CN203653465U - Continuous production device for benzoic acid - Google Patents
Continuous production device for benzoic acid Download PDFInfo
- Publication number
- CN203653465U CN203653465U CN201320704922.1U CN201320704922U CN203653465U CN 203653465 U CN203653465 U CN 203653465U CN 201320704922 U CN201320704922 U CN 201320704922U CN 203653465 U CN203653465 U CN 203653465U
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- tower
- hood
- gas
- rotating disk
- reaction
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- WPYMKLBDIGXBTP-UHFFFAOYSA-N benzoic acid Chemical compound OC(=O)C1=CC=CC=C1 WPYMKLBDIGXBTP-UHFFFAOYSA-N 0.000 title claims abstract description 38
- 238000010924 continuous production Methods 0.000 title claims abstract description 18
- 239000005711 Benzoic acid Substances 0.000 title abstract 6
- 235000010233 benzoic acid Nutrition 0.000 title abstract 6
- 238000006243 chemical reaction Methods 0.000 claims abstract description 52
- 239000007788 liquid Substances 0.000 claims abstract description 30
- 238000009826 distribution Methods 0.000 claims abstract description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 9
- 238000007599 discharging Methods 0.000 claims abstract description 7
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 68
- 239000007789 gas Substances 0.000 claims description 39
- 238000010521 absorption reaction Methods 0.000 claims description 10
- 230000008676 import Effects 0.000 claims description 6
- 239000011148 porous material Substances 0.000 claims description 6
- 239000007792 gaseous phase Substances 0.000 claims description 3
- 238000009434 installation Methods 0.000 claims description 3
- 239000007791 liquid phase Substances 0.000 claims description 3
- 239000007858 starting material Substances 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 12
- 239000000047 product Substances 0.000 abstract description 7
- 239000006227 byproduct Substances 0.000 abstract description 6
- 238000001816 cooling Methods 0.000 abstract description 6
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 239000003054 catalyst Substances 0.000 abstract description 3
- 238000001704 evaporation Methods 0.000 abstract 1
- 230000008020 evaporation Effects 0.000 abstract 1
- 238000006555 catalytic reaction Methods 0.000 description 3
- 238000007600 charging Methods 0.000 description 3
- 238000010923 batch production Methods 0.000 description 2
- SESFRYSPDFLNCH-UHFFFAOYSA-N benzyl benzoate Chemical compound C=1C=CC=CC=1C(=O)OCC1=CC=CC=C1 SESFRYSPDFLNCH-UHFFFAOYSA-N 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- LPNBBFKOUUSUDB-UHFFFAOYSA-N p-toluic acid Chemical compound CC1=CC=C(C(O)=O)C=C1 LPNBBFKOUUSUDB-UHFFFAOYSA-N 0.000 description 2
- 230000021715 photosynthesis, light harvesting Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 150000003613 toluenes Chemical class 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- WVDDGKGOMKODPV-UHFFFAOYSA-N Benzyl alcohol Chemical compound OCC1=CC=CC=C1 WVDDGKGOMKODPV-UHFFFAOYSA-N 0.000 description 1
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229960004217 benzyl alcohol Drugs 0.000 description 1
- 235000019445 benzyl alcohol Nutrition 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
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 239000011572 manganese Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- -1 phenyl aldehydes Chemical class 0.000 description 1
- 230000001020 rhythmical effect Effects 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to a continuous production device for benzoic acid. The continuous production device comprises a reaction tower, a cooling device, an oil-water separator and an absorbing tower, wherein one or more gas-liquid distribution stirrers communicated with a gas inlet are arranged at the bottom inside the reaction tower; two tubular heat exchangers are arranged at the middle part of the reaction tower; and a benzoic acid discharging hole at the upper part of the reaction tower is connected with a benzoic acid flash evaporation tower. According to the continuous production device for benzoic acid disclosed by the utility model, selectivity of a catalyst to a benzoic acid product, gas-liquid mixing and heat exchange can be improved by adopting the device to realize continuous production, and therefore, energy consumption in the process is lowered, low-pressure steam can be continuously produced, product quality and productivity can be improved, byproducts can be reduced, and production cost can be lowered.
