CN110498726A - The extractant modified technique of acetonitrile method light dydrocarbon separation - Google Patents
The extractant modified technique of acetonitrile method light dydrocarbon separation Download PDFInfo
- Publication number
- CN110498726A CN110498726A CN201810478365.3A CN201810478365A CN110498726A CN 110498726 A CN110498726 A CN 110498726A CN 201810478365 A CN201810478365 A CN 201810478365A CN 110498726 A CN110498726 A CN 110498726A
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- CN
- China
- Prior art keywords
- acetonitrile
- extractant
- light dydrocarbon
- separation
- method light
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/10—Purification; Separation; Use of additives by extraction, i.e. purification or separation of liquid hydrocarbons with the aid of liquids
Abstract
The present invention relates to the extractant modified techniques of acetonitrile method light dydrocarbon separation, it include light dydrocarbon raw material and acetonitrile, additional proportion is propyl alcohol 1-10% in the extractant of acetonitrile method light dydrocarbon separation, acetone 1-10%, propenyl 1-10%, water 1-10%, to change the composition of the acetonitrile in extracting system, change the effect of extracting of acetonitrile, improve its extraction yield, reduce the ratio of acetonitrile and C_5 olefins that production extraction process needs, to reduce the steam consumption of production process, the heat of waste water passes to cracking c_5 raw material in washing simultaneously, the temperature of raw material increases, reduce the energy consumption of light dydrocarbon pretreatment system, energy conservation and environmental protection, improve effect of extracting.
Description
Technical field
The present invention relates to industrial chemicals technical fields, more specifically refer to the modified work of the extractant of acetonitrile method light dydrocarbon separation
Skill.
Background technique
The extraction process of country's acetonitrile method light dydrocarbon separator uses pure acetonitrile at present, and production extraction process needs
Acetonitrile and the ratios of C_5 olefins be 6-8:1, the acetonitrile internal circulating load of production process is larger, and the extractant of circulation is recycled at one
Period, (cycle period referred to that acetonitrile itself does not consume in systems, i.e., as shown in Figure 1, original acetonitrile is first mixed into light dydrocarbon
Extraction A tower, subsequently into extraction B tower, enter back into extraction C tower, then into cross after acetonitrile recovery tower return to it is mixed with light dydrocarbon material
Closing into extraction A tower is a cycle period) in, to pass through multiple condensation and vaporization, to cause a large amount of steam and circulation cold
But the waste of water.
Therefore, it is necessary to develop the extractant modified technique of acetonitrile method light dydrocarbon separation.
Summary of the invention
Present invention aims to overcome that the defect of the prior art, provides the extractant modified technique of acetonitrile method light dydrocarbon separation,
Energy conservation and the technique for improving acetonitrile extraction effect.
In order to solve the above technical problems, the present invention provides the extractant modified technique of acetonitrile method light dydrocarbon separation,
It include light dydrocarbon raw material and acetonitrile, additional proportion is propyl alcohol 1- in the extractant of the acetonitrile method light dydrocarbon separation
10%, acetone 1-10%, propenyl 1-10%, water 1-10%；The extractant add respectively extracting system extraction tower A and
In extraction tower C, keeps the pure acetonitrile of solvent modified, the effect of extracting of solvent is improved, to reduce solvent recycling amount.
Further scheme is, when the pure acetonitrile extraction, the ratio of acetonitrile and C_5 olefins is that 6-8:1 is down to acetonitrile and carbon
The ratio of five alkene is 3-4:1.
Further scheme is that the acetonitrile in the extracting system drops to acetonitrile internal circulating load 36- for internal circulating load 72-96 tons per hour
48 tons.
Further scheme is that the extracting system can save 3-5 tons of steam consumption per hour.
Compared with the prior art, the invention has the advantages that: technique of the invention is in acetonitrile method light dydrocarbon separator
The modifying agent of the similar compatibilities such as propyl alcohol, acetone, propenyl, water is added in extractant, changes the effect of extracting of acetonitrile, improves its extraction
Rate is taken, the ratio of acetonitrile and C_5 olefins that production extraction process needs is reduced, to reduce the steam consumption of production process.
Detailed description of the invention
Fig. 1 is the flow diagram for the extractant modified technique that the acetonitrile method light dydrocarbon of the specific embodiment of the invention separates.
Specific embodiment
The invention will now be described in further detail with reference to the accompanying drawings.
It include light dydrocarbon raw material and acetonitrile as shown in Figure 1, specific embodiments of the present invention one, the separation of acetonitrile method light dydrocarbon
Additional proportion is propyl alcohol 1-10%, acetone 1-10%, propenyl 1-10%, water 1-10% in extractant；The separation of acetonitrile method light dydrocarbon
Extractant added in the extraction tower A and extraction tower C of extracting system respectively, keep the pure acetonitrile of solvent modified.
Wherein the ratio of acetonitrile and C_5 olefins is that 6-8:1 is down to acetonitrile and the ratio of C_5 olefins is when pure acetonitrile extraction
3-4:1。
The acetonitrile of the above extracting system drops to 36-48 tons of acetonitrile internal circulating load for internal circulating load 72-96 tons per hour.
