CN202643600U - Energy-saving oxyanthraquinone production device - Google Patents
Energy-saving oxyanthraquinone production device Download PDFInfo
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- CN202643600U CN202643600U CN2012202987300U CN201220298730U CN202643600U CN 202643600 U CN202643600 U CN 202643600U CN 2012202987300 U CN2012202987300 U CN 2012202987300U CN 201220298730 U CN201220298730 U CN 201220298730U CN 202643600 U CN202643600 U CN 202643600U
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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
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Abstract
The utility model discloses an energy-saving oxyanthraquinone production device, which relates to the technical field of a production device for preparing anthraquinone from anthracene serving as a raw material through air oxidation. According to the energy-saving oxyanthraquinone production device, oxidation reaction heat brought out by high-temperature molten salt and a high-temperature material is fully utilized, constant temperature air is preheated through a molten salt-air heat exchanger and a material-air heat exchanger in a flame arrestor; preheated air is provided for a hot blast furnace; after the oxidation reaction heat energy is recovered by the heat exchangers, air inlet temperature of the hot blast furnace is changed from constant temperature of the original device into 180-200 DEG C; and thus, the coal consumption of the hot blast furnace is greatly reduced, and an energy-saving effect is achieved.
Description
Technical field
The utility model technology relates to take anthracene as raw material, through atmospheric oxidation, makes the production equipment technical field of anthraquinone.
Background technology
Take anthracene as raw material, through atmospheric oxidation, the dyestuff intermediate anthraquinone that makes (is commonly called as: the oxidation anthraquinone, to be different from synthetic anthraquinone) production, existing many decades is historical in China, technical process is: the anthracene of content 〉=90% is dropped into molten anthracene still heating and melting, squeeze into the vaporization still with submerged pump, in the vaporization still, pass into the 0.03Mpa superheated vapour again, make anthracene gasification, enter mixing tank, and enter the fixed bed oxidizer that phosphorus/vanadium catalyst is housed after 〉=250 ℃ of warm airs mix, make anthracene be oxidized to anthraquinone, because the empty ratio of anthracene, catalyst activity, the isoparametric impact of oxidizing reaction temperature, the simultaneously certain side reaction of association, oxidized byproduct is Tetra hydro Phthalic anhydride or until carbonic acid gas and water, what of side reaction directly affect the consumption of quality and the raw material anthracene of resultant anthraquinone.
The means of control oxidizing reaction state are in this device: 1, adopt the method for the flow of control superheated vapour to control the anthracene vaporization amount that enters oxidizer.2, employing is regulated the emptying method of roots blower air cushioning tank blow-off valve and is entered the oxidizer air capacity.3, adopt the fused salt recycle system to function of environment heat emission, take away reaction heat, to keep the relatively stable of temperature of reaction.
The defective that above-mentioned three kinds of control methods exist is: 1, in the manual operation regulation process, be difficult to precisely control, temperature of reaction is the result of many constitutive equations such as heat of being removed by anthracene quantity of steam, air capacity, speed of response (speed of response is subjected to again the variation of temperature of reaction and changes), reaction heat, salt bath, the particularly variation of temperature of reaction, bring the variation of oxidizing reaction speed, bring the variation of reaction heat, if side reaction is risen, reaction heat discharges in a large number, the more difficult grasp of temperature of reaction.During 2, because of the catalyst cycle activation, need than Wind Volume, so the configuration of roots blower air quantity is higher, and the wind supply quantity when normally producing is about 2/3 of nominal air delivery, and all the other air quantity of 1/3 are namely emptying by surge tank, cause electric weight to waste in a large number.3, oxidizing reaction thermal recovery fused salt circulation, is reacted in a large number heat energy and is not utilized to function of environment heat emission by pipeline fused salt storage tank.
Summary of the invention
The utility model purpose is to propose to overcome the energy-saving oxidation anthraquinone production equipment that there is above problem in existing production industry.
The utility model comprises blower fan, also comprise the molten anthracene still, anthracene vaporization still, mixing tank, oxidizer, spark arrester and the cooling cylinder that are connected in series successively by pipeline, entrance end at described mixing tank also connects hotblast stove, also comprises the fused salt recycle system of carrying out heat exchange with described oxidizer; It is characterized in that: material-air heat exchanger is set in spark arrester, in the pipeline of the described fused salt recycle system, is connected in series fused salt-air heat exchanger; The delivery port of blower fan connects the air cushioning tank, and at the air cushioning tank three airouts are set: primary outlet is connected to the air intlet of hotblast 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, and the airout of material-air heat exchanger is connected to the air intlet of hotblast stove again; The air intlet that the 3rd air flow rate adjustment valve connects fused salt-air heat exchanger is passed through in the 3rd outlet, and the airout of described fused salt-air heat exchanger also is connected to the air intlet end of hotblast stove again.
The utility model principle of work is: the freezing air that adopts the air cushioning tank that blower fan is supplied with is divided into three the tunnel: first via freezing air can directly enter the airduct that supplies of hotblast stove; The the second road freezing air enters the material-air heat exchanger in the spark arrester, carry out heat exchange with the high-temperature material that enters in the spark arrester after the oxidizer reaction, can make the material cooling in the spark arrester, make simultaneously the freezing air that enters in material-air heat exchanger in the spark arrester obtain heating up, by the airout end of the material-air heat exchanger in the spark arrester enter hotblast stove for airduct; The heat with from the fused salt recycle system that the Third Road freezing air enters fused salt-air heat exchanger carries out heat exchange, and the air after this is heated enters hotblast stove for airduct by the exit end of the air of fused salt-air heat exchanger.
