CN209508088U - A kind of methylarenes oxidation system - Google Patents
A kind of methylarenes oxidation system Download PDFInfo
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- CN209508088U CN209508088U CN201821943291.8U CN201821943291U CN209508088U CN 209508088 U CN209508088 U CN 209508088U CN 201821943291 U CN201821943291 U CN 201821943291U CN 209508088 U CN209508088 U CN 209508088U
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- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 23
- 230000003647 oxidation Effects 0.000 title claims abstract description 21
- 239000007788 liquid Substances 0.000 claims abstract description 148
- 230000008676 import Effects 0.000 claims abstract description 25
- 238000004891 communication Methods 0.000 claims abstract description 4
- 238000006243 chemical reaction Methods 0.000 claims description 50
- 239000000945 filler Substances 0.000 claims description 15
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 3
- 238000005325 percolation Methods 0.000 claims 2
- 230000006837 decompression Effects 0.000 claims 1
- 239000007789 gas Substances 0.000 abstract description 60
- WPYMKLBDIGXBTP-UHFFFAOYSA-N benzoic acid Chemical compound OC(=O)C1=CC=CC=C1 WPYMKLBDIGXBTP-UHFFFAOYSA-N 0.000 abstract description 8
- 150000003934 aromatic aldehydes Chemical class 0.000 abstract description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 5
- 239000001301 oxygen Substances 0.000 abstract description 5
- 229910052760 oxygen Inorganic materials 0.000 abstract description 5
- 238000012546 transfer Methods 0.000 abstract description 5
- 230000008901 benefit Effects 0.000 abstract description 3
- 230000000149 penetrating effect Effects 0.000 abstract description 3
- 230000004044 response Effects 0.000 abstract description 2
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 9
- 238000007710 freezing Methods 0.000 description 9
- 230000008014 freezing Effects 0.000 description 9
- 239000000047 product Substances 0.000 description 8
- 239000005416 organic matter Substances 0.000 description 7
- 239000000463 material Substances 0.000 description 5
- 239000012071 phase Substances 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 description 4
- 239000012530 fluid Substances 0.000 description 4
- 239000000376 reactant Substances 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 239000005711 Benzoic acid Substances 0.000 description 2
- 239000006004 Quartz sand Substances 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical group O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- -1 aldehyde radical Chemical class 0.000 description 2
- HUMNYLRZRPPJDN-UHFFFAOYSA-N benzaldehyde Chemical compound O=CC1=CC=CC=C1 HUMNYLRZRPPJDN-UHFFFAOYSA-N 0.000 description 2
- 235000010233 benzoic acid Nutrition 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 2
- 229910052573 porcelain Inorganic materials 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000036632 reaction speed Effects 0.000 description 2
- 241000208340 Araliaceae Species 0.000 description 1
- 235000005035 Panax pseudoginseng ssp. pseudoginseng Nutrition 0.000 description 1
- 235000003140 Panax quinquefolius Nutrition 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 125000003178 carboxy group Chemical group [H]OC(*)=O 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000000796 flavoring agent Substances 0.000 description 1
- 239000002778 food additive Substances 0.000 description 1
- 235000013373 food additive Nutrition 0.000 description 1
- 235000013355 food flavoring agent Nutrition 0.000 description 1
- 239000003205 fragrance Substances 0.000 description 1
- 230000006870 function Effects 0.000 description 1
- 235000008434 ginseng Nutrition 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 125000000956 methoxy group Chemical group [H]C([H])([H])O* 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000011368 organic material Substances 0.000 description 1
- QNGNSVIICDLXHT-UHFFFAOYSA-N para-ethylbenzaldehyde Natural products CCC1=CC=C(C=O)C=C1 QNGNSVIICDLXHT-UHFFFAOYSA-N 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 150000003254 radicals Chemical class 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000012855 volatile organic compound Substances 0.000 description 1
Classifications
-
- 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
Abstract
The utility model discloses a kind of methylarenes oxidation systems, ultra-fine bubble breaker including tower reactor and the lower part Qi Nei, ultra-fine bubble breaker includes the gas-liquid channel for being connected to the air chamber of gas feed and being vertically in air chamber, gas-liquid channel is the pipeline for penetrating through air chamber, pipe side wall has the stomata of connection air chamber, tower reactor includes offgas outlet, circulating liquid outlet and circulating liquid import, the top of liquid charging stock inlet communication tower reactor, offgas outlet is set to the top of tower reactor, circulating liquid outlet passes through circulating liquid inlet communication gas-liquid channel by liquid circulation line, liquid circulating pipe road is provided with circulating pump, and it is connected to product exit.Methylarenes efficient oxidation reaction system described in the utility model has the advantages that gas pressure drop is small, gas-liquid mass transfer response area is big, and gas effciency is high, and efficiency is high, prepares aromatic aldehyde or aromatic acid suitable for air or oxygen oxidation methylarenes.
Description
Technical field
The utility model belongs to field of chemical engineering, and in particular to a kind of methylarenes oxidation system.
Background technique
Aromatic aldehyde and aromatic acid refer generally to the compound that aldehyde radical or carboxyl are directly connected on phenyl ring, they are in medicine, pesticide
Equal fields are widely applied, and are important intermediate, synthesis flavouring agent raw material and food additives.Aromatic aldehyde and aromatic acid are usually
By base substituted on phenyl ring (such as-CH3、-OCH3、-NO2Deng) methylarenes by oxygen (air) oxidation obtain.Such as to diformazan
Benzene (PX) obtains terephthalic acid (TPA) using air oxidation in acetic acid solvent under the effect of MC catalyst system；Toluene is in high temperature
Air oxidation produces benzoic acid under condition of high voltage.The liquid phase oxidation of toluene class aromatic hydrocarbons is limited by gas-liquid mass transfer, since oxygen is anti-
Answer the solubility in object system not high, need to keep excess air flow and higher temperature (120 DEG C~170 DEG C) and pressure (1~
10bar) to strengthen mass transfer, high temperature and pressure exhaust emissions is easily caused to carry large amount of organic material secretly, leads to explosion danger or serious
VOCs pollution.
The reaction that existing methylarenes liquid phase oxidation generates aromatic aldehyde is substantially the kettle under pressurization and hot conditions
Formula intermittent reaction.Methylarenes oxidation reaction mechanism is free chain reaction, and reaction under high pressure to combine more between free radical
To be rapid, but a large amount of by-product can be generated in this way, by-product increases, and not only wastes raw material, but also to reaction product
Separation increases cost.Moreover, the reaction of existing methylarenes liquid phase oxidation generation aromatic aldehyde and direction acid is between traditional
It is carried out in formula of having a rest stirred tank or tower blistering reaction system, the general character disadvantage of batch type kettle and tower blistering reaction system
Be: bubble diameter is big, reaction speed is slow, oxygen utilization rate is low, energy consumption is high.Wherein, after the diameter of bubble is greater than 2mm, gas phase
Mass transfer rate will drastically reduce, so that reaction rate is also impacted.In addition, the tail gas emptying at the top of reaction system also results in sternly
The material and energy loss and environmental pollution problem of weight.
Utility model content
The utility model aims to solve at least one of the technical problems existing in the prior art.For this purpose, the utility model mentions
A kind of efficient methylarenes oxidation system that can effectively improve gas effciency and capacity usage ratio out.
To achieve the above object, the utility model adopts the following technical solutions:
A kind of methylarenes oxidation system, including liquid charging stock import, gas feed, product exit, tower reaction
Device and ultra-fine bubble breaker, the ultra-fine bubble breaker are set to lower part in the tower reactor,
The ultra-fine bubble breaker includes air chamber and gas-liquid channel, and the gas feed passes through institute by the first pipeline
The wall for stating tower reactor is connected to the air chamber, and the gas-liquid channel is vertically arranged in the air chamber, and the gas-liquid is logical
Road is the pipeline for penetrating through the air chamber, and the pipe side wall is provided with the stomata of several connection air chambers, the gas-liquid
Channel is connected to the bottom of the tower reactor and the upper space of the ultra-fine bubble breaker,
The tower reactor include offgas outlet, circulating liquid outlet and circulating liquid import, the liquid charging stock into
Mouth is connected to the top of the tower reactor, and the offgas outlet is set to the top of the tower reactor, the circulation fluid
Body outlet passes through gas-liquid channel described in the circulating liquid inlet communication, the liquid circulating pipe road by liquid circulation line
It is provided with circulating pump, the liquid circulation line is connected to the product exit.Enter the gas of gas-liquid channel by high speed from stomata
The liquid of flowing is cut, and can be obtained micron-class superfine bubble stream.