Entire extracting system can save 3-5 tons of steam consumption per hour.
As shown in Figure 1, detailed process is as follows: propyl alcohol, acetone, third being added in the extractant of acetonitrile method light dydrocarbon separator
The modifying agent one or more of the similar compatibilities such as enol, water mix, additional proportion propyl alcohol 1-10%, and acetone 1-10% is added, adds
Enter propenyl 1-10%, water 1-10% is added, thus change the composition of the acetonitrile in extracting system, modified change extractant
Effect of extracting, can by the ratio of acetonitrile when pure acetonitrile extraction and C_5 olefins be 6-8:1, acetonitrile internal circulating load hourly
72-96 tons, the ratio of modified acetonitrile and C_5 olefins drops to 3-4:1, and acetonitrile internal circulating load hourly drops to 36-48 tons, from
And the internal circulating load of extractant in systems is reduced, the temperature for recycling acetonitrile is 50 DEG C or so, and 100 DEG C of the solvent temperature in tower
Left and right is equivalent to and saves 36-48 tons of acetonitrile per hour and be heated to 100 DEG C of energy consumption from 50 DEG C, to reduce extraction process
Steam consumption, extracting system can save 3-5 tons of steam consumption (steam pressure 3.5Mpa) per hour.
Technique of the invention is that additional proportion is propyl alcohol 1-10%, acetone 1- in the extractant of acetonitrile method light dydrocarbon separation
10%, propenyl 1-10%, water 1-10%, thus change the composition of the acetonitrile in extracting system, modified change extractant
Effect of extracting, acetonitrile internal circulating load hourly drops to 36-48 tons, to reduce the internal circulating load of extractant in systems, from
And the steam consumption of extraction process is reduced, extracting system can save 3-5 tons of steam consumption per hour, and energy conservation and environmental protection improves
Effect of extracting.
The foregoing is merely this patent preferred embodiments, not limit this patent range, all using specification and attached
Equivalent structure or equivalent flow shift made by figure content is directly or indirectly used in other relevant technical fields, belongs to
The scope of this patent.
Claims (4)
1. a kind of extractant modified technique of acetonitrile method light dydrocarbon separation, it is characterised in that: it include light dydrocarbon raw material and acetonitrile, it is described
Additional proportion is propyl alcohol 1-10%, acetone 1-10%, propenyl 1-10%, water 1- in the extractant of acetonitrile method light dydrocarbon separation
10%；The extractant of the acetonitrile method light dydrocarbon separation is added respectively in the extraction tower A and extraction tower B of extracting system, makes solvent
Pure acetonitrile is modified.
2. the extractant modified technique of acetonitrile method light dydrocarbon separation as described in claim 1, it is characterised in that: the pure acetonitrile extraction
When taking, the ratio of the acetonitrile and C_5 olefins is that be down to acetonitrile and the ratio of C_5 olefins be 3-4:1 to 6-8:1.
3. the extractant modified technique of acetonitrile method light dydrocarbon separation as described in claim 1, it is characterised in that: the extracting system
Acetonitrile drop to 36-48 tons of acetonitrile internal circulating load for internal circulating load 72-96 tons per hour.
4. the extractant modified technique of acetonitrile method light dydrocarbon separation as described in claim 1, it is characterised in that: the extracting system
3-5 tons of steam consumption can be saved per hour.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201810478365.3A CN110498726A (en) | 2018-05-18 | 2018-05-18 | The extractant modified technique of acetonitrile method light dydrocarbon separation |
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| CN201810478365.3A CN110498726A (en) | 2018-05-18 | 2018-05-18 | The extractant modified technique of acetonitrile method light dydrocarbon separation |
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| CN102452883A (en) * | 2010-10-22 | 2012-05-16 | 中国石油化工股份有限公司 | Method of separating C5 fraction by using DMF mixed solvent |
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Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB855760A (en) * | 1958-09-17 | 1960-12-07 | Exxon Research Engineering Co | Recovery of isoprene by fractionation and extractive distillation |
| GB1113279A (en) * | 1965-10-18 | 1968-05-08 | Exxon Research Engineering Co | Isoprene purification process |
| US4419188A (en) * | 1980-06-02 | 1983-12-06 | Mccall Thomas F | Thermally coupled extractive distillation process |
| EP1069101A1 (en) * | 1999-07-12 | 2001-01-17 | Basf Aktiengesellschaft | Process for the preparation of C5-/C6-olefins |
| CN1709841A (en) * | 2005-06-29 | 2005-12-21 | 烟台大学 | Method for separating butene and tetrane using acetonitrile series mixed solvent |
| CN101450885A (en) * | 2007-12-07 | 2009-06-10 | 中国石油化工股份有限公司 | Method for separating carbon 5 fraction by one-stage extraction and rectification |
| CN101798255A (en) * | 2009-02-11 | 2010-08-11 | 中国石油天然气股份有限公司 | Method for separating diolefin from petroleum cracking C5 fraction by acetonitrile |
| CN101544534A (en) * | 2009-04-16 | 2009-09-30 | 中国石油兰州石油化工公司 | Method for directly separating and purifying cyclopentene from C5 raw material adopting extraction and distillation technology |
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Application publication date: 20191126 |