CN106318459A - Optimized utilization method for light naphtha - Google Patents
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Abstract
The invention discloses an optimized utilization method for light naphtha. According to the method, firstly, the light naphtha passes through an adsorptive separation unit, adsorbed remaining oil rich in iso-alkanes and desorbed oil rich in n-alkanes can be obtained separately, and the desorbed oil can directly serve as an ethylene cracking stock; and the adsorbed remaining oil then passes through a rectifying unit, and a gasoline mixture rich in iso-C6 and high-purity isopentane can be obtained separately. According to the optimized utilization method for the light naphtha, an adsorptive separation-rectifying separation coupled process is adopted, the adsorptive separation unit uses a high-performance adsorbent, and the adsorbent can be used for achieving the distinct partition of the n-alkanes and the iso-alkanes according to molecular dimension difference, so that the selectivity is high, and the regeneration effect is good; and compared with the traditional multi-tower precise rectification, the method has the advantages that the energy consumption is low, and both the product purity and the product yield are relatively high.
Description
Technical field
A kind of method that the present invention relates to light naphthar Optimum utilization.
Background technology
Light naphthar refers to the light component that boiling range is 30-60 DEG C produced in Crude Oil Processing, essentially from refining
The courses of processing such as the oil Atmospheric vacuum of device, being hydrocracked of coking and aromatic device, reformation.In light naphthar
Isoparaffin content is 55%-65% (wt), and during directly as ethylene cracking material, yield of ethene is low, cracking performance
Can be poor；Simultaneously because C5 fraction content is higher, during as gasoline blending stock, can limit because vapour pressure is high
It is as the ratio of gasoline blending stock.The at present utilization of light naphthar also with above-mentioned directly as ethylene cracking material and
Gasoline blending stock is main, it addition, also have document propose use multitower rectifying process produce high-purity solvent oil and
The products such as gasoline blend component, to improve the utilization rate of light naphthar resource, but due in light naphthar just, different
Structure component relative volatility is less, and when using rectification process, rectifying column mostly is precise rectification tower, and the number of plates is most
Up to a hundred pieces, raw material separates through rectification repeatedly, and overall energy consumption is higher.
Patent CN200410048351.6, CN200510027614.X, 201210050806.2 report employing
Absorption or the method for absorption-rectification process Optimum utilization Petroleum, Petroleum is divided into the desorption rich in normal hydrocarbon
Oil product and the residual oil absorber rich in non-normal hydrocarbons.Desorption oil is as the steam crack material of high-quality or by essence
Evaporate and cut into close-cut fraction and then produce reagent and high-quality solvent naphtha product.Inhale excess oil former as the catalytic reforming of high-quality
Material or clean gasoline with high octane blend component.
Patent CN201110425362.1 uses extraction, utilizes double solvents to be divided into Petroleum rich in alkane
Raffinate oil and rich in cycloalkane and the tapped oil of aromatic hydrocarbons, then with rectificating method, by tapped oil and extraction used
Agent separates；Raffinating oil after isolation of purified enters ethylene cracker cracking, tapped oil as cracking stock
Catalytic reforming unit is entered as reformer feed.
Zhang Deshun etc. report employing and are hydrocracked light naphthar production isopentane production technology, by accurate essence
Evaporating-adsorb process integration and produce isopentane, obtain isopentane content and be higher than 92%, olefin(e) centent is less than 50ppm.
The compositing characteristic with reforming raffinate oil is tested by Chemical Engineering associating National Key Laboratory of East China University of Science, with
N-alkanes in reforming raffinate oil is carried out adsorbing separation and divides ADSORPTION IN A FIXED BED by 5A molecular sieve shape-selective absorption feature
Separating process process is studied, and has investigated operation temperature and the midbarrel cutting ratio shadow to normal hexane purity
Ring.Test result indicate that, at adsorption desorption temperature 280 DEG C, oil Feed space velocities 94h-1, desorbing agent air speed 8lh-1
Under conditions of midbarrel cutting ratio 13%, obtain desorption that normal hexane mass fraction is 96.04% oil and
Isohydrocarbon mass fraction is the suction excess oil of 89.21%.It is 99.1% that desorption oil can get purity through batch rectification
Normal hexane, inhales excess oil and meets 6# solvent naphtha prescription.
Zhai Wanjun uses 5A molecular sieve to be that the ADSORPTION IN A FIXED BED isolation technics of adsorbent is by the positive structure in Petroleum
Alkane separation, has inquired into different pressures, temperature, air speed and adsorbent and has used the cycle to adsorbing separation effect
Impact, result show pressure be 0.5MPa, temperature be 300 DEG C, absorption air speed 0.5h-1, it is desorbed air speed 230
h-1(hydrogen is desorbing agent) separation condition preferably.Dynamic adsorbance is 3.0%, it is possible to achieve inhale excess oil
In normal paraffin content ＜ 3%, the total response rate of n-alkane reaches the preferable separating effect of 95%.Report
In the document in road, it is the method for full fraction naphtha Optimum utilization mostly, has no with light naphthar as raw material,
Use absorption-rectification coupling technique to produce high-quality ethylene cracking material, high-octane gasoline blending stock and height simultaneously
The report of purity isopentane.
Summary of the invention
A kind of method that the invention provides light naphthar Optimum utilization, light naphthar is through adsorbing separation, rectification
Separate, the ethylene cracking material rich in n-alkane, low steam can be respectively obtained, press high-octane gasoline to be in harmonious proportion
Material and highly purified isopentane product.This technological process is simple, and energy consumption is low, can greatly improve pumice
The utilization rate of cerebrol resource.
The technical scheme is that a kind of adsorbing separation and rectification separation coupling technique, light naphthar first passes through suction
Attached separative element, enters back into follow-up rectification separative element, can be rich in the ethylene cracking material of n-alkane, richness
Gasoline blending stock containing isomery carbon six alkane and high-purity isopentane product, it specifically comprises the following steps that
Step 1: light naphthar initially enter adsorption separation unit just carrying out, isomery separate, adsorption separation unit
Including procedure below:
(1) absorption: light naphthar heating vaporization enters the ADSORPTION IN A FIXED BED tower equipped with adsorbent to adsorption temp,
N-alkane in Light Naphtha is adsorbed in tower the adsorbent of filling, and isoparaffin not to be adsorbed is from absorption
Tower outlet is flowed out, and is referred to as inhaling excess oil；
(2) displacement in the middle of: the leftover materials of bed dead space are put by the method for purging gas or blood pressure lowering
Swap out, referred to as middle oil；
(3) desorbing: the method that adsorption bed is combined by evacuation or evacuation and gas purging further will
The n-alkane of absorption desorbs from adsorbent, is referred to as being desorbed oil, rich in normal paraffin component in desorption oil,
Can be directly as ethylene cracking material；
Step 2: inhale excess oil and enter follow-up weight-removing column separation of carbon five, carbon six isoparaffin, obtain at the bottom of tower rich in
The component of isomery carbon six alkane, can be directly as gasoline blending stock, and the light component of tower top enters lightness-removing column；
Step 3: the light component from weight-removing column tower top enters lightness-removing column, and lightness-removing column tower top is rich in butane
Liquefied gas, be highly purified isopentane product at the bottom of tower.
The invention provides the method for light naphthar Optimum utilization in, can be given birth to by absorption-rectification step simultaneously
Produce high-quality ethylene cracking material, high-octane gasoline blending stock and high-purity isopentane, be compared with prior art one
Plant separating technology the finest, efficient.It addition, the core cell adsorption separation process of this technology and existing report
Road is the most otherwise varied, only can be only achieved high-purity isopentane by the selection of this absorption-rectification separating technology
The requirement of product.
In above-mentioned process, light naphthar is from oil field light hydrocarbon, the tops of oil refining apparatus, Atmospheric vacuum, coking
Device light naphthar, aromatic hydrogenation cracking, reformer light naphthar, refinery gas separating device pentane and ethylene dress
Put pentane fractions or the mixture of above-mentioned logistics of cracking by-product.
The above-mentioned adsorption separation unit mentioned is that multitower is heated pressure-variable adsorption flow process, and adsorption tower is ADSORPTION IN A FIXED BED tower,
Its adsorbent loaded is modenite, phosphate molecule sieve and A type molecular sieve, preferably phosphoric acid molecules of salt
Sieve.
The process conditions of above-mentioned multitower adsorption separation unit are: absorption, middle displacement and desorption temperature are
80-350 DEG C, adsorptive pressure 0.15-9.5MPa (absolute pressure), middle displacement pressure is 0.1-2MPa (absolute pressure),
Desorption pressures is 0.1 × 10-3-0.08MPa (absolute pressure), the sorption cycle cycle is 5-120min.
