CN110283068A - A kind of benzoic acid process units reacting thermal drivers air compressor - Google Patents
A kind of benzoic acid process units reacting thermal drivers air compressor Download PDFInfo
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- CN110283068A CN110283068A CN201910487603.1A CN201910487603A CN110283068A CN 110283068 A CN110283068 A CN 110283068A CN 201910487603 A CN201910487603 A CN 201910487603A CN 110283068 A CN110283068 A CN 110283068A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
- C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
- C07C51/255—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting
- C07C51/265—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting having alkyl side chains which are oxidised to carboxyl groups
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- 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
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Abstract
The invention discloses a kind of benzoic acid process units, including condensing-type steam turbine, condensing water cooler and demineralized water pressure-raising/deoxygenation/water supplement apparatus etc. for reacting thermal drivers air compressor.The gas outlet of steam generator, condensing-type steam turbine, condensing water cooler, demineralized water pressure-raising/deoxygenation/water supplement apparatus and steam generator water inlet be sequentially connected it is logical；Motor provided by the invention, the power before oxidation reaction as driving air compressor, after oxidation reaction starts, the energy of steam is converted mechanical energy by condensing-type steam turbine, drives air compressor；Condensing-type steam turbine power output band engine-driven air compressor is low-quality reaction heat field upgrade using optimal path is had found, and reduces power consumption, energy conservation and environmental protection；Device adjustment is only unfolded in steam utilization link, includes that reaction hot steam generator does not constitute any influence to oxidation unit, safety economy is easy to apply.
Description
Technical field
The invention belongs to chemical fields, and in particular to a kind of toluene liquid-phase air oxidation for reacting thermal drivers air compressor
Benzoic acid process units.
Background technique
Benzoic acid (C6H5COOH chemical products) are important, synthetic fibers, resin, coating, rubber, cigarette are widely used in
The industries such as grass.Its main production is toluene liquid-phase air oxidation process.It is shown below, in urging for soluble cobalt or manganese salt
Under change effect, the oxygen direct oxidation in raw material liquid phase toluene and air generates benzoic acid.155~165 DEG C of reaction temperature, pressure
0.6~0.7MPag.Due to by-product benzyl alcohol, benzaldehyde and Ergol etc., subsequent workshop section is there are also rectification cell and recycles not
React the tail gas treating unit of toluene.
Strongly exothermic in view of reacting, prior art recycles it more and 0.4MPag saturated vapor (151.9 DEG C of saturation temperature) occurs,
But since grade is low, device cannot be utilized, and be usually vented, and serious energy dissipation is caused.And reacting air compressor is
By electrical energy drive, if the energy of produced 0.4MPag steam can be recycled by condensing-type steam turbine to replace being driven by electricity
Air compressor can not only recycle the energy of the steam of emptying, moreover it is possible to device power consumption is reduced, for energy-saving, and protection environment
It is very significant.
Summary of the invention
Low low-pressure steam emptying is produced in order to solve existing toluene liquid-phase air oxidation process benzoic acid device reaction heat, is not returned
The shortcomings that utilizing is received, the purpose of the present invention is to provide a kind of toluene liquid-phase air oxidation benzene for reacting thermal drivers air compressor
Formic acid process units.
The object of the invention is realized at least through one of following technical scheme.
The present invention provides a kind of benzoic acid process units for reacting thermal drivers air compressor, including motor, air
Compressor, oxidation unit, toluene feed device and tail gas condensation device；The oxidation unit includes oxidation reactor and steam hair
Raw device, the bottom of the oxidation reactor passes sequentially through to be connected at the top of steam generator and oxidation reactor, the oxidation
Reactor reacts under the effect of the catalyst for toluene and compressed air, forms reaction product benzoic acid, tail gas and reaction heat；
The steam generator is for generating steam；Motor is for driving air compressor；Air compressor and oxidation reactor phase
Connection, air compressor are compressed for air；The toluene feed device is connected with oxidation reactor；The tail gas condensing dress
It sets and is connected with oxidation reactor, for receiving the tail gas of oxidation reactor discharge and isolating from tail gas unreacted first
Benzene, unreacted toluene are again introduced into oxidation reactor, and the process units further includes condensing-type steam turbine, condensing water cooler
With demineralized water pressure-raising/deoxygenation/water supplement apparatus, steam generator is equipped with gas outlet and water inlet, and the gas outlet of steam generator is coagulated
Vapour formula steam turbine, condensing water cooler, demineralized water pressure-raising/deoxygenation/water supplement apparatus and steam generator water inlet be sequentially connected
It is logical；Condensing-type steam turbine is used to convert the thermal energy of steam to mechanical energy, drives air compressor；Condensing water cooler is used for will
Steam is cooled to liquid phase, obtains condensed water；Demineralized water pressure-raising/deoxygenation/water supplement apparatus is used for by condensed water pressure-raising, deoxygenation and cold
The amount of makeup water when water shortage of condensate；Steam is discharged into condensing water cooler after doing work in condensing-type steam turbine and condenses,
Obtain condensed water；Condensed water passes through demineralized water pressure-raising/deoxygenation/water supplement apparatus again, obtains deaerated water, and deaerated water enters steaming by water inlet
In vapour generator.
