CN102952562A - Petronaphthalene rectification reflux temperature control device and control method thereof - Google Patents
Petronaphthalene rectification reflux temperature control device and control method thereof Download PDFInfo
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- CN102952562A CN102952562A CN2012104468238A CN201210446823A CN102952562A CN 102952562 A CN102952562 A CN 102952562A CN 2012104468238 A CN2012104468238 A CN 2012104468238A CN 201210446823 A CN201210446823 A CN 201210446823A CN 102952562 A CN102952562 A CN 102952562A
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Abstract
The invention relates to the field of petronaphthalene rectification technology, in particular to a petronaphthalene rectification reflux temperature control device and a control method thereof; the petronaphthalene rectification reflux temperature control device comprises a rectification tower, a condenser, a reflux tank, a tower top reflux pump, a naphthalene gas absorption tank and a naphthalene gas absorption tower; the upper end of the naphthalene gas absorption tank and the lower end of the naphthalene gas absorption tower are fixedly connected together and communicated with each other, a rectification tower air outlet is arranged at the top of the rectification tower, a rectification tower liquid inlet is arranged in the upper part of the rectification tower, the rectification tower air outlet and a tube pass inlet of the condenser are fixedly connected together by a first pipeline, and a tube pass outlet of the condenser and a top inlet of the reflux tank are fixedly connected together by a second pipeline. Through the combination of the rectification tower, the condenser, the reflux tank, the tower top reflux pump, the naphthalene gas absorption tank and the naphthalene gas absorption tower, the purposes of easily controlling the reflux temperature and recovering naphthalene gas can be realized, the petroleum naphthalene refined reflux temperature control device and the control method thereof have the characteristics of easily controlling the reflux temperature and being environment-friendly, the production efficiency is improved and the production cost is saved.
Description
Technical field
The present invention relates to petronaphthalene distillation technology field, is a kind of petronaphthalene rectifying reflux temperature control device and control method thereof.
Background technology
Be the white plates crystal under the petronaphthalene normal temperature, have special odor, volatile, easily distillation, density 1.162,80.5 ℃ of fusing points, 217.9 ℃ of boiling points, water insoluble, be dissolved in ethanol and ether etc.When adopting rectifier unit that ethylene bottom oil is carried out cutting and separating, because petronaphthalene component wherein is because of the character that high temperature is easily vaporized, low temperature easily solidifies, so reflux temperature control difficulty is larger.
Summary of the invention
The invention provides a kind of petronaphthalene rectifying reflux temperature control device and control method thereof, overcome the deficiency of above-mentioned prior art, the uppity problem of reflux temperature when it can effectively solve ethylene bottom oil and carries out cutting and separating.
One of technical scheme of the present invention realizes by following measures: a kind of petronaphthalene rectifying reflux temperature control device comprises rectifying tower, condenser, return tank, trim the top of column pump, naphthalene aspiration closed cans and naphthalene gas absorption tower; The lower end on the upper end of naphthalene aspiration closed cans and naphthalene gas absorption tower is fixed together and communicates, at the top of rectifying tower the rectifying tower air outlet is arranged, on the top of rectifying tower the rectifying tower fluid inlet is arranged, the tube side import of rectifying tower air outlet and condenser is fixed together by the first pipeline, the tube side outlet of condenser and the top inlet of return tank are fixed together by the second pipeline, the import of the outlet at bottom of return tank and trim the top of column pump is fixed together by the 3rd pipeline, and trim the top of column pump outlet and rectifying tower fluid inlet are fixed together by the 4th pipeline; At the top on naphthalene gas absorption tower air outlet, naphthalene gas absorption tower is arranged, inner chamber top on naphthalene gas absorption tower is installed with spray thrower, inner chamber middle part on naphthalene gas absorption tower is installed with filler, in filler, be installed with steam coils, the top inlet of the top exit of return tank and naphthalene aspiration closed cans is fixed together by the 5th pipeline, outlet at bottom in naphthalene aspiration closed cans is fixedly connected with the 6th pipeline, import at spray thrower is installed with the 7th pipeline, the outer end of the 7th pipeline is positioned at outside the naphthalene gas absorption tower, import at steam coils is fixedly connected with respectively the 8th pipeline and the 9th pipeline with exporting, the outer end of the 8th pipeline and the 9th pipeline is positioned at outside the naphthalene aspiration closed cans, shell side import at condenser is fixedly connected with the tenth pipeline, shell side outlet at condenser is fixedly connected with the 11 pipeline, on the tenth pipeline, be installed with respectively thermometer and valve, be installed with thermometer at the second line.
The below is the further optimization and/or improvements to one of foregoing invention technical scheme:
There are hot-water cylinder, hot water circulating pump and water cooler in the above-mentioned outside at condenser; Be installed with the thermal oil coil pipe in hot-water cylinder, be fixedly connected with respectively the 12 pipeline and the 13 pipeline in the import of thermal oil coil pipe and outlet, the outer end of the 12 pipeline and the 13 pipeline is positioned at outside the hot-water cylinder; The outlet at bottom of hot-water cylinder and the import of hot water circulating pump are fixed together by the 14 pipeline, the tube side import of hot water circulation pump outlet and water cooler is fixed together by the 15 pipeline, the tube side outlet of water cooler and the shell side import of condenser are fixed together by the tenth pipeline, the shell side outlet of condenser and the top inlet of hot-water cylinder are fixed together by the 11 pipeline, shell side import at water cooler is fixedly connected with the 16 pipeline, is fixedly connected with the 17 pipeline in the outlet of the shell side of water cooler.
Above-mentionedly be installed with the 18 pipeline at the 4th pipeline, be fixedly connected with the 19 pipeline in air outlet, naphthalene gas absorption tower, be installed with vacuum pump at the 19 pipeline.
Two of technical scheme of the present invention realizes by following measures: a kind of control method of petronaphthalene rectifying reflux temperature control device, carry out in the steps below: the first step, contain the naphthalene mass percent less than 20% naphthalene gas absorption liquid by passing in the spray thrower of the 7th pipeline in the naphthalene gas absorption tower, naphthalene gas absorption liquid enters in the naphthalene aspiration closed cans and by the 6th pipeline after by the ejection of the spray thrower in the naphthalene gas absorption tower and discharges; Second step passes into steam by the 8th pipeline in steam coils, then steam flows out by the 9th pipeline; The 3rd step passed into hot water by the tenth pipeline in the shell side of condenser, then hot water flows out by the 11 pipeline; The 4th step, naphthalene steam in the rectifying tower enters in the tube side of condenser by the first pipeline, naphthalene steam carries out heat exchange with hot water in the condenser shell side and is separated into the gas-liquid mixed phase, gas-liquid mixed enters in the return tank by the second pipeline, the temperature out that gas-liquid mixed goes out the condenser tube side mutually is controlled to be 80 ℃ to 90 ℃, gas-liquid mixed enters mutually and is separated into gas phase and liquid phase in the return tank, liquid phase is successively by the 3rd pipeline, trim the top of column pump and the 4th pipeline enter in the rectifying tower, gas phase in the return tank enters in the naphthalene gas absorption tower by the 5th pipeline and naphthalene aspiration closed cans successively, and spray thrower sprays that the naphthalene gas absorption liquid that gets off is reverse to contact the reaction of generation mass-and heat-transfer in the gas phase in the naphthalene gas absorption tower and the naphthalene gas absorption tower; In the 5th step, the gas phase that is not absorbed by naphthalene gas absorption liquid after the reaction of generation mass-and heat-transfer is discharged by the 19 pipeline and vacuum pump, and the naphthalene gas absorption liquid after the absorption gas phase flows in the naphthalene aspiration closed cans and discharges by the 6th pipeline.
The below is two further optimization and/or improvements to the foregoing invention technical scheme:
The inlet temperature that above-mentioned hot water advances the condenser shell side is 80 ℃, and the temperature out that hot water goes out the condenser shell side is 80 ℃ to 90 ℃.
Above-mentioned vapor temperature is 120 ℃ to 170 ℃, and vapor pressure is 0.3Mpa to 0.8Mpa.
Above-mentioned rectifying tower pressure on top surface is-70kpa is to-92kpa.