Above-mentioned suction multitower adsorption separation unit is isothermal pressure-changing operation, absorption, middle displacement and desorption process operation
Temperature is identical, but operation pressure is different.Absorption, middle displacement and desorption process operation temperature are identical, for
80-350℃。
The method desorption process temperature of the present invention a kind of light naphthar Optimum utilization is identical with adsorption temp, for
80-350 DEG C, the desorption method used is: (1) evacuation desorbing；(2) evacuation boils with under normal pressure simultaneously
Point incoagulable gas (the N less than 25 DEG C2、H2、Ar、He、CH4、CO2) or with low carbon atom N-alkanes
Hydrocarbon (n-propane or normal butane) purging desorbing；(3) evacuation steams with ammonia, steam or ammonia and water simultaneously
Vapour displacement desorption.
The above-mentioned weight-removing column mentioned, the number of plates is 40-150 block, and feed tray is 20-75, and reflux ratio is 2-15；
The above-mentioned dehydrogenation tower mentioned, the number of plates is 10-100 block, and feed tray is 5-50, and reflux ratio is 2-10；
The method of above-mentioned a kind of light naphthar Optimum utilization is the technique of a kind of adsorbing separation and rectification separation coupling,
Adsorption separation unit flow process is that multitower is heated pressure-variable adsorption flow process (or referred to as pressure-variable adsorption full-boiled process flow process).Multitower
Pressure-variable adsorption flow process (or referred to as pressure-variable adsorption full-boiled process flow process) preferably two towers to ten towers are heated pressure-variable adsorption flow process.
Beneficial effect:
Light naphthar is first passed through adsorption separation unit by the present invention, can respectively obtain the suction excess oil rich in isoparaffin
And the desorption oil rich in n-alkane, desorption oil can be directly as ethylene cracking material；Inhale excess oil again through rectification list
Unit, can respectively obtain the gasoline blending stock rich in isomery carbon six and highly purified isopentane.Present invention employs
Adsorbing separation-rectification separation coupling technique, adsorption separation unit uses high-performance adsorbent, and adsorbent can basis
The difference of molecular dimension realizes positive structure, isoparaffin is clearly split, and selectivity is high, favorable regeneration effect, with tradition
Multitower precise distillation compare, energy consumption is low, product purity and yield the highest.With the adsorbing separation work reported
Skill is compared, and the desorption mode that evacuation desorbing of the present invention or evacuation and purging combine can be effective
Reduce the dividing potential drop of adsorbed component, increase the desorbing motive force of adsorbed component, and then improve following of adsorption bed
Ring adsorbance and the purity of product and yield.
It is 0-0.5% that the present invention obtains inhaling normal paraffin content in excess oil by adsorbing separation-rectification separation coupling technique
(wt), in desorption oil, normal paraffin content is 95%～100% (wt), and during as ethylene cracking material, ethylene is received
Rate ＞ 40%；In weight-removing column materials at bottom of tower, normal paraffin content is 0%-1% (wt), during as gasoline blending stock,
Octane number (RON) ＞ 80；In lightness-removing column materials at bottom of tower, isopentane content 98.5%～99.9% (wt), the most different
Pentane >=99% (wt).
Accompanying drawing explanation
Fig. 1 is absorption-rectification coupling technique Optimum utilization light naphthar schematic flow sheet, and adsorption separation unit is adopted
Heating pressure-variable adsorption flow process with two towers, desorption mode uses vacuum desorption or purging desorbing, wherein T1, T2,
Being two ADSORPTION IN A FIXED BED towers equipped with adsorbent, D1 is weight-removing column, and D2 is lightness-removing column, and H1 is adsorption tower
Feeding vaporizer, P1 is vacuum pump；1 is raw material, and 2 for inhaling excess oil, and 3 is middle oil, and 4 is desorption oil, 5
For purge gas, 6 is weight-removing column tower reactor isomery carbon six component, and 7 is lightness-removing column liquid of top of the tower activating QI component, and 8 is de-
Light tower tower reactor isopentane component.
