CN208406934U - Unsym-trimethyl benzene oxidation separation device - Google Patents
Unsym-trimethyl benzene oxidation separation device Download PDFInfo
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- CN208406934U CN208406934U CN201820668199.9U CN201820668199U CN208406934U CN 208406934 U CN208406934 U CN 208406934U CN 201820668199 U CN201820668199 U CN 201820668199U CN 208406934 U CN208406934 U CN 208406934U
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- 238000000926 separation method Methods 0.000 title claims abstract description 51
- 238000007254 oxidation reaction Methods 0.000 title abstract description 25
- 230000003647 oxidation Effects 0.000 title abstract description 17
- 239000007788 liquid Substances 0.000 claims abstract description 103
- GWHJZXXIDMPWGX-UHFFFAOYSA-N 1,2,4-trimethylbenzene Chemical compound CC1=CC=C(C)C(C)=C1 GWHJZXXIDMPWGX-UHFFFAOYSA-N 0.000 claims abstract description 50
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 42
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 87
- 238000007664 blowing Methods 0.000 claims description 41
- 239000000945 filler Substances 0.000 claims description 25
- 238000010992 reflux Methods 0.000 claims description 18
- 208000002925 dental caries Diseases 0.000 claims description 12
- 238000009826 distribution Methods 0.000 claims description 8
- 239000000919 ceramic Substances 0.000 claims description 3
- 239000002826 coolant Substances 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims description 3
- 238000003466 welding Methods 0.000 claims description 2
- 230000015572 biosynthetic process Effects 0.000 claims 1
- 239000004744 fabric Substances 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 abstract description 22
- SRPWOOOHEPICQU-UHFFFAOYSA-N trimellitic anhydride Chemical compound OC(=O)C1=CC=C2C(=O)OC(=O)C2=C1 SRPWOOOHEPICQU-UHFFFAOYSA-N 0.000 abstract description 7
- 230000001590 oxidative effect Effects 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 21
- 238000000034 method Methods 0.000 description 16
- 239000012071 phase Substances 0.000 description 11
- 230000008569 process Effects 0.000 description 11
- 238000004519 manufacturing process Methods 0.000 description 7
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 6
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 6
- 238000001816 cooling Methods 0.000 description 6
- ARCGXLSVLAOJQL-UHFFFAOYSA-N trimellitic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C(C(O)=O)=C1 ARCGXLSVLAOJQL-UHFFFAOYSA-N 0.000 description 6
- 239000000203 mixture Substances 0.000 description 5
- 238000009835 boiling Methods 0.000 description 4
- 239000000376 reactant Substances 0.000 description 4
- 239000002904 solvent Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 150000008065 acid anhydrides Chemical class 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000012827 research and development Methods 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- RVHSTXJKKZWWDQ-UHFFFAOYSA-N 1,1,1,2-tetrabromoethane Chemical compound BrCC(Br)(Br)Br RVHSTXJKKZWWDQ-UHFFFAOYSA-N 0.000 description 1
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 229940006460 bromide ion Drugs 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003426 co-catalyst Substances 0.000 description 1
- 229940011182 cobalt acetate Drugs 0.000 description 1
- QAHREYKOYSIQPH-UHFFFAOYSA-L cobalt(II) acetate Chemical compound [Co+2].CC([O-])=O.CC([O-])=O QAHREYKOYSIQPH-UHFFFAOYSA-L 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 208000012839 conversion disease Diseases 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
- 229940071125 manganese acetate Drugs 0.000 description 1
- UOGMEBQRZBEZQT-UHFFFAOYSA-L manganese(2+);diacetate Chemical compound [Mn+2].CC([O-])=O.CC([O-])=O UOGMEBQRZBEZQT-UHFFFAOYSA-L 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 229910052573 porcelain Inorganic materials 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The application provides a pseudocumene oxidizing and separating device, which comprises an oxidizing kettle, a first-stage condenser, a vapor-liquid separating tower and a second-stage condenser, wherein an exhaust port is arranged on the oxidizing kettle and is communicated with the top of the first-stage condenser through a gas-phase pipeline; this application vapour-liquid separation efficiency is high, can keep the concentration of oxidation cauldron normal water in relatively lower state for the reaction can forward go on, improves trimellitic anhydride oxidation efficiency.