Above-mentioned naphthalene gas absorption liquid is the aromatic hydrocarbon oil washing lotion.
Hot water in the above-mentioned condenser shell side enter in the hot-water cylinder by the 11 pipeline and with hot-water cylinder in the thermal oil coil pipe in thermal oil carry out heat exchange, hot water in the hot-water cylinder after the heat exchange enters in the tube side of water cooler by the 14 pipeline, hot water circulating pump and the 15 pipeline successively, enter in the tube side of condenser by the tenth pipeline after the recirculated water heat exchange in hot water in the water cooler tube side and the water cooler shell side, hot water forms circulation in the tube side of condenser.
The present invention is used in conjunction with by rectifying tower, condenser, return tank, trim the top of column pump, naphthalene aspiration closed cans and naphthalene gas absorption tower, realized that reflux temperature is easy to control and reclaim the purpose of naphthalene gas, have the advantages that to be easy to control reflux temperature and environmental protection, improve production efficiency, saved production cost.
Description of drawings
Accompanying drawing 1 is process flow diagram of the present invention.
Coding in the accompanying drawing is respectively: 1 is rectifying tower, and 2 is condenser, and 3 is return tank, 4 is the trim the top of column pump, and 5 is naphthalene aspiration closed cans, and 6 is naphthalene gas absorption tower, 7 is the first pipeline, and 8 is the second pipeline, and 9 is the 3rd pipeline, 10 is the 4th pipeline, and 11 is spray thrower, and 12 is filler, 13 is steam coils, and 14 is the 5th pipeline, and 15 is the 6th pipeline, 16 is the 7th pipeline, and 17 is the 8th pipeline, and 18 is the 9th pipeline, 19 is the tenth pipeline, and 20 is the 11 pipeline, and 21 is valve, 22 is hot-water cylinder, and 23 is hot water circulating pump, and 24 is water cooler, 25 is the thermal oil coil pipe, and 26 is the 12 pipeline, and 27 is the 13 pipeline, 28 is the 14 pipeline, 29 is the 15 pipeline, and 30 is the 16 pipeline, and 31 is the 17 pipeline, 32 is the 18 pipeline, and 33 is the 19 pipeline.
Embodiment
The present invention is not subjected to the restriction of following embodiment, can determine concrete embodiment according to technical scheme of the present invention and practical situation.
Embodiment 1, and this petronaphthalene rectifying reflux temperature control device comprises rectifying tower 1, condenser 2, return tank 3, trim the top of column pump 4, naphthalene aspiration closed cans 5 and naphthalene gas absorption tower 6; The lower end on the upper end of naphthalene aspiration closed cans 5 and naphthalene gas absorption tower 6 is fixed together and communicates, at the top of rectifying tower 1 the rectifying tower air outlet is arranged, on the top of rectifying tower 1 the rectifying tower fluid inlet is arranged, the tube side import of rectifying tower air outlet and condenser 2 is fixed together by the first pipeline 7, the tube side outlet of condenser 2 and the top inlet of return tank 3 are fixed together by the second pipeline 8, the import of the outlet at bottom of return tank 3 and trim the top of column pump 4 is fixed together by the 3rd pipeline 9, and the outlet of trim the top of column pump 4 and rectifying tower fluid inlet are fixed together by the 4th pipeline 10; At the top on naphthalene gas absorption tower 6 air outlet, naphthalene gas absorption tower is arranged, inner chamber top on naphthalene gas absorption tower 6 is installed with spray thrower 11, inner chamber middle part on naphthalene gas absorption tower 6 is installed with filler 12, in filler 12, be installed with steam coils 13, the top inlet of the top exit of return tank 3 and naphthalene aspiration closed cans 5 is fixed together by the 5th pipeline 14, outlet at bottom in naphthalene aspiration closed cans 5 is fixedly connected with the 6th pipeline 15, import at spray thrower 11 is installed with the 7th pipeline 16, the outer end of the 7th pipeline 16 is positioned at outside the naphthalene gas absorption tower 6, import at steam coils 13 is fixedly connected with respectively the 8th pipeline 17 and the 9th pipeline 18 with exporting, the outer end of the 8th pipeline 17 and the 9th pipeline 18 is positioned at outside the naphthalene aspiration closed cans 5, shell side import at condenser 2 is fixedly connected with the tenth pipeline 19, shell side outlet at condenser 2 is fixedly connected with the 11 pipeline 20, be installed with respectively thermometer and valve 21 on the tenth pipeline 19,8 are installed with thermometer on the second line.