Preferably, the oxidation unit further includes reaction cycle pump, and the reaction cycle pump is used for pressure-raising reaction product, institute
The bottom for stating oxidation reactor passes sequentially through to be connected at the top of reaction cycle pump and steam generator and oxidation reactor；It is described
Reaction heat successively obtains steam after reaction cycle pump and steam generator.
Preferably, the bottom setting air inlet and discharge port of the oxidation reactor, air inlet is for being continuously passed through compression
Air, discharge port are used to for reaction product benzoic acid and reaction heat being discharged；The toluene includes raw material toluene, freshening toluene and tail
The unreacted toluene isolated in gas；Air compressor is connected with air inlet；The top of the oxidation reactor be arranged into
Material mouth and gas outlet, for being continuously passed through toluene and catalyst, gas outlet is then used to that tail gas to be discharged the feed inlet；The toluene
Feeding device is connected with feed inlet, for handling raw material toluene and freshening toluene, it is made to meet toluene liquid-phase air oxidation process
Reaction requirement；The tail gas condensation device be connected respectively with gas outlet and feed inlet, for receive gas outlet discharge
Tail gas and unreacted toluene is isolated from tail gas, unreacted toluene is again introduced into oxidation reactor from feed inlet.
Preferably, the process units further includes gear-box and generator；Gear-box is used for condensing-type steam turbine
Power passes to generator, and generator is used to convert electric energy for the mechanical energy that condensing-type steam turbine obtains.
Preferably, the temperature of the deaerated water is 100~104 DEG C.
Preferably, the process units further includes air water cooler, water distributing can, and the air water cooler is for cooling compression
Air, water distributing can are used to separate the liquid phase generated in compressed air by condensation；The air compressor includes air one stage of compression
Machine and air split-compressor, air stage compressor, air water cooler, water distributing can and air split-compressor are sequentially communicated,
Air split-compressor is connected with the air inlet of oxidation reactor.
Preferably, the toluene feed device includes toluene surge tank and toluene feed pump, and toluene surge tank is for storing
Raw material toluene and freshening toluene, toluene feed pump is for pressure-raising raw material toluene and freshening toluene, toluene surge tank, toluene feed pump
It is sequentially communicated with the feed inlet of oxidation reactor.
Preferably, the tail gas condensation device includes tail gas air cooler, tail gas aqueous device, toluene circulating pump, tail gas level-one
Surge tank, tail gas cryogenic device and tail gas level 2 buffering tank；Tail gas air cooler and tail gas aqueous device are used for cooled exhaust gas；Tail gas level-one
Surge tank is for separating unreacted toluene, water phase in tail gas；Toluene circulating pump is isolated for pressure-raising tail gas first-level buffer tank
Toluene；Tail gas cryogenic device is used for further cooled exhaust gas；Tail gas level 2 buffering tank for separate in tail gas remaining water phase and
Oily phase；The gas outlet of the oxidation reactor, tail gas air cooler, tail gas aqueous device, tail gas first-level buffer tank, tail gas cryogenic device,
Tail gas level 2 buffering tank is sequentially connected logical, the toluene circulating pump feed inlet phase with tail gas first-level buffer tank and oxidation reactor respectively
Connection, tail gas isolate unreacted toluene in tail gas first-level buffer tank, and unreacted toluene passes through after toluene circulating pump
Feed inlet enters oxidation reactor.
Preferably, the pressure of the steam is 0.4~0.45MPag.
