CN101298446B - Industrialized production process of benzoic anhydride - Google Patents
Industrialized production process of benzoic anhydride Download PDFInfo
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- CN101298446B CN101298446B CN2008100399891A CN200810039989A CN101298446B CN 101298446 B CN101298446 B CN 101298446B CN 2008100399891 A CN2008100399891 A CN 2008100399891A CN 200810039989 A CN200810039989 A CN 200810039989A CN 101298446 B CN101298446 B CN 101298446B
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Abstract
A method for manufacturing phthalic anhydride by industrial naphthalene includes the following steps: 1) the industrial naphthalene is heated in a carburetor until being completely vaporized; 2) the vaporized naphthalene enters a naphthalene-air mixer by a venturi tube and is fully mixed with the reaction air; 3) the fully mixed naphthalene-air mixing air enters a fixed bed vapor phase reactor for reaction, and then the phthalic anhydride is obtained. The method can be used for leading the industrial naphthalene to be completely vaporized and fully mixed with the air, thereby improving the yield of the phthalic anhydride and simultaneously being capable of solving the problem that the nozzle in the conventional ejection type vaporization technique is easy to be plugged.
Description
Technical field
The present invention relates to the Fixed Bed Gas Phase catalyzed oxidation and produce the method for phthalic anhydride, is the method that raw material Fixed Bed Gas Phase catalyzed oxidation is produced phthalic anhydride by NAPTHALENE FLAKES. (INDUSTRIAL GRADE particularly.
Background technology
The operational path that phthalic anhydride (also claiming Tetra hydro Phthalic anhydride) is produced is divided into two kinds of naphthalene method and o-Xylol methods (O-X) with the raw material difference.Adopt German DAVY, Lurgi and BASF AG, Italian LONZA company, Japan to touch the 60-80g Technology of coal company research and development mostly from the eighties of countries in the world phthalic anhydride production so far, but all adopting o-Xylol is the Fixed Bed Gas Phase oxidizing process route of raw material, so far overall craft technological improvement is little, China's Nanjing petrochemical industry, Qilu Petrochemicals etc. all are the Technology that raw material is introduced Lurgi company with the o-Xylol, adopt the catalyst fixed bed catalyzed oxidation of BasF to produce phthalic anhydride.
The phthalic anhydride production equipment that with the o-Xylol is raw material abroad accounts for more than 90% of phthalic anhydride throughput, and China is that the phthalic anhydride plant of raw material accounts for 98% of domestic phthalic anhydride throughput with the o-Xylol.
Constantly soaring and global o-Xylol is in short supply along with crude oil price in the world, the cost of producing phthalic anhydride with o-Xylol has not had clear superiority.
The naphthalene method is produced phthalic anhydride technology two kinds, and a kind of is that NAPTHALENE FLAKES. (INDUSTRIAL GRADE liquefaction enters fluidized-bed and produces phthalic anhydride through catalytic oxidation, and this raw materials technology unit consumption height, phthalic anhydride yield only 80% causes the waste of naphthalene resource.Another kind is produced phthalic anhydride for the NAPTHALENE FLAKES. (INDUSTRIAL GRADE vaporization enters fixed bed through catalytic gas phase oxidation.
Reaction process is:
The theoretical yield that NAPTHALENE FLAKES. (INDUSTRIAL GRADE is produced phthalic anhydride is 115.6%, and it is about 106% that the high energy of NAPTHALENE FLAKES. (INDUSTRIAL GRADE actual recovery perfect condition reaches, but still do not have the example report at present.
In the prior art, be raw material fixed bed catalytic oxidation method technology with the NAPTHALENE FLAKES. (INDUSTRIAL GRADE with o-Xylol be the technology of raw material basic identical only be that the charging of NAPTHALENE FLAKES. (INDUSTRIAL GRADE is different.And select different catalyzer and different vaporization modes, all can exert an influence to the phthalic anhydride yield.
With the NAPTHALENE FLAKES. (INDUSTRIAL GRADE be raw material fixed bed catalytic oxidation method produce phthalic anhydride process substantially as shown in Figure 1.In the at present domestic and international NAPTHALENE FLAKES. (INDUSTRIAL GRADE system phthalic anhydride method, steam heating is generally adopted in the vaporization of NAPTHALENE FLAKES. (INDUSTRIAL GRADE, electrically heated or heat-conducting oil heating, and hybrid mode is generally jet-type, and the disadvantage of jet-type is that shower nozzle is often easily stopped up by NAPTHALENE FLAKES. (INDUSTRIAL GRADE.
Table 1 is in several prior art processes, and NAPTHALENE FLAKES. (INDUSTRIAL GRADE vaporization hybrid mode is to the situation that influences of phthalic anhydride yield.
Table 1
| Country | Scale | The vaporization hybrid mode | Technique effect | The phthalic anhydride yield |
| Czech | 20,000 tons/year | Jet-type | Can not vaporize fully, easily stifled | 90％ |
| China | 20,000 tons/year | Jet-type | The part drop is arranged | 89％ |
| China | 5000 tons/year | Liquid | Fluidized-bed | 80％ |
China's utility application 92203628.4 discloses a kind of atomizing or vapourizing unit, and discloses the method that a kind of low-pressure gasifying inleting naphthalene legal system is equipped with phthalic anhydride in the application for a patent for invention 92101462.7.According to the record in these two applications, by under the impact of high velocity air, the liquid naphthalene that the larynx neck position of Venturi meter is entered fully atomizes or vaporizes.Its vaporization rate can reach 89～93%.The naphthalene of vaporization enters fluidized-bed reactor by the jet pipe injection and reacts.
Summary of the invention
The technical problem to be solved in the present invention is that easily stifled, the NAPTHALENE FLAKES. (INDUSTRIAL GRADE of jet-type blended shower nozzle can not be vaporized fully in the prior art, and the naphthalene of vaporization can not full and uniformly mix with air.The invention provides a kind of method of producing phthalic anhydride, NAPTHALENE FLAKES. (INDUSTRIAL GRADE is vaporized fully and air is full and uniform mixes with reaction, enter the fixed-bed reactor reaction then, produce the yield of phthalic anhydride to improve NAPTHALENE FLAKES. (INDUSTRIAL GRADE by improving technology by NAPTHALENE FLAKES. (INDUSTRIAL GRADE.
The method that NAPTHALENE FLAKES. (INDUSTRIAL GRADE of the present invention is produced phthalic anhydride comprises the steps:
1) NAPTHALENE FLAKES. (INDUSTRIAL GRADE heats vaporization fully in vaporizer;
2) Qi Hua naphthalene enters naphthalene-air mixer by Venturi tube, with reaction air thorough mixing;
3) well-mixed naphthalene-air Mixture enters the fixed-bed catalytic Gas-phase reactor and reacts, and obtains phthalic anhydride.
Of the present invention the technology that improves the phthalic anhydride yield has two gordian techniquies by NAPTHALENE FLAKES. (INDUSTRIAL GRADE production phthalic anhydride, and one is the vaporization fully of NAPTHALENE FLAKES. (INDUSTRIAL GRADE, and another is the naphthalene of vaporization and the thorough mixing of reaction air.
The NAPTHALENE FLAKES. (INDUSTRIAL GRADE vaporization: can vaporize fully for guaranteeing NAPTHALENE FLAKES. (INDUSTRIAL GRADE, the present invention has adopted the mode that heating is vaporized NAPTHALENE FLAKES. (INDUSTRIAL GRADE in vaporizer.
Preferably, adopt the to drive steam heating vaporizer that switches mutually with the naphthalene electric heating carburetor with can be with ordinary production the time.
Adopt electric heating carburetor that NAPTHALENE FLAKES. (INDUSTRIAL GRADE is warming up to vaporization temperature when going into operation,, reach vaporization fully as 220 ℃～250 ℃.
Adopt steam-heated vaporizer during ordinary production.Vaporizer can be the conventional vaporizer of this area, as the vapour one liquid equilibrated vaporizer that can keep certain liquid.Can one mass flowmeter be arranged in the import that NAPTHALENE FLAKES. (INDUSTRIAL GRADE enters vaporizer, also setting-mass flowmeter in the outlet of naphthalene vaporizer.By the vaporizer float controller valve setting flow that automatically adjusts, naphthalene is fully vaporized to guarantee that naphthalene vaporizer liquid level reaches.
Preferably, the vaporizer tank level control is 30～80%.
The vaporizer temperature out of NAPTHALENE FLAKES. (INDUSTRIAL GRADE vaporization is 220～250 ℃; Pressure is 003-0.05MPa.
According to the present invention, in step 2) in air through pressurization, heating after produce negative pressure by Venturi tube, the NAPTHALENE FLAKES. (INDUSTRIAL GRADE of vaporization is sent into mixing tank, make the NAPTHALENE FLAKES. (INDUSTRIAL GRADE and reaction air thorough mixing of vaporization.
Preferably, described air is pressurized to 0.04MPa～0.06MPa by gas blower.
Preferably, described air is heated to 180 ℃～200 ℃ by air preheater.
Preferably, the temperature of the gas mixture of described naphthalene-air mixer is 180 ℃～220 ℃, and the pressure of gas mixture is greater than 0.03MPa and less than 0.06MPa.
Among the present invention, the NAPTHALENE FLAKES. (INDUSTRIAL GRADE flow is 2217kg/h～5216kg/h, and air flow quantity is 30000NM
3/ h～65000NM
3/ h.
Among the present invention, the air approach Venturi tube of pressurized, heated produces negative pressure, sucks the NAPTHALENE FLAKES. (INDUSTRIAL GRADE naphthalene steam of vaporization fully in the Venturi tube and sends into naphthalene-air mixer, and naphthalene steam and air enter reactor after reaching thorough mixing again in naphthalene-air mixer.The present invention adopts vaporizer that NAPTHALENE FLAKES. (INDUSTRIAL GRADE is vaporized fully and enters mixing tank by Venturi tube, has avoided the NAPTHALENE FLAKES. (INDUSTRIAL GRADE blocking problem.
In addition, the present invention also can utilize the vaporization thermal source of reaction heat as NAPTHALENE FLAKES. (INDUSTRIAL GRADE, and the superheated vapour circulation that reactor is come out is not only energy-conservation, stable but also control easily.
In the prior art, the air of heating and naphthalene directly mix and enter reactor by the mode of spraying, and cause the naphthalene vaporization not exclusively, air and naphthalene undercompounding, and also shower nozzle is easily stifled.
The present invention vaporizes naphthalene by heating in vaporizer fully, after naphthalene steam being sucked Venturi tube and enters air-naphthalene mixing tank mixing through Venturi tube by the air that heats then, the naphthalene of vaporization is mixed with air is full and uniform, enter reactor and carry out catalytic oxidation, obtain the phthalic anhydride product of high yield.
Description of drawings
Fig. 1 is the process flow diagram that the NAPTHALENE FLAKES. (INDUSTRIAL GRADE of prior art is produced phthalic anhydride.
Fig. 2 is the process flow diagram that NAPTHALENE FLAKES. (INDUSTRIAL GRADE of the present invention is produced phthalic anhydride.
Fig. 3 is in the embodiment of technology of the present invention, and NAPTHALENE FLAKES. (INDUSTRIAL GRADE is vaporized fully in vaporizer and entered naphthalene-air mixer blended process synoptic diagram through Venturi tube.
Fig. 4 is the structural representation of Venturi tube used in an embodiment of the invention.
Fig. 5 is the partial enlarged drawing of Fig. 4.
Description of reference numerals
T-11 condenser formula steam turbine (N1.73-4.0)
G-11 gas blower (BII 1330-1.56/0.948)
FIL-11 air filter (3500 * 3000 * 2500)
T-12A/B measures naphthalene jar (5000 * 5500)
E-11 air preheater (F=500M
2)
F-14 naphthalene air mixer (F=7.6M
2)
EJ-11 Venturi tube (φ 902 * 2830)
E-13 naphthalene vaporizer (φ 700 * 1000)
C-13 driving naphthalene electric heating carburetor (700KW)
G-15A/B naphthalene tail pump (RCB-2/0.8)
G-16A/B naphthalene fresh feed pump (HA25-200)
The L1CAHL tank level control
The larynx footpath section of 111 necking down pipes
The undergauge section of 112 necking down pipes
The extension diameter section of 113 necking down pipes
The undergauge section port of 114 necking down pipes
The extension diameter section port of 115 necking down pipes
The tubular stinger of 116 Venturi tubes
1161 outer tubes
Pipe in 1162
The import of pipe in 1163
The outlet of pipe in 1164
Embodiment
40,000 tons of/year production equipments with NAPTHALENE FLAKES. (INDUSTRIAL GRADE production phthalic anhydride are example below, introduce the present invention in more detail.
The technical process of NAPTHALENE FLAKES. (INDUSTRIAL GRADE production phthalic anhydride of the present invention as shown in Figure 2.
NAPTHALENE FLAKES. (INDUSTRIAL GRADE heats fully vaporization in vaporizer after, be mixed and fed into naphthalene-air mixer with the air of heating and pressurizing by Venturi tube, full and uniform blended naphthalene-air Mixture enters fixed bed catalytic reactor and carries out catalyzed oxidation and produce phthalic anhydride.
