CN1600833A - Method for eliminating arene from kerosene distillation fraction - Google Patents
Method for eliminating arene from kerosene distillation fraction Download PDFInfo
- Publication number
- CN1600833A CN1600833A CN 03126437 CN03126437A CN1600833A CN 1600833 A CN1600833 A CN 1600833A CN 03126437 CN03126437 CN 03126437 CN 03126437 A CN03126437 A CN 03126437A CN 1600833 A CN1600833 A CN 1600833A
- Authority
- CN
- China
- Prior art keywords
- sorbent material
- kerosene fraction
- quality
- accordance
- agent
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
Abstract
This invention provides a method for removing aromatic hydrocarbons from kerosene fraction. It is characterized by that: the raw material kerosene fraction is contacted with adsorbent at temp. of 25-100 deg.C to adsorbing the aromatic hydrocarbon therewith. The normal paraffin hydrocarbon is used as desorption agent, such as C5-C7 paraffin hydrocarbon, to proceed desorption of above-said adsorbent absorbing aromatic hydrocarbons already. Said adsorbent can be selected from silicon dioxide, NaX or NaY. The kerosene produced by using said process for removing aromatic hydrocarbons can be excellent raw material of steamed cracking.
Description
Technical field
The present invention is the method for fractionation by adsorption turpentole fraction, specifically, is a kind of process for purification that removes the aromatic hydrocarbons in the kerosene fraction by fractionation by adsorption.
Background technology
Steam cracking is the major technique means of producing ethene.At present, 60% of steam crack material comes from the petroleum naphtha fraction, but because the restriction of crude resources and existing refinery throughput, further increases the petroleum naphtha fraction and satisfies the ethylene production demand and be difficult to reach in short duration.Expand the steam crack material resource, the heavy cracking stock that adopts high quality is one of effective measure of alleviating this contradiction.
Contain more paraffinic hydrocarbons in the virgin kerosene, be a kind of effective heavy cracking stock, but wherein contain a certain amount of aromatic hydrocarbons.According to the reaction principle of preparing ethylene by steam cracking, there is certain difference in the split product of different hydrocarbons, and wherein normal paraffin cracking ethylene yield is the highest, and isomerization alkanes cracking propene yield is the highest.Along with the increase of hydro carbons carbon number in the raw material, the difference between them reduces.Have monocyclic naphthenic hydrocarbon cracking ethylene, propene yield is all higher, two rings or the above naphthenic hydrocarbon of two rings are easy to coking influences the operational cycle, the aromatic hydrocarbons cracking has only dehydrogenation reaction, can not generate the alkane product, has a strong impact on the operational cycle.So, have only behind the arene engaging scraping in the kerosene fraction, just can effectively improve the steam cracking operational cycle.
The method that removes aromatic hydrocarbons from fraction oil mainly contains solvent extraction process, is solvent with N-Methyl pyrrolidone (NMP) generally, aromatic hydrocarbons is dissolved in the solvent form by extracting and is rich in the solution of aromatic hydrocarbons, thereby alkane is separated with aromatic hydrocarbons.As USP4333824, USP4342646 and USP4390418 all adopt N-Methyl pyrrolidone be in the solvent extracted lube aromatic hydrocarbons to make lubricant base.USP3654137 and USP3691061 then adopt solvent extraction process to remove aromatic hydrocarbons in the solar oil, and the treated oil that takes off behind the virtue combines with Deep Catalytic Cracking process, can increase gasoline output, improve gasoline octane rating.
Above-mentioned employing N-Methyl pyrrolidone is the method that solvent extraction removes aromatic hydrocarbons in the fraction oil, though but the aromatic hydrocarbons in the effective elimination fraction oil, the operating process energy consumption is bigger.And adopt adsorption separating method also is a kind of effective ways that remove aromatic hydrocarbons in the fraction oil, and as USP3,378,486, USP3,373,103 adopt the 5A molecular sieves to remove aromatic hydrocarbons in kerosene, solvent oil, the raw gasline.
USP5,220,099 use the zeolite adsorbents refining hydrocarbon raw material, remove aromatic hydrocarbon impurities wherein.Aromaticity content is 0.1-10% in the described raw material, and zeolite adsorbents is NaX or MgY, and the desorbing agent of use contains at least 95% toluene.
Summary of the invention
The purpose of this invention is to provide the method for alkane and aromatic hydrocarbons in a kind of fractionation by adsorption kerosene fraction, this method operating process is simple, expense is low, and it is few to separate the alkane component aromaticity content that obtains, and is fine preparing ethylene by steam cracking raw material.
The method that removes aromatic hydrocarbons in the kerosene fraction provided by the invention comprises the kerosene fraction is contacted with sorbent material at 25-100 ℃, fractionation by adsorption aromatic hydrocarbons wherein, and then with C
5-C
7Normal paraffin be desorbing agent, the sorbent material that has adsorbed aromatic component is carried out desorption, described sorbent material is selected from silicon-dioxide, NaX or NaY.
The present invention utilizes the method for fractionation by adsorption that the alkane in the kerosene fraction is separated with aromatic hydrocarbons, thereby removes aromatic component wherein, and the high-quality cracking stock is provided.Present method uses the low-carbon (LC) normal paraffin to be desorbing agent, and desorbing agent toxicity is little than aromatic hydrocarbons, and is cheap and easy to get, and with the initial boiling point of kerosene fraction 20 ℃ difference is arranged, and the aromatic hydrocarbons in the desorption liquid can be separated with desorbing agent by simple distillation, recycles.In addition, the present invention is before desorption manipulation, replace the raw material that is present between absorbent particles with squeezing agent earlier, make desorbing agent be used for the aromatic hydrocarbons of desorption sorbent material substantially fully, reduce the material quantity that contains in the desorption liquid, improve separation efficiency thus, make the present invention can be used for handling the higher kerosene fraction of aromaticity content.Usedly squeeze agent and have stronger polarity, and certain boiling-point difference is arranged, adopt simple distillation to separate with desorbing agent with raw material with desorbing agent and absorption raw material.
Description of drawings
Fig. 1 is the schematic flow sheet of the inventive method.
Embodiment
The present invention adopts adsorption method of separation that the alkane in the kerosene fraction is separated with aromatic hydrocarbons.During operation, the kerosene fraction is by sorbent material, and aromatic component wherein is adsorbed, and alkane component is then adsorbent bed as inhaling the excess oil outflow, thereby reaches the aromatic hydrocarbons that removes the kerosene fraction, the purpose of kerosene raffinate raw material.Described sorbent material reach absorption saturated after, desorbing agent is fed adsorbent bed, stripping aromatic hydrocarbons wherein, sorbent material can be reused.
The sorbent used median size of the present invention is the 0.1-0.8 millimeter, and wherein the diameter particle that accounts for 10-20 quality %, 0.2-0.65 millimeter for the 0.65-0.8 mm granules particle that accounts for 70-80 quality %, 0.1-0.2 millimeter accounts for 5-10 quality %.The active ingredient of sorbent material is silicon-dioxide, NaX or NaY.Preferred sorbent material is a silicon-dioxide, and wherein the hole of 40-50 accounts for 80% of total pore volume at least, and The adsorbed hydroxyl content is 0.5-3.0 mmole/gram SiO
2When selecting for use NaX or NaY to be the adsorbent activity component, also should contain an amount of binding agent in the sorbent material, the preferred aluminum oxide of binding agent, its content should be 5-15 quality %, are beneficial to moulding.Binder content is the least possible under the situation that guarantees working strength in the sorbent material, to increase adsorption efficiency.
The preferred 25-50 of temperature ℃ of fractionation by adsorption of the present invention operation.During lock out operation, absorption raw material kerosene fraction and desorbing agent are 0.5-10.0 hour by the volume space velocity of sorbent material
-1, preferred 0.5-2.0 hour
-1, the volume ratio of kerosene fraction or desorbing agent and sorbent material is 0.5-10.0, preferred 0.5-2.0.
Be to improve the desorption effect, before sorbent material is carried out desorption, in sorbent material, feed earlier and squeeze agent, describedly squeeze that agent is selected from Virahol, isopropylcarbinol, tertiary amyl alcohol or any two kinds mixture in them, or the mixture of described three kinds of materials.Squeezing the volume space velocity of agent by sorbent material is 0.5-10.0 hour
-1, preferred 0.5-2.0 hour
-1, the volume ratio of squeezing agent and sorbent material is 0.5-10.0, preferred 0.5-2.0.
Desorbing agent that the present invention selects for use and aromatic hydrocarbons, squeeze between agent and the raw material and all to have bigger boiling-point difference, thus can adopt simple distillation with desorbing agent with aromatic hydrocarbons, squeeze agent and separate with raw material, separate the desorbing agent that obtains and squeeze that agent is all capable of circulation to be utilized again.
