CN103506060B - Energy-saving type oxyanthraquinone production device - Google Patents
Energy-saving type oxyanthraquinone production device Download PDFInfo
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- CN103506060B CN103506060B CN201210210135.1A CN201210210135A CN103506060B CN 103506060 B CN103506060 B CN 103506060B CN 201210210135 A CN201210210135 A CN 201210210135A CN 103506060 B CN103506060 B CN 103506060B
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- air
- heat exchanger
- fused salt
- blast stove
- temperature
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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
Abstract
An energy-saving type oxyanthraquinone production device is disclosed, the technology relates to the technical field of production device for preparing anthraquinone by taking anthracene as raw material and carrying out air oxidation. The device makes full use of oxidation reaction heat brought out by a high-temperature molten salt and high-temperature materials, normal-temperature air is preheated through a molten salt-air heat exchanger and a material-air heat exchanger in a fire barrier, the preheated air is provided for a hot blast stove, after the oxidation reaction heat energy is recycled by the heat exchangers, an air inlet temperature of the hot blast stove is changed from an original device room-temperature temperature into a hot air temperature of 180 DEG C-200 DEG C, and thus the device greatly reduces the coal consumption amount of the hot blast stove and has the energy saving effect.
Description
Technical field
It is raw material that the technology of the present invention relates to anthracene, through air oxidation, and the process units technical field of obtained anthraquinone.
Background technology
Take anthracene as raw material, through air oxidation, obtained dyestuff intermediate anthraquinone (is commonly called as: oxidation anthraquinone, with be different from synthesis anthraquinone) production, many decades history is had in China, technical process is: the anthracene of content >=90% is dropped into molten anthracene still heating and melting, vaporization still is squeezed into submerged pump, 0.03Mpa superheated steam is passed into again in vaporization still, anthracene is gasified, enter blender, the fixed bed oxidator that phosphorus/vanadium catalyst is housed is entered after mixing with >=250 DEG C of hot-airs, anthracene is made to be oxidized to anthraquinone, due to anthracene sky ratio, catalyst activity, the isoparametric impact of oxidizing reaction temperature, the side reaction that association is simultaneously certain, oxidized byproduct is phthalic anhydride or until carbon dioxide and water, the number of side reaction, directly affect the quality of product anthraquinone and the consumption of raw material anthracene.
In this device, the means of controlled oxidization reactiveness are: 1, adopt the method for the flow controlling superheated steam to control the anthracene vaporization amount entering oxidator.2, adopt the method emptying to roots blower air cushioning tank atmospheric valve to regulate and enter oxidator air capacity.3, adopt the fused salt circulatory system to function of environment heat emission, take away reaction heat, to maintain the relatively stable of reaction temperature.
The defect that above-mentioned three kinds of control methods exist is: 1, in manual operation regulation process, be difficult to precisely control, reaction temperature is the result of many constitutive equations such as the heat removed by anthracene quantity of steam, air capacity, reaction speed (reaction speed changes by the change of reaction temperature again), reaction heat, salt bath, the particularly change of reaction temperature, bring the change of oxidation reaction speed, bring the change of reaction heat, if side reaction is risen, reaction heat discharges in a large number, the more difficult grasp of reaction temperature.2, because of catalyst cycle activate time, need comparatively Wind Volume, therefore the configuration of roots blower air quantity is higher, and wind supply quantity when normally producing is about 2/3 of nominal air delivery, all the other air quantity of 1/3 are namely emptying by surge tank, cause electricity to waste in a large number.3, oxidation reaction heat adopts fused salt circulation, and by pipeline fused salt storage tank to function of environment heat emission, a large amount of reaction heat energy is not utilized.
Summary of the invention
The present invention seeks to propose to overcome the energy-saving oxidation anthraquinone process units that existing production industry exists above problem.