Description
Technical field
This application involves chemicals production engineering device technique fields more particularly to a kind of pseudocumene to aoxidize separator.
Background technique
In current acid anhydride production process partially, wherein industrial production trimellitic acid in oxidation operation, mainly uses inclined front three
Benzene liquid-phase air oxidation is produced, and the method is using pseudocumene as raw material, and with air oxidant, cobalt acetate and manganese acetate are
Major catalyst, tetrabromoethane are co-catalyst, under 200-220 DEG C and 2.0-2.3MPa pressure condition, are used in acetic acid solution
Pseudocumene is aoxidized and generates trimellitic acid by compressed air.This method consumption of raw materials is low；But the requirement to equipment is very high, it is main
If bromide ion difficulty removes, it is present in each process of inclined acid anhydride production, compared with corrosive equipment.Oxidation reaction process is that heat release is anti-
It answers, acetic acid is solvent, and under the action of exothermic heat of reaction, the water and solvent acetic acid for reacting generation are in high-temperature gas from reaction mass
It steams, is by raw material pseudocumene and solvent and promotor investment batching kettle in production at present for a large amount of consumption for avoiding acetic acid
It is sent into a feed chamber heating after heating mixing, is heated to be transferred to stills for air blowing reaction after initiation temperature again；Most of second of generation
The mixture of acid and water is back to after cooling in kettle in reaction solution, and trimellitic acid, acetic acid and the water of generation are transferred to crystallization together
Then kettle places into kettle depickling, dehydration, is back to concentrate recycling after acetic acid and water cooling.Stills for air blowing are used on oxidation unit
Top gas phase increases multi-stage condensing device and cools down to acetic acid steam, then is back in stills for air blowing, and even so, acetic acid still has greatly
Amount, which steams, not to be recycled, and rear road is emitted into the recycling of acetic acid tank by tail gas absorber absorption again, but during the reaction, great Liang Sheng
At water be also mingled with wherein, be back to the progress that reaction is affected in kettle, cause to have part material inclined three be carried over is not engaged in it is anti-
It answers, influences exhaust emissions index, and absorb heel row to acetic acid tank and carry out concentrate recycling, this solvent acetic acid after the recovery compares
The concentration of industrial acetic is low, and the increased water in part inhibits the progress of pseudocumene oxidation reaction again.So removal reaction life
Cheng Shui is most important to promotion oxidation reaction conversion ratio.
Therefore, how to be directed to disadvantage present in the above-mentioned prior art and carry out research and development improvement, actually exerted needed for relevant industry
Power research and development target, the application designer in view of this, be think and creation idea, designed then with the experience of many years, pass through
In many ways sampling test is inquired into and is studied, and repeatedly amendment improvement, be releasing the application.
Such as application No. is: 201520421013.6 Chinese patent discloses a kind of process tower vapor-liquid separating device, by
Tower top cooling system, tower bottom cooling system, heat-conducting oil heating system, process tower composition, wherein process tower include spray sprinkler head,
18 layers of float valve tray, 18 layers of float valve tray are distributed in process tower from bottom to up, and spray sprinkler head is located at the top of process tower, the
The upper end of 18 layers of float valve tray, it is characterized in that increasing Pall ring in two layers of 18 layers of float valve tray upper end of process tower；This application
In process of production, part ethylene glycol does random motion in Pall ring in the mixed vapour of uplink in process tower, increases it
Residence time in float valve tray makes full use of shower water to make its trapping that contacts with each other, and reduces ethylene glycol waste to reach
Purpose, but this application increases the reaction producing level of reactant by increasing residence time of the reactant in tower, in this way
Production efficiency is reduced instead, further increases production cost.
Summary of the invention
(1) technical problems to be solved
In view of above-mentioned technical problem, this application provides a kind of structure is simple, vapor-liquid separation efficiency is high, is able to maintain stills for air blowing
The concentration of middle water is in relatively low state, so that reaction positive can carry out, improves inclined the three of trimellitic anhydride oxidation efficiency
Toluene oxidation separator.
