CN1566282A - Process for deep dearylation of hydrocarbon oil - Google Patents
Process for deep dearylation of hydrocarbon oil Download PDFInfo
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- CN1566282A CN1566282A CN 03147984 CN03147984A CN1566282A CN 1566282 A CN1566282 A CN 1566282A CN 03147984 CN03147984 CN 03147984 CN 03147984 A CN03147984 A CN 03147984A CN 1566282 A CN1566282 A CN 1566282A
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Abstract
The invention discloses a process for deep dearylation of hydrocarbon oil which comprises, charging raw oil and hydrogen gas into hydrogenation reactor, contacting hydrodealkylation catalyst, isolating the reacted articles to obtain gaseous phase and liquid phase product, wherein the gaseous phase product is compressed for cycling use, the liquid phase product is isolated to obtain destination product of low aromatic hydrocarbons.
Description
Technical field
The invention belongs to a kind of method of hydrogenation treatment of hydrocarbon oil, more particularly, is the method that belongs to a kind of hydrocarbon ils deeply de-aromatizing.
Background technology
Among a lot of hydrocarbon ils such as kerosene, diesel oil, some special solvent wet goods, aromatic hydrocarbons is considered to a kind of undesirable components always.Too high aromaticity content can make smoke point be reduced to unacceptable degree in the aviation kerosene; Some solvent oils are in order to improve use properties and hygienic safety, and regulation must be reduced to aromatic hydrocarbons very low level; In diesel oil distillate, the too high oil density that not only makes of aromaticity content rises, and economic benefit descends, and the cetane value of oil product is reduced, and causes the use properties of diesel oil to reduce greatly.Current, along with the increase of environmental protection pressure, new diesel oil specification is except proposing the higher requirement sulphur content, and the requirement of aromaticity content is also become more and more harsher.
US5258346 has disclosed the aromatic hydrocarbon hydrogenation catalyst of a kind of Ni of reduction as active ingredient, can be applicable to various oil products especially than the hydrogenation aromatics-removing of heavy hydrocarbon stream.This patent thinks that the sulfur poisoning-resistant ability key of Ni/ supported catalyst is to improve pore distribution.Even like this, the anti-sulphur ability of reduction Ni also is very limited, and the sulphur content of test raw material only is 4ppm in the example 8, in industrial application certain difficulty is arranged obviously.
US5609752 discloses a kind of method that improves the distillate cetane value, and this method can be processed catalytic diesel oil, straight-run diesel oil, gas oil (do and can arrive about 390 ℃) or its mixing oil.The catalyst system therefor reactive metal is at least a among VIII family and Mo, the W, and contains precious metals pt, and carrier then is the beta-molecular sieve through hydrothermal treatment consists, makes binding agent with aluminum oxide.This catalyzer is to raw material impurity content requirement harshness, and the raw material sulfur-bearing is lower than 20ppm, the nitrogenous 1ppm of being lower than in the example that provides.This method is a kind of mild hydrocracking process in essence, and catalyzer must bring difficulty to operation through reduction, sulfuration twice program, can not deeply de-aromatizing.
US6210563 discloses a kind of method of hydrotreating that improves diesel cetane-number.This method can be processed light cycle oil, heavy cycle oil, the clarification wet goods of 175～400 ℃ of boiling ranges.It requires the sulphur content of charging to be lower than 600ppm, nitrogen content is lower than 50ppm.Therefore, if processing sulphur, raw material such as light cycle oil that nitrogen content is high, it is necessary carrying out the hydrogenation pre-treatment.This method can be passed through a kind of novel precious metal/large pore molecular sieve catalyzer and realize the selective opening reaction.Though this method can improve the diesel product cetane value, can not deeply de-aromatizing.
EP699,733 disclose a kind of two-stage hydrogenation process of distillate, first section employing is the Hydrobon catalyst of active component with cobalt-molybdenum, nickel-molybdenum or nickel-cobalt, makes the outlet sulphur content not be higher than 0.05w%, and second section is adopted the noble metal type catalyzer to carry out aromatic hydrogenation.Between one, two section, have two high pressure hot separators at least, and the bottom of two separators is all introduced hydrogen or hydrogen-rich gas and is carried out gas and carry.One, two sections high-temperature high-pressure separators that two one-tenth series are set are in order to remove dissolved hydrogen sulfide in one section liquid product more up hill and dale.This technology in depress operation, first section in order to take off feed sulphur content below the 500ppm, adopted higher temperature of reaction, enters the saturated performance of high aromatic hydrocarbons of utilizing noble metal catalyst after second section and operating under the low temperature relatively.
US5789637 disclosed a kind of in order to strengthen noble metal type catalyzer (Pt/ aluminum oxide/halogen) hydrogenation activity in system (as raw material) annotate the method for chlorine.The sulphur content that requires raw material is preferably in below the 800ppm below 2000ppm.Annotate the concentration of chlorine at 5～70ppm to raw material.This technology not only requires to annotate chlorine in raw material, and it takes off the fragrant degree of depth and not really high, and its arene engaging scraping rate does not reach the purpose that the degree of depth is taken off virtue below 60%.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of method of hydrocarbon ils deeply de-aromatizing.
Method provided by the invention comprises: stock oil and hydrogen enter hydrogenator, contact with catalytic hydro-dearomatization catalyst, reacted logistics obtains gas-phase product and liquid product through the high-pressure separator separation, wherein gas-phase product recycles, liquid product then obtains the purpose product of low aromatic hydrocarbons after light pressure separator and stabilizer tower are further isolated the gaseous state lighter hydrocarbons, described catalytic hydro-dearomatization catalyst is an active metal component with VIII family precious metal, to be selected from zeolite, heat-resistant inorganic oxide, gac, carbon fiber, the mixture of one or more in the clay is a carrier.
This method processing condition relax, and reaction pressure is a mesolow, and temperature of reaction is low, the air speed height, and the purpose product aromaticity content that obtains is low, noble metal catalyst aromatic hydrogenation activity height, anti-sulphur, nitrogen poisoning performance are good.
Description of drawings
Accompanying drawing is the method synoptic diagram of a kind of hydrocarbon ils deeply de-aromatizing provided by the invention.
Embodiment
Method provided by the invention is so concrete enforcement:
Stock oil and hydrogen are mixed into hydrogenator, contact with catalytic hydro-dearomatization catalyst.Because the catalytic hydro-dearomatization catalyst that is adopted has excellent aromatic hydrogenation saturated activity, and reaction can be carried out, avoided the restriction of chemical equilibrium to the aromatic hydrogenation reaction under lower temperature.Reacted logistics enters cold high pressure separator, be divided into gas phase and liquid product in the cold high pressure separator reactant flow, the compressed machine recycle of gas-phase product, liquid product then enter the cold low separator for further separation and go out dissolved lighter hydrocarbons and hydrogen sulfide in the liquid product, ammonia.Liquid product is after stabilizer tower is sloughed C
5Obtain high-quality low aromatics diesel, kerosene or other high-quality purpose product behind the following gas.
Described stock oil can be that boiling point is 125～625 ℃ various hydrocarbon ils, be selected from one or more the mixture in the oil product that various diesel oil distillates, kerosene(oil)fraction, solvent oil and other need take off aromatic hydrocarbons, wherein diesel oil distillate is one or more the mixture that is selected from straight-run diesel oil, catalytic cracking diesel oil, coker gas oil or thermally splitting diesel oil.The sulphur content of stock oil should not be preferably in below the 500ppm greater than 1000ppm, and optimal situation is below 100ppm.The raw material nitrogen content is not more than 200ppm, and is the most desirable below 50ppm.
The processing condition of this method are: hydrogen dividing potential drop 2.0～6.4 MPas, volume space velocity 1.0～4.0 hours
-1, 220～350 ℃ of temperature of reaction, hydrogen to oil volume ratio 200～650Nm
3/ m
340～60 ℃ of the service temperatures of cold high pressure separator.
The mixture of one or more of its active metal component of described catalytic hydro-dearomatization catalyst VIII family precious metal.Carrier is selected from one or more the mixture in zeolite, heat-resistant inorganic oxide, gac, carbon fiber, the clay.
Preferred catalytic hydro-dearomatization catalyst consists of: the precious metal of 0.1～10 heavy % and the mesoporous Si-Al carrier of surplus.
This Preparation of catalysts method is as follows:
Earlier with the moulding of mesoporous Si-Al carrier, the carrier after the moulding is 80 ℃～140 ℃ dryings 2～10 hours, then 400～650 ℃ of following roastings 2～10 hours.The platinum that uses, palladium solution are muriate, oxymuriate or the ammonium salt of platinum, palladium.Used saturated pickling process dipping 1～8 hour, and descended dry 2～10 hours at 80 ℃～140 ℃ then, 400～650 ℃ of following roastings 2～10 hours.The content of noble metal platinum, palladium is 0.1～10 heavy %, and the weight ratio of platinum, palladium is 0.1～10: 1.
When stock oil character was abominable, said process was suitable for combining application with other hydrogenation preprocessing process.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed.
Accompanying drawing is the method synoptic diagram of a kind of hydrocarbon ils deeply de-aromatizing provided by the invention.
