CN101732883A - Adsorptive rectification tower for decoloring aromatic solvent oil and process method thereof - Google Patents
Adsorptive rectification tower for decoloring aromatic solvent oil and process method thereof Download PDFInfo
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- CN101732883A CN101732883A CN201010032301A CN201010032301A CN101732883A CN 101732883 A CN101732883 A CN 101732883A CN 201010032301 A CN201010032301 A CN 201010032301A CN 201010032301 A CN201010032301 A CN 201010032301A CN 101732883 A CN101732883 A CN 101732883A
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Abstract
The invention relates to a method for decoloring aromatic solvent oil-an adsorptive rectification decoloring method. An adsorptive rectification tower for decoloring the aromatic solvent oil comprises a rectification tower, and is characterized in that: the upper part of the rectification tower is provided with an adsorption device; and the top of the adsorption device is provided with a tower top reflux condensation device and the bottom of the adsorption device is provided with a rectifying section so as to form the adsorptive rectification tower. In the method for operating the adsorptive rectification tower for decoloring the aromatic solvent oil, the operation pressure of the tower top is between 0.01 and 0.05 MPa; the operation temperature of the tower top is between 100 and 170 DEG C; the operation temperature of the tower bottom is between 130 and 200 DEG C; the reflux ratio is between 0.8 and 1.5; the method is operated at normal pressure or reduced pressure and performs continuous or intermittent adsorptive rectification decoloring; the aromatic solvent oil with low chroma is acquired on the tower top; and heavy aromatic components are acquired on the tower bottom.
Description
Technical field
The present invention relates to a kind of method---absorption distillation decoloring method of solvent naphtha decolouring, be specially adapted to the deep decoloring aromatic solvent oil of colourity is obtained the superficial aromatic solvent naphtha of colourity.
Background technology
Aromatic solvent naphtha is widely used in the every field of national economy, is a class important chemical material.The colourity of aromatic solvent naphtha is the important indicator of aromatic solvent naphtha product quality, directly influences the range of application of aromatic solvent naphtha, if colourity is too high, the scope of application just is restricted greatly.Derive from the aromatic solvent naphtha of petrochemical industry and Coal Chemical Industry, usually colourity is very high, the processing of need decolouring.
Decoloring aromatic solvent oil method commonly used at present has absorption method, rectification method etc.
The absorption method decolouring is to add wait to decolour aromatic solvent naphtha and adsorbent in container, operates under conditions such as certain solid-to-liquid ratio, temperature, pressure, stirring, the time of staying, carries out decoloring aromatic solvent oil.The major defect of this method is to use a large amount of adsorbents, also will carry out Separation of Solid and Liquid, adsorbent cost and reclaimer operation expense height, and the aromatic solvent naphtha loss is big.
The rectification method decolouring has overcome the shortcoming of adsorbent decolouring, but decolorizing effect is usually undesirable, and the aromatic solvent naphtha colourity after the decolouring does not reach the effect of absorption method decolouring.
Summary of the invention
According to industrial needs, the invention provides a kind of new decoloring aromatic solvent oil equipment---adsorptive rectification tower and process thereof, be used for removing the substance that show color of aromatic solvent naphtha, reduce the colourity of aromatic solvent oil product, improve the quality of aromatic solvent naphtha.
This equipment is achieved in that
The adsorptive rectification tower that is used for decoloring aromatic solvent oil, comprise a rectifying column, it is characterized in that: an adsorbent equipment is installed on the top in rectifying column, and this is the overhead condensation reflux above adsorbent equipment, be rectifying section below, just formed an adsorptive rectification tower.
Treat the decolouring aromatic solvent naphtha with adsorptive rectification tower and carry out absorption distillation decolouring operation, the distillation process of rectifying section removes most of substance that show color, and remaining a small amount of substance that show color is adsorbed the adsorbents adsorb of device.
Described rectifying column adopts stuffing rectification column, or adopts plate distillation column.
Described adsorbent equipment is one and the isometrical empty tube of rectifying tower body, and empty tube bottom is adorned a porous plate, in order to carry the adsorbent of loading in the empty tube.This is the overhead condensation reflux above adsorbent equipment, is rectifying section below.
Adsorbent in the adsorbent equipment of described adsorptive rectification tower adopts one or more mixing in active carbon, activated coke, molecular sieve, the macroreticular resin.