The pressure of compressed air is 0.6~0.7MPag when preferably, into oxidation reactor.
Compared to the prior art, the invention has the advantages that and advantage:
(1) condensing-type steam turbine provided by the invention recycles the energy of low pressure 0.4~0.45MPag saturated vapor, it
It is to convert low low-pressure steam pressure energy and thermal energy to the preferred approach of mechanical energy under the conditions of the prior art；
(2) motor provided by the invention, the power before oxidation reaction as driving air compressor, oxidation reaction are opened
After beginning, the thermal energy of steam is converted mechanical energy by condensing-type steam turbine, drives air compressor, condensing-type steam turbine power output
Band engine-driven air compressor is low-quality reaction heat (155~165 DEG C) field upgrade using optimal path is had found, and reduces electric power
Consumption, energy conservation and environmental protection；
(3) the present invention provides a kind of recycling of reaction heat during extensive toluene liquid-phase air oxidation and the dress utilized
It sets, it includes that reaction hot steam generator does not constitute any influence to oxidation unit that device adjustment, which is only unfolded in steam utilization link,
Safety economy is easy to apply.
Detailed description of the invention
Fig. 1 is the schematic diagram for the toluene liquid-phase air oxidation process benzoic acid device that embodiment 1 provides；
Fig. 2 is that a kind of toluene liquid-phase air oxidation benzoic acid for reaction thermal drivers air compressor that embodiment 2 provides is raw
Produce the schematic diagram of device；
Wherein 1- air stage compressor；2- air water cooler；3- water distributing can；4- air split-compressor；5- motor；
6- oxidation reactor；7- reaction cycle pump；8- steam generator；9- tail gas air cooler；10- tail gas aqueous device；11- toluene buffering
Tank；12- toluene feed pump；13- toluene circulating pump；14- tail gas first-level buffer tank；15- tail gas cryogenic device；16- tail gas second level is slow
Rush tank；17- condensing turbine；18- gear-box；19- motor/generator；20- condensing water cooler；21- demineralized water pressure-raising/remove
Oxygen/water supplement apparatus.
Specific embodiment
Below with reference to embodiment and attached drawing, the present invention is described in detail, and embodiments of the present invention are not limited thereto.
Comparative example
It is raw that this comparative example provides a kind of toluene liquid-phase air oxidation process benzoic acid with motor driven air compressor
It produces device (scale: 80,000 tons), the motor of the present apparatus is the sole power of air compressor, and the process units includes electronic
Machine 5, air compressor, oxidation unit, toluene feed device and tail gas condensation device；The oxidation unit includes oxidation reactor
6, reaction cycle pump 7 and steam generator 8, the bottom of the oxidation reactor 6 pass sequentially through reaction cycle pump 7 and steam generation
Device 8 is connected with the top of oxidation reactor 6, and the oxidation reactor 6 is anti-under the effect of the catalyst for toluene and air
It answers, forms reaction product benzoic acid, tail gas and reaction heat；The reaction cycle pump 7 is used for pressure-raising reaction product；The steam hair
Raw device 8 is for producing 0.4MPag steam；The reaction heat successively obtains steam after reaction cycle pump 7 and steam generator 8；
The bottom setting air inlet and discharge port of the oxidation reactor 6, the air inlet is for being continuously passed through compressed air, discharge port
For reaction product benzoic acid and reaction heat to be discharged；Motor 5 is for driving air compressor；Air compressor and air inlet
It is connected, is compressed for air；The top setting feed inlet of the oxidation reactor and gas outlet, the feed inlet is for continuous
It is passed through toluene and catalyst, gas outlet is then used to be discharged tail gas, and the toluene feed device is connected with feed inlet, for handling