Description
Technical field
The utility model relates to phenylformic acid field, especially a kind of phenylformic acid continuous production device.
Background technology
Industrial phenylformic acid is to make with atmospheric oxidation toluene under the catalyzer such as cobalt, manganese exists.Because catalyzed reaction is exothermic process and catalyzer is high to temperature requirement, dependency is strong, therefore temperature is higher, and catalyzed reaction is faster, catalyzed reaction is faster, and temperature is just higher, forms vicious cycle, therefore too high, the poor selectivity of catalyst activity, can cause that by product increases, poor selectivity.Along with temperature constantly raises, even there will be temperature runaway, cause reaction tower out of control, set off an explosion.Gas and methylbenzene raw material all enter from reaction tower bottom at present, because gas distribution is inhomogeneous, cause catalyst selectivity poor, cause the problem such as low conversion rate and by product height to occur.In sum, in order to control the selectivity of temperature and the process of raising, ensure safety in production, benzoic batch production technique just becomes to be the theme.
Batch production technique (discontinuous reaction) is that charging, discharging and cleaning need to complete under stopped status, though this rhythmic reaction be widely used, but there is many defects in it:
1, reaction is to carry out at a certain temperature, so the every batch of initial material all needs heating, and enter normal oxidising process need cooling, so cause energy consumption large.
2, charging and discharging need to shut down, and lose time, reduce work efficiency.
3, when gas is discharged, can take part toluene out of, this toluene is 160 ℃ of left and right, must carry out cooling process.Conventionally adopt water coolant to carry out at present cooling, the water coolant after heat exchange becomes hot water, and because existing reaction is discontinuous reaction, the hot water therefore obtaining after heat exchange can not effectively recycle, and causes equally energy dissipation.
4, reaction tower inner air pressure is 0.7Mpa, need to use air compressor to maintain, and when charging and discharging, compressor, substantially in idling conditions, wastes energy.
5, unit volume output is little.
6, the heat temperature raising process in reaction is to be first preheating to 110 ℃, passes into part 0.7Mpa air, and heat release is warming up to 160 ℃, and then passes into air reaction, more cooling.This reaction process temperature is wayward, and excess Temperature or the too low by products such as a large amount of phenyl aldehydes, phenylcarbinol, peruscabin that all can produce, cause unstable product quality, low conversion rate, and transformation efficiency is generally 50-55% at present.
7, after cooling, there are catalyzer, peruscabin can how much have some to be deposited in reactor bottom, need stop cleaning, cause the working hour to extend.
8, employment is many, cost is high.
Summary of the invention
The purpose of this utility model is to overcome the deficiencies in the prior art, provides a kind of and can increase work efficiency, products quality guarantee, minimizing energy dissipation, improves the phenylformic acid continuous production device of conversion rate of products.
The utility model solves its technical problem and is achieved through the following technical solutions:
A kind of phenylformic acid continuous production device, comprise reaction tower, refrigerating unit, water-and-oil separator and absorption tower, the bottom of reaction tower arranges toluene liquid inlet opening and inlet mouth, the pneumatic outlet at reaction tower top connects refrigerating unit, the gaseous phase outlet of this refrigerating unit connects absorption tower, the toluene liquid inlet opening of one of them outlet ligation tower on absorption tower; The liquid-phase outlet of refrigerating unit connects a water-and-oil separator, the toluene liquid inlet opening of one of them outlet ligation tower of this water-and-oil separator, it is characterized in that: one or more gas-liquid distribution agitator being communicated with inlet mouth is installed in the bottom of reaction tower inside, the middle part of reaction tower arranges two tubular heat exchangers, and the phenylformic acid discharge port on reaction tower top connects a phenylformic acid flashing tower.
And, described gas-liquid distribution agitator comprises hood-shaped rotating disk and inlet pipe, on the cover body of this hood-shaped rotating disk, make one group of pore, hood-shaped rotating disk coaxial rotation is arranged on the upper end of inlet pipe, on the sidewall of inlet pipe, make the gas branch pipes of discharging more, this goes out gas branch pipe and is all connected with inlet pipe and is positioned at hood-shaped rotating disk inside, and one group of baffle plate is installed on the inner side-wall of hood-shaped rotating disk, the corresponding baffle plate of every discharge gas branch pipe.
