CN104058920B - A kind of take alkane as the method for extraction agent separation of extractive distillation propylene-propane - Google Patents
A kind of take alkane as the method for extraction agent separation of extractive distillation propylene-propane Download PDFInfo
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- CN104058920B CN104058920B CN201310701140.7A CN201310701140A CN104058920B CN 104058920 B CN104058920 B CN 104058920B CN 201310701140 A CN201310701140 A CN 201310701140A CN 104058920 B CN104058920 B CN 104058920B
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Abstract
The invention discloses a kind of take alkane as the method for extraction agent separation of extractive distillation propylene-propane, propylene content 20(wt) %-80(wt) enter in the middle part of extractive distillation column after the extraction agent heat exchange through being separated with knockout tower of the propylene-propane mixture of %, propylene-propane mixture is in rectifying section and extraction agent adverse current, reflux after overhead condenser condensation, part extraction propylene product enters propylene product storage tank; Extracting rectifying tower reactor material enters in the middle part of extraction agent and propane knockout tower, knockout tower tower reactor is equipped with reboiler, tower top has condenser, tower top material is after condenser condenses, backflow, part extraction bromopropane product enters propane tank, the extraction agent of tower reactor after the heat exchange of extracting rectifying tower reactor reboiler, then with the propylene-propane mixture heat exchange of charging after enter tower from extractive distillation column top.After being separated, purified propylene reaches 99.7(wt) %, the present invention is simultaneously by extraction agent and rectifying tower reactor material and the heat exchange of charging step, and reduce energy consumption, be separated one ton of product energy consumption and only need 1.0-1.2Gcal, prior art needs 1.8-2.0Gcal.
Description
Technical field
The invention belongs to vitochemical separation technology field, relating to a kind of take alkane as the method for extraction agent separation of extractive distillation propylene-propane.
Background technology
Propylene is colourless inflammable gas at normal temperatures and pressures, is heavier than air, and forms explosive mixture with air, and limits of explosion (volume), dissolves in ethanol and ether, be slightly soluble in water.
Propylene is one of petrochemical complex basic raw material, in order to produce multiple important Organic Chemicals, can produce vinyl cyanide, propylene oxide, epoxy chloropropane, Virahol, butanols, octanol etc., also directly can synthesize polypropylene, second propane etc.Third rare raw material doing polypropylene, Virahol, also can do the raw material of the product such as acrylic fibers, acrylonitrile, and propylene is very large in the requirement of China, and it is the important raw and processed materials of three large synthetic materialss.
The source of propylene is mainly through 3 approach: the by product (accounting for 68%) of ethylene plant's steam cracking, catalytic cracking by product (accounting for 29%), remaining 3% is obtained by methods such as conversion of olefines, dehydrogenating propane and preparing olefin by conversion of methanols.Adopt petroleum naphtha to be that the steam cracking gained propylene of raw material is generally 0.50-0.65 with the yield ratio of ethene, and the conventional yield of the propylene of the fluid catalytic cracking of refinery (FCC) device by-product only have 3%-6%.So be difficult at short notice realize by the steam cracking of routine and the problem of catalytic cracking unit solution propylene shortage, dehydrogenating propane will become one of propylene important sources.