The boiling range that fractionation by adsorption raw material of the present invention is selected from various explained hereafter is 140-270 ℃ a kerosene, the kerosene fraction that preferred virgin kerosene fraction or secondary processing technologies such as catalytic cracking, delayed coking produce.
C in the described kerosene fraction
8-C
14Paraffinicity be 20-50 quality %, C
8-C
16Naphthene content be 20-50 quality %, C
8-C
14Aromaticity content be 10-15 quality %.
The described fractionation by adsorption of the inventive method adopts the placed in-line adsorptive separation technology of multicolumn, and general adsorption column is 3-6, and series connection each other is to reach best adsorption effect and to guarantee that the aromaticity content of inhaling excess oil reaches prescribed value.During adsorption operations, absorption, desorption hockets, to guarantee whole adsorption operations system continuous operation.
Below in conjunction with Fig. 1 adsorptive separation technology flow process of the present invention is described briefly.Among Fig. 1, three adsorption columns are connected in parallel to each other, the kerosene fraction enters system by material feeding tube line 41, enter into adsorption column 1,2,3 through pipeline 12,22,32 respectively, through selective adsorption, the kerosene raffinate fraction that contains a small amount of aromatic hydrocarbons is entered by pipeline 15,25,35 respectively inhales excess oil pipeline 44, and the discharge system is delivered to and inhaled in the surplus liquid knockout tower.After inhaling surplus liquid knockout tower separation, the desorbing agent that cat head is discharged returns desorbing agent pipeline 43, recycle; The kerosene raffinate fraction that obtains at the bottom of the tower is as the raw material of steam cracking.
After treating that adsorbents adsorb is saturated, will squeeze agent and feed pipeline 42, feed in three adsorption columns through pipeline 13,23,33 respectively again, the kerosene fraction in the dead volume between absorbent particles will be cemented out.The liquid that squeezes that contains kerosene feedstock flows into washing fluid pipeline 46 by pipeline 16,26 and 36, delivers to and squeezes in the liquid knockout tower.The overhead product that squeezes the liquid knockout tower is the lighter liquid that squeezes, it is incorporated into squeeze liquid feeding line 42, return adsorption system and recycle, the bottom product that squeezes the liquid knockout tower turns back to kerosene feedstock feeding line 41 and carries out fractionation by adsorption again for not taking off the kerosene fraction of aromatic hydrocarbons.
After treating that the displacement of kerosene fraction finishes in the dead volume in the adsorption column, carry out desorption manipulation.With desorbing agent by desorbing agent feeding line 43 feeding systems, introduce in three adsorption columns by pipeline 11,21 and 31 respectively again, be rich in the kerosene fraction of aromatic hydrocarbons and enter desorption liquid pipeline 45 discharge systems by pipeline 14,24 and 34, deliver in the desorption liquid knockout tower with the mixture that squeezes liquid and desorbing agent on a small quantity.The desorbing agent that desorption liquid knockout tower cat head is discharged after fractionation is incorporated desorbing agent feeding line 43 into, returns adsorption system and recycles, and ejecta squeezes liquid feeding line 42 for squeezing liquid, incorporating in the middle of the desorption liquid knockout tower, returns adsorption system and recycles; Be the kerosene fraction that is rich in aromatic hydrocarbons at the bottom of the tower of desorption liquid knockout tower, can directly go gasoline attemperation apparatus or aromatic hydrocarbons to utilize system.
In the operation of actual fractionation by adsorption, can with adsorb, squeeze, desorption respectively in three adsorption columns by above-mentioned flow process in turn switching carry out, also three posts can be pressed the described series connection of dotted line after, adsorb successively, squeeze, desorption manipulation.
Below by example in detail the present invention, but the present invention is not limited to this.
Example 1
The preparation sorbent material.