And described inlet pipe is L shaped pipe, vertical section of this L shaped pipe is stretched in hood-shaped rotating disk, and this is vertically connected with hood-shaped dial rotation the upper end of section, goes out gas branch pipe and is installed in vertical section above and is connected with vertical intersegmental part.
And, along the circumferential uniform four discharge gas branch pipes of making, on the inner side-wall of hood-shaped rotating disk, along four baffle plates of circumferential uniform installation, this baffle plate all vertically arranges on the sidewall of described inlet pipe.
And described inlet pipe axle center is less than the distance of axle center to baffle plate to the distance that goes out gas branch pipe outermost edge.
And the angle between described baffle plate and hood-shaped rotating disk inner side-wall is 50-70 degree; Described go out the exit angle of gas branch pipe be 50-70 degree.
And two described tubular heat exchanger series connection arrange, the general import of this tubular heat exchanger is connected with an interchanger flashing tower with general export, on this interchanger flashing tower, water at low temperature import is installed, and the top of this interchanger flashing tower arranges low-pressure steam outlet.
And, the outlet of the toluene gas of described phenylformic acid flashing tower with enter reaction tower toluene liquid starting material pipeline and be connected.
Advantage of the present utility model and beneficial effect are:
1, this device is by installing one or more gas-liquid distribution agitator in the bottom of reaction tower, air distribution is controlled and the gas-liquid mixture of reaction tower bottom is stirred by gas-liquid distribution agitator, can make the reaction of reaction tower bottom evenly, be conducive to keep catalyzer gentle stable, the heat exchange that act as of stirring provides good condition, thereby can maintain the equilibrium of reaction tower bottom temp, be similarly benzoic continuous production processes and provide the foundation.In addition, the operation of this gas-liquid distribution agitator does not need power, energy-conserving and environment-protective.
2, this device adopts the tubular heat exchanger of two series connection to control the temperature of reaction in reaction tower, has guaranteed that temperature of reaction maintains a stable scope, is similarly benzoic continuous production processes and provides the foundation.
3, owing to using this device can realize continuous production, therefore can Reaction time shorten, improve transformation efficiency, reduce by product.
4, in this device, tubular heat exchanger is exported continuous water vapour (133 ℃, 0.3Mpa), for other explained hereafter of later stage, can play the effect of energy-saving and emission-reduction.
5, use this device can be shortened to 6.4h left and right the reaction times, thereby enhance productivity.In addition, this device also has and can reduce air compressor energy consumption, reduces the plurality of advantages such as cost of labor.
6, the reaction tower of this device connects a phenylformic acid flashing tower, and it can separate 40% unconverted toluene gas, and this toluene gas is got back to opening for feed, can improve the inlet temperature of methylbenzene raw material.
7, in phenylformic acid flashing tower, water-and-oil separator and the absorption tower in this device, the toluene gas of isolating is all got back to the toluene liquid inlet opening of reaction tower, the serialization of implementation procedure.
8, the utility model is a kind of phenylformic acid continuous production device, owing to adopting this device can improve selectivity, gas-liquid mixed and the thermal exchange of catalyzer para Toluic Acid product, realize continuously and producing, therefore in having reduced process energy consumption, production low-pressure steam continuously, improves the quality of products with production capacity, reduces by product, reduces production costs.
Accompanying drawing explanation
Fig. 1 is schematic diagram of the present utility model;
Fig. 2 is the front view of distribution agitator;
Fig. 3 is the sectional view of Fig. 2;
Fig. 4 is the schematic top plan view one (removing the upper surface of hood-shaped rotating disk) of Fig. 2;
Fig. 5 is the schematic top plan view two (removing the upper surface of hood-shaped rotating disk) of Fig. 2.
Embodiment
Below by specific embodiment, the utility model is described in further detail, and following examples are descriptive, is not determinate, can not limit protection domain of the present utility model with this.