Be no matter steam cracking and catalytic cracking or dehydrogenating propane, all there is the sepn process of propylene-propane, the separation method of current propylene-propane is divided into low-pressure distillation, high-pressure rectification and low pressure heat pump distillation 3 kinds of operating method according to working pressure difference usually.High-pressure process, because tower top temperature is higher than 40 DEG C, can produce backflow by cooling water condensation, and tower reactor can with low-pressure steam or hot water heating, and equipment is simple, and shortcoming is that reflux ratio is large, and stage number is many.Adopt low-pressure process, propylene propane relative volatility is high, thus reduce stage number and reflux ratio, but tower top need adopt the cryogen condensation lower than water coolant, now often adopts heat pump, namely the low temperature hydrocarbon vapour steamed using tower top is as refrigeration cycle cryogen, send to tower reactor heat exchange after compressed raising pressure and temperature, release heat and the liquid that congeals into, part discharging, partial reflux, this flow process is complicated.Propylene tower adopts high pressure and cooling water system mostly in recent years.Because high-pressure process exists the shortcoming that relative volatility is low, reflux ratio is large, stage number is many, someone adopts extracting rectifying flow process to improve and optimizate it, its ultimate principle is different based on propane-propylene electronic cloud mobility, extraction agent is also different to their interaction force, thus they are separated, the moisture CH of solvent selection
3cN (acetonitrile), forms azeotrope containing water-acetonitrile and propylene, reaches separation of extractive distillation propylene-propane effect.This flow process is made up of 4 towers, and tower 1 is extractive distillation column, and tower top isolates propane; Tower 2 is stripping towers, and tower reactor is extracted agent and recycles, and overhead gas major part is propylene; Tower 3 is water wash columns, washes the ACN contained in propylene off, and tower top obtains product propylene; Tower 4 is extraction agent recovery towers, and a small amount of ACN in recycle-water, loses to avoid ACN.But CH
3cN toxicity is large, adopts containing water-acetonitrile, and produce sewage and have a strong impact on environment, this requirements of process 4 towers simultaneously, equipment is many, and investment is large.
In order to address these problems, the present invention adopts alkane to make extraction agent, makes alkane extract propane in propylene-propane mixture thus realizes the separation of propylene-propane.
Summary of the invention
The present invention adopts alkane to make extraction agent, two-tower process, achieves propylene-propane high efficiency separation object.
technical scheme:
A kind of take alkane as the method for extraction agent separation of extractive distillation propylene-propane, propylene content 20(wt) %-80(wt) enter in the middle part of extractive distillation column after the extraction agent heat exchange through being separated with knockout tower of the propylene-propane mixture of %, propylene-propane mixture is in rectifying section and extraction agent adverse current, reflux after overhead condenser condensation, part extraction propylene product enters propylene product storage tank; Extracting rectifying tower reactor material enters in the middle part of extraction agent and propane knockout tower, knockout tower tower reactor is equipped with reboiler, tower top has condenser, tower top material is after condenser condenses, backflow, part take bromopropane product to enter propane tank, the extraction agent of tower reactor after the heat exchange of extracting rectifying tower reactor reboiler, then with the propylene-propane mixture heat exchange of charging after enter tower from extractive distillation column jacking.
In described propylene-propane mixture, propylene content is 50(wt) %-80(wt) %.
Described extraction agent is Skellysolve A, iso-pentane.
The theoretical plate number of described extractive distillation column is 40-60 block.
The theoretical plate number of described knockout tower is 10-15 block.
Described propylene-propane mixture and the weight ratio of extraction agent are 0.5:1-1:3.
Described extracting rectifying tower reactor temperature 50-55 DEG C.
Described extracting rectifying column overhead temperatures 40-45 DEG C, pressure is 1.2-1.5MPa.
Described separation bottom temperature 60-65 DEG C.
Described separation tower top temperature 46-50 DEG C, pressure is 1.1-1.3MPa.
Described extractive distillation column reflux ratio is 8-15.
Described knockout tower reflux ratio 2-3.
Described extractive distillation column propylene-propane mixture feed zone stage number is 10-15.
Described knockout tower feed zone stage number is 4-7.
Described separation tower reactor reboiler low-pressure steam makes thermal source.
Described extractive distillation column and knockout tower item condenser water coolant make refrigerant.
invention has feature and effect
The present invention uses alkane to make extraction agent, and particularly use Skellysolve A to make extraction agent, the propane in extractive distillation column in counter-current extraction propylene-propane mixture, reaches propylene and be separated object with propane, and after being separated, purified propylene reaches 99.7(wt) %.The present invention is simultaneously by extraction agent and rectifying tower reactor material and the heat exchange of charging step, and reduce energy consumption, be separated one ton of product energy consumption and only need 1.0-1.2Gcal, prior art needs 1.8-2.0Gcal.