Further, the height of the ultra-fine bubble breaker is 100~1000mm.
Further, the gas-liquid channel has 3~20.
Further, the cross section of the gas-liquid channel is rectangular, and the rectangular width is 5~50mm.
Further, the cross section of the gas-liquid channel is rectangular, rectangular a length of tower reactor diameter
0.1~0.8 times, 0.6~0.9 times of a height of ultra-fine bubble breaker height of the gas-liquid channel.
Further, the top in the tower reactor be pre-reaction section, the pre-reaction section top setting described in
Liquid charging stock import is provided with several first dual-flow trays in the pre-reaction section.
Further, the diameter of the pre-reaction section is 400mm, a height of 6000mm.
Further, the lower diameter of the tower reactor is 600mm, a height of 4000mm.
Further, the liquid circulation outlet is set on the side wall of the tower reactor, and is located at described super
Between thin bubble breaker and the pre-reaction section.
Further, the liquid circulating pipe road is additionally provided with gas-liquid separator, the separation gas of the gas-liquid separator
Pre-reaction section described in outlet.
Further, the liquid circulating pipe road is additionally provided with heat exchanger.
Further, the gas-liquid separator includes several second dual-flow trays and filler, second dual-flow tray position
In the filler top.Gas-liquid separator can effectively separate the bubble in circulating liquid with liquid.
Further, the filler is corrosion-and high-temp-resistant filler.
Further, the filler is quartz sand or porcelain ball.
Further, the diameter of the filler is 1mm.
Further, the tower reactor further includes overflow baffle, and the overflow baffle is arranged in the tower reaction
On the side wall of device and the circulating liquid outlet is closed on, the upper edge of the overflow baffle is located at the upper of circulating liquid outlet
Side.
Further, the bottom of the tower reactor is provided with slag-drip opening.
Further, the offgas outlet is connected with steam generator, and the tail gas provides heat for the steam generator
Energy.Steam generator is used to pipette the heat in reactor discharge tail gas, efficiently utilizes thermal energy.
Further, the steam generator further includes clear water import and vapor outlet port.Clear water vapour in steam generator
Change, takes away the heat in the tail gas.
Further, the steam temperature of the steam generator is 120 DEG C~140 DEG C.
Further, the offgas outlet is connected with pressure reducing radiator.Pressure reducing radiator can be used for that tail gas is made to cool down.
Further, the pressure reducing radiator includes the first condensate outlet, described in the first condensate outlet connection
Tower reactor.Pressure reducing radiator can trap the organic matter in gas phase when depressurizing cooled exhaust gas, be transmitted back to tower reactor after
Continuous reaction, to efficiently utilize reactant.
Further, the pressure reducing radiator operating pressure is 1.1 ~ 2bar.
Further, the pressure reducing radiator is set to after the steam generator.
Further, cooled exhaust gas outlet, cooled exhaust gas outlet connection are provided at the top of the pressure reducing radiator
There is condenser, the condenser includes the second condensate outlet, and second condensate outlet connects the tower reactor.It is cold
Condenser is for further condensing the organic matter in cooled exhaust gas, and being transmitted back to tower reactor, the reaction was continued, thus more efficiently
Utilize reactant.
Further, second condensate outlet is also connected with the pressure reducing radiator.The cryogenic liquid that condenser obtains
Part is delivered to pressure reducing radiator, and the utilization rate of the cooling efficiency of pressure reducing radiator and the low temperature of condenser can be improved.
Further, the operation temperature of -30 DEG C of condenser use~5 DEG C.
Further, the condenser further includes freezing liquid import and freezing liquid outlet.It is the condensation using freezing liquid
Device provides low temperature.
Further, the condenser further includes condensation offgas outlet, and the condensation offgas outlet is connected with vent gas treatment
System.
When in use, liquid is driven methylarenes oxidation system described in the utility model by the circulating pump, warp
It is delivered in the gas-liquid channel by the liquid circulation line, gas is delivered to the air chamber via the gas feed
In, the gas-liquid channel is entered by the stomata, is cut to form ultra-fine bubble stream by the swiftly flowing liquid, it is described super
It after thin bubble stream reaction, is exported and is flowed out by the circulating liquid, part returns to via the circulating liquid import described again
The reaction was continued in tower reactor, partially obtains product by product exit.
