In above-mentioned technical proposal, it is preferable that overflow weir is set to baffle one side edge, the overflow weir edge of neighbouring baffle
Reactor axially symmetric disposition.
In above-mentioned technical proposal, it is preferable that the sectional area of hydraulic barrier (8) accounts for the 50%-99% of reactor cross section product, more
Preferred scope is 50%-80%.
In above-mentioned technical proposal, it is preferable that the height of weir plate of hydraulic barrier (8) is the 1%-20% of reactor diameter,
More preferable range is 5%-10%.
It can achieve following effect: liquid-inlet distributor (5) and gas feed distributor by adopting the above technical scheme
(10) setting ensure that being uniformly distributed on entire bed section after gas feed enters reactor, effectively have adjusted gas
The uniformity for feeding the dissolution degree in liquid reactants ensure that warm in the utilization rate and catalyst bed layer cross section of catalyst
Degree is uniformly distributed, and is conducive to the reactivity worth for improving catalyst.The setting of liquid hydraulic barrier (8) effectively increases liquid
Product ensure that the separation for wherein carrying gas phase secretly in the residence time in the reactor.
Detailed description of the invention
Fig. 1 is the heterophase reactor according to the present invention for ethylene carbonate Lipase absobed.
Fig. 2 is the schematic diagram of Section A-A in Fig. 1.
Fig. 3 is the schematic diagram of section B-B in Fig. 1.
In Fig. 1,2,3,1 is liquid inlet opening, and 2 be gas feed mouth, and 3 be gas discharge mouth, and 4 be liquid outlet opening, 5
It is catalyst support sieve plate for liquid-inlet distributor, 6,7 be catalyst layer, and 8 be liquid hydraulic barrier, and 9 be porcelain layers of balls, and 10 are
Gas feed distributor.
Heterophase reactor workflow in Fig. 1 are as follows: liquid phase epoxidation ethane is by liquid inlet opening (1) through liquid-inlet distributor
(5) enter in reactor, and set up liquid level in reactor, which is higher than supporting screening plate (6) on catalyst, is lower than liquid
Feed inlet (1).Gas phase carbon dioxide blasts reactor after gas feed distributor (10) is uniformly distributed by gas feed mouth (2)
Interior, carbon dioxide flows up through supporting screening plate (6) and lower part porcelain layers of balls (9) and is reacted afterwards into catalyst layer (7), not instead
The carbon dioxide answered is flowed out by reactor head gas discharge mouth (3).Liquid phase epoxidation ethane and gas phase carbon dioxide are in catalyst
Catalysis reaction occurs in layer (7), generates ethylene carbonate ester products, product is produced with liquid form outflow catalyst layer (7), the liquid
It further include the carbon dioxide of gas phase in object.Product liquid flows subsequently through liquid hydraulic barrier (8), guarantees in enough residence times
Under, gas phase carbon dioxide in liquid product by separating, and final liquid product is through liquid outlet opening (4) outflow reactor.
The present invention will be further described below by way of examples.
Specific embodiment
[embodiment 1]
By Fig. 1, Fig. 2, gas -liquid -solid three -phase reactor diameter is 500mm, and catalyst bed is 1 layer, liquid-inlet distribution
Each branch pipe of device and gas feed distributor and general pipeline are round tube, are distributed in cross, each branch pipe of liquid-inlet distributor
Between interval 60 ° of angles installation, 30 ° of interval angles installation between each branch pipe of gas feed distributor.The branch pipe of liquid-inlet distributor
On open up 1 row's aperture, 2 row's apertures are opened up on the branch pipe of gas feed distributor, the angle between every rows of openings direction be 90 °.
Percent opening is 30% on the branch pipe of gas feed distributor.Reactor lower part liquid phase hydraulic barrier number is 2 pieces, every piece of baffle plate
Spacing is identical, and is in 90 ° of angles with shell.The sectional area of hydraulic barrier accounts for the 70% of reactor cross section product.Height of weir plate is
The 10% of reactor diameter.Under the above structural parameters, by the present invention to ethylene oxide and carbon dioxide synthesizing ethylene carbonate
Reactor is designed, available ideal reaction effect, and the same sectional uniform degree maximum deviation of catalyst bed is less than
2.0%, radial temperature difference is less than 1.0 DEG C, and gas phase fraction is less than 2.0% in product liquid.
[embodiment 2]
By Fig. 1, Fig. 2, gas -liquid -solid three -phase reactor diameter is 1000mm, and catalyst bed is 2 layers, is arranged in interlayer
Each branch pipe and general pipeline of gas feed distributor, liquid-inlet distributor and gas feed distributor are round tube, are in cross phase
Distribution is handed over, interval 45° angle degree is installed between each branch pipe of liquid-inlet distributor, and 30 ° of angles are spaced between each branch pipe of gas feed distributor
Degree installation.2 row's apertures are opened up on the branch pipe of liquid-inlet distributor, the angle between every rows of openings direction is 90 °；Gas feed
3 row's apertures are opened up on the branch pipe of distributor, the angle between every rows of openings direction is 45 °.On the branch pipe of gas feed distributor
Percent opening is 25%.Reactor lower part liquid phase hydraulic barrier number is 5 pieces, and every piece of baffle(s) spacing is identical, and is in 90 ° with shell
Angle.The sectional area of hydraulic barrier accounts for the 60% of reactor cross section product.Height of weir plate is the 8% of reactor diameter.Above
Under structural parameters, ethylene oxide and carbon dioxide synthesizing ethylene carbonate reactor are designed by the present invention, it is available
Ideal reaction effect, the same sectional uniform degree maximum deviation of catalyst bed is less than 2.5%, and radial temperature difference is less than 1.5 DEG C, liquid
Gas phase fraction is less than 2.2% in body product.
[embodiment 3]
By Fig. 1, Fig. 2, gas -liquid -solid three -phase reactor diameter is 1500mm, and catalyst bed is 3 layers, is arranged in interlayer
Each branch pipe and general pipeline of gas feed distributor, liquid-inlet distributor and gas feed distributor are round tube, are in cross phase
Distribution is handed over, 60 ° of interval angle is installed between each branch pipe of liquid-inlet distributor, and 30 ° of angles are spaced between each branch pipe of gas feed distributor
Degree installation.2 row's apertures are opened up on the branch pipe of liquid-inlet distributor, the angle between every rows of openings direction is 60 °；Gas feed
3 row's apertures are opened up on the branch pipe of distributor, the angle between every rows of openings direction is 30 °.On the branch pipe of gas feed distributor
Percent opening is 40%.Reactor lower part liquid phase hydraulic barrier number is 6 pieces, and every piece of baffle(s) spacing is identical, and is in 90 ° with shell
Angle.The sectional area of hydraulic barrier accounts for the 65% of reactor cross section product.Height of weir plate is the 5% of reactor diameter.Above
Under structural parameters, ethylene oxide and carbon dioxide synthesizing ethylene carbonate reactor are designed by the present invention, it is available
Ideal reaction effect, the same sectional uniform degree maximum deviation of catalyst bed is less than 2.5%, and radial temperature difference is less than 2.0 DEG C, liquid
Gas phase fraction is less than 2.0% in body product.
[embodiment 4]
By Fig. 1, Fig. 2, gas -liquid -solid three -phase reactor diameter is 300mm, and catalyst bed is 1 layer, liquid-inlet distribution
Each branch pipe of device and gas feed distributor and general pipeline are round tube, are distributed in cross, each branch pipe of liquid-inlet distributor
Between interval 60 ° of angles installation, 30 ° of interval angles installation between each branch pipe of gas feed distributor.The branch pipe of liquid-inlet distributor
On open up 1 row's aperture；1 row's aperture is opened up on the branch pipe of gas feed distributor.Percent opening on the branch pipe of gas feed distributor
It is 20%.Reactor lower part does not set liquid phase hydraulic barrier.Under the above structural parameters, by the present invention to ethylene oxide and dioxy
Change carbon synthesizing ethylene carbonate reactor to be designed, available ideal reaction effect, the same section of catalyst bed is equal
Evenness maximum deviation is less than 2.2%, and radial temperature difference is less than 1.5 DEG C, and gas phase fraction is less than 2.5% in product liquid.
[embodiment 5]
By Fig. 1, Fig. 2, gas -liquid -solid three -phase reactor diameter is 3000mm, and catalyst bed is 4 layers, is arranged in interlayer
Each branch pipe and general pipeline of gas feed distributor, liquid-inlet distributor and gas feed distributor are round tube, are in cross phase
Distribution is handed over, 60 ° of interval angle is installed between each branch pipe of liquid-inlet distributor, and 15 ° of angles are spaced between each branch pipe of gas feed distributor
Degree installation.2 row's apertures are opened up on the branch pipe of liquid-inlet distributor, the angle between every rows of openings direction is 90 °；Gas feed
3 row's apertures are opened up on the branch pipe of distributor, the angle between every rows of openings direction is 30 °.On the branch pipe of gas feed distributor
Percent opening is 45%.Reactor lower part liquid phase hydraulic barrier number is 5 pieces, and every piece of baffle(s) spacing is identical, and is in 90 ° with shell
Angle.The sectional area of hydraulic barrier accounts for the 75% of reactor cross section product.Height of weir plate is the 10% of reactor diameter.Above
Under structural parameters, ethylene oxide and carbon dioxide synthesizing ethylene carbonate reactor are designed by the present invention, it is available
Ideal reaction effect, the same sectional uniform degree maximum deviation of catalyst bed is less than 2.5%, and radial temperature difference is less than 2.0 DEG C, liquid
Gas phase fraction is less than 1.5% in body product.