Embodiment 2, are with the difference of embodiment 1: hot-water cylinder 22, hot water circulating pump 23 and water cooler 24 are arranged in the outside of condenser 2; Be installed with thermal oil coil pipe 25 in hot-water cylinder 22, the outer end that is fixedly connected with respectively the 12 pipeline 26 and the 13 pipeline 27, the 12 pipelines 26 and the 13 pipeline 27 in the import of thermal oil coil pipe 25 and outlet is positioned at outside the hot-water cylinder 22; The import of the outlet at bottom of hot-water cylinder 22 and hot water circulating pump 23 is fixed together by the 14 pipeline 28, the tube side import of the outlet of hot water circulating pump 23 and water cooler 24 is fixed together by the 15 pipeline 29, the tube side outlet of water cooler 24 and the shell side import of condenser 2 are fixed together by the tenth pipeline 19, the shell side outlet of condenser 2 and the top inlet of hot-water cylinder 22 are fixed together by the 11 pipeline 20, shell side import at water cooler 24 is fixedly connected with the 16 pipeline 30, is fixedly connected with the 17 pipeline 31 in the outlet of the shell side of water cooler 24.
Embodiment 3, are with the difference of embodiment 1 and embodiment 2: be installed with the 18 pipeline 32 at the 4th pipeline 10, be fixedly connected with the 19 pipeline 33 in 6 air outlets, naphthalene gas absorption tower, be installed with vacuum pump at the 19 pipeline 33.Like this, occur it not to be discharged by the 19 pipeline 33 and vacuum pump by the gas phase of naphthalene gas absorption liquid absorption after the mass-and heat-transfer reaction.
Embodiment 4, a kind of control method of petronaphthalene rectifying reflux temperature control device, carry out in the steps below: the first step, contain the naphthalene mass percent less than 20% naphthalene gas absorption liquid by passing in the spray thrower 11 of the 7th pipeline 16 in the naphthalene gas absorption tower 6, naphthalene gas absorption liquid enters in the naphthalene aspiration closed cans 5 and by the 6th pipeline 15 after by spray thrower 11 ejections in the naphthalene gas absorption tower 6 and discharges; Second step passes into steam by the 8th pipeline 17 in steam coils 13, then steam flows out by the 9th pipeline 18; The 3rd step passed into hot water by the tenth pipeline 19 in the shell side of condenser 2, then hot water flows out by the 11 pipeline 20; The 4th step, naphthalene steam in the rectifying tower 1 enters in the tube side of condenser 2 by the first pipeline 7, naphthalene steam carries out heat exchange with hot water in condenser 2 shell sides and is separated into the gas-liquid mixed phase, gas-liquid mixed enters in the return tank 3 by the second pipeline 8, the temperature out that gas-liquid mixed goes out condenser 2 tube sides mutually is controlled to be 80 ℃ to 90 ℃, gas-liquid mixed enters mutually and is separated into gas phase and liquid phase in the return tank 3, liquid phase is successively by the 3rd pipeline 9, trim the top of column pump 4 and the 4th pipeline 10 enter in the rectifying tower 1, gas phase in the return tank 3 enters in the naphthalene gas absorption tower 6 by the 5th pipeline 14 and naphthalene aspiration closed cans 5 successively, and the naphthalene gas absorption liquid that spray thrower 11 sprays in the gas phase in the naphthalene gas absorption tower 6 and the naphthalene gas absorption tower 6 is reverse to contact the reaction of generation mass-and heat-transfer; In the 5th step, the gas phase that is not absorbed by naphthalene gas absorption liquid after the reaction of generation mass-and heat-transfer is discharged by the 19 pipeline 33 and vacuum pump, and the naphthalene gas absorption liquid after the absorption gas phase flows in the naphthalene aspiration closed cans 5 and discharges by the 6th pipeline 15.The naphthalene gas absorption liquid that sprays by spray thrower 11 in the gas phase in the naphthalene gas absorption tower 6 and the naphthalene gas absorption tower 6 is reverse to contact the reaction of generation mass-and heat-transfer, has prevented that naphthalene steam from being carried secretly to vacuum pump, stops up vacuum pump inlet after the cooling; By in the 8th pipeline 17, passing into steam, prevent gas phase crystallization in filler.