Preferably, the tail gas for reacting generation enters exhaust gas processing device via the offgas outlet.The vent gas treatment
Device includes steam generator, pressure reducing radiator or the condenser.
Methylarenes oxidation system described in the utility model, by the way that ultra-fine bubble breaker is arranged, so as to
Using quick movement of the circulating liquid in gas-liquid channel, the gas for entering air chamber forms micron-sized ultra-fine bubble, from
And gas liquid film product is significantly increased, gas-liquid mass transfer speed is improved, reaction process is accelerated, improves gas effciency, in turn
Can relative reduction reaction system operating pressure and temperature, as a result, reduce exhaust emissions amount and caused by energy and material
Loss, is greatly reduced environmental pollution.
Methylarenes oxidation system described in the utility model, with bubble diameter is small, gas pressure drop is small, gas-liquid passes
Qualitative response area is big, gas effciency is high, efficiency is high, reaction speed is high, gas effciency is high, organic matter content is low in tail gas
The advantages that, the thermal energy and pressure energy in tail gas can be effectively recycled, air or oxygen oxidation methylarenes preparation fragrance is suitable for
Aldehyde or aromatic acid.
Detailed description of the invention
The above-mentioned and/or additional aspect and advantage of the utility model from the description of the embodiment in conjunction with the following figures will
Become obvious and be readily appreciated that, in which:
Fig. 1 is the structural schematic diagram of methylarenes oxidation system described in the utility model embodiment 1.
Fig. 2 is ultra-fine bubble breaker schematic diagram described in the utility model.
Wherein, 1 is tower reactor, and 2 be steam generator, and 3 be pressure reducing radiator, and 4 be condenser, and 101 be ultra-fine gas
Destroyer is steeped, 102 be gas feed, and 103 be circulating pump, and 104 be heat exchanger, and 105 be product exit, and 106 be gas-liquid separator,
1061 be the second dual-flow tray, and 1062 be filler, and 107 be circulating liquid outlet, and 108 be the outlet of separation gas, and 110 be liquid charging stock
Import, 111 be the first dual-flow tray, and 112 be slag-drip opening, and 113 be offgas outlet, and 114 be circulating liquid import, and 202 be clear water
Import, 204 be vapor outlet port, and 303 be cooled exhaust gas outlet, and 304 be the first condensate outlet, and 402 be the second condensate outlet,
403 be freezing liquid import, and 404 be condensation offgas outlet, and 405 be freezing liquid outlet, and 1011 be air chamber, and 2012 be that gas-liquid is logical
Road.
Specific embodiment
The embodiments of the present invention are described below in detail, examples of the embodiments are shown in the accompanying drawings, wherein from beginning
Same or similar element or element with the same or similar functions are indicated to same or similar label eventually.Below by ginseng
The embodiment for examining attached drawing description is exemplary, and is only used for explaining the utility model, and should not be understood as to the utility model
Limitation.
In the description of the present invention, it should be noted that unless otherwise clearly defined and limited, term " is pacified
Dress ", " connected ", " connection ", " connection " shall be understood in a broad sense, for example, it may be being fixedly connected, may be a detachable connection,
Or it is integrally connected；It can be mechanical connection, be also possible to be electrically connected；It can be directly connected, intermediary can also be passed through
It is indirectly connected, can be the connection inside two elements.For the ordinary skill in the art, it can be managed with concrete condition
Solve the concrete meaning of above-mentioned term in the present invention.
Embodiment 1
As shown in Figs. 1-2, a kind of methylarenes oxidation system, including liquid charging stock import 110, gas feed 102,
Product exit 105, tower reactor 1 and ultra-fine bubble breaker 101, the ultra-fine bubble breaker 101 are set to the tower
Lower part in formula reactor 1,
The ultra-fine bubble breaker 101 includes air chamber 1011 and gas-liquid channel 1012, and the gas feed 102 passes through
The wall that first pipeline passes through the tower reactor 1 is connected to the air chamber 1011, and the gas-liquid channel 1012 is vertically arranged at
In the air chamber 1011, the gas-liquid channel 1012 is the pipeline for penetrating through the air chamber 1011, the pipe side wall setting
There is the stomata of several connection air chambers 1011, the gas-liquid channel 1012 is connected to bottom and the institute of the tower reactor 1
The upper space of ultra-fine bubble breaker 101 is stated,
The tower reactor 1 includes offgas outlet 113, circulating liquid outlet 107 and circulating liquid import 114, described
Liquid charging stock import 110 is connected to the top of the tower reactor 1, and the offgas outlet 113 is set to the tower reactor 1
Top, circulating liquid outlet 107 passes through the circulating liquid import 114 by liquid circulation line and is connected to the gas-liquid
Channel 1012, the liquid circulating pipe road are provided with circulating pump 103, and the liquid circulation line is connected to the product exit
105.The gas for entering gas-liquid channel from stomata is cut by swiftly flowing liquid, can be obtained micron-class superfine bubble stream.