The utility model takes full advantage of the oxidation reaction heat that high-temperature molten salt and high-temperature material are taken out of, by material-air heat exchanger preheating normal temperature air in fused salt-air heat exchanger and the spark arrester, for hotblast stove provides preheated air, after interchanger reclaims oxidizing reaction heat energy, the inlet temperature of hotblast stove becomes 180 ℃～200 ℃ hot blasts from the normal temperature temperature of original device, greatly reduce the consumption of coal of hotblast stove, had energy-conservation effect.
In addition, blower fan described in the utility model can be regulated air quantity according to processing requirement for adopting the roots blower of converter technique, produces anthraquinone per ton and can save power consumption 35% than original device.
Description of drawings
Fig. 1 is a kind of structural representation of the present utility model.
Embodiment
As shown in Figure 1, the utility model connects air cushioning tank 2 at the air outlet of frequency conversion roots blower 1, molten anthracene still 3, anthracene vaporization still 4, mixing tank 5, oxidizer 6, spark arrester 7 and multi-stage condensing case 8 are connected in series successively by pipeline, entrance end at mixing tank 5 also is connected in series hotblast stove 9, fused salt tank 10 links to each other with oxidizer 6, realizes heat exchange by the fused salt recycle system.Air cushioning tank 2 is serially connected on the air outlet and the pipeline between the hotblast stove 9 of frequency conversion roots blower 1.At spark arrester 7 interior layout material-air heat exchangers 15.
Air cushioning tank 2 is provided with three exit end, the first exit end is connected to supplying on the airduct of hotblast stove 9 by variable valve 11 and pipeline, the second exit end is connected to the entrance end of the air of fused salt-air heat exchanger 14 by variable valve 12 and pipeline, and the 3rd exit end is connected to the air intlet end of the material-air heat exchanger 15 in the spark arrester 1 by variable valve 13 and pipeline.
The fused salt import and export pipeline of fused salt-air heat exchanger 14 is serially connected in the fused salt recycle system of oxidizer 6 and fused salt tank 10, and the airout end of the material-air heat exchanger 15 in the exit end of the air system of fused salt heat exchanging device 14 and the spark arrester 7 all is connected to supplying on the airduct of hotblast stove 9 by pipeline respectively.
Entrance end at anthracene vaporization still 4 also is connected with superheated steam generator 17 by variable valve 16.
Pipeline serial connection trip valve 18 between mixing tank 5 and oxidizer 6, the pipeline serial connection blow-off valve 19 between trip valve 18 and mixing tank 5.
Claims (2)
1. energy-saving oxidation anthraquinone production equipment, comprise blower fan, also comprise the molten anthracene still, anthracene vaporization still, mixing tank, oxidizer, spark arrester and the cooling cylinder that are connected in series successively by pipeline, entrance end at described mixing tank also connects hotblast stove, also comprises the fused salt recycle system of carrying out heat exchange with described oxidizer; It is characterized in that: material-air heat exchanger is set in spark arrester, in the pipeline of the described fused salt recycle system, is connected in series fused salt-air heat exchanger; The delivery port of blower fan connects the air cushioning tank, and at the air cushioning tank three airouts are set: primary outlet is connected to the air intlet of hotblast 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, and the airout of material-air heat exchanger is connected to the air intlet of hotblast stove again; The air intlet that the 3rd air flow rate adjustment valve connects fused salt-air heat exchanger is passed through in the 3rd outlet, and the airout of described fused salt-air heat exchanger also is connected to the air intlet end of hotblast stove again.
2. described energy-saving oxidation anthraquinone production equipment according to claim 1 is characterized in that described blower fan is the roots blower of propulsion source for adopting frequency transformer, variable-frequency motor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012202987300U CN202643600U (en) | 2012-06-25 | 2012-06-25 | Energy-saving oxyanthraquinone production device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012202987300U CN202643600U (en) | 2012-06-25 | 2012-06-25 | Energy-saving oxyanthraquinone production device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202643600U true CN202643600U (en) | 2013-01-02 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012202987300U Expired - Fee Related CN202643600U (en) | 2012-06-25 | 2012-06-25 | Energy-saving oxyanthraquinone production device |
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| CN (1) | CN202643600U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103506060A (en) * | 2012-06-25 | 2014-01-15 | 江苏润江精细化工有限公司 | Energy-saving type oxyanthraquinone production device |
| CN110590527A (en) * | 2019-08-19 | 2019-12-20 | 浙江工业大学 | Process for continuously synthesizing anthraquinone by liquid phase method and synthesis system thereof |
-
2012
- 2012-06-25 CN CN2012202987300U patent/CN202643600U/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103506060A (en) * | 2012-06-25 | 2014-01-15 | 江苏润江精细化工有限公司 | Energy-saving type oxyanthraquinone production device |
| CN103506060B (en) * | 2012-06-25 | 2015-01-07 | 江苏润江精细化工有限公司 | Energy-saving type oxyanthraquinone production device |
| CN110590527A (en) * | 2019-08-19 | 2019-12-20 | 浙江工业大学 | Process for continuously synthesizing anthraquinone by liquid phase method and synthesis system thereof |
| 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 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130102 Termination date: 20190625 |
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| CF01 | Termination of patent right due to non-payment of annual fee |