Embodiment
Below in conjunction with specific embodiment, invention is described further, but invention is not limited.
example 1
Weight concentration be 20% propylene-propane mixture enter with 1250kg/h flow the 12nd piece of column plate place that theoretical plate number is the extractive distillation column of 50, from separation tower reactor out Skellysolve A after rectifying tower reboiler and the heat exchange of rectifying tower bottoms, enter tower from extractive distillation column the 48th block of column plate after feed exchanger and the heat exchange of propylene-propane mixture again, carry out counter-current extraction with propylene-propane mixture, the flow of extraction agent Skellysolve A is 2500kg/h.Control tower item temperature 40-45 DEG C, pressure 1.2-1.5MPa, the propylene of tower top enters overhead condenser condensation and enters backflash and reflux through reflux pump, controls reflux ratio (weight ratio) 9-10, bottom temperature 50-55 DEG C.
It is 12 knockout towers the 5th block of column plates that extracting rectifying tower reactor liquid relies on pressure itself to enter theoretical plate number, carry out the separation of propane-Skellysolve A, tower top temperature 46-50 DEG C, pressure is 1.1-1.3MPa, the propane of tower top enters the backflow of knockout tower backflash after overhead condenser condensation, and reflux ratio (weight ratio) is 2-3; The reboiler low-pressure steam of tower reactor heats, control temperature 60-65 DEG C.After being separated, extraction agent enters extractive distillation column top after step heat exchange.
Result of implementation, through gas chromatographic analysis, separation of propylene purity is 99.75(wt) %, meet polymerization-grade propylene requirement; Purified propylene oxide reaches 98(wt) more than %, containing propylene lower than 1(wt) %.
example 2
Weight concentration be 40% propylene-propane mixture enter with 1250kg/h flow the 10th piece of column plate place that theoretical plate number is the extractive distillation column of 60, from separation tower reactor out Skellysolve A after rectifying tower reboiler and the heat exchange of rectifying tower bottoms, enter tower from extractive distillation column the 58th block of column plate after feed exchanger and the heat exchange of propylene-propane mixture again, carry out counter-current extraction with propylene-propane mixture, the flow of extraction agent Skellysolve A is 3000kg/h.Control tower item temperature 40-45 DEG C, pressure 1.2-1.5MPa, the propylene of tower top enters overhead condenser condensation and enters backflash and reflux through reflux pump, controls reflux ratio (weight ratio) 9-10, bottom temperature 50-55 DEG C.
It is 12 knockout towers the 5th piece of column plate places that extracting rectifying tower reactor liquid relies on pressure itself to enter theoretical plate number, carry out the separation of propane-Skellysolve A, tower top temperature 46-50 DEG C, pressure is 1.1-1.3MPa, the propane of tower top enters the backflow of knockout tower backflash after overhead condenser condensation, and reflux ratio (weight ratio) is 2-3; The reboiler low-pressure steam of tower reactor heats, control temperature 60-65 DEG C.After being separated, extraction agent enters extractive distillation column top after step heat exchange.
Result of implementation, through gas chromatographic analysis, separation of propylene purity is 99.85(wt) %, meet polymerization-grade propylene requirement; Purified propylene oxide reaches 98(wt) more than %, containing propylene lower than 1(wt) %.
example 3
Weight concentration be 50% propylene-propane mixture enter with 1250kg/h flow the 12nd piece of column plate place that theoretical plate number is the extractive distillation column of 40, from separation tower reactor out Skellysolve A after rectifying tower reboiler and the heat exchange of rectifying tower bottoms, enter tower from extractive distillation column the 39th block of column plate after feed exchanger and the heat exchange of propylene-propane mixture again, carry out counter-current extraction with propylene-propane mixture, the flow of extraction agent iso-pentane is 1700kg/h.Control tower item temperature 40-45 DEG C, pressure 1.2-1.5MPa, the propylene of tower top enters overhead condenser condensation and enters backflash and reflux through reflux pump, controls reflux ratio (weight ratio) 9-10, bottom temperature 50-55 DEG C.