The height of the ultra-fine bubble breaker 101 is 100~1000mm.
The gas-liquid channel 1012 has 3~20.
The cross section of the gas-liquid channel 1012 be it is rectangular, the rectangular width be 5~50mm.
The cross section of the gas-liquid channel 1012 be it is rectangular, the 0.1 of rectangular a length of 1 diameter of tower reactor
~0.8 times, 0.6~0.9 times of a height of ultra-fine 101 height of bubble breaker of the gas-liquid channel.
Top in the tower reactor 1 is pre-reaction section, and the liquid charging stock is arranged in the top of the pre-reaction section
Import 110 is provided with several first dual-flow trays 111 in the pre-reaction section.
The liquid circulation outlet 107 is set on the side wall of the tower reactor 1, and is located at the ultra-fine bubble
Between destroyer 101 and the pre-reaction section.
The liquid circulating pipe road is additionally provided with gas-liquid separator 106, the separation gas outlet of the gas-liquid separator 106
The 108 connection pre-reaction sections.
The liquid circulating pipe road is additionally provided with heat exchanger 104.
The gas-liquid separator 106 includes several second dual-flow trays 1061 and filler 1062, second dual-flow tray
1061 are located at 1062 top of filler.Gas-liquid separator 106 can effectively separate the bubble in circulating liquid with liquid.
The filler 1062 is corrosion-and high-temp-resistant filler.
The filler 1062 is quartz sand or porcelain ball.
The diameter of the filler 1062 is 1mm.
The tower reactor 1 further includes overflow baffle, and the side wall of the tower reactor 1 is arranged in the overflow baffle
Above and the circulating liquid outlet 107 is closed on, the upper edge of the overflow baffle is located at the top of circulating liquid outlet 107.
The bottom of the tower reactor 1 is provided with slag-drip opening 112.
The offgas outlet 113 is connected with steam generator 2, and the tail gas of the tower reactor 1 is steam generation
Device provides thermal energy.Steam generator 2 is used to pipette the heat in reactor discharge tail gas, efficiently utilizes thermal energy.
The steam generator 2 further includes clear water import 202 and vapor outlet port 204.Clear water vapour in steam generator 2
Change, takes away the heat in tail gas.
The steam temperature of the steam generator 2 is 120 DEG C~140 DEG C.
The offgas outlet 113 is connected with pressure reducing radiator 3.Pressure reducing radiator 3 can be used for that tail gas is made to cool down.
The pressure reducing radiator 3 includes the first condensate outlet 304, and first condensate outlet 304 connects the tower
Formula reactor 1.Pressure reducing radiator 3 can trap the organic matter in gas phase when depressurizing cooled exhaust gas, be transmitted back to tower reactor 1
The reaction was continued, to efficiently utilize reactant.
3 operating pressure of pressure reducing radiator is 1.1 ~ 2bar.
The pressure reducing radiator 3 is set to after the steam generator 2.
The top of the pressure reducing radiator 3 is provided with cooled exhaust gas outlet 303, and the cooled exhaust gas outlet 303 is connected with
Condenser 4, the condenser 4 include the second condensate outlet 402, and second condensate outlet 402 connects described tower anti-
Answer device 1.Condenser 4 is for further condensing the organic matter in cooled exhaust gas, and being transmitted back to tower reactor 1, the reaction was continued, thus
More efficiently utilize reactant.
Second condensate outlet 402 is also connected with the pressure reducing radiator 3.The cryogenic liquid part that condenser 4 obtains
It is delivered to pressure reducing radiator 3, the utilization rate of the cooling efficiency of pressure reducing radiator 3 and the low temperature of condenser 4 can be improved.