Embodiment 5, and as the optimization of above-described embodiment: the inlet temperature that hot water advances condenser 2 shell sides is 80 ℃, and the temperature out that hot water goes out condenser 2 shell sides is 80 ℃ to 90 ℃.
Embodiment 6, and as the optimization of above-described embodiment: vapor temperature is 120 ℃ to 170 ℃, and vapor pressure is 0.3Mpa to 0.8Mpa.
Embodiment 7, as the optimization of above-described embodiment: rectifying tower 1 tower top pressure is-70kpa is to-92kpa.
Embodiment 8, and as the optimization of above-described embodiment: naphthalene gas absorption liquid is the aromatic hydrocarbon oil washing lotion.
Embodiment 9, optimization as above-described embodiment: the hot water in condenser 2 shell sides enter in the hot-water cylinder 22 by the 11 pipeline 20 and with hot-water cylinder 22 in thermal oil coil pipe 25 in thermal oil carry out heat exchange, hot water in the hot-water cylinder 22 after the heat exchange enters in the tube side of water cooler 24 by the 14 pipeline 28, hot water circulating pump 23 and the 15 pipeline 29 successively, enter in the tube side of condenser 24 by the tenth pipeline 19 after the recirculated water heat exchange in hot water in water cooler 24 tube sides and water cooler 24 shell sides, hot water forms circulation in the tube side of condenser 2.During driving, passing into thermal oil by the 12 pipeline 26 in the thermal oil coil pipe 25 heats the hot water in the hot-water cylinder 22, the cat head generation naphthalene for the treatment of rectifying tower 1 returns when heating up in a steamer, close gradually heat-conducting oil heating, enable recirculated water in the water cooler 24 and keep hot water to advance condenser 2 shell side inlet temperatures be 80 ℃.
Above technical characterictic has consisted of embodiments of the invention, and it has stronger adaptability and implementation result, can increase and decrease according to actual needs non-essential technical characterictic, satisfies the demand of different situations.
Claims (10)
1. a petronaphthalene rectifying reflux temperature control device is characterized in that comprising rectifying tower, condenser, return tank, trim the top of column pump, naphthalene aspiration closed cans and naphthalene gas absorption tower; The lower end on the upper end of naphthalene aspiration closed cans and naphthalene gas absorption tower is fixed together and communicates, at the top of rectifying tower the rectifying tower air outlet is arranged, on the top of rectifying tower the rectifying tower fluid inlet is arranged, the tube side import of rectifying tower air outlet and condenser is fixed together by the first pipeline, the tube side outlet of condenser and the top inlet of return tank are fixed together by the second pipeline, the import of the outlet at bottom of return tank and trim the top of column pump is fixed together by the 3rd pipeline, and trim the top of column pump outlet and rectifying tower fluid inlet are fixed together by the 4th pipeline; At the top on naphthalene gas absorption tower air outlet, naphthalene gas absorption tower is arranged, inner chamber top on naphthalene gas absorption tower is installed with spray thrower, inner chamber middle part on naphthalene gas absorption tower is installed with filler, in filler, be installed with steam coils, the top inlet of the top exit of return tank and naphthalene aspiration closed cans is fixed together by the 5th pipeline, outlet at bottom in naphthalene aspiration closed cans is fixedly connected with the 6th pipeline, import at spray thrower is installed with the 7th pipeline, the outer end of the 7th pipeline is positioned at outside the naphthalene gas absorption tower, import at steam coils is fixedly connected with respectively the 8th pipeline and the 9th pipeline with exporting, the outer end of the 8th pipeline and the 9th pipeline is positioned at outside the naphthalene aspiration closed cans, shell side import at condenser is fixedly connected with the tenth pipeline, shell side outlet at condenser is fixedly connected with the 11 pipeline, on the tenth pipeline, be installed with respectively thermometer and valve, be installed with thermometer at the second line.