Can reach 106% in order to ensure product phthalic anhydride yield, one of critical process be NAPTHALENE FLAKES. (INDUSTRIAL GRADE vaporize fully and with the thorough mixing of air, so the vaporization of the difference of NAPTHALENE FLAKES. (INDUSTRIAL GRADE and blended mode have a direct impact the phthalic anhydride yield.
Benzoic anhydride producing process flow process of the present invention has increased NAPTHALENE FLAKES. (INDUSTRIAL GRADE vaporizer, Venturi tube and naphthalene-air mixer on the basis of the technical process of prior art NAPTHALENE FLAKES. (INDUSTRIAL GRADE (or o-Xylol) production phthalic anhydride.
Fig. 3 is that NAPTHALENE FLAKES. (INDUSTRIAL GRADE of the present invention is produced in the technology of phthalic anhydride, and the naphthalene heating is vaporized in vaporizer, and carries out blended process synoptic diagram by Venturi tube and mixing tank air-naphthalene.
The present invention is provided with two vaporizers, i.e. steam heating vaporizer E-13 and electric heating carburetor C-13.Wherein adopt the steam heating vaporizer during ordinary production, heating steam at this moment can come the superheated vapour of autoreactor.Adopt electric heating carburetor during driving, to guarantee the vaporization fully of naphthalene.
(E-13 C-13) can be the vaporizer of this area routine to the naphthalene vaporizer, as the vaporizer of the vapor-liquid equilibrium that can keep certain liquid level.
For guaranteeing that NAPTHALENE FLAKES. (INDUSTRIAL GRADE can vaporize fully, adopted steam-heated vaporizer during ordinary production of the present invention, (φ 700mm * 1000mm), can keep the vapour one liquid balance of certain liquid in the vaporizer, the heating-surface area of vaporizer is 90m as E-13
2Import before naphthalene enters vaporizer is provided with mass flowmeter, and naphthalene vaporizer outlet is settings-under meter also, and by being arranged on float controller valve on the vaporizer setting flow that automatically adjusts, assurance naphthalene vaporizer liquid level reaches naphthalene is fully vaporized.
The vaporization flow of NAPTHALENE FLAKES. (INDUSTRIAL GRADE is by the liquid-level controller L1CAHL control of naphthalene vaporizer, and general tank level control is 30～80%, and heating is 6.0MPa with the pressure of steam.
Venturi tube of the present invention can be any suitable Venturi tube.Fig. 4 is the structural representation of the Venturi tube of an embodiment.Venturi tube EJ-11 comprises necking down pipe 110 and tubular stinger 116.The necking down pipe comprises larynx footpath section 111, undergauge section 112, extension diameter section 113, undergauge section port one 14, extension diameter section port one 15.Wherein, tubular stinger 116 is inserted into the certain depth of larynx footpath section by the top of undergauge section 112.Larynx footpath section diameter is φ 710mm, the diameter of extension diameter section port one 15 is φ 902, the diameter of undergauge section port one 14 is φ 902mm, the necking down pipe total length of Venturi tube is 2830mm, wherein the length of larynx footpath section 111 is 710mm, undergauge section 112 length are 520mm, and the length of extension diameter section 113 is 1600mm.Tubular stinger 116 comprises outer tube 1161, interior pipe 1162, interior pipe import 1163 and interior pipe outlet 1164.Interior pipe 1162 extend into the middle part of necking segment, and interior pipe outlet 1164 is bent upwards.Interior pipe exit diameter is φ 219.The vaporization naphthalene enters and upwards spouting by the outlet 1164 of interior pipe from interior pipe import 1163.And air enters from the necking segment port one 14 of reducing pipe, by throat neck section 111 and expand cervical part of esophagus 113 and come out by expansion tube port one 15, the negative pressure that air produces during through the necking down pipe of Venturi tube will suck by the naphthalene steam that interior pipe outlet 1164 is come out be mixed and fed in the necking down pipes with the direct-connected naphthalene of the extension diameter section port of Venturi tube-air mixer F-14 in.
NAPTHALENE FLAKES. (INDUSTRIAL GRADE is to produce the main raw material of phthalic anhydride in the present invention.
The used NAPTHALENE FLAKES. (INDUSTRIAL GRADE of the present invention can be the NAPTHALENE FLAKES. (INDUSTRIAL GRADE of extracting from coal tar, also can be from the synthetic naphthalene of the oil of market purchasing.