Get 150 gram silochroms (Haiyang Chemical Plant, Qingdao's production), activation is 2.5 hours in 150 ℃ of air, make adsorbent A, wherein the hole of 40-50 accounts for 92% of total pore volume, median size is the 0.1-0.8 millimeter, wherein diameter is that the particle that particle that the particle of 0.65-0.8 millimeter accounts for 20 quality %, 0.2-0.65 millimeter accounts for 70 quality %, 0.1-0.2 millimeter accounts for 10 quality %, and The adsorbed hydroxyl content is 2.0 mmoles/gram SiO
2
Example 2
After getting 92 gram NaX zeolites and 8 grams aluminium hydrate powders being mixed, roller forming, the deionized water that sprays into during spin amount to 10 grams.Then ball is sieved into particle diameter and be 0.2～0.8 millimeter bead, 540 ℃ of roastings 4 hours make adsorbent B, wherein contain the NaX zeolite of 92 quality %, and all the other are γ-Al
2O
3
Example 3
Following example carries out kerosene fraction fractionation by adsorption and takes off the aromatic hydrocarbons experiment.
Get the adsorption column that 100 gram adsorbent A place 20 * 1200 millimeters of φ, feed kerosene feedstock and carry out adsorption operations.Operational condition is: 25 ℃, during kerosene feed volume air speed 1.0
-1, feed oil/agent mass ratio 0.8.Wait to adsorb saturated after, in adsorption column, feed and squeeze the agent Virahol, the kerosene fraction in the dead volume in the adsorption column is cemented out from adsorption column, Virahol feed volume air speed is 1.0 o'clock
-1, the volume ratio of Virahol charging and sorbent material is 0.3.Feed the desorbing agent normal hexane to adsorption column then, the feed volume air speed of normal hexane is 2.0 o'clock
-1, the volume ratio of normal hexane charging and sorbent material is 1.5.The character and the composition of used kerosene feedstock and suction excess oil see Table 1, and with respect to raw material, the yield of inhaling excess oil is 91 quality %.
Example 4
Method by example 3 is carried out adsorption operations, and different is that adsorption temp is 50 ℃, and kerosene feedstock feed volume air speed is 0.5 o'clock
-1, charging and sorbent material volume are than 0.65.Wait to adsorb saturated after, do to squeeze agent with Virahol, be desorbing agent with the Skellysolve A then, under 50 ℃, carry out desorption.Character and composition that gained is inhaled excess oil see Table 1, and with respect to charging, the yield of inhaling kerosene fraction in the excess oil is 94 quality %.
Example 5
Method by example 3 is carried out adsorption operations, and the different sorbent materials that is to use is an adsorbent B, and character and composition that gained is inhaled excess oil see Table 1, and with respect to charging, the yield of inhaling kerosene fraction in the excess oil is 92 quality %.
Example 6
Method by example 3 is carried out adsorption operations, and the different agent of squeezing that are to use are isopropylcarbinol, and character and composition that gained is inhaled excess oil see Table 1, and with respect to charging, the yield of inhaling kerosene fraction in the excess oil is 93 quality %.
As shown in Table 1, after fractionation by adsorption, the aromaticity content of inhaling in the excess oil significantly reduces, and paraffinicity increases to some extent.
Example 7
This example takes off fragrant kerosene fraction and does not take off the aromatic hydrocarbons fraction fractionation by adsorption and carries out the cracking contrast experiment.
Carry out the cracking experiment on simulation cracking evaluation experimental device, simulator is made up of feed system, scission reaction system and low temperature separation process system three parts, and complete assembly is by a computer-controlled operation and monitoring operation.The cracking operation condition is: 830 ℃ of heater outlet temperatures, control cracking are carried out under high severity, outlet of still pressure 211KPa, 0.39 second residence time, water oil quality than 0.60, treatment capacity 1-3 kilogram/hour.Respectively with the kerosene fraction that takes off aromatic hydrocarbons in the kerosene fraction that takes off virtue without fractionation by adsorption and the example 3 directly as steam crack material, carry out cracking experiment by above-mentioned condition, the results are shown in Table 2.As shown in Table 2, take off kerosene fraction behind the virtue after cracking, cracking main products yields such as ethene, propylene improve, and the tar yield greater than 240 ℃ in the cracking liquid-phase product is low, and hydrogen richness height in the liquid-phase product can guarantee that pyrolyzer has long running period.