Claims (7)
1. a kind of gas -liquid -solid three -phase reactor for ethylene carbonate Lipase absobed includes liquid outlet opening (4), liquid from bottom to top
Supporting screening plate (6), lower part porcelain ball under body hydraulic barrier (8), gas feed mouth (2), gas feed distributor (10), catalyst
Supporting screening plate (6), liquid inlet opening (1), liquid-inlet distributor (5) on layer, catalyst layer (7), top porcelain layers of balls, catalyst
And gas discharge mouth (3), liquid inlet opening (1) are connected with liquid-inlet distributor (5), are located at the upper of catalyst layer (7)
Portion；Gas feed mouth (2) is connected with gas feed distributor (10), is located at the lower part of catalyst layer (7)；Gas discharge mouth
(3) top and bottom of reactor are located at liquid outlet opening (4), wherein gas feed distributor (10) and liquid into
Mouth distributor (5) includes general pipeline and branch pipe, and the aperture being provided on the aperture or branch pipe of at least 1 row at least 1 row on branch pipe is short
Pipe；Liquid hydraulic barrier (8) includes radial baffle and the overflow weir positioned at side, and the number of the hydraulic barrier (8) is 3-50,
Overflow weir is set to baffle one side edge, and the overflow weir of neighbouring baffle is axially and symmetrically disposed along reactor；The baffling gear
The height of weir plate of plate (8) is the 5%-10% of reactor diameter.
2. the gas -liquid -solid three -phase reactor according to claim 1 for ethylene carbonate Lipase absobed, it is characterised in that institute
State catalyst layer (7) and be at least 1 layer, when catalyst layer (7) are more than 1 layer, installed in the space between catalyst layer gas into
Mouth distributor (10).
3. the gas -liquid -solid three -phase reactor according to claim 1 for ethylene carbonate Lipase absobed, it is characterised in that institute
Each branch pipe of liquid-inlet distributor (5) and gas feed distributor (10) is stated with general pipeline in distribution is intersected, is spaced between each branch pipe
Equal angular installation.
4. the gas -liquid -solid three -phase reactor according to claim 1-3 for ethylene carbonate Lipase absobed, special
When sign is that aperture or aperture short tube are 1 row on the branch pipe of the liquid-inlet distributor (5) and gas feed distributor (10),
Along reactor axial aperture or mounting opening short tube.
5. the gas -liquid -solid three -phase reactor according to claim 1-3 for ethylene carbonate Lipase absobed, special
Sign be on the branch pipe of the liquid-inlet distributor (5) and gas feed distributor (10) aperture or aperture short tube for 2 rows or
When above, the angle between every rows of openings direction is identical.
6. the gas -liquid -solid three -phase reactor according to claim 1-3 for ethylene carbonate Lipase absobed, special
Sign is on the branch pipe of the gas feed distributor (10) that percent opening is 5-50%.
7. the gas -liquid -solid three -phase reactor according to claim 1 for ethylene carbonate Lipase absobed, it is characterised in that institute
The sectional area for stating hydraulic barrier (8) accounts for the 50%-99% of reactor cross section product.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201510540715.0A CN106475017B (en) | 2015-08-28 | 2015-08-28 | Heterophase reactor for ethylene carbonate Lipase absobed |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510540715.0A CN106475017B (en) | 2015-08-28 | 2015-08-28 | Heterophase reactor for ethylene carbonate Lipase absobed |
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| Publication Number | Publication Date |
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| CN106475017A CN106475017A (en) | 2017-03-08 |
| CN106475017B true CN106475017B (en) | 2019-04-12 |
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| CN111087378B (en) * | 2019-12-27 | 2022-10-21 | 江苏奥克化学有限公司 | Method for preparing ethylene carbonate |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201529518U (en) * | 2009-05-13 | 2010-07-21 | 中国石油化工股份有限公司 | Gas-liquid-solid three-phase fixed bubbling column reactor |
| CN103084084A (en) * | 2011-11-02 | 2013-05-08 | 中国石油化工股份有限公司 | Liquid collecting, mixing, and uniform distributing device |
| CN203417665U (en) * | 2013-08-08 | 2014-02-05 | 攀钢集团攀枝花钢铁研究院有限公司 | Combined type liquid-solid fluidization reactor |
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2015
- 2015-08-28 CN CN201510540715.0A patent/CN106475017B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201529518U (en) * | 2009-05-13 | 2010-07-21 | 中国石油化工股份有限公司 | Gas-liquid-solid three-phase fixed bubbling column reactor |
| CN103084084A (en) * | 2011-11-02 | 2013-05-08 | 中国石油化工股份有限公司 | Liquid collecting, mixing, and uniform distributing device |
| CN203417665U (en) * | 2013-08-08 | 2014-02-05 | 攀钢集团攀枝花钢铁研究院有限公司 | Combined type liquid-solid fluidization reactor |
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