The quality index of NAPTHALENE FLAKES. (INDUSTRIAL GRADE meets the standard of coking naphthalene GB/T6699-1998.Its ctystallizing point ≮ 78.3 ℃, non-volatile matter ≯ 0.04, ash content ≯ 0.01, purity＞95.5%.
NAPTHALENE FLAKES. (INDUSTRIAL GRADE enters naphthalene test tank T-12A/B with molten state and sends into naphthalene vaporizer E-13 or C-13 by naphthalene canned-motor pump G-16A/B again.
During ordinary production, NAPTHALENE FLAKES. (INDUSTRIAL GRADE is heated to 220～250 ℃ in naphthalene vaporizer E-13, vaporization fully, and pressure is 0.03-0.05MPa.The naphthalene steam that produces sucks and mixing by the heating and pressurizing air that Venturi tube is entered Venturi tube, enters then among the naphthalene air mixer F-14, carries out fully and uniformly mixing.Mixed uniformly naphthalene-air Mixture enters in the fixed bed catalytic reactor reacts.
The ratio flow control of NAPTHALENE FLAKES. (INDUSTRIAL GRADE and air is set control by gas blower G-11.
The processing condition of setting:
Air: flow is 30000NM
3/ hr～65000NM
3/ hr, temperature is 180～200 ℃, pressure is 0.04～0.06MPa
NAPTHALENE FLAKES. (INDUSTRIAL GRADE: flow is 2217kg/hr～5216kg/hr, and temperature is 220 ℃～250 ℃.
Heating steam: 6.0MPa (saturation steam), flow are 2～3t/hr.
Raw material: NAPTHALENE FLAKES. (INDUSTRIAL GRADE purity＞95.5%.
Because NAPTHALENE FLAKES. (INDUSTRIAL GRADE is a flammable and explosive substance, and when ordinary production, be in limits of explosion, normally carry out for guaranteeing to produce, prevent that burst accident from taking place, the necessary electrostatic grounding of naphthalene system all devices and pipeline has all been installed emergency cutting off valve before advancing naphthalene vaporizer E-13, naphthalene air mixer F-14.
Fig. 3 is a schematic flow sheet, is mainly used in the explanation vaporization and mixes related equipment and technology.Usually in Industrial processes, also comprise other not shown conventional equipments, be not elaborated at this.
Oxygen is the another kind of raw material that phthalic anhydride is produced, the oxygen that present embodiment needs is from air, and air is sucked by condensing steam turbine GT-11 blower G-11 through air filter FIL-11, pressure-controlling is at 0.06MPa, and the rotating speed of control steam turbine GT-11 comes the control air flow.
The air that comes out from gas blower G-11 through metering after, the air preheater E-11 that is introduced into a two-section type is heated to 180 ℃, abundant, the uniform mixing of naphthalene steam that enters naphthalene-air mixer F-14 then and come from naphthalene vaporizer E-13, and be about 180 ℃～220 ℃ with temperature, pressure is greater than 0.03, enters reactor less than the gaseous phase of 0.06MPa.
G-11 is a single hop radial gas blower, and T-11 directly drives by the condensing-type steam turbine, and the required steam of steam turbine is provided by the pyrogenetic 6.0MPa superheated vapour of naphthalene oxidizing reaction.
Driving initial stage naphthalene is by vaporizer C-13 vaporization, and vaporizer C-13 is by the electric heater heating of 700KW.After the question response system is normal, switch to by the vaporizer E-13 of 6.0MPa steam as thermal source.
In naphthalene-air mixer F-14 screen cloth has been installed, purpose is to guarantee naphthalene and air thorough mixing dripless.
The NAPTHALENE FLAKES. (INDUSTRIAL GRADE of vaporizing among the present invention is identical with the process that mitigation gas catalyzed oxidation in fixed-bed reactor of air is produced phthalic anhydride and its last handling process and prior art.As adopt the BASF-0429 catalyzer, 80 restrain catalyzer (being that NAPTHALENE FLAKES. (INDUSTRIAL GRADE content reaches 80 grams in every cubic metres of air).Reactant gases obtains the thick product of phthalic anhydride through gas cooling and switching condensation, and the thick product of phthalic anhydride obtains the product phthalic anhydride through Overheating Treatment and rectifying again.