Detailed description of the invention
The technical process of 1 couple of present invention illustrates below in conjunction with the accompanying drawings.Raw material light naphthar 1 initially enters vapour
Change device H1, at 80-350 DEG C, vaporize under 0.15-9.5MPa (absolute pressure), after vaporization, enter adsorption tower T1,
At 80-350 DEG C, under the conditions of 0.15-9.5MPa (absolute pressure), the n-alkane in light naphthar is adsorbed in tower
Adsorbent, isoparaffin not to be adsorbed from adsorption column outlet flow out, be referred to as inhale excess oil 2, inhale excess oil
It is directly entered follow-up rectification cell；After T1 tower adsorption process completes, by purge gas 5 or the side of blood pressure lowering
Formula, cements out the material in bed dead space, referred to as middle oil 3；Then adsorption tower continues through purging
Gas 5 or the mode of vacuum pump P1 evacuation decompression, desorb absorption n-alkane in adsorbent duct
Coming, be referred to as desorption oil 4, so far T1 tower completes whole absorption-centre displacement-desorption process, T2 and T1
Tower blocked operation, distributes according to pressure swing adsorption cycles process and time, is in the various process of pressure-cycling respectively；
Above-mentioned suction excess oil 2 enters weight-removing column D1, and weight-removing column kettle material is the component 6 rich in carbon six isoparaffin,
Overhead stream enters lightness-removing column D2, and lightness-removing column tower top obtains liquefied gas component 7, and tower reactor obtains isopentane component 8.
Embodiment 1
Normal paraffin content be 25% light naphthar enter carburator H1,150 DEG C, vaporize under 0.7MPa,
Enter equipped with in the ADSORPTION IN A FIXED BED tower of modenite after vaporization, 150 DEG C, adsorb 30min under 0.7MPa,
N-alkane in light naphthar is adsorbed by modenite, inhales excess oil and flows out from adsorption column outlet, wherein N-alkanes
Hydrocarbon content is 0.3%；
After adsorption process terminates, at 150 DEG C, nitrogen under the conditions of 0.2MPa, is used to carry out middle displacement, by bed
Material in layer dead space purges out, and the time is 5min；
After middle replacement process terminates, the mode using evacuation and nitrogen purging to combine carries out desorbing,
150 DEG C, under the conditions of 0.05MPa, being desorbed by the n-alkane being adsorbed in modenite, the time is 25min,
In desorption oil, normal paraffin content is 99.5%, is 41.8% as yield of ethene during ethylene cracking material.
The suction excess oil of above-mentioned adsorption separation unit enters de-weight D1, and the number of plates is 60, and feedboard is the 30th piece,
Reflux ratio is 20 (quality), and in kettle material, normal paraffin content is 0.45%, and octane number (RON) is 81.2,
Tower top material enters lightness-removing column D2, and the number of plates 10, feedboard is the 5th piece, and reflux ratio is 5 (quality), tower
Top obtains liquefied gas fraction, and kettle material isopentane purity is 99.8%.
Embodiment 2
Normal paraffin content be 25% light naphthar enter carburator H1,80 DEG C, vaporize under 0.15MPa,
Enter equipped with in the ADSORPTION IN A FIXED BED tower of modenite after vaporization, 80 DEG C, adsorb 30min under 0.15MPa,
N-alkane in light naphthar is adsorbed by modenite, inhales excess oil and flows out from adsorption column outlet, wherein N-alkanes
Hydrocarbon content is 0.25%；
After adsorption process terminates, at 80 DEG C, the pressure in bed is down to 0.1MPa, by reducing bed pressure
Power discharges the material in dead space, and the time is 5min；
After middle replacement process terminates, bed is evacuated to 0.1 × 10-3MPa, at 80 DEG C, 0.1 × 10-3MPa
Under the conditions of carry out vacuum desorption, the n-alkane being adsorbed in modenite is desorbed, the time is 25min,
In desorption oil, normal paraffin content is 99.3%, is 41.7% as yield of ethene during ethylene cracking material.
The suction excess oil of above-mentioned adsorption separation unit enters de-weight D1, and the number of plates is 40, and feedboard is the 40th piece,
Reflux ratio is 2 (quality), and in kettle material, normal paraffin content is 0.5%, and octane number (RON) is 81.0,
Tower top material enters lightness-removing column D2, the number of plates 30, and feedboard is the 10th piece, and reflux ratio is 2 (quality),
Tower top obtains liquefied gas fraction, and tower reactor five material pentane purity is 99.5%.
Embodiment 3
Normal paraffin content be 35% light naphthar enter carburator H1,350 DEG C, vaporize under 9.5MPa,
Enter equipped with in the ADSORPTION IN A FIXED BED tower of SAPO-17 aluminium phosphate molecular sieve after vaporization, at 350 DEG C, 9.5MPa
Lower absorption 10min, the n-alkane in light naphthar is adsorbed by SAPO-17 aluminium phosphate molecular sieve, inhales excess oil
Flowing out from adsorption column outlet, wherein normal paraffin content is 0.15%；
After adsorption process terminates, 350 DEG C, use under the conditions of 2MPa nitrogen to carry out middle displacement, by bed
Material in dead space purges out, and the time is 2min；
After middle replacement process terminates, use the mode desorbing that evacuation and steam purging combine, at 350 DEG C,
Carry out under the conditions of 0.08MPa purging desorbing, the n-alkane being adsorbed in modenite is desorbed, the time
For 8min, in desorption oil, normal paraffin content is 99.1%, is 41.6% as yield of ethene during ethylene cracking material.
The suction excess oil of above-mentioned adsorption separation unit enters de-weight D1, and the number of plates is 150, and feedboard is the 75th piece,
Reflux ratio is 15 (quality), and in kettle material, normal paraffin content is 0.3%, and octane number (RON) is 81.5,
Tower top material enters lightness-removing column D2, the number of plates 100, and feedboard is the 50th piece, and reflux ratio is 5 (quality),
Tower top obtains liquefied gas fraction, and kettle material isopentane purity is 99.4%.
Claims (10)
1. a method for light naphthar Optimum utilization, specifically comprises the following steps that
Step 1: light naphthar initially enter adsorption separation unit just carrying out, isomery separate, adsorption separation unit
Including procedure below:
(1) absorption: light naphthar heating vaporization enters the ADSORPTION IN A FIXED BED tower equipped with adsorbent to adsorption temp,
N-alkane in Light Naphtha is adsorbed in tower the adsorbent of filling, and isoparaffin not to be adsorbed is from absorption
Tower outlet is flowed out, and is referred to as inhaling excess oil；
(2) displacement in the middle of: the leftover materials of bed dead space are put by the method for purging gas or blood pressure lowering
Swap out, referred to as middle oil；
(3) desorbing: adsorption bed will be inhaled by the method for purging and the combination of evacuation or evacuation further
Attached n-alkane desorbs from adsorbent, is referred to as being desorbed oil；
Step 2: inhale excess oil and enter follow-up weight-removing column separation of carbon five, carbon six isoparaffin, obtain at the bottom of tower rich in
The component of isomery carbon six alkane, the light component of tower top enters lightness-removing column；
Step 3: the light component from weight-removing column tower top enters lightness-removing column, and lightness-removing column tower top is rich in butane
Liquefied gas, be isopentane at the bottom of tower.
Method the most according to claim 1, it is characterised in that: in described method light naphthar from
Oil field light hydrocarbon, the tops of oil refining apparatus, Atmospheric vacuum, coking plant light naphthar, aromatic hydrogenation cracking, weight
Engagement positions light naphthar, refinery gas separating device pentane and the pentane fractions of ethylene unit cracking by-product or above-mentioned logistics
Mixture.
Method the most according to claim 1, it is characterised in that: described adsorption separation unit is multitower
Heating pressure-variable adsorption flow process, adsorption tower is ADSORPTION IN A FIXED BED tower, and its adsorbent loaded is modenite, phosphoric acid
Molecules of salt sieve or A type molecular sieve.
Method the most according to claim 3, it is characterised in that: described adsorbent is phosphate molecule
Sieve.
Method the most according to claim 1, it is characterised in that: described multitower adsorption separation unit
Process conditions are: absorption, middle displacement and desorption temperature are 80-350 DEG C, and absorption absolute pressure is 0.15-9.5MPa,
Middle displacement absolute pressure is 0.1-2MPa, and desorbing absolute pressure is 0.1 × 10-3-0.08MPa, the sorption cycle cycle is
5-120min。
Method the most according to claim 1, it is characterised in that: described multitower adsorption separation unit is
Isothermal pressure-changing operates, and absorption, middle displacement and desorption process operation temperature are identical, for 80-350 DEG C.
Method the most according to claim 1, it is characterised in that: described desorption method is:
(1) evacuation desorbing；
(2) evacuation is less than the incoagulable gas of 25 DEG C simultaneously with boiling point under normal pressure, and incoagulable gas is N2、
H2、Ar、He、CH4、CO2, or with low carbon atom n-alkane, n-alkane is n-propane or positive fourth
Alkane；
(3) evacuation is simultaneously with ammonia, steam or ammonia and water vapour displacement desorption.
Method the most according to claim 1, it is characterised in that: described weight-removing column, the number of plates is 40-150
Block, feed tray is 20-75, and reflux ratio is 2-15.
Method the most according to claim 1, it is characterised in that: described dehydrogenation tower, the number of plates is 10-100
Block, feed tray is 5-50, and reflux ratio is 2-10.
10. the method described in claim 1, it is characterised in that: described adsorption separation unit flow process is two towers
Heat pressure-variable adsorption flow process to ten towers.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107746366A (en) * | 2017-10-11 | 2018-03-02 | 中石化上海工程有限公司 | The method that isopentane is extracted from naphtha |
| CN107964424A (en) * | 2017-12-05 | 2018-04-27 | 东营市俊源石油技术开发有限公司 | A kind of apparatus and method for being hydrogenated with rectifying separation joint-product customization feed naphtha |
| CN111099956A (en) * | 2019-11-20 | 2020-05-05 | 复榆(张家港)新材料科技有限公司 | Method for separating C6 mixed hydrocarbon by two-stage PSA |
| CN111471488A (en) * | 2019-01-23 | 2020-07-31 | 内蒙古伊泰宁能精细化工有限公司 | High-purity environment-friendly isoparaffin solvent oil and application thereof |
| CN113845400A (en) * | 2020-06-28 | 2021-12-28 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene from light gasoline |
| CN115505419A (en) * | 2021-06-23 | 2022-12-23 | 中国石化工程建设有限公司 | Light naphtha positive structuring method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1212993A (en) * | 1997-09-11 | 1999-04-07 | 日挥株式会社 | Petroleum processing method and apparatus |
| WO2002036716A1 (en) * | 2000-10-30 | 2002-05-10 | Uop Llc | Ethylene production by steam cracking of normal paraffins |
| CN1664075A (en) * | 2004-03-02 | 2005-09-07 | 催化蒸馏技术公司 | Process for the hydrodesulfurization of naphtha |
| CN103254932A (en) * | 2013-05-22 | 2013-08-21 | 南京工业大学 | Process for extracting C4-C6 normal paraffins and co-producing isopentane and isomeric hexane from light naphtha |
-
2015
- 2015-07-01 CN CN201510379026.6A patent/CN106318459A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1212993A (en) * | 1997-09-11 | 1999-04-07 | 日挥株式会社 | Petroleum processing method and apparatus |
| WO2002036716A1 (en) * | 2000-10-30 | 2002-05-10 | Uop Llc | Ethylene production by steam cracking of normal paraffins |
| CN1664075A (en) * | 2004-03-02 | 2005-09-07 | 催化蒸馏技术公司 | Process for the hydrodesulfurization of naphtha |
| CN103254932A (en) * | 2013-05-22 | 2013-08-21 | 南京工业大学 | Process for extracting C4-C6 normal paraffins and co-producing isopentane and isomeric hexane from light naphtha |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107746366A (en) * | 2017-10-11 | 2018-03-02 | 中石化上海工程有限公司 | The method that isopentane is extracted from naphtha |
| CN107964424A (en) * | 2017-12-05 | 2018-04-27 | 东营市俊源石油技术开发有限公司 | A kind of apparatus and method for being hydrogenated with rectifying separation joint-product customization feed naphtha |
| CN111471488A (en) * | 2019-01-23 | 2020-07-31 | 内蒙古伊泰宁能精细化工有限公司 | High-purity environment-friendly isoparaffin solvent oil and application thereof |
| CN111099956A (en) * | 2019-11-20 | 2020-05-05 | 复榆(张家港)新材料科技有限公司 | Method for separating C6 mixed hydrocarbon by two-stage PSA |
| CN111099956B (en) * | 2019-11-20 | 2023-05-16 | 复榆(张家港)新材料科技有限公司 | Method for separating C6 mixed hydrocarbon by using two-stage PSA |
| CN113845400A (en) * | 2020-06-28 | 2021-12-28 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene from light gasoline |
| CN115505419A (en) * | 2021-06-23 | 2022-12-23 | 中国石化工程建设有限公司 | Light naphtha positive structuring method |
| CN115505419B (en) * | 2021-06-23 | 2023-11-03 | 中国石化工程建设有限公司 | Light naphtha orthographic structuring method |
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