(2) technical solution
This application provides a kind of pseudocumenes to aoxidize separator, including stills for air blowing, first-stage condenser, vapor-liquid separation tower
And secondary condenser, the shell cooling medium of the secondary condenser are circulating water,
Stills for air blowing, the stills for air blowing are equipped with exhaust outlet, and the exhaust outlet passes through gas phase pipeline and the first-stage condenser
Top be connected,
Refluxing opening is additionally provided at the top of the stills for air blowing, the refluxing opening passes through the bottom of liquid pipe and the first-stage condenser
Portion is connected, and is back in the stills for air blowing for that will cool down acetic acid；
First-stage condenser, the first-stage condenser are equipped with steam network management, and the shell of the first-stage condenser accesses 90 DEG C
Hot water, the middle and lower part of the first-stage condenser is connected by gas phase pipeline with the vapor-liquid separation tower；
Vapor-liquid separation tower, the bottom of the vapor-liquid separation tower pass through the refluxing opening phase of liquid pipe and the stills for air blowing
Connection, for the acetic acid of vapor-liquid separation to be back in the stills for air blowing；
The top of the vapor-liquid separation tower at the top of gas phase pipeline and the second level condenser by being connected, the vapour-liquid
The top of knockout tower is additionally provided with inlet, and the inlet of the vapor-liquid separation tower is cool solidifying by liquid pipe and the second level
The bottom of device is connected, the reflux for condensate liquid；
The vapor-liquid separation tower is equipped with drain pipe, discharge of the drain pipe for the condensate liquid of reflux.
In some embodiments of the present application, the vapor-liquid separation tower further includes filler, distributor, collecting tank, annular receipts
Catch basin and collection ring flat-plate, the filler, the distributor, the collecting tank, the annular catch tray and the collection ring flat-plate are equal
Equipped with multiple.
In some embodiments of the present application, the filler and the distributor are welded to connect, and the distributor is removable
Distributor is unloaded, the collecting tank is arranged above the distributor, the side wall weldering for collecting ring flat-plate and the vapor-liquid separation tower
It connects in succession.
In some embodiments of the present application, the annular catch tray includes that two cavitys found bucket and overflow pipe, described to overflow
Flow tube setting is stood between bucket in two cavitys.
In some embodiments of the present application, two cavitys found the baffle and the ring baffle that bucket is the collecting tank
The cavity to be formed is welded with the vapor-liquid separation tower.
The overflow in liquid and the annular catch tray in some embodiments of the present application, in the collecting tank
Pipe is connected, and opening is equipped in the middle part of the collecting tank, and the overflow pipe runs through the opening of the collecting tank, passes through for condensate liquid
The distributor is distributed to filler downwards.
In some embodiments of the present application, two cavitys stand and are equipped with several baffle pieces above bucket, and the filler is pottery
Porcelain filling.
In some embodiments of the present application, there are two the drain pipe is set, the drain pipe is arranged at the vapour-liquid
Knockout tower is connected on side wall with the collecting tank.
In some embodiments of the present application, the secondary condenser is gone back on the side wall of vapor-liquid separation tower one end
Equipped with gas outlet, for discharging not cooled steam.
In some embodiments of the present application, liquid thermometer, the liquid phase is arranged in secondary condenser bottom bobbin carriage
Thermometer adjusts valve regulation temperature by circulating water.
(3) beneficial effect
It can be seen from the above technical proposal that the application at least has the advantages that one of them:
(1) pseudocumene provided by the present application aoxidizes separator, and reactant is discharged in the reaction water that oxidation reaction is generated
System, acetic acid Returning reacting system keep the concentration of water in stills for air blowing to be in relatively low state, ensure that reaction forward into
Row, improves trimellitic anhydride oxidation efficiency；
(2) pseudocumene oxidation separator provided by the present application can be by oxidation reaction by the first-stage condenser of setting
The heat of generation is shifted by way of heat exchange to be used for steam for other processes；
(3) pseudocumene provided by the present application aoxidizes separator, filler, the distributor, receipts being arranged in vapor-liquid separation tower
Collect slot, annular catch tray and collect ring flat-plate, condensed fluid can be made by distribution, and the liquid to after being collected below slot is uniformly distributed, and is guaranteed
Density of the liquid distribution in filler；
(4) pseudocumene oxidation separator provided by the present application makes largely to be gathered in collection by the drain pipe of setting
Water discharge in slot, allows the water of generation to be no longer back in stills for air blowing, the concentration of water in stills for air blowing is kept to be in relatively low shape
State, so that reaction positive can carry out；
(5) pseudocumene provided by the present application aoxidizes separator, and structure is simple, and vapor-liquid separation efficiency is high, is able to maintain oxygen
The concentration for changing water in kettle is in relatively low state, so that reaction positive can carry out, improves trimellitic anhydride oxidation efficiency,
Conducive to large-scale promotion.