A kind of phenylformic acid continuous production device, comprise reaction tower 4, refrigerating unit 2, water-and-oil separator 3 and absorption tower 1, the bottom of reaction tower arranges toluene liquid inlet opening and inlet mouth, the pneumatic outlet at reaction tower top connects refrigerating unit, the gaseous phase outlet of this refrigerating unit connects absorption tower, the toluene liquid inlet opening of one of them outlet ligation tower on absorption tower; The liquid-phase outlet of refrigerating unit connects a water-and-oil separator, the toluene liquid inlet opening of one of them outlet ligation tower of this water-and-oil separator.
Innovative point of the present utility model is: one or more gas-liquid distribution agitator 5 being communicated with inlet mouth is installed in the bottom of reaction tower inside, this gas-liquid distribution agitator comprises hood-shaped rotating disk 10 and inlet pipe 11, on the cover body of this hood-shaped rotating disk, make one group of pore 9, this pore built in the top board of hood-shaped rotating disk cover body and or sidewall on, pore quantity is not limit, and diameter can be adjusted as required.Hood-shaped rotating disk coaxial rotation is arranged on the upper end of inlet pipe, makes the gas branch pipes 12 of discharging on the sidewall of inlet pipe more, as shown in Figure 4 and Figure 5, goes out gas branch pipe shape and does not limit, and this goes out gas branch pipe and is all connected with inlet pipe and is positioned at hood-shaped rotating disk inside.Its concrete syndeton is: inlet pipe is L shaped pipe, and vertical section of this L shaped pipe is stretched in hood-shaped rotating disk, and this is vertically connected with hood-shaped dial rotation the upper end of section, goes out gas branch pipe and is installed in vertical section above and is connected with vertical intersegmental part.
One group of baffle plate 13 is installed, the corresponding baffle plate of every discharge gas branch pipe on the inner side-wall of hood-shaped rotating disk.Angle between baffle plate and hood-shaped rotating disk inner side-wall is 50-70 degree, and the exit angle that goes out gas branch pipe is also 50-70 degree, and inlet pipe axle center is less than the distance of axle center to baffle plate to the distance that goes out gas branch pipe outermost edge, when avoiding rotating baffle plate with go out gas branch pipe and bump.The quantity of baffle plate and the row that goes out gas branch pipe are not limit, and in the present embodiment, on the sidewall of inlet pipe, along circumferential uniform four discharge gas branch pipes of making, on the inner side-wall of hood-shaped rotating disk, along four baffle plates of circumferential uniform installation, this baffle plate all vertically arranges.Between every discharge gas branch pipe and baffle plate separately, all form a gas shock region 14, pore is arranged on the hood-shaped rotating disk faceshield side wall and or top board away from this region.
The middle part of reaction tower arranges two tubular heat exchangers 6, these two tubular heat exchanger series connection arrange, the general import of this tubular heat exchanger is connected with an interchanger flashing tower 7 with general export, on this interchanger flashing tower, water at low temperature import is installed, and the top of this interchanger flashing tower arranges low-pressure steam outlet.
The phenylformic acid discharge port on reaction tower top connects a phenylformic acid flashing tower 8, the toluene liquid inlet opening of the toluene gas outlet ligation tower of this phenylformic acid flashing tower.
Claims (8)
1. a phenylformic acid continuous production device, comprise reaction tower, refrigerating unit, water-and-oil separator and absorption tower, the bottom of reaction tower arranges toluene liquid inlet opening and inlet mouth, the pneumatic outlet at reaction tower top connects refrigerating unit, the gaseous phase outlet of this refrigerating unit connects absorption tower, the toluene liquid inlet opening of one of them outlet ligation tower on absorption tower; The liquid-phase outlet of refrigerating unit connects a water-and-oil separator, the toluene liquid inlet opening of one of them outlet ligation tower of this water-and-oil separator, it is characterized in that: one or more gas-liquid distribution agitator being communicated with inlet mouth is installed in the bottom of reaction tower inside, the middle part of reaction tower arranges two tubular heat exchangers, and the phenylformic acid discharge port on reaction tower top connects a phenylformic acid flashing tower.