Toluene makes it meet the reaction requirement of toluene liquid-phase air oxidation process；The tail gas condensation device and gas outlet and feed inlet phase
Connection, for handling tail gas and isolating from tail gas unreacted toluene, unreacted toluene is again introduced into oxygen from feed inlet
Change reactor 6.The process units further includes air water cooler 2, water distributing can 3, and the air water cooler 2 is empty for cooling compression
Gas, water distributing can 3 are used to separate the liquid phase generated in compressed air by condensation；The air compressor includes air stage compressor
1 and air split-compressor 4, air stage compressor 1, air water cooler 2, water distributing can 3 and air split-compressor 4 successively connect
Logical, air split-compressor 4 is connected with the air inlet of oxidation reactor 6.The toluene feed device includes toluene surge tank
11 and toluene feed pump 12, toluene surge tank 11 is for storing raw material toluene and freshening toluene, and toluene feed pump 12 is for pressure-raising
The feed inlet of raw material toluene and freshening toluene, toluene surge tank 11, toluene feed pump 12 and oxidation reactor 6 is sequentially communicated.Institute
Stating tail gas condensation device includes tail gas air cooler 9, tail gas aqueous device 10, toluene circulating pump 13, tail gas first-level buffer tank 14, tail gas
Deep freezer 15 and tail gas level 2 buffering tank 16；Tail gas air cooler 9 is used for cooled exhaust gas；Tail gas aqueous device 10 is used for cooled exhaust gas；
Toluene circulating pump 13 is used for the toluene that pressure-raising tail gas first-level buffer tank is isolated；Tail gas first-level buffer tank 14 is for separating in tail gas
Toluene and water phase；Tail gas cryogenic device 15 is used for further cooled exhaust gas；Tail gas level 2 buffering tank 16 is for separating reaction end gas
In remaining water phase and oily phase；The gas outlet of the oxidation reactor 6, tail gas air cooler 9, tail gas aqueous device 10, tail gas level-one
Surge tank 14, tail gas cryogenic device 15, tail gas level 2 buffering tank 16 are sequentially connected logical, and toluene circulating pump 13 is slow with tail gas level-one respectively
Tank 14 is rushed to be connected with the feed inlet of oxidation reactor 6.
As shown in Figure 1,18699.0Nm3/ h, 0.0MPag, 20 DEG C of air through air stage compressor 1 to 0.183MPag,
40 DEG C are cooled to through air water cooler 2 again, after water distributing can 3, is depressed into 0.7MPag into air split-compressor 4,183.5 DEG C,
Oxidation reactor 6 is entered by air inlet again.Based on isentropic efficiency 75%, air stage compressor 1 and air split-compressor 4
Need shaft work 1875.6kw.Meanwhile 10.6t/h, 40 DEG C, the raw material toluene of 0.4MPag with it is de- light from piptonychia benzene column, benzaldehyde
The laggard toluene surge tank 11 of recycling toluene mixing of tower, crude benzol tower, after toluene feed pumps 12 pressure-raisings, with liquid cooling in tail gas
Mutually circulation toluene is mixed into oxidation reactor 6, and oxidation reaction occurs under the effect of the catalyst.Reaction product (37.9t/h,
0.72MPag, 165 DEG C) automatic oxidation reaction device 6 bottom discharge port outflow, realize product point from force feed downstream rectification cell
From, and the 14.55MW (1249.6 × 10 discharged in reaction process4Kcal/h) reaction heat is then taken out by circulation logistics, through steaming
Vapour generator 8 generates 0.4MPag saturated vapor 22.6t/h and (is changed into the unit of 0.4MPag saturated vapor by 104 DEG C of deaerated water
Enthalpy difference is 55.2 × 104Kcal/t meter), due to not having purposes, steam is vented.Tail gas is by the outlet at the top of oxidation reactor 6
Mouth discharge, is cooled to 40 DEG C into tail gas first-level buffer tank 14 through tail gas air cooler 9 and tail gas aqueous device 10, the circulation first isolated
Benzene mixes after the pressurization of toluene circulating pump 13 with raw material toluene, isolates the tail gas gas phase of circulation toluene then through tail gas cryogenic device 15
Tail gas treating unit is sent through tail gas level 2 buffering tank 16 after cooling.