Detailed description of the invention
Fig. 1 is the structural schematic diagram that the application pseudocumene aoxidizes separator.
[the application main element symbol description]
1, stills for air blowing；101, refluxing opening；102, exhaust outlet；2, first-stage condenser；3, vapor-liquid separation tower；4, B-grade condensation
Device；5, filler；6, distributor；7, collecting tank；8, overflow pipe；9, drain pipe；10, ring flat-plate is collected；11, gas outlet.
Specific embodiment
This application provides a kind of structure is simple, vapor-liquid separation efficiency is high, and the concentration for being able to maintain water in stills for air blowing is in phase
Trimellitic anhydride oxidation efficiency is improved, conducive to inclined the three of large-scale promotion so that reaction positive can carry out to lower state
Toluene oxidation separator.
For the purposes, technical schemes and advantages of the application are more clearly understood, below in conjunction with specific embodiment, and reference
The application is further described in attached drawing.
In the exemplary embodiment of the application, a kind of pseudocumene oxidation separator is provided.Such as Fig. 1 institute
Show, the application includes stills for air blowing 1, first-stage condenser 2, vapor-liquid separation tower 3 and secondary condenser 4, the shell of the secondary condenser 4
Layer cooling medium is circulating water,
Stills for air blowing 1, the stills for air blowing 1 are equipped with exhaust outlet 102, and the exhaust outlet 102 passes through gas phase pipeline and described one
The top of grade condenser 2 is connected,
Refluxing opening 101 is additionally provided at the top of the stills for air blowing 1, the refluxing opening 101 is cold by liquid pipe and the level-one
The bottom of condenser 2 is connected, and is back in the stills for air blowing 1 for that will cool down acetic acid；
First-stage condenser 2, the first-stage condenser 2 are equipped with steam network management, the shell access 90 of the first-stage condenser 2
DEG C hot water, the middle and lower part of the first-stage condenser 2 is connected by gas phase pipeline with the vapor-liquid separation tower 33；
Vapor-liquid separation tower 3, the bottom of the vapor-liquid separation tower 3 pass through the reflux of liquid pipe and the stills for air blowing 11
Mouth 101 is connected, for the acetic acid of vapor-liquid separation to be back in the stills for air blowing 1；
The top of the vapor-liquid separation tower 3 at the top of gas phase pipeline and the second level condenser by being connected, the vapour
The top of liquid knockout tower 3 is additionally provided with inlet, and the inlet of the vapor-liquid separation tower 3 passes through liquid pipe and the second level
The bottom of condenser is connected, the reflux for condensate liquid；
The vapor-liquid separation tower 3 is equipped with drain pipe 9, discharge of the drain pipe 9 for the condensate liquid of reflux；The application
Reaction system is discharged in the reaction water that oxidation reaction is generated, and acetic acid Returning reacting system keeps the concentration of water in stills for air blowing 1 to be in
Relatively low state ensure that reaction forward carries out, improve trimellitic anhydride oxidation efficiency.
Each component part of the present embodiment is described in detail individually below:
Specifically, in this embodiment of the application, as shown in Figure 1, the vapor-liquid separation tower 3 further includes filler 5, distribution
Device 6, collecting tank 7, annular catch tray and collection ring flat-plate 10, the filler 5, the distributor 6, the collecting tank 7, the annular
Catch tray and the collection ring flat-plate 10 are equipped with multiple, condensed water and the vapor of rising can be filtered for multiple times, and
Condensed water is discharged.