2. petronaphthalene rectifying reflux temperature control device according to claim 1 is characterized in that there are hot-water cylinder, hot water circulating pump and water cooler in the outside of condenser; Be installed with the thermal oil coil pipe in hot-water cylinder, be fixedly connected with respectively the 12 pipeline and the 13 pipeline in the import of thermal oil coil pipe and outlet, the outer end of the 12 pipeline and the 13 pipeline is positioned at outside the hot-water cylinder; The outlet at bottom of hot-water cylinder and the import of hot water circulating pump are fixed together by the 14 pipeline, the tube side import of hot water circulation pump outlet and water cooler is fixed together by the 15 pipeline, the tube side outlet of water cooler and the shell side import of condenser are fixed together by the tenth pipeline, the shell side outlet of condenser and the top inlet of hot-water cylinder are fixed together by the 11 pipeline, shell side import at water cooler is fixedly connected with the 16 pipeline, is fixedly connected with the 17 pipeline in the outlet of the shell side of water cooler.
3. petronaphthalene rectifying reflux temperature control device according to claim 1 and 2, it is characterized in that being installed with the 18 pipeline on the 4th pipeline, be fixedly connected with the 19 pipeline in air outlet, naphthalene gas absorption tower, be installed with vacuum pump at the 19 pipeline.
4. one kind according to claim 1 and 2 or the control method of 3 described petronaphthalene rectifying reflux temperature control device, it is characterized in that carrying out in the steps below: the first step, contain the naphthalene mass percent less than 20% naphthalene gas absorption liquid by passing in the spray thrower of the 7th pipeline in the naphthalene gas absorption tower, naphthalene gas absorption liquid enters in the naphthalene aspiration closed cans and by the 6th pipeline after by the ejection of the spray thrower in the naphthalene gas absorption tower and discharges; Second step passes into steam by the 8th pipeline in steam coils, then steam flows out by the 9th pipeline; The 3rd step passed into hot water by the tenth pipeline in the shell side of condenser, then hot water flows out by the 11 pipeline; The 4th step, naphthalene steam in the rectifying tower enters in the tube side of condenser by the first pipeline, naphthalene steam carries out heat exchange with hot water in the condenser shell side and is separated into the gas-liquid mixed phase, gas-liquid mixed enters in the return tank by the second pipeline, the temperature out that gas-liquid mixed goes out the condenser tube side mutually is controlled to be 80 ℃ to 90 ℃, gas-liquid mixed enters mutually and is separated into gas phase and liquid phase in the return tank, liquid phase is successively by the 3rd pipeline, trim the top of column pump and the 4th pipeline enter in the rectifying tower, gas phase in the return tank enters in the naphthalene gas absorption tower by the 5th pipeline and naphthalene aspiration closed cans successively, and spray thrower sprays that the naphthalene gas absorption liquid that gets off is reverse to contact the reaction of generation mass-and heat-transfer in the gas phase in the naphthalene gas absorption tower and the naphthalene gas absorption tower; In the 5th step, the gas phase that is not absorbed by naphthalene gas absorption liquid after the reaction of generation mass-and heat-transfer is discharged by the 19 pipeline and vacuum pump, and the naphthalene gas absorption liquid after the absorption gas phase flows in the naphthalene aspiration closed cans and discharges by the 6th pipeline.
5. the control method of petronaphthalene rectifying reflux temperature control device according to claim 4 is characterized in that the inlet temperature that hot water advances the condenser shell side is 80 ℃, and the temperature out that hot water goes out the condenser shell side is 80 ℃ to 90 ℃.
6. according to claim 4 or the control method of 5 described petronaphthalene rectifying reflux temperature control device, it is characterized in that vapor temperature is 120 ℃ to 170 ℃, vapor pressure is 0.3Mpa to 0.8Mpa.
7. according to claim 4 or the control method of 5 described petronaphthalene rectifying reflux temperature control device, it is characterized in that the rectifying tower pressure on top surface for-70kpa to-92kpa.
8. the control method of petronaphthalene rectifying reflux temperature control device according to claim 6, it is characterized in that the rectifying tower pressure on top surface for-70kpa to-92kpa.