Embodiment
Present embodiments provide a kind of toluene liquid-phase air oxidation benzoic acid production dress for reacting thermal drivers air compressor
It sets, as shown in Fig. 2, the reaction heat during the toluene liquid-phase air oxidation of recycling is converted machinery by condensing-type steam turbine
Can, drive air compressor, the process units compares with the process units of embodiment 1, further include condensing-type steam turbine 17,
Water recirculator 20 and demineralized water pressure-raising/deoxygenation/water supplement apparatus 21, steam generator 8 are equipped with gas outlet and water inlet, steam
Gas outlet, condensing-type steam turbine 17, condensing water cooler 20, demineralized water pressure-raising/deoxygenation/water supplement apparatus 21 and the steaming of generator 8
The water inlet of vapour generator 8 is sequentially connected logical；Condensing-type steam turbine 17 is used to convert mechanical energy for the thermal energy of steam, drives
Air compressor；Condensing water cooler 20 is used to steam being cooled to liquid phase, obtains condensed water；Demineralized water pressure-raising/deoxygenation/water supplement apparatus
21 by condensed water pressure-raising, deoxygenation and in condensation water quantity deficiency for supplementing；The steam that steam generator 8 generates
After (22.6t/h, 0.4MPag, 151.9 DEG C) does work in condensing-type steam turbine 17, condensing (9kPaa, 43.8 DEG C, band liquid are obtained
8.03%), condensing is discharged into condensing water cooler 20 and condenses, and obtains condensed water；Condensed water passes through demineralized water pressure-raising/deoxygenation/benefit again
Wetting system 21 obtains deaerated water (104 DEG C), and deaerated water is entered in steam generator 8 by water inlet.Air compressor is by condensing-type
Steam turbine driving, extra turbine shaft work are generated electricity by generator 19, and gear-box 18 is used for the dynamic of condensing-type steam turbine
Power passes to generator, drives air compressor by motor 5 when starting oxidation reaction or when shaft work deficiency.
It is compared with comparative example, embodiment increases condensing-type steam turbine 17, gear-box 18, condensing water cooler 20, desalination
Water pressure-raising/deoxygenation/water supplement apparatus 21 is arranged on steam-return line, not to oxidation reaction apparatus and subsequent rectifying and vent gas treatment
Unit generates any influence, easy to implement.
The efficiency of comparative example and embodiment is as shown in table 1~3.
1 comparative example air compressor power consumption condition of table
* it is calculated based on air compressor isentropic Compression efficiency 75%.
2 embodiment condensing-type steam turbine of table acting situation
* it is calculated based on condensing-type steam turbine isentropic efficiency of expansion 60%.
Table 3 implements condensing water cooling and consumes recirculated water situation
| Title | Cooling load/104kcal/h | Recycle water consumption/t/h* |
| Condensing water cooling | 1189.9 | 1487.4 |
* 8 DEG C of differential thermal calculations of recirculated water are based on.
As it can be seen that comparative example is compared, in embodiment:
1) coagulating gas formula steam turbine 17 can contribute 2263.6kW, save air compressor power consumption 1875.6kW；
2) the newly-increased circulation water consume 1487.4t/h of condensing water cooler 20, corresponding water circulating pump power consumption 189.1kW is (based on circulation
Pump efficiency 75% calculates)；
3) it coagulates 17 pumped vacuum systems of gas formula steam turbine and consumes 1.0MPag, 250 DEG C of superheated steam about 2.0t/h.
By 0.8 yuan/kWh of electricity price for industrial uses, monovalent 0.21 yuan/t, 1.0MPag steam unit price 200 yuan/t, device of recirculated water
Year, which goes into operation 8400 hours, counts, and in the case where not considering power generation, embodiment is compared with comprehensive 535.0 ten thousand yuan/year of synergy of comparative example；Consider
In the case where power generation, embodiment is compared with comprehensive 795.7 ten thousand yuan/year of synergy of comparative example.
The above embodiment is a preferred embodiment of the present invention, but embodiments of the present invention are not by above-described embodiment
Limitation, other any changes, modifications, substitutions, combinations, simplifications made without departing from the spirit and principles of the present invention,
It should be equivalent substitute mode, be included within the scope of the present invention.