It is 10 knockout towers the 5th block of column plates that extracting rectifying tower reactor liquid relies on pressure itself to enter theoretical plate number, carry out the separation of propane-iso-pentane, tower top temperature 46-50 DEG C, pressure is 1.1-1.3MPa, the propane of tower top enters the backflow of knockout tower backflash after overhead condenser condensation, and reflux ratio (weight ratio) is 2-3; The reboiler low-pressure steam of tower reactor heats, control temperature 60-65 DEG C.After being separated, extraction agent enters extractive distillation column top after step heat exchange.
Result of implementation, through gas chromatographic analysis, separation of propylene purity is 99.70(wt) %, meet polymerization-grade propylene requirement; Purified propylene oxide reaches 98(wt) more than %, containing propylene lower than 1(wt) %.
example 4
Weight concentration be 80% propylene-propane mixture enter with 1250kg/h flow the 12nd piece of column plate place that theoretical plate number is the extractive distillation column of 50, from separation tower reactor out Skellysolve A after rectifying tower reboiler and the heat exchange of rectifying tower bottoms, enter tower from extractive distillation column the 48th block of column plate after feed exchanger and the heat exchange of propylene-propane mixture again, carry out counter-current extraction with propylene-propane mixture, the flow of extraction agent Skellysolve A is 1250kg/h.Control tower item temperature 40-45 DEG C, pressure 1.2-1.5MPa, the propylene of tower top enters overhead condenser condensation and enters backflash and reflux through reflux pump, controls reflux ratio (weight ratio) 9-10, bottom temperature 50-55 DEG C.
It is 15 knockout towers the 5th block of column plates that extracting rectifying tower reactor liquid relies on pressure itself to enter theoretical plate number, carry out the separation of propane-Skellysolve A, tower top temperature 46-50 DEG C, pressure is 1.1-1.3MPa, the propane of tower top enters the backflow of knockout tower backflash after overhead condenser condensation, and reflux ratio (weight ratio) is 2-3; The reboiler low-pressure steam of tower reactor heats, control temperature 60-65 DEG C.After being separated, extraction agent enters extractive distillation column top after step heat exchange.
Result of implementation, through gas chromatographic analysis, separation of propylene purity is 99.80(wt) %, meet polymerization-grade propylene requirement; Purified propylene oxide reaches 98(wt) more than %, containing propylene lower than 1(wt) %.
example 5
Weight concentration be 70% propylene-propane mixture enter with 1250kg/h flow the 12nd piece of column plate place that theoretical plate number is the extractive distillation column of 50, from separation tower reactor out Skellysolve A after rectifying tower reboiler and the heat exchange of rectifying tower bottoms, enter tower from extractive distillation column the 48th block of column plate after feed exchanger and the heat exchange of propylene-propane mixture again, carry out counter-current extraction with propylene-propane mixture, the flow of extraction agent Skellysolve A is 675kg/h.Control tower item temperature 40-45 DEG C, pressure 1.2-1.5MPa, the propylene of tower top enters overhead condenser condensation and enters backflash and reflux through reflux pump, controls reflux ratio (weight ratio) 9-10, bottom temperature 50-55 DEG C.
It is 10 knockout towers the 5th block of column plates that extracting rectifying tower reactor liquid relies on pressure itself to enter theoretical plate number, carry out the separation of propane-Skellysolve A, tower top temperature 46-50 DEG C, pressure is 1.1-1.3MPa, the propane of tower top enters the backflow of knockout tower backflash after overhead condenser condensation, and reflux ratio (weight ratio) is 2-3; The reboiler low-pressure steam of tower reactor heats, control temperature 60-65 DEG C.After being separated, extraction agent enters extractive distillation column top after step heat exchange.