Specifically, the filler 5 is welded to connect with the distributor 6, the distributor 6 is detachable distributor 6, described
Collecting tank 7 is arranged above the distributor 6, and the collection ring flat-plate 10 is connect with the sidewall weld of the vapor-liquid separation tower 3, if
The dismountable distributor 6 set can adjust the quantity of 6 distributor pipe of distributor according to the amount and reaction environment of different reactants,
Adaptability is stronger.
Specifically, in this embodiment of the application, as shown in Figure 1, the annular catch tray includes that two cavitys found bucket
With overflow pipe 8, the setting of overflow pipe 8 is stood between bucket in two cavitys；Two cavitys found the gear that bucket is the collecting tank 7
The cavity that plate and the welding of the ring baffle and the vapor-liquid separation tower 3 are formed, can be used to store liquid；
Specifically, the liquid in the collecting tank 7 is connected with the overflow pipe 8 in the annular catch tray, it is described
Opening is equipped in the middle part of collecting tank 7, the overflow pipe 8 runs through the opening of the collecting tank 7, passes through the distributor for condensate liquid
6 are distributed to filler 5 downwards；The filler 5 that is arranged in the application vapor-liquid separation tower, distributor 6, collecting tank 7, annular catch tray and
Ring flat-plate 10 is collected, condensed fluid can be made by distribution, and the liquid to after being collected below slot 7 is uniformly distributed, and ensure that liquid distribution in filling out
The density of material 5.
Specifically, in this embodiment of the application, as shown in Figure 1, two cavitys, which are stood, is equipped with several baffles above bucket
Piece, the filler 5 are ceramic packing.The cavity of setting, which founds bucket baffle piece, to lead to annular receipts for the whereabouts liquid of top filler 5
In catch basin, gas continues to rise by distributor 6 and annular catch tray gap；Further increase the efficiency of vapor-liquid separation.
Specifically, the drain pipe 9 is arranged at the same side wall of the vapor-liquid separation tower 3 there are two the drain pipe 9 sets
On, it is connected with the collecting tank 7, further, the bottom of collecting tank 7, the row that the application passes through setting is arranged in leakage fluid dram 9
Liquid pipe 9 is discharged the water being largely gathered in collecting tank 7, the water of generation is allowed no longer to be back in stills for air blowing 1, keeps in stills for air blowing 1
The concentration of water is in relatively low state, so that reaction positive can carry out.
Specifically, in this embodiment of the application, as shown in Figure 1, the secondary condenser 4 is close to the vapor-liquid separation
It is additionally provided with gas outlet 11 on the side wall of 3 one end of tower, for discharging not cooled steam；The 4 bottom bobbin carriage of secondary condenser
Liquid thermometer is set, and the liquid thermometer adjusts valve regulation temperature by circulating water.
Specific working principle: stills for air blowing 1 carry out pseudocumene oxidation reaction during acetic acid steam by with exhaust outlet 102
The gas phase pipeline of connection enters inside first-stage condenser 2,2 shell of first-stage condenser access 90 DEG C of hot water and with high temperature acetic acid steam
The steam for generating 0.8MPa after heat exchange is sent outside to steam pipe network；The acetic acid of 2 bottom coohng of first-stage condenser passes through 1 top of stills for air blowing
Refluxing opening 101 is back in stills for air blowing 1, and continuation goes out the torrid zone that oxidation reaction generates, and ensure that the safety of reaction carries out, not cold
But part acetic acid and a large amount of aqueous mixtures that generate enters vapor-liquid separation tower 3, and 3 top of vapor-liquid separation tower is provided with vapour-liquid mass point
From ceramic packing section filler 5,5 sections of filler top welds dismountable distributors 6, is collecting tank 7 above distributor 6, collects
Slot 7 is connect with the overflow pipe 8 of annular catch tray, and 3 top of vapor-liquid separation tower at the top of gas phase pipeline and secondary condenser 4 by connecting
It connects, lower part is separately connected 1 overhead reflux mouth 101 of first-stage condenser 2 and stills for air blowing.2 bottom of first-stage condenser enters vapor-liquid separation
Acetic acid and aqueous mixtures in tower 3, since the boiling point under acetic acid normal pressure is 117.9 DEG C, higher than the boiling point of water, in suction function
Under, the boiling point of acetic acid, which remains unchanged, is higher than the boiling point of water, and therefore, the result of heat exchange becomes the part water in liquid on steam again
It rises, and the part acetic acid in tail gas is captured into liquid, by the gas-liquid separation tower of gas-liquid separator, so that reaching second level
In the gas of the lower section of condenser 4,95% the above are water vapour, only a small amount of acetic acid steam, gases to continue to ascend into second level
Condenser 4, in secondary condenser 4, through cooling, (it is recirculated water that secondary condenser, which condenses 4 shell cooling mediums, and bottom bobbin carriage is set
Liquid thermometer is set, temperature is adjusted by circulation water regulating valve), heat is taken away, so that the steam in secondary condenser 4 is condensed into
Liquid, condensed liquid flow downwardly into collecting tank 7, and the overflow pipe 8 of the intermediate setting high liquid level of collecting tank 7 can make in this way
A large amount of water aggregation is obtained here, being then discharged by the drain pipe 9 of 7 bottom of collecting tank, the water of generation is allowed no longer to be back to stills for air blowing 1
It is interior；The uncooled gas in part continues to rise, and can be discharged from gas outlet 11 and carry out subsequent processing.Condensed liquid removes fraction
Outside being discharged, again from 8 overflow of overflow pipe after most of full collecting tank 7 of stream, progress gas-liquid point in filler 5 is entered after distributor 6
From ensure that baffle of the liquid distribution above the density of filler 5, the vertical bucket of two cavitys is by the whereabouts liquid of top filler 5
Body is led in annular catch tray, and gas continues to rise by distributor 6 and annular catch tray gap；As liquid trickles downwards,
The content of acetic acid constantly increases, and flows into tower body bottom, is then back in stills for air blowing 1 in the refluxing opening 101 through stills for air blowing 1；It protects
The concentration for holding water in stills for air blowing 1 is in relatively low state, so that reaction positive can carry out, improves trimellitic anhydride oxidation
Efficiency.
So far, attached drawing is had been combined the present embodiment is described in detail.According to above description, those skilled in the art
There should be clear understanding to the application.
It should be noted that in attached drawing or specification text, the implementation for not being painted or describing is affiliated technology
Form known to a person of ordinary skill in the art, is not described in detail in field.In addition, the above-mentioned definition to each element and method is simultaneously
It is not limited only to various specific structures, shape or the mode mentioned in embodiment.
It should also be noted that, can provide the demonstration of the parameter comprising particular value herein, but these parameters are without definite etc.
In corresponding value, but analog value can be similar in acceptable error margin or design constraint.The side mentioned in embodiment
It is only the direction with reference to attached drawing to term, such as "upper", "lower", "front", "rear", "left", "right" etc., is not used to limit this
The protection scope of application.In addition, unless specifically described or the step of must sequentially occur, the sequences of above-mentioned steps there is no restriction in
It is listed above, and can change or rearrange according to required design.And above-described embodiment can be based on design and reliability
Consider, the collocation that is mixed with each other is used using or with other embodiments mix and match, i.e., the technical characteristic in different embodiments can be with
Freely form more embodiments.
Particular embodiments described above has carried out further in detail the purpose of the application, technical scheme and beneficial effects
Describe in detail it is bright, it is all it should be understood that be not intended to limit this application the foregoing is merely the specific embodiment of the application
Within spirit herein and principle, any modification, equivalent substitution, improvement and etc. done should be included in the guarantor of the application
Within the scope of shield.
Claims (10)
1. a kind of pseudocumene aoxidizes separator, it is characterised in that: including stills for air blowing (1), first-stage condenser (2), vapour-liquid point
From tower (3) and secondary condenser (4), the shell cooling medium of the secondary condenser (4) is circulating water,
Stills for air blowing (1), the stills for air blowing (1) are equipped with exhaust outlet (102), and the exhaust outlet (102) passes through gas phase pipeline and institute
It states and is connected at the top of first-stage condenser (2),
It is additionally provided with refluxing opening (101) at the top of the stills for air blowing (1), the refluxing opening (101) passes through liquid pipe and the level-one
The bottom of condenser (2) is connected, and is back in the stills for air blowing (1) for that will cool down acetic acid；
First-stage condenser (2), the first-stage condenser (2) are equipped with steam network management, and the shell of the first-stage condenser (2) accesses
The middle and lower part of 90 DEG C of hot water, the first-stage condenser (2) is connected by gas phase pipeline with the vapor-liquid separation tower (3) 3；
The bottom of vapor-liquid separation tower (3), the vapor-liquid separation tower (3) passes through liquid pipe and described time of the stills for air blowing (1) 1
Head piece (101) is connected, for the acetic acid of vapor-liquid separation to be back in the stills for air blowing (1)；
The top of the vapor-liquid separation tower (3) at the top of gas phase pipeline and the second level condenser by being connected, the vapour-liquid
The top of knockout tower (3) is additionally provided with inlet, and the inlet of the vapor-liquid separation tower (3) passes through liquid pipe and described two
The bottom of grade condenser is connected, the reflux for condensate liquid；
The vapor-liquid separation tower (3) is equipped with drain pipe (9), discharge of the drain pipe (9) for the condensate liquid of reflux.
2. pseudocumene according to claim 1 aoxidizes separator, it is characterised in that: the vapor-liquid separation tower (3) is also
Including filler (5), distributor (6), collecting tank (7), annular catch tray and ring flat-plate (10) are collected, the filler (5), the distribution
Device (6), the collecting tank (7), the annular catch tray and the collection ring flat-plate (10) are equipped with multiple.
3. pseudocumene according to claim 2 aoxidizes separator, it is characterised in that: the filler (5) and described point
Cloth device (6) is welded to connect, and the distributor (6) is detachable distributor (6), and the collecting tank (7) is arranged in the distributor
(6) top, collection ring flat-plate (10) connect with the sidewall weld of the vapor-liquid separation tower (3).
4. pseudocumene according to claim 2 aoxidizes separator, it is characterised in that: the annular catch tray includes two
A cavity founds bucket and overflow pipe (8), and overflow pipe (8) setting is stood between bucket in two cavitys.
5. pseudocumene according to claim 4 aoxidizes separator, it is characterised in that: it is described that two cavitys, which found bucket,
The baffle of collecting tank (7) and the cavity for collecting ring flat-plate (10) and the vapor-liquid separation tower (3) welding formation.
6. pseudocumene according to claim 4 aoxidizes separator, it is characterised in that: the liquid in the collecting tank (7)
Body is connected with the overflow pipe (8) in the annular catch tray, and opening, the overflow are equipped in the middle part of the collecting tank (7)
The opening that (8) run through the collecting tank (7) is managed, for condensate liquid by the distributor (6) downwards distribution to filler (5).
7. pseudocumene according to claim 6 aoxidizes separator, it is characterised in that: two cavitys stand and set above bucket
There are several baffle pieces, the filler (5) is ceramic packing.
8. pseudocumene according to claim 2 aoxidizes separator, it is characterised in that: the drain pipe (9) is equipped with two
A, the drain pipe (9) is arranged at the vapor-liquid separation tower (3) on side wall, is connected with the collecting tank (7).
9. pseudocumene according to claim 1 aoxidizes separator, it is characterised in that: the secondary condenser (4) is leaned on
Gas outlet (11) are additionally provided on the side wall of nearly described vapor-liquid separation tower (3) one end, for discharging not cooled steam.
10. pseudocumene according to claim 9 aoxidizes separator, it is characterised in that: secondary condenser (4) bottom
Liquid thermometer is arranged in portion's bobbin carriage, and the liquid thermometer adjusts valve regulation temperature by circulating water.
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| CN201820668199.9U CN208406934U (en) | 2018-05-04 | 2018-05-04 | Unsym-trimethyl benzene oxidation separation device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108355593A (en) * | 2018-05-04 | 2018-08-03 | 南通百川新材料有限公司 | Unsym-trimethyl benzene oxidation separation device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108355593A (en) * | 2018-05-04 | 2018-08-03 | 南通百川新材料有限公司 | Unsym-trimethyl benzene oxidation separation device |
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