Claims (10)
1. a kind of benzoic acid process units for reacting thermal drivers air compressor, including motor, air compressor, oxidation dress
It sets, toluene feed device and tail gas condensation device；The oxidation unit includes oxidation reactor and steam generator, the oxidation
The bottom of reactor passes sequentially through to be connected at the top of steam generator and oxidation reactor, and the oxidation reactor is used for toluene
It is reacted under the effect of the catalyst with compressed air, forms reaction product benzoic acid, tail gas and reaction heat；The steam generator
For generating steam；Motor is for driving air compressor；Air compressor is connected with oxidation reactor, air compressor
It is compressed for air；The toluene feed device is connected with oxidation reactor；The tail gas condensation device and oxidation reactor
It is connected, for receiving the tail gas of oxidation reactor discharge and isolating from tail gas unreacted toluene, unreacted toluene
It is again introduced into oxidation reactor, which is characterized in that the process units further includes condensing-type steam turbine, condensing water cooler and removes
Salt water pressure-raising/deoxygenation/water supplement apparatus, steam generator are equipped with gas outlet and water inlet, the gas outlet of steam generator, condensing-type
Steam turbine, condensing water cooler, demineralized water pressure-raising/deoxygenation/water supplement apparatus and steam generator water inlet be sequentially connected it is logical；It is solidifying
Vapour formula steam turbine is used to convert the thermal energy of steam to mechanical energy, drives air compressor；Condensing water cooler is used for steam
It is cooled to liquid phase, obtains condensed water；Demineralized water pressure-raising/deoxygenation/water supplement apparatus is used for by condensed water pressure-raising, deoxygenation and in condensed water
Water shortage when amount of makeup water；Steam is discharged into condensing water cooler after doing work in condensing-type steam turbine and condenses, and obtains cold
Condensate；Condensed water passes through demineralized water pressure-raising/deoxygenation/water supplement apparatus again, obtains deaerated water, and deaerated water enters steam by water inlet and sends out
In raw device.
2. the benzoic acid process units of reaction thermal drivers air compressor according to claim 1, which is characterized in that described
Oxidation unit further includes reaction cycle pump, and the reaction cycle pump is used for pressure-raising reaction product, the bottom of the oxidation reactor
It passes sequentially through and is connected at the top of reaction cycle pump and steam generator and oxidation reactor；The reaction heat is successively by reaction
Steam is obtained after circulating pump and steam generator.
3. the benzoic acid process units of reaction thermal drivers air compressor according to claim 1, which is characterized in that described
The bottom setting air inlet and discharge port of oxidation reactor, for air inlet for being continuously passed through compressed air, discharge port is used for will be anti-
Product benzoic acid and reaction heat is answered to be discharged；The toluene includes the unreacted isolated in raw material toluene, freshening toluene and tail gas
Toluene；Air compressor is connected with air inlet；The top setting feed inlet and gas outlet of the oxidation reactor, it is described into
For being continuously passed through toluene and catalyst, gas outlet is then used to that tail gas to be discharged material mouth；The toluene feed device and feed inlet phase
Connection, for handling raw material toluene and freshening toluene, makes it meet the reaction requirement of toluene liquid-phase air oxidation process；The tail gas
Condensing unit be connected respectively with gas outlet and feed inlet, for receiving the tail gas of gas outlet discharge and isolating from tail gas
Unreacted toluene, unreacted toluene are again introduced into oxidation reactor from feed inlet.
4. the benzoic acid process units of reaction thermal drivers air compressor according to claim 1, which is characterized in that described
Process units further includes gear-box and generator；Gear-box is used to the power of condensing-type steam turbine passing to generator, sends out
Motor is used to convert electric energy for the mechanical energy that condensing-type steam turbine obtains.
5. the benzoic acid process units of reaction thermal drivers air compressor according to claim 1, which is characterized in that described
The temperature of deaerated water is 100 ~ 104 DEG C.
6. the benzoic acid process units of reaction thermal drivers air compressor according to claim 3, which is characterized in that described
Process units further includes air water cooler, water distributing can, and the air water cooler is for cooling down compressed air, and water distributing can is for separating
Because of the liquid phase of condensation generation in compressed air；The air compressor includes air stage compressor and air split-compressor,
Air stage compressor, air water cooler, water distributing can and air split-compressor are sequentially communicated, air split-compressor and oxidation
The air inlet of reactor is connected.
7. the benzoic acid process units of reaction thermal drivers air compressor according to claim 3, which is characterized in that described
Toluene feed device includes toluene surge tank and toluene feed pump, and toluene surge tank is used to store raw material toluene and freshening toluene,
Toluene feed pump is for pressure-raising raw material toluene and freshening toluene, the charging of toluene surge tank, toluene feed pump and oxidation reactor
Mouth is sequentially communicated.