The present invention includes blower fan, also comprise be connected in series successively by pipeline molten anthracene still, anthracene vaporization still, blender, oxidator, spark arrester and cooling cylinder, also connect hot-blast stove at the entrance point of described blender, also comprise the fused salt circulatory system of carrying out heat exchange with described oxidator; It is characterized in that: material-air heat exchanger is set in spark arrester, in the pipeline of the described fused salt circulatory system, be connected in series fused salt-air heat exchanger; The delivery outlet of blower fan connects air cushioning tank, air cushioning tank arranges three air outlet slits: primary outlet is connected to the air intlet of hot-blast stove by the first air flow rate adjustment valve; Second outlet is connected to the air intlet of material-air heat exchanger by the secondth air flow rate adjustment valve, the air outlet slit of material-air heat exchanger is connected to the air intlet of hot-blast stove again; 3rd outlet connects the air intlet of fused salt-air heat exchanger by the 3rd air flow rate adjustment valve, the air outlet slit of described fused salt-air heat exchanger is also connected to the air intlet end of hot-blast stove again.
Operation principle of the present invention is: adopt air cushioning tank that the cold air that blower fan supplies is divided into three tunnels: first via cold air directly can enter the confession airduct of hot-blast stove; Second road cold air enters the material-air heat exchanger in spark arrester, the high-temperature material entered after reacting with oxidator in spark arrester carries out heat exchange, the material in spark arrester can be made to lower the temperature, make the cold air entered in spark arrester in material-air heat exchanger be heated up simultaneously, entered the confession airduct of hot-blast stove by the air outlet slit end of the material-air heat exchanger in spark arrester; What the 3rd road cold air entered fused salt-air heat exchanger carries out heat exchange with the heat from the fused salt circulatory system, this heat after air enter hot-blast stove for airduct by the port of export of the air of fused salt-air heat exchanger.
The present invention takes full advantage of the oxidation reaction heat that high-temperature molten salt and high-temperature material are taken out of, by material in fused salt-air heat exchanger and spark arrester-air heat exchanger preheating normal temperature air, for hot-blast stove provides preheated air, reclaim after oxidation reaction heat energy through heat exchanger, the EAT of hot-blast stove becomes 180 DEG C ~ 200 DEG C hot blasts from the normal temperature temperature of original device, greatly reduce the coal consumption of hot-blast stove, there is energy-conservation effect.
Separately, blower fan of the present invention is the roots blower adopting converter technique, can regulate air quantity, produce anthraquinone per ton and can save power consumption 35% than original device according to technological requirement.
Accompanying drawing explanation
Fig. 1 is a kind of structural representation of the present invention.
Detailed description of the invention
As shown in Figure 1, the present invention connects air cushioning tank 2 at the air outlet of frequency conversion roots blower 1, molten anthracene still 3, anthracene vaporization still 4, blender 5, oxidator 6, spark arrester 7 and multi-stage condensing case 8 are connected in series successively by pipeline, hot-blast stove 9 is also connected in series at the entrance point of blender 5, fused salt tank 10 is connected with oxidator 6, realizes heat exchange by the fused salt circulatory system.Air cushioning tank 2 is serially connected on the pipeline between the air outlet of frequency conversion roots blower 1 and hot-blast stove 9.Material-air heat exchanger 15 is arranged in spark arrester 7.
Air cushioning tank 2 is provided with three ports of export, first port of export is connected on the confession airduct of hot-blast stove 9 by control valve 11 and pipeline, second port of export is connected to the entrance point of the air of fused salt-air heat exchanger 14 by control valve 12 and pipeline, the 3rd port of export is connected to the air intlet end of the material-air heat exchanger 15 in spark arrester 1 by control valve 13 and pipeline.
The fused salt of fused salt-air heat exchanger 14 is imported and exported pipeline and is serially connected in oxidator 6 with the fused salt circulatory system of fused salt tank 10, the air outlet slit end of the material-air heat exchanger 15 in the port of export of the air system of fused salt heat exchanging device 14 and spark arrester 7 all respectively by pipeline be connected to hot-blast stove 9 on airduct.