Table 1
| Project | Kerosene feedstock | Inhale excess oil | |||
| Example 3 | Example 4 | Example 5 | Example 6 | ||
| Density, gram per centimeter 3 | ????0.7905 | ????0.7813 | ????0.7805 | ????0.7814 | ????0.7804 |
| Carbon content, quality % hydrogen richness, quality % | ????85.66 ????14.34 | ????85.08 ????14.63 | ????85.01 ????14.72 | ????85.12 ????14.58 | ????85.02 ????14.73 |
| C 8-C 14Paraffinic hydrocarbons, quality % | ????47.7 | ????53.4 | ????54.1 | ????53.2 | ????53.9 |
| Total naphthenic hydrocarbon, quality % | ????40.0 | ????42.8 | ????43.1 | ????42.7 | ????43.0 |
| Total aromatic hydrocarbons, quality % | ????12.3 | ????3.8 | ????2.8 | ????4.1 | ????3.1 |
Table 2
| Stock oil | Kerosene feedstock | Adsorption dearylating kerosene | |
| Cracking severity water oil quality ratio | High severity 0.60 | High severity 0.60 | |
| The gaseous products yield, quality % | Cracking gas yield hydrogen methane ethylene-ethane acrylonitrile-butadiene mixed C4Total triolefin yield, quality % | ????69.91 ????0.74 ????14.02 ????28.44 ????3.44 ????13.66 ????4.67 ????3.55 ????46.77 | ?????74.02 ?????0.73 ?????13.88 ?????30.61 ?????3.64 ?????14.52 ?????4.89 ?????3.71 ?????50.02 |
| The liquid-phase product yield, quality % | Cracked oil yield C 5-180 ℃ of fraction 180-204 ℃ fraction＞204 ℃ of total triphen yields of fraction | ????30.09 ????15.56 ????2.45 ????12.08 ????9.82 | ?????25.98 ?????13.04 ?????2.51 ?????10.43 ?????7.94 |
| Liquid-phase product | The fraction scope, ℃ hydrogen richness, quality % | ????46-413 ????7.64 | ?????46-389 ?????8.12 |
Annotate: total triolefin is ethene, propylene and divinyl, and total triphen is benzene, toluene and dimethylbenzene
Claims (10)
1, a kind of method that removes aromatic hydrocarbons in the kerosene fraction comprises the kerosene fraction is contacted with sorbent material at 25-100 ℃, fractionation by adsorption aromatic hydrocarbons wherein, and then with C
5-C
7Normal paraffin be desorbing agent, the sorbent material that has adsorbed aromatic component is carried out desorption, described sorbent material is selected from silicon-dioxide, NaX or NaY.
2, in accordance with the method for claim 1, the The adsorbed hydroxyl content that it is characterized in that described silicon-dioxide is 0.5-3.0 mmole/gram SiO
2
3, in accordance with the method for claim 1, the hole that it is characterized in that 40-50 in the described silicon-dioxide accounts for 80% of total pore volume at least.
4, in accordance with the method for claim 1, the median size that it is characterized in that described sorbent material is the 0.1-0.8 millimeter, and wherein diameter is that the particle that particle that the particle of 0.65-0.8 millimeter accounts for 10-20 quality %, 0.2-0.65 millimeter accounts for 70-80 quality %, 0.1-0.2 millimeter accounts for 5-10 quality %.
5, in accordance with the method for claim 1, it is characterized in that described adsorption temp is 25-50 ℃.
6, in accordance with the method for claim 1, it is characterized in that described kerosene fraction and desorbing agent are 0.5-10.0 hour by the volume space velocity of sorbent material
-1, the volume ratio of kerosene fraction or desorbing agent and sorbent material is 0.5-2.0.
7, in accordance with the method for claim 1, before it is characterized in that sorbent material carried out desorption, in sorbent material, feed earlier and squeeze agent, describedly squeeze that agent is selected from Virahol, isopropylcarbinol, tertiary amyl alcohol or any two kinds mixture in them, or the mixture of described three kinds of materials.
8, in accordance with the method for claim 7, it is characterized in that squeezing the volume space velocity of agent by sorbent material is 0.5-10.0 hour
-1, the volume ratio of squeezing agent and sorbent material is 0.5-2.0.
9, in accordance with the method for claim 1, it is characterized in that it is 140-270 ℃ the virgin kerosene fraction or the kerosene fraction of secondary processing technology generation that described kerosene fraction is selected from boiling range.