From the hydrocarbon oil crude material of pipeline 1 after preheating, mix with new hydrogen after pipeline 3 is mixed with hydrogen-rich gas from pipeline 25 again and enter interchanger 5 through pipeline 4 from pipeline 2, after reactant flow heat exchange from pipeline 10, enter process furnace 7 through pipeline 6, logistics after the heating enters the hydrogenation dearomatization hydrocarbon reactor 9 that catalytic hydro-dearomatization catalyst is housed through pipeline 8, with through pipeline 27,28 enter the hydrogen-rich gas contact between reactor region, reactant flow enters interchanger 5 through pipeline 10, after raw material heat exchange from pipeline 4, successively through pipeline 11, water cooler 12, pipeline 13 enters cold high pressure separator 14, enter cold low separator 16 from the isolated liquid phase stream in cold high pressure separator 14 bottoms through pipeline 15, from the isolated fuel gas in cold low separator 16 tops through pipeline 18 caterpillars, enter stabilizer tower 19 from the isolated liquid phase stream in cold low separator 16 bottoms through pipeline 17, separate the fuel gas that obtains, the purpose product is respectively through pipeline 20,21 caterpillars.
Behind pipeline 22, compressor 23, pipeline 24, be divided into two-way successively from the isolated gaseous stream in cold high pressure separator 14 tops, wherein one the tunnel through pipeline 25 with go hydrogenation dearomatization hydrocarbon reactor 9 after raw material from pipeline 3 mixes, another Lu Zejing pipeline 26 enters the intersegmental of reactor 9 through pipeline 27,28 respectively again.
Method advantage provided by the invention is:
1, this method can be handled the various hydrocarbon ils that comprise diesel oil distillate, kerosene(oil)fraction, solvent oil to the wide adaptability of raw material.
2, purpose product yield and arene engaging scraping rate height, yield are more than 99 heavy %, and purpose product aromaticity content can be reduced to below the 0.1 heavy %.
3、。Compare with traditional hydrofining technology, saved fractionation apparatus in the back system, greatly reduce plant investment and operational cost.
4, noble metal catalyst aromatic hydrogenation activity height, anti-sulphur, nitrogen poisoning performance are good.Catalyzer is used for oil product and takes off aromatic hydrocarbons, and processing condition relax, and reaction pressure can be mesolow, and temperature of reaction is low, and the air speed height is that treatment capacity is big.
The following examples will give further instruction to present method, but therefore not limit present method.
Catalyst preparation step used among the embodiment is as follows:
(1), the moulding of carrier.Take by weighing the industrial mesoporous Si-Al powder 1500g (butt) that the Chang Ling catalyst plant is produced, with an amount of commercially available sesbania powder thorough mixing, adding deionized water mixes and to pinch, extrusion, make the trilobal cross bar of 1.6 millimeters of circumscribed circle diameters, 120 ℃ dry 2 hours down, 650 ℃ of following roastings 2 hours, the carrier after the moulding.
(2), the preparation of platinum palladium mixing solutions.Take by weighing commercially available H
2PtCl 23g and PdCl 27g, add an amount of concentrated hydrochloric acid and proper amount of deionized water, be heated to 100 ℃ and keep making it abundant dissolving in 30 minutes, then solution is quantitatively transferred in the volumetric flask of 250mL, be made into the platinum palladium solution that 250mL platinum, palladium concentration are respectively 4.5mg/mL, 16.3mg/mL.
(3), Preparation of catalysts.Take by weighing the platinum palladium solution of carrier and 30mL after the 100g moulding, prepare steeping fluid, impregnated carrier 4 hours, then 120 ℃ dry 2 hours down, 450 ℃ of following roastings 4 hours, obtain catalyzer.This catalyzer platiniferous 0.11 heavy %, palladium 0.47 heavy %, all the other are carrier.
Embodiment 1
Present embodiment is stock oil with the solvent oil, and its character is as shown in table 1.Test according to flow process shown in the drawings.Test-results is as shown in table 2, and as can be seen from Table 2, the aromaticity content of product is lower than 0.5 heavy %.
Embodiment 2
Present embodiment is stock oil with the diesel oil distillate, and its character is as shown in table 3.Test according to flow process shown in the drawings.Test-results is as shown in table 4, and as can be seen from Table 4, the aromaticity content of product is 5.4 heavy %.