The operation temperature of -30 DEG C~5 DEG C of 4 use of condenser.
The condenser 4 further includes freezing liquid import 403 and freezing liquid outlet 405.It is the condenser 4 using freezing liquid
Low temperature is provided.
The condenser 4 further includes condensation offgas outlet 404, and the condensation offgas outlet 404 is connected with vent gas treatment system
System.
Include: using the course of work that above-mentioned reaction system carries out the reaction of methylarenes efficient oxidation
After the fresh material preheating of the toluene of 20kg/h cobalt-containing catalyst 0.5wt%, enter from liquid charging stock import 110 pre- anti-
Enter tower reactor lower part, tower reactor ontology after answering the high-temperature gas risen in Duan Yucong tower reactor to come into full contact with
160 DEG C of temperature, pressure 9bar.Gas-liquid mixture in tower reactor enters gas-liquid separator through circulating liquid outlet 107
106, after gas-liquid separation, partially liq is sent into ultra-fine gas through circulation fluid import 114 by circulating pump 103 after the heat exchange of heat exchanger 104
In the gas-liquid channel 1012 for steeping destroyer 101, rest part liquid has product exit to send to subsequent processing.By other imports 102
The gas for sending the air chamber 1011 to ultra-fine bubble breaker 101, enters back into gas-liquid channel 1012, by gas-liquid channel 1012
High-speed liquid is cut to form ultra-fine bubble after, tower reactor bottom is downwardly into together with liquid, is then broken by ultra-fine bubble
Outside millstone together upwards.Gas-liquid is partially separated in the middle part of tower reactor ontology, and liquid carries part bubble through circulating liquid
Outlet 107 continues cycling through, and gas continues upwardly into pre-reaction section, with the cold liquid charging stock contact heat-exchanging being added from top
Afterwards, enter steam generator 2 through offgas outlet 113, after temperature is down to 130 DEG C, into pressure reducing radiator 3.Pressure reducing radiator 3 is grasped
Make pressure be 1.5bar, and using by condenser conveying come the second condensate liquid (- 10 DEG C) condensing trapping gas phase in organic matter,
The first condensed fluid of gained (30 DEG C) send that the reaction was continued to pre-reaction section through the first condensate outlet；The tail that pressure reducing radiator 3 is discharged
Gas goes successively to condenser 4, using -30 DEG C of cryogenic freezing liquid cold-trap organic matter therein, and controls having in gas phase
Machine object amount, and give through the second condensate outlet to pressure reducing radiator 3, the tail gas that condenser 4 is discharged is sent to exhaust treatment system.Tower
The diameter of 1 lower part of formula reactor is 600mm, a height of 4000mm, pre-reaction section diameter 400mm, high 6000mm.Ultra-fine bubble breaking
Device 101 is 300mm high, and 5 gas-liquid channels 1012 are arranged.0.15mPa, 30m3/h air enter ultra-fine bubble through gas feed 102
The air chamber 1011 of destroyer 101 then enters gas-liquid channel 1012, is broken for by the high-speed liquid in gas-liquid channel 1012 micro-
Meter level bubble, and it is downwardly into tower reactor bottom together with liquid.The flow of circulating liquid is 4m3/ h, by heat exchanger
After 104, the temperature of circulation fluid is down to 145 DEG C.The toluene conversion per pass of entire reaction process is 20%, and benzaldehyde is selectively
7%, benzoic acid is selectively 90%.
In the description of this specification, reference term " one embodiment ", " some embodiments ", " illustrative examples ",
The description of " example ", " specific example " or " some examples " etc. means specific features described in conjunction with this embodiment or example, knot
Structure, material or feature are contained at least one embodiment or example of the utility model.In the present specification, to above-mentioned art
The schematic representation of language may not refer to the same embodiment or example.Moreover, description specific features, structure, material or
Person's feature can be combined in any suitable manner in any one or more of the embodiments or examples.
While there has been shown and described that the embodiments of the present invention, it will be understood by those skilled in the art that:
These embodiments can be carried out with a variety of variations, modification, replacement in the case where not departing from the principles of the present invention and objective
And modification, the scope of the utility model are defined by the claims and their equivalents.
Claims (10)
1. a kind of methylarenes oxidation system, which is characterized in that including liquid charging stock import, gas feed, product exit,
Tower reactor and ultra-fine bubble breaker, the ultra-fine bubble breaker are set to lower part in the tower reactor,
The ultra-fine bubble breaker includes air chamber and gas-liquid channel, and the gas feed passes through the tower by the first pipeline
The wall of formula reactor is connected to the air chamber, and the gas-liquid channel is vertically arranged in the air chamber, and the gas-liquid channel is
The pipeline of the air chamber is penetrated through, the pipe side wall is provided with the stomata of several connection air chambers, the gas-liquid channel
It is connected to the bottom of the tower reactor and the upper space of the ultra-fine bubble breaker,
The tower reactor includes that offgas outlet, circulating liquid outlet and circulating liquid import, the liquid charging stock import connect
Lead to the top of the tower reactor, the offgas outlet is set to the top of the tower reactor, and the circulating liquid goes out
Mouth passes through gas-liquid channel described in the circulating liquid inlet communication by liquid circulation line, and the liquid circulating pipe road is arranged
There is circulating pump, the liquid circulation line is connected to the product exit.
2. reaction system according to claim 1, which is characterized in that the top in the tower reactor is pre-reaction
The liquid charging stock import is arranged in section, the top of the pre-reaction section, and several first percolation towers are provided in the pre-reaction section
Plate.
3. reaction system according to claim 2, which is characterized in that the liquid circulating pipe road is additionally provided with gas-liquid point
From device, pre-reaction section described in the separation gas outlet of the gas-liquid separator.
4. reaction system according to claim 3, which is characterized in that the gas-liquid separator includes several second percolation towers
Plate and filler, second dual-flow tray are located at the filler top.
5. reaction system according to claim 1, which is characterized in that the offgas outlet is connected with steam generator, institute
It states the tail gas of tower reactor and provides thermal energy for the steam generator.
6. reaction system according to claim 1, which is characterized in that the offgas outlet is connected with pressure reducing radiator.
7. reaction system according to claim 6, which is characterized in that the pressure reducing radiator includes that the first condensate liquid goes out
Mouthful, first condensate outlet connects the tower reactor.
8. reaction system according to claim 6, which is characterized in that be provided with cooling tail at the top of the pressure reducing radiator
Gas outlet, the cooled exhaust gas outlet are connected with condenser, and the condenser includes the second condensate outlet, second condensation
Liquid outlet connects the tower reactor.
9. reaction system according to claim 8, which is characterized in that second condensate outlet is also connected with the decompression
Cooler.
10. reaction system according to claim 1, which is characterized in that the tower reactor further includes overflow baffle, institute
State overflow baffle and be arranged on the side wall of the tower reactor and close on circulating liquid outlet, the overflow baffle it is upper
Along the top for being located at circulating liquid outlet.
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| CN201821943291.8U CN209508088U (en) | 2018-11-23 | 2018-11-23 | A kind of methylarenes oxidation system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111217671A (en) * | 2018-11-23 | 2020-06-02 | 南京延长反应技术研究院有限公司 | Methyl aromatic hydrocarbon oxidation reaction system and use method thereof |
| CN111569788A (en) * | 2020-03-31 | 2020-08-25 | 南京延长反应技术研究院有限公司 | External micro-interface oxidation system and method for preparing terephthalic acid from p-xylene |
| WO2021097794A1 (en) * | 2019-11-22 | 2021-05-27 | 南京延长反应技术研究院有限公司 | Aerobic fermentation system and process |
-
2018
- 2018-11-23 CN CN201821943291.8U patent/CN209508088U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111217671A (en) * | 2018-11-23 | 2020-06-02 | 南京延长反应技术研究院有限公司 | Methyl aromatic hydrocarbon oxidation reaction system and use method thereof |
| WO2021097794A1 (en) * | 2019-11-22 | 2021-05-27 | 南京延长反应技术研究院有限公司 | Aerobic fermentation system and process |
| CN111569788A (en) * | 2020-03-31 | 2020-08-25 | 南京延长反应技术研究院有限公司 | External micro-interface oxidation system and method for preparing terephthalic acid from p-xylene |
| CN111569788B (en) * | 2020-03-31 | 2023-04-11 | 南京延长反应技术研究院有限公司 | External micro-interface oxidation system and method for preparing terephthalic acid from p-xylene |
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