10, in accordance with the method for claim 1, it is characterized in that C in the described kerosene fraction
8-C
14Paraffinicity be 20-50 quality %, C
8-C
16Naphthene content be 20-50 quality %, C
8-C
14Aromaticity content be 10-15 quality %.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03126437 CN1261532C (en) | 2003-09-28 | 2003-09-28 | Method for eliminating arene from kerosene distillation fraction |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03126437 CN1261532C (en) | 2003-09-28 | 2003-09-28 | Method for eliminating arene from kerosene distillation fraction |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1600833A true CN1600833A (en) | 2005-03-30 |
| CN1261532C CN1261532C (en) | 2006-06-28 |
Family
ID=34658801
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 03126437 Expired - Lifetime CN1261532C (en) | 2003-09-28 | 2003-09-28 | Method for eliminating arene from kerosene distillation fraction |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1261532C (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101921608A (en) * | 2009-06-09 | 2010-12-22 | 武汉保华石化新材料开发有限公司 | Method for removing colloid asphalt from catalytic slurry oil by using solid-phase adsorbent |
| CN114917865A (en) * | 2022-06-06 | 2022-08-19 | 中海油天津化工研究设计院有限公司 | Aromatic hydrocarbon adsorbent and application thereof in increasing yield of ethylene cracking raw material |
-
2003
- 2003-09-28 CN CN 03126437 patent/CN1261532C/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101921608A (en) * | 2009-06-09 | 2010-12-22 | 武汉保华石化新材料开发有限公司 | Method for removing colloid asphalt from catalytic slurry oil by using solid-phase adsorbent |
| CN101921608B (en) * | 2009-06-09 | 2013-05-01 | 武汉保华石化新材料开发有限公司 | Method for removing colloid asphalt from catalytic slurry oil by using solid-phase adsorbent |
| CN114917865A (en) * | 2022-06-06 | 2022-08-19 | 中海油天津化工研究设计院有限公司 | Aromatic hydrocarbon adsorbent and application thereof in increasing yield of ethylene cracking raw material |
| CN114917865B (en) * | 2022-06-06 | 2023-08-22 | 中海油天津化工研究设计院有限公司 | Aromatic hydrocarbon adsorbent and application thereof in yield-increasing ethylene cracking raw material |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1261532C (en) | 2006-06-28 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105542835B (en) | A kind of method that moving-bed adsorption separates polycyclic aromatic hydrocarbon | |
| CN1285707C (en) | Naphtha optimized utilization method | |
| KR101895091B1 (en) | Hydrocracking process with feed/bottoms treatment | |
| CN105542849B (en) | A kind of method that diesel oil and light aromatics are cleaned by poor ignition quality fuel production | |
| US8986622B2 (en) | Apparatus for upgrading whole crude oil to remove nitrogen and sulfur compounds | |
| CN1292050C (en) | Method for separating normal alkane from full fraction naphtha | |
| TWI413636B (en) | Ethylene production by steam cracking of normal paraffins | |
| CN105349175B (en) | Sulfide and the method for aromatic hydrocarbons a kind of while in adsorbing and removing diesel oil | |
| CN105368482B (en) | The method of polycyclic aromatic hydrocarbon in a kind of multitower adsorbing and removing diesel oil in parallel | |
| CN105969422A (en) | Method using absorption separation to produce solvent oil | |
| CN102452885B (en) | Adsorption and separation method of C5 and C6 isomerization product | |
| CN1261533C (en) | Process for adsorption desulfurization of gasoline | |
| CN1800309A (en) | Process for desulphurizing a hydrocarbon cut in a simulated moving bed | |
| CN1216968C (en) | Method for separating and refining etherification material from catalytic cracking gasoline | |
| CN113372953A (en) | Method for adsorbing and separating saturated hydrocarbon and unsaturated hydrocarbon by FCC (fluid catalytic cracking) gasoline | |
| CN101423772B (en) | Method for adsorption separation of aromatic hydrocarbon from naphtha | |
| CN105585401A (en) | Method for producing propylene | |
| CN109022020B (en) | Method for multi-component adsorption separation of diesel oil | |
| CN101333145B (en) | Method for adsorbing and separating arene from naphtha | |
| CN101255088B (en) | Hydrocarbon separation | |
| CN1261532C (en) | Method for eliminating arene from kerosene distillation fraction | |
| US11326112B1 (en) | Integrated hydrocracking/adsorption and aromatic recovery complex to utilize the aromatic bottoms stream | |
| CN1634812A (en) | Method for separating n-alkane from C5 to C6 alkane isomerized products | |
| CN100389100C (en) | Process for preparing olefin by cracking of kerosene distillate | |
| CN104017602B (en) | A kind of reformed pre-hydrogenated tops preprocess method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20060628 |