2. phenylformic acid continuous production device according to claim 1, it is characterized in that: described gas-liquid distribution agitator comprises hood-shaped rotating disk and inlet pipe, on the cover body of this hood-shaped rotating disk, make one group of pore, hood-shaped rotating disk coaxial rotation is arranged on the upper end of inlet pipe, on the sidewall of inlet pipe, make the gas branch pipes of discharging more, this goes out gas branch pipe and is all connected with inlet pipe and is positioned at hood-shaped rotating disk inside, and one group of baffle plate is installed on the inner side-wall of hood-shaped rotating disk, the corresponding baffle plate of every discharge gas branch pipe.
3. gas liquid reaction distribution agitator according to claim 2, it is characterized in that: described inlet pipe is L shaped pipe, vertical section of this L shaped pipe is stretched in hood-shaped rotating disk, this is vertically connected with hood-shaped dial rotation the upper end of section, goes out gas branch pipe and is installed in vertical section above and is connected with vertical intersegmental part.
4. gas liquid reaction distribution agitator according to claim 2, is characterized in that: on the sidewall of described inlet pipe, along the circumferential uniform four discharge gas branch pipes of making, on the inner side-wall of hood-shaped rotating disk, along four baffle plates of circumferential uniform installation, this baffle plate all vertically arranges.
5. gas liquid reaction distribution agitator according to claim 2, is characterized in that: described inlet pipe axle center is less than the distance of axle center to baffle plate to the distance that goes out gas branch pipe outermost edge.
6. gas liquid reaction distribution agitator according to claim 2, is characterized in that: the angle between described baffle plate and hood-shaped rotating disk inner side-wall is 50-70 degree; Described go out the exit angle of gas branch pipe be 50-70 degree.
7. phenylformic acid continuous production device according to claim 1, it is characterized in that: two described tubular heat exchanger series connection arrange, the general import of this tubular heat exchanger is connected with an interchanger flashing tower with general export, on this interchanger flashing tower, water at low temperature import is installed, the top of this interchanger flashing tower arranges low-pressure steam outlet.
8. phenylformic acid continuous production device according to claim 1, is characterized in that: the outlet of the toluene gas of described phenylformic acid flashing tower with enter reaction tower toluene liquid starting material pipeline and be connected.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320704922.1U CN203653465U (en) | 2013-11-08 | 2013-11-08 | Continuous production device for benzoic acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320704922.1U CN203653465U (en) | 2013-11-08 | 2013-11-08 | Continuous production device for benzoic acid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203653465U true CN203653465U (en) | 2014-06-18 |
Family
ID=50919878
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201320704922.1U Expired - Lifetime CN203653465U (en) | 2013-11-08 | 2013-11-08 | Continuous production device for benzoic acid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203653465U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103601638A (en) * | 2013-11-08 | 2014-02-26 | 天津东大化工集团有限公司 | Continuous production process and device of benzoic acid |
| CN106977389A (en) * | 2017-04-01 | 2017-07-25 | 来安县万博丰环保科技有限公司 | A kind of benzoic acid continuous production processes and its device |
| CN110922323A (en) * | 2019-11-27 | 2020-03-27 | 天津东大化工集团有限公司 | Thermoelectric coupling efficient energy-saving emission-reducing process for producing benzoic acid by continuous catalytic oxidation of toluene |
-
2013
- 2013-11-08 CN CN201320704922.1U patent/CN203653465U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103601638A (en) * | 2013-11-08 | 2014-02-26 | 天津东大化工集团有限公司 | Continuous production process and device of benzoic acid |
| CN103601638B (en) * | 2013-11-08 | 2015-06-24 | 天津东大化工集团有限公司 | Continuous production process and device of benzoic acid |
| CN106977389A (en) * | 2017-04-01 | 2017-07-25 | 来安县万博丰环保科技有限公司 | A kind of benzoic acid continuous production processes and its device |
| CN110922323A (en) * | 2019-11-27 | 2020-03-27 | 天津东大化工集团有限公司 | Thermoelectric coupling efficient energy-saving emission-reducing process for producing benzoic acid by continuous catalytic oxidation of toluene |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20140618 |