Result of implementation, through gas chromatographic analysis, separation of propylene purity is 99.75(wt) %, meet polymerization-grade propylene requirement; Purified propylene oxide reaches 98(wt) more than %, containing propylene lower than 1(wt) %.
Claims (9)
1. one kind take alkane as the method for extraction agent separation of extractive distillation propylene-propane, enter in the middle part of extractive distillation column after the extraction agent heat exchange through being separated with knockout tower of the propylene-propane mixture of propylene weight content 20%-80%, propylene-propane mixture is in rectifying section and extraction agent adverse current, reflux after overhead condenser condensation, part extraction propylene product enters propylene product storage tank; Extracting rectifying tower reactor material enters in the middle part of extraction agent and propane knockout tower, knockout tower tower reactor is equipped with reboiler, tower top has condenser, tower top material is after condenser condenses, backflow, part take bromopropane product to enter propane tank, the extraction agent of tower reactor after the heat exchange of extracting rectifying tower reactor reboiler, then with the propylene-propane mixture heat exchange of charging after enter tower from extractive distillation column jacking; Described extraction agent is Skellysolve A, iso-pentane.
2. according to claim 1 take alkane as the method for extraction agent separation of extractive distillation propylene-propane, it is characterized in that in described propylene-propane mixture, propylene weight content is 50%-80%.
3. according to claim 1 take alkane as the method for extraction agent separation of extractive distillation propylene-propane, and it is characterized in that the theoretical plate number of described extractive distillation column is 40-60 block, the theoretical plate number of described knockout tower is 10-15 block.
4. according to claim 1 take alkane as the method for extraction agent separation of extractive distillation propylene-propane, it is characterized in that the weight ratio of described propylene-propane mixture and extraction agent is 0.5:1-1:3.
5. according to claim 1 take alkane as the method for extraction agent separation of extractive distillation propylene-propane, and it is characterized in that described extracting rectifying tower reactor temperature 50-55 DEG C, tower top temperature 40-45 DEG C, pressure is 1.2-1.5MPa.
6. according to claim 1 take alkane as the method for extraction agent separation of extractive distillation propylene-propane, and it is characterized in that described separation bottom temperature 60-65 DEG C, tower top temperature 46-50 DEG C, pressure is 1.1-1.3MPa.
7. according to claim 1 take alkane as the method for extraction agent separation of extractive distillation propylene-propane, it is characterized in that described extractive distillation column reflux ratio is 8-15, knockout tower reflux ratio 2-3.
8. according to claim 1 take alkane as the method for extraction agent separation of extractive distillation propylene-propane, and it is characterized in that described extractive distillation column propylene-propane mixture feed zone stage number is 10-15, knockout tower feed zone stage number is 4-7.
9. according to claim 1 take alkane as the method for extraction agent separation of extractive distillation propylene-propane, and it is characterized in that described separation tower reactor reboiler low-pressure steam makes thermal source, extractive distillation column and knockout tower item condenser water coolant make refrigerant.
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| CN107011110B (en) * | 2017-05-19 | 2023-11-03 | 张家港市华昌新材料科技有限公司 | Method for separating propylene propane |
| CN112479801A (en) * | 2020-12-22 | 2021-03-12 | 福建久策气体股份有限公司 | Electronic-grade propylene rectification and purification method |
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| CN101028987A (en) * | 2006-12-29 | 2007-09-05 | 中国石油化工股份有限公司 | Method and apparatus for extracting, rectifying and separating propane and propylene by separated wall tower |
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| CN101028987A (en) * | 2006-12-29 | 2007-09-05 | 中国石油化工股份有限公司 | Method and apparatus for extracting, rectifying and separating propane and propylene by separated wall tower |
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| Title |
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| 丙烷―丙烯萃取精馏过程的模拟研究;杨德明;《石油与天然气化工》;20061231;第35卷(第1期);第26-28页 * |
| 萃取精馏分离乙烷/乙烯的溶剂;易波等;《化工学报》;20010630;第52卷(第6期);第549-552页 * |
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