In addition, the present invention also utilizes the vaporization thermal source of reaction heat as NAPTHALENE FLAKES. (INDUSTRIAL GRADE, and the high pressure superheated steam that reactor is come out is circulated to the heating vaporization that is used for naphthalene in the vaporizer, and the thermal treatment and the rectifying that are used for the thick product of phthalic anhydride, and is not only energy-conservation, stable but also control easily.
Technology of the present invention sees Table 2 with domestic and international phthalic anhydride production technology comparative result.
Table 2
| Company | Scale | Naphthalene air mixed mode | The naphthalene vaporization effect | The phthalic anhydride yield | The equipment effect |
| Czech company | 20,000 tons/year | Spray nozzle type | The part drop is arranged | 90％ | Shower nozzle is easily stifled |
| Domestic certain company | 20,000 tons/year | Spray nozzle type | The part drop is arranged | 89％ | Shower nozzle is easily stifled |
| Domestic certain company | 0.5 ten thousand tons/year | Spray nozzle type | Liquefaction | 80％ | Shower nozzle is easily stifled |
| The present invention | 40,000 tons/year | Venturi meter | Vaporization fully | 106％ | Not stifled |
Though abovely the present invention has been carried out comparatively detailed explanation by specific embodiment, be not limited to these embodiment, under the condition that does not break away from the present invention's design, other more diverse equivalent embodiment can also be arranged.
Claims (10)
1. the method that NAPTHALENE FLAKES. (INDUSTRIAL GRADE is produced phthalic anhydride comprises the steps:
1) NAPTHALENE FLAKES. (INDUSTRIAL GRADE heats vaporization fully in vaporizer;
2) Qi Hua naphthalene enters naphthalene-air mixer by Venturi tube, with reaction air thorough mixing;
3) well-mixed naphthalene-air Mixture enters the Fixed Bed Gas Phase catalyticreactor and reacts, and obtains phthalic anhydride.
2. method according to claim 1 is characterized in that, the vaporizer temperature out of NAPTHALENE FLAKES. (INDUSTRIAL GRADE vaporization is 220 ℃～250 ℃; Pressure is 0.03～0.05MPa.
3. method according to claim 1 and 2 is characterized in that, in step 2) in air through pressurization, heating after produce negative pressure by Venturi tube, the NAPTHALENE FLAKES. (INDUSTRIAL GRADE of vaporization is sent into mixing tank.
4. method according to claim 3 is characterized in that, at the vaporizer entrance and exit mass flowmeter is set respectively, and regulates the setting flow automatically by the vaporizer float controller valve, to guarantee that the vaporizer liquid level reaches NAPTHALENE FLAKES. (INDUSTRIAL GRADE and fully vaporizes.
5. method according to claim 4 is characterized in that tank level control is 30～80%.
6. method according to claim 3 is characterized in that described air is pressurized to 0.04MPa～0.06MPa by gas blower.
7. method according to claim 3 is characterized in that, described air is heated to 180 ℃～200 ℃ by air preheater.
8. method according to claim 3 is characterized in that, the temperature of the gas mixture of described naphthalene-air mixer is 180 ℃～220 ℃, and the pressure of gas mixture is greater than 0.03MPa with less than 0.06MPa.
9. method according to claim 3 is characterized in that, the NAPTHALENE FLAKES. (INDUSTRIAL GRADE flow is 2217kg/h～5216kg/h, and air flow quantity is 30000NM
3/ h～65000NM
3/ h.
10. method according to claim 3 is characterized in that, utilizes the thermogenetic steam of reaction that the NAPTHALENE FLAKES. (INDUSTRIAL GRADE that enters before the vaporizer is heated.
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| CN103032860B (en) * | 2012-12-25 | 2015-05-06 | 上海建安化工设计有限公司 | Naphthalene vaporizer |
| CN106349199A (en) * | 2016-08-25 | 2017-01-25 | 开封市九泓化工有限公司 | Method and device for preparing phthalic anhydride by virtue of naphthalene method and prepared phthalic anhydride |
| CN109298726B (en) * | 2018-09-29 | 2022-01-28 | 青海盐湖工业股份有限公司 | Method and system for heating EDC cracking furnace |
| CN110180464A (en) * | 2019-06-28 | 2019-08-30 | 邢台旭阳化工有限公司 | Phthalic anhydride gas phase naphthalene feeder |
| CN113465408B (en) * | 2021-05-25 | 2023-08-15 | 西安航天华威化工生物工程有限公司 | Vaporizer (ZA) |
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