Table 1
Project stock oil
Density (20 ℃), g/cm
30.8031
Refractive power, nD
201.4478
Sulphur content, ppm 619
Nitrogen content, ppm 4
Total aromaticity content, heavy % 11.8
Boiling range (ASTM D-86), ℃
Initial boiling point 189
50％ 222
90％ 231
Table 2
Processing condition
Hydrogen dividing potential drop 6.4
Temperature of reaction 285
Hydrogen-oil ratio, Nm
3/ m
3550
Volume space velocity, h
-11.3
Product property
Density (20 ℃), g/cm
30.7930
Refractive power, nD
201.4400
Total aromaticity content, heavy %＜0.5
Boiling range (ASTM D-86), ℃
Initial boiling point 187
50％ 220
Do 230
Table 3
The project diesel raw material
Density (20 ℃), g/cm
30.8624
Total sulfur, ppm 56
Total nitrogen, ppm 5
Aniline point, ℃ 59.2
Refractive power, nD
201.4802
Total aromaticity content, heavy % 35.2
Boiling range (ASTM D-86), ℃
Initial boiling point 188
50％ 275
Do 375
Table 4
Processing condition
The hydrogen dividing potential drop, MPa 4.5
Temperature of reaction, ℃ 300
Hydrogen-oil ratio, Nm
3/ m
3500
Volume space velocity, h
-12.0
Product property
Density (20 ℃), g/cm
30.8421
Refractive index, nD
201.4619
Total sulfur, ppm＜15
Total aromaticity content, heavy % 5.4
Boiling range (ASTM D-86), ℃
Initial boiling point 181
50％ 267
Do 374
Claims (6)
1, a kind of method of hydrocarbon ils deeply de-aromatizing, stock oil and hydrogen enter hydrogenator, contact with catalytic hydro-dearomatization catalyst, reacted logistics obtains gas-phase product and liquid product through separation, wherein gas-phase product recycles, liquid product is then further isolated the purpose product that the gaseous state lighter hydrocarbons obtain low aromatic hydrocarbons, it is characterized in that described catalytic hydro-dearomatization catalyst is an active metal component with VIII family precious metal, is carrier with one or more the mixture that is selected from zeolite, heat-resistant inorganic oxide, gac, carbon fiber, the clay.
2, according to the method for claim 1, it is characterized in that described stock oil is various hydrocarbon ils, be selected from one or more the mixture in various diesel oil distillates, kerosene(oil)fraction, the solvent oil.
3,, it is characterized in that described diesel oil distillate is one or more the mixture that is selected from straight-run diesel oil, catalytic cracking diesel oil, coker gas oil or thermally splitting diesel oil according to the method for claim 2.
4,, it is characterized in that processing condition are: hydrogen dividing potential drop 2.0～6.4 MPas, volume space velocity 1.0～4.0 hours according to the method for claim 1
-1, 220～350 ℃ of temperature of reaction, hydrogen to oil volume ratio 200～650Nm
3/ m
340～60 ℃ of the service temperatures of cold high pressure separator.
5,, it is characterized in that described liquid product further isolates gaseous state lighter hydrocarbons method and be meant and adopt light pressure separator to separate with stabilizer tower and do not comprise the separation column separation method according to the method for claim 1.
6,, it is characterized in that described catalytic hydro-dearomatization catalyst weighs the precious metal of % by 0.1～10 and the mesoporous Si-Al carrier of surplus is formed according to the method for claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03147984 CN1267538C (en) | 2003-06-30 | 2003-06-30 | Process for deep dearylation of hydrocarbon oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03147984 CN1267538C (en) | 2003-06-30 | 2003-06-30 | Process for deep dearylation of hydrocarbon oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1566282A true CN1566282A (en) | 2005-01-19 |
| CN1267538C CN1267538C (en) | 2006-08-02 |
Family
ID=34472122
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 03147984 Expired - Lifetime CN1267538C (en) | 2003-06-30 | 2003-06-30 | Process for deep dearylation of hydrocarbon oil |
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| Country | Link |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101993727A (en) * | 2010-11-26 | 2011-03-30 | 开滦能源化工股份有限公司 | Method for producing solvent oil |
| CN112138706A (en) * | 2020-09-15 | 2020-12-29 | 大连理工大学 | Sulfur-tolerant hydrogenation catalyst for hydrogen transfer system and preparation method thereof |
| US11046899B2 (en) | 2019-10-03 | 2021-06-29 | Saudi Arabian Oil Company | Two stage hydrodearylation systems and processes to convert heavy aromatics into gasoline blending components and chemical grade aromatics |
-
2003
- 2003-06-30 CN CN 03147984 patent/CN1267538C/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101993727A (en) * | 2010-11-26 | 2011-03-30 | 开滦能源化工股份有限公司 | Method for producing solvent oil |
| US11046899B2 (en) | 2019-10-03 | 2021-06-29 | Saudi Arabian Oil Company | Two stage hydrodearylation systems and processes to convert heavy aromatics into gasoline blending components and chemical grade aromatics |
| US11459516B2 (en) | 2019-10-03 | 2022-10-04 | Saudi Arabian Oil Company | Two stage hydrodearylation systems to convert heavy aromatics into gasoline blending components and chemical grade aromatics |
| CN112138706A (en) * | 2020-09-15 | 2020-12-29 | 大连理工大学 | Sulfur-tolerant hydrogenation catalyst for hydrogen transfer system and preparation method thereof |
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| Publication number | Publication date |
|---|---|
| CN1267538C (en) | 2006-08-02 |
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Granted publication date: 20060802 |