8. the benzoic acid process units of reaction thermal drivers air compressor according to claim 3, which is characterized in that described
Tail gas condensation device include tail gas air cooler, tail gas aqueous device, toluene circulating pump, tail gas first-level buffer tank, tail gas cryogenic device and
Tail gas level 2 buffering tank；Tail gas air cooler and tail gas aqueous device are used for cooled exhaust gas；Tail gas first-level buffer tank is for separating tail gas
In unreacted toluene, water phase；Toluene circulating pump is used for the toluene that pressure-raising tail gas first-level buffer tank is isolated；Tail gas cryogenic device is used
In further cooled exhaust gas；Tail gas level 2 buffering tank is for separating remaining water phase and oily phase in tail gas；The oxidation reactor
Gas outlet, tail gas air cooler, tail gas aqueous device, tail gas first-level buffer tank, tail gas cryogenic device, tail gas level 2 buffering tank successively phase
Connection, toluene circulating pump are connected with the feed inlet of tail gas first-level buffer tank and oxidation reactor respectively, and tail gas is in tail gas level-one
Unreacted toluene is isolated in surge tank, unreacted toluene enters oxidation reaction after toluene circulating pump, through feed inlet
Device.
9. the benzoic acid process units of reaction thermal drivers air compressor according to claim 1, which is characterized in that described
The pressure of steam is 0.4 ~ 0.45MPag.
10. the benzoic acid process units of reaction thermal drivers air compressor according to claim 1, which is characterized in that into
The pressure of compressed air is 0.6 ~ 0.7MPag when entering oxidation reactor.
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0279288A2 (en) * | 1987-02-14 | 1988-08-24 | Hüls Aktiengesellschaft | Process and apparatus for producing benzene-carboxylic acids or benzene-dicarboxylic-acid esters |
| CN1522996A (en) * | 2003-09-12 | 2004-08-25 | 湖南大学 | Process for preparing benzaldehyde, phenylcarbinol and benzoic acid |
| WO2008105084A1 (en) * | 2007-02-28 | 2008-09-04 | Hitachi Plant Technologies, Ltd. | Method for the treatment of waste gas from oxidation and the recovery of energy |
| CN102861542A (en) * | 2012-09-27 | 2013-01-09 | 天津东大化工集团有限公司 | Methylbenzene oxidation tower in 10000-tone level benzoic acid production |
| CN105503567A (en) * | 2016-01-15 | 2016-04-20 | 湖南弘润化工科技有限公司 | Device and method for continuously producing benzoic acid and byproduct benzaldehyde |
| CN105617959A (en) * | 2016-01-15 | 2016-06-01 | 湖南弘润化工科技有限公司 | Reaction device for continuously producing benzoic acid by virtue of toluene liquid-phase air oxidation method |
| CN105669398A (en) * | 2016-01-15 | 2016-06-15 | 湖南弘润化工科技有限公司 | Device for producing benzaldehyde and method thereof |
-
2019
- 2019-06-05 CN CN201910487603.1A patent/CN110283068A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0279288A2 (en) * | 1987-02-14 | 1988-08-24 | Hüls Aktiengesellschaft | Process and apparatus for producing benzene-carboxylic acids or benzene-dicarboxylic-acid esters |
| CN1522996A (en) * | 2003-09-12 | 2004-08-25 | 湖南大学 | Process for preparing benzaldehyde, phenylcarbinol and benzoic acid |
| WO2008105084A1 (en) * | 2007-02-28 | 2008-09-04 | Hitachi Plant Technologies, Ltd. | Method for the treatment of waste gas from oxidation and the recovery of energy |
| CN102861542A (en) * | 2012-09-27 | 2013-01-09 | 天津东大化工集团有限公司 | Methylbenzene oxidation tower in 10000-tone level benzoic acid production |
| CN105503567A (en) * | 2016-01-15 | 2016-04-20 | 湖南弘润化工科技有限公司 | Device and method for continuously producing benzoic acid and byproduct benzaldehyde |
| CN105617959A (en) * | 2016-01-15 | 2016-06-01 | 湖南弘润化工科技有限公司 | Reaction device for continuously producing benzoic acid by virtue of toluene liquid-phase air oxidation method |
| CN105669398A (en) * | 2016-01-15 | 2016-06-15 | 湖南弘润化工科技有限公司 | Device for producing benzaldehyde and method thereof |
Non-Patent Citations (2)
| Title |
|---|
| 区灿棋，吕德伟编著: "《石油化工氧化反应工程与工艺》", 31 July 1992, 北京：中国石化出版社 * |
| 编；郭晓光等译: "《实用节能全书》", 30 November 1987, 化学工业出版社 * |
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