Also be connected with superheated steam generator 17 by control valve 16 at the entrance point of anthracene vaporization still 4.
Pipeline between blender 5 and oxidator 6 is connected in series stop valve 18, the pipeline between stop valve 18 and blender 5 is connected in series atmospheric valve 19.
Claims (1)
1. energy-saving oxidation anthraquinone process units, comprise blower fan, also comprise be connected in series successively by pipeline molten anthracene still, anthracene vaporization still, blender, oxidator, spark arrester and cooling cylinder, also connect hot-blast stove at the entrance point of described blender, also comprise the fused salt circulatory system of carrying out heat exchange with described oxidator; It is characterized in that: material-air heat exchanger is set in spark arrester, in the pipeline of the described fused salt circulatory system, be connected in series fused salt-air heat exchanger; The delivery outlet of blower fan connects air cushioning tank, air cushioning tank arranges three air outlet slits: primary outlet is connected to the air intlet of hot-blast stove by the first air flow rate adjustment valve; Second outlet is connected to the air intlet of material-air heat exchanger by the second air flow rate adjustment valve, the air outlet slit of material-air heat exchanger is connected to the air intlet of hot-blast stove again; 3rd outlet connects the air intlet of fused salt-air heat exchanger by the 3rd air flow rate adjustment valve, the air outlet slit of described fused salt-air heat exchanger is also connected to the air intlet end of hot-blast stove; Described blower fan is employing frequency converter, variable-frequency motor is the roots blower of power source; The fused salt import and export pipeline of fused salt-air heat exchanger circulates with oxidator and fused salt tank and is connected in series.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210210135.1A CN103506060B (en) | 2012-06-25 | 2012-06-25 | Energy-saving type oxyanthraquinone production device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210210135.1A CN103506060B (en) | 2012-06-25 | 2012-06-25 | Energy-saving type oxyanthraquinone production device |
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| Publication Number | Publication Date |
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| CN103506060A CN103506060A (en) | 2014-01-15 |
| CN103506060B true CN103506060B (en) | 2015-01-07 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201210210135.1A Expired - Fee Related CN103506060B (en) | 2012-06-25 | 2012-06-25 | Energy-saving type oxyanthraquinone production device |
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Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11183881B2 (en) | 2015-09-11 | 2021-11-23 | Yank Technologies, Inc. | Injection molding electroplating for three-dimensional antennas |
| CN110002984B (en) * | 2019-04-30 | 2024-01-02 | 山西豪仑科化工有限公司 | System and method for anthraquinone upgrading |
| CN110590527B (en) * | 2019-08-19 | 2022-07-12 | 浙江工业大学 | Process for continuously synthesizing anthraquinone by liquid phase method and synthesis system thereof |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3855252A (en) * | 1968-07-15 | 1974-12-17 | Ashland Oil Inc | Liquid phase oxidation of condensed-ring aromatic hydrocarbons |
| US4446070A (en) * | 1981-06-10 | 1984-05-01 | Hri, Inc. | Catalytic oxidation of polynuclear aromatic hydrocarbons |
| CN202643600U (en) * | 2012-06-25 | 2013-01-02 | 江苏润江精细化工有限公司 | Energy-saving oxyanthraquinone production device |
-
2012
- 2012-06-25 CN CN201210210135.1A patent/CN103506060B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3855252A (en) * | 1968-07-15 | 1974-12-17 | Ashland Oil Inc | Liquid phase oxidation of condensed-ring aromatic hydrocarbons |
| US4446070A (en) * | 1981-06-10 | 1984-05-01 | Hri, Inc. | Catalytic oxidation of polynuclear aromatic hydrocarbons |
| CN202643600U (en) * | 2012-06-25 | 2013-01-02 | 江苏润江精细化工有限公司 | Energy-saving oxyanthraquinone production device |
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| CN103506060A (en) | 2014-01-15 |
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Granted publication date: 20150107 Termination date: 20190625 |