9. according to claim 4 or 5 or 6 or 7 or 8 described petronaphthalene rectifying reflux temperature control device and control methods thereof, it is characterized in that naphthalene gas absorption liquid is the aromatic hydrocarbon oil washing lotion.
10. according to claim 4 or 5 or the control method of 6 or 7 or 8 or 9 described petronaphthalene rectifying reflux temperature control device, it is characterized in that hot water in the condenser shell side enters in the hot-water cylinder by the 11 pipeline and with hot-water cylinder in the thermal oil coil pipe in thermal oil carry out heat exchange, hot water in the hot-water cylinder after the heat exchange is successively by the 14 pipeline, hot water circulating pump and the 15 pipeline enter in the tube side of water cooler, enter in the tube side of condenser by the tenth pipeline after the recirculated water heat exchange in hot water in the water cooler tube side and the water cooler shell side, hot water forms circulation in the tube side of condenser.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201210446823.8A CN102952562B (en) | 2012-11-11 | 2012-11-11 | Petronaphthalene rectification reflux temperature control device and control method thereof |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201210446823.8A CN102952562B (en) | 2012-11-11 | 2012-11-11 | Petronaphthalene rectification reflux temperature control device and control method thereof |
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| CN102952562A true CN102952562A (en) | 2013-03-06 |
| CN102952562B CN102952562B (en) | 2014-04-30 |
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| CN201210446823.8A Expired - Fee Related CN102952562B (en) | 2012-11-11 | 2012-11-11 | Petronaphthalene rectification reflux temperature control device and control method thereof |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104877696A (en) * | 2015-05-08 | 2015-09-02 | 新疆独山子天利实业总公司 | Tar separation device |
| CN107510949A (en) * | 2017-09-26 | 2017-12-26 | 深圳市蓝石环保科技有限公司 | A kind of MVR vapo(u)rization systems |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3151176A (en) * | 1962-08-08 | 1964-09-29 | California Research Corp | Production of naphthalene |
| CN2797370Y (en) * | 2005-07-04 | 2006-07-19 | 段晨阳 | Distillation equipment for increasing phenol and naphthalene output in coal-tar oil processing |
| CN101250084A (en) * | 2008-04-01 | 2008-08-27 | 常熟市联邦化工有限公司 | Method for preparing petroleum naphthalene by using C+10 heavy aromatic hydrocarbon as raw material |
| CN101812311A (en) * | 2009-12-17 | 2010-08-25 | 曲靖众一精细化工股份有限公司 | Method for effectively refining tar anthracene oil and concentrating naphthalene |
| JP4592529B2 (en) * | 2005-08-08 | 2010-12-01 | Ｊｆｅケミカル株式会社 | Process for producing refined naphthalene absorption oil |
-
2012
- 2012-11-11 CN CN201210446823.8A patent/CN102952562B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3151176A (en) * | 1962-08-08 | 1964-09-29 | California Research Corp | Production of naphthalene |
| CN2797370Y (en) * | 2005-07-04 | 2006-07-19 | 段晨阳 | Distillation equipment for increasing phenol and naphthalene output in coal-tar oil processing |
| JP4592529B2 (en) * | 2005-08-08 | 2010-12-01 | Ｊｆｅケミカル株式会社 | Process for producing refined naphthalene absorption oil |
| CN101250084A (en) * | 2008-04-01 | 2008-08-27 | 常熟市联邦化工有限公司 | Method for preparing petroleum naphthalene by using C+10 heavy aromatic hydrocarbon as raw material |
| CN101812311A (en) * | 2009-12-17 | 2010-08-25 | 曲靖众一精细化工股份有限公司 | Method for effectively refining tar anthracene oil and concentrating naphthalene |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104877696A (en) * | 2015-05-08 | 2015-09-02 | 新疆独山子天利实业总公司 | Tar separation device |
| CN107510949A (en) * | 2017-09-26 | 2017-12-26 | 深圳市蓝石环保科技有限公司 | A kind of MVR vapo(u)rization systems |
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| Publication number | Publication date |
|---|---|
| CN102952562B (en) | 2014-04-30 |
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