The adsorptive rectification tower method of operating that is used for decoloring aromatic solvent oil, operating pressure cat head 0.01～0.05MPa, 100 ℃～170 ℃ of operating temperature cats head, at the bottom of the tower 130～200 ℃, reflux ratio 0.8～1.5, normal pressure or decompression operation carry out continuously or intermittently absorption distillation decolouring, cat head obtains low colourity aromatic solvent naphtha, is the aromatic hydrocarbons heavy ends at the bottom of the tower.
The invention has the advantages that, owing in adsorptive rectification tower, made up rectifying section and adsorbent equipment, rectifying section removes most of substance that show color, adsorbent equipment removes remaining substance that show color, rectifying section has alleviated the absorption burden of adsorbent, and adsorbent equipment has overcome rectifying section separating power defect of insufficient, has greatly improved the efficient of decoloring aromatic solvent oil, save a large amount of adsorbents, simplified operation greatly.
Description of drawings
Fig. 1 is the adsorptive rectification tower schematic diagram of continued operation, and 1 is rectifying section among the figure, the 2nd, and adsorbent equipment, the 3rd, overhead condensation reflux, S1 are chargings, and S2 is aromatic hydrocarbons heavy ends at the bottom of the tower, and S3 is an overhead product.
The adsorptive rectification tower of intermittently operated follows the absorption distillation tower structure of continued operation identical, so difference is in preceding disposable being fed in the tower still of driving, the disposable discharge aromatic hydrocarbons heavy ends from the tower still in the back of stopping provide schematic diagram no longer in addition.
The specific embodiment
Following examples are used for further specifying content of the present invention, do not limit application of the present invention.Colourity is the nickel-to-cobalt ratio look without exception.
Referring to accompanying drawing 1: the adsorptive rectification tower that is used for decoloring aromatic solvent oil, comprise a rectifying column, it is characterized in that: an adsorbent equipment 2 is installed on the top in rectifying column, and this is overhead condensation reflux 3 above adsorbent equipment 2, be rectifying section 1 below, just formed an adsorptive rectification tower.
No. 15 aromatic solvent naphthas of pseudocumene tower background color degree from catalytic reforming carbon nine system pseudocumene devices feed adsorptive rectification tower from rectifying section 1, and the rectifying section of adsorptive rectification tower adopts the packed tower form, and its rectifying section is loaded structured packing.Adsorbent equipment is one and the isometrical empty tube of absorption distillation tower body, and empty tube bottom has porous plate, loads 13X type molecular sieve, 1.2 meters of adsorbent equipment height, 8 meters of the packed heights of rectifying section, operating pressure cat head 0.05MPa (absolute pressure), 130 ℃ of operating temperature cats head, at the bottom of the tower 160～170 ℃, reflux ratio 1.1 is carried out the absorption distillation decolouring continuously, and cat head obtains No. 0.5 solvent naphtha of colourity, yield 75% is the aromatic hydrocarbons heavy ends at the bottom of the tower.
From No. 11 aromatic solvent naphthas of carbon nine hydrogenation rectifying colourities, feed an adsorptive rectification tower, the rectifying section of adsorptive rectification tower adopts porous plate plate column form.Adsorbent equipment is one and the isometrical empty tube of absorption distillation tower body, and empty tube bottom has porous plate, loads activated coke in the empty tube, 10 meters of rectifying section height, 1.5 meters of adsorbent equipment height, operating pressure cat head 0.03MPa (absolute pressure), 110 ℃ of operating temperature cats head, at the bottom of the tower 170～180 ℃, reflux ratio 1.5 is carried out the absorption distillation decolouring continuously, and cat head obtains No. 2 solvent naphthas of colourity, yield 83% is the aromatic hydrocarbons heavy ends at the bottom of the tower.
From No. 11 aromatic solvent naphthas of carbon nine hydrogenation rectifying colourities, feed an adsorptive rectification tower, the rectifying section of adsorptive rectification tower adopts the board-like turriform formula of T type float valve.Adsorbent equipment is one and the isometrical empty tube of absorption distillation tower body, and empty tube bottom has porous plate, loads activated carbon in the empty tube, 10 meters of rectifying section height, 1.5 meters of adsorbent equipment height, operating pressure cat head 0.02MPa (absolute pressure), reflux ratio 1.5,110 ℃ of operating temperature cats head, at the bottom of the tower 170～180 ℃, carry out the absorption distillation decolouring continuously, cat head obtains No. 1 solvent naphtha of colourity, yield 85% is the aromatic hydrocarbons heavy ends at the bottom of the tower.
Embodiment 4
No. 15 aromatic solvent naphthas of pseudocumene tower background color degree from catalytic reforming carbon nine system pseudocumene devices feed an adsorptive rectification tower, and the rectifying section of adsorptive rectification tower adopts the packed tower form, and rectifying section is loaded structured packing.Adsorbent equipment is one and the isometrical empty tube of absorption distillation tower body, and empty tube bottom has porous plate, loads the BS-55 macroporous absorbent resin in the empty tube, 8 meters of packing section height, 1.2 meters of adsorbent equipment height, operating pressure cat head 0.01MPa (absolute pressure), 100 ℃ of operating temperature cats head, at the bottom of the tower 130～140 ℃, reflux ratio 1.1 is carried out the absorption distillation decolouring continuously, and cat head obtains No. 1 solvent naphtha of colourity, yield 77% is the aromatic hydrocarbons heavy ends at the bottom of the tower.
Embodiment 5
From No. 9 aromatic solvent naphthas of carbon nine hydrogenation rectifying colourities, feed an adsorptive rectification tower, the rectifying section of adsorptive rectification tower adopts the packed tower form, and rectifying section is loaded structured packing.Adsorbent equipment is one and the isometrical empty tube of absorption distillation tower body, and empty tube bottom has porous plate, loads activated carbon and activated coke according to 1: 1 (weight) in the empty tube, 3 meters of rectifying section height, 1.5 meters of adsorbent equipment height, atmospheric operation, 160 ℃ of operating temperature cats head, at the bottom of the tower 170～180 ℃, reflux ratio 1.0 is carried out the absorption distillation decolouring continuously, and cat head obtains No. 1 solvent naphtha of colourity, yield 90% is the aromatic hydrocarbons heavy ends at the bottom of the tower.
Embodiment 6
From No. 9 aromatic solvent naphthas of carbon nine hydrogenation rectifying colourities, feed an adsorptive rectification tower, the rectifying section of adsorptive rectification tower adopts the packed tower form, and rectifying section is loaded structured packing.Adsorbent equipment is one and the isometrical empty tube of absorption distillation tower body, and empty tube bottom has porous plate, loads activated carbon and activated coke according to 1: 1 (weight) in the empty tube, 3 meters of rectifying section height, 1.5 meters of adsorbent equipment height, atmospheric operation, 170 ℃ of operating temperature cats head, at the bottom of the tower 200 ℃, reflux ratio 0.8 is intermittently carried out the absorption distillation decolouring, and cat head obtains No. 2 solvent naphthas of colourity, yield 85% is the aromatic hydrocarbons heavy ends at the bottom of the tower.
Claims (5)
1. the adsorptive rectification tower that is used for decoloring aromatic solvent oil comprises a rectifying column, it is characterized in that: an adsorbent equipment is installed on the top in rectifying column, has just formed an adsorptive rectification tower.
2. the adsorptive rectification tower that is used for decoloring aromatic solvent oil according to claim 1 is characterized in that: described rectifying column adopts stuffing rectification column, or adopts plate distillation column.
3. the adsorptive rectification tower that is used for decoloring aromatic solvent oil according to claim 1 is characterized in that: described adsorbent equipment is one and the isometrical empty tube of rectifying tower body, and empty tube bottom is adorned a porous plate, in order to carry the adsorbent of loading in the empty tube.
4. according to claim 1 or the 3 described adsorptive rectification towers that are used for decoloring aromatic solvent oil, it is characterized in that: the adsorbent in the described adsorbent equipment adopts one or more mixing in active carbon, activated coke, molecular sieve, the macroreticular resin.
5. the adsorptive rectification tower method of operating that is used for decoloring aromatic solvent oil, it is characterized in that: operating pressure cat head 0.01～0.05MPa, 100 ℃～170 ℃ of operating temperature cats head, at the bottom of the tower 130～200 ℃, reflux ratio 0.8～1.5, normal pressure or decompression operation carry out continuously or intermittently absorption distillation decolouring, cat head obtains low colourity aromatic solvent naphtha, is the aromatic hydrocarbons heavy ends at the bottom of the tower.
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| CN106902770A (en) * | 2017-03-14 | 2017-06-30 | 安徽海德石油化工有限公司 | Adsorbent for decoloring aromatic solvent oil and preparation method thereof |
| CN110180202A (en) * | 2019-07-05 | 2019-08-30 | 黄河三角洲京博化工研究院有限公司 | The production system and production method of a kind of low coloration high boiling aromatic hydrocarbon solvent of width boiling range |
| CN110893285A (en) * | 2019-12-18 | 2020-03-20 | 大连福佳·大化石油化工有限公司 | Method for resolving PX by using low-consumption desorbent in desorbent regeneration tower |
| CN111234106A (en) * | 2020-03-11 | 2020-06-05 | 恒河材料科技股份有限公司 | Preparation method of liquid modified aromatic hydrocarbon petroleum resin |
| CN114292165A (en) * | 2021-12-10 | 2022-04-08 | 四川天采科技有限责任公司 | Partition wall tower type isopropanol solution adsorption, rectification, separation and purification method |
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| CN114715860A (en) * | 2022-04-27 | 2022-07-08 | 宏芯气体(上海)有限公司 | Ultra-high purity nitrogen production device capable of removing impurities |
| CN114836235A (en) * | 2022-05-09 | 2022-08-02 | 中海油天津化工研究设计院有限公司 | Method for separating aromatic hydrocarbon by coupling distillate oil adsorption and rectification |
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| CN1027888C (en) * | 1992-09-29 | 1995-03-15 | 北京化工学院 | Process for preparing n-decane from liquid wax |
| CN1045286C (en) * | 1995-03-30 | 1999-09-29 | 中国石油化工总公司石油化工科学研究院 | Technique for prepn. of high pureness meta-dimethyl benzene |
| DE19903566A1 (en) * | 1999-01-29 | 2000-08-03 | Linde Ag | Process for recovering an ethylene-rich fraction |
| CN1102591C (en) * | 1999-09-29 | 2003-03-05 | 中国石油化工集团公司 | Process for purifying and refining macrocyclic diester musk compounds |
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2010
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| CN106902770A (en) * | 2017-03-14 | 2017-06-30 | 安徽海德石油化工有限公司 | Adsorbent for decoloring aromatic solvent oil and preparation method thereof |
| CN110180202A (en) * | 2019-07-05 | 2019-08-30 | 黄河三角洲京博化工研究院有限公司 | The production system and production method of a kind of low coloration high boiling aromatic hydrocarbon solvent of width boiling range |
| CN110180202B (en) * | 2019-07-05 | 2021-10-26 | 黄河三角洲京博化工研究院有限公司 | Production system and production method of wide-distillation-range low-chroma high-boiling-point aromatic solvent |
| CN110893285A (en) * | 2019-12-18 | 2020-03-20 | 大连福佳·大化石油化工有限公司 | Method for resolving PX by using low-consumption desorbent in desorbent regeneration tower |
| CN111234106A (en) * | 2020-03-11 | 2020-06-05 | 恒河材料科技股份有限公司 | Preparation method of liquid modified aromatic hydrocarbon petroleum resin |
| CN114292165A (en) * | 2021-12-10 | 2022-04-08 | 四川天采科技有限责任公司 | Partition wall tower type isopropanol solution adsorption, rectification, separation and purification method |
| CN114591144A (en) * | 2021-12-10 | 2022-06-07 | 浙江天采云集科技股份有限公司 | One-tower type isopropanol solution adsorption, rectification, separation and purification method |
| CN114591144B (en) * | 2021-12-10 | 2023-11-21 | 浙江天采云集科技股份有限公司 | Tower type isopropanol solution adsorption, rectification, separation and purification method |
| CN114715860A (en) * | 2022-04-27 | 2022-07-08 | 宏芯气体(上海)有限公司 | Ultra-high purity nitrogen production device capable of removing impurities |
| CN114715860B (en) * | 2022-04-27 | 2023-10-27 | 宏芯气体(上海)有限公司 | Impurity-removing ultra-high purity nitrogen making device |
| CN114836235A (en) * | 2022-05-09 | 2022-08-02 | 中海油天津化工研究设计院有限公司 | Method for separating aromatic hydrocarbon by coupling distillate oil adsorption and rectification |
| CN114836235B (en) * | 2022-05-09 | 2023-11-07 | 中海油天津化工研究设计院有限公司 | Method for separating aromatic hydrocarbon by adsorption and rectification coupling of distillate oil |
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| CN101732883B (en) | 2012-05-30 |
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