CN109385305A - A method of low-sulphur oil is produced by sulfur-bearing straight-run naphtha - Google Patents
A method of low-sulphur oil is produced by sulfur-bearing straight-run naphtha Download PDFInfo
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- CN109385305A CN109385305A CN201810857369.2A CN201810857369A CN109385305A CN 109385305 A CN109385305 A CN 109385305A CN 201810857369 A CN201810857369 A CN 201810857369A CN 109385305 A CN109385305 A CN 109385305A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/10—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including alkaline treatment as the refining step in the absence of hydrogen
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A method of low-sulphur oil is produced by sulfur-bearing straight-run naphtha, include the following steps: to contact sulfur-bearing straight-run naphtha with inorganic alkali solution and carries out alkali cleaning, remove the hydrogen sulfide and most of mercaptan in naphtha, naphtha after alkali cleaning is washed, then it is contacted with modifying catalyst, modification reaction is carried out under conditions of 200~500 DEG C, 0.2~3.0MPa, obtains 90 or more research octane number (RON), gasoline of the sulfur content less than 10 μ g/g.
Description
Technical field
The present invention is a kind of method for producing gasoline by sulfur-bearing straight-run naphtha, specifically, being one kind by sulfur-bearing straight run
The method of naphtha production low sulfur clean gasoline.
Background technique
Naphtha generally all contains more sulphur especially from the straight-run naphtha of crude oil atmospheric distillation process, and pungent
Alkane value is lower, is not suitable for directly as gasoline component.Conventional straight-run naphtha sulfur method includes hydrogenation method and alkali wash, is added
The benefit of hydrogen method is the sulfur content in naphtha can be down to lower level, but the disadvantage is that need to build at petroleum naphtha hydrogenation
Device is managed, and needs more hydrogen, investment and operating cost are higher.Alkali wash can be made with lower investment and operating cost
Sulfur content in naphtha reduces, but alkali wash can only remove whole hydrogen sulfide and most of mercaptan sulfur in naphtha, to stone
Thioether and disulfide in cerebrol can not then remove.
Conventional naphtha process is that naphtha first passes through hydrodesulfurization at present, then using reformation and isomerization
Process improves the octane number of naphtha, to produce low-sulfur and the higher gasoline blend component of octane number.Using this combination
Technical process process straight-run naphtha, advantage is that product octane number is higher, and sulfur content is lower, the disadvantage is that investment and processing cost compared with
Height, and the gasoline products arene content produced is higher.
CN201210035100.9 discloses a kind of process of naphtha room temperature desulfurization；Equipment include settling tank and
Desulfurization reactor；Settle 2~3 times that tank volume is desulfurization reactor volume；Desulfurization reactor is fixed bed desulfurization reactor, bottom
Portion is filled with molecular sieve or porcelain ball inert substance, and desulfurizing agent is seated on molecular sieve or porcelain ball inert substance, molecular sieve or porcelain
Ball inert substance filling height is that desulfurizing agent loads between the 1/10~1/3 of height；Naphtha enters settling tank, and to carry out sedimentation de-
Water；The water that settling tank generates is discharged by the drain valve of bottom；Dewatered naphtha enters fixed bed desulfurization reactor and is taken off
Reaction of Salmon-Saxl desulfurization；The water that desulfurization reactor bottom is built up is discharged by the drain valve that desulfurization reactor bottom is arranged.The method can prevent
Water damage caused by intensity of desulfurizer that the water carried secretly in naphtha and reaction generate, desulfurizing agent can continuous application 1 year with
On.
CN201610473218.8 discloses a kind of technique of naphtha production aromatic hydrocarbons.The group technology step includes:
Hydrodesulfurizationunit unit, aromatisation unit, extraction unit and rectification cell.The process conditions of the aromatisation unit include: catalysis
The filling of agent cycle rate 260kg/h, first reactor catalyst and second reactor catalyst are compared for 1:1.The catalyst
For zeolite molecular sieve catalyst.Combination unit used in the group technology successively includes adding hydrogen according to naphtha production aromatics process
Desulfurizer, aromatisation device, extraction device and rectifier unit.The molecular sieve catalyst that the method uses have good sulfur resistive,
Anti- nitrogen ability, raw material is not necessarily to deep processing, and aromatics yield is not limited by feedstock oil arene underwater content, and raw material is not required to pre- point
It evaporates.
CN02805032.0 discloses method that is a kind of while being fractionated and handle full boiling range naphtha stream.Full boiling range naphtha stream is first
It first passes through while thioetherification or selection adds hydrogen, be separated into light boiling range naphtha, mid range naphtha and heavy boiling range naphtha.In
Between the naphtha of boiling range contain or mixtures thereof thiophene, alkadienes, according to its composition, can through the second thioetherification or selection plus hydrogen,
It is then delivered to hydrofining reactor, or entire intermediate stream can be delivered directly to finishing reactor.Bottom product is through simultaneously
Hydrodesulfurization and fractionation processing, in conjunction with overhead and bottom product be admitted to finishing reactor.From finishing reactor
Effluent new full boiling range naphtha stream can be formed in conjunction with light boiling range naphtha, contain substantially less than raw material total
Sulphur.Naphtha component is handled by using this method, it is therefore an objective to which the higher standard for meeting sulphur removal can retain alkene while can be most
Advantageously remove sulphur compound.
CN200710120343.1 is related to a kind of method of catalytic gasoline hydrogenation modifying, is by the full faction cut of gasoline
Light fraction, heavy fraction；Cut point is 60 DEG C~80 DEG C；Light gasoline fractions remove mercaptan therein through alkali cleaning；Heavy gasoline fractions with
Hydrogen carry out catalytic desulfurhydrogenation, denitrogenation, olefin saturation, reaction effluent or reaction effluent removing hydrogen sulfide after with it is pungent
Alkane value restores catalyst contact, carries out isomerization, aromatisation and building-up reactions, separation hydrogenated oil obtains lighter hydrocarbons and gasoline evaporates
Point, the hydrogen-rich gas of gas-liquid separation tank deck is recycled after hydrogen sulfide stripping tank, the lighter hydrocarbons for stablizing tower top return to fractionating tank
Again it is fractionated；Hydrofining reaction condition is 1.5~3.0MPa of hydrogen partial pressure；250~320 DEG C of reaction temperature；Liquid hourly space velocity (LHSV) 3.0~
5.0h- 1, hydrogen/oil is than 200~500Nm3/m3；Product gasoline sulfur content < 100ppm, octane number is constant, and yield of gasoline reaches
98.5 weight %.
Summary of the invention
The object of the present invention is to provide a kind of method by sulfur-bearing straight-run naphtha production low-sulphur oil, the method is high in production
Sulphur therein can be effectively removed while octane rating gasoline, obtain clean gasoline with high octane product.
A kind of method by sulfur-bearing straight-run naphtha production low-sulphur oil provided by the invention, includes the following steps:
(1) sulfur-bearing straight-run naphtha is contacted with inorganic alkali solution and carries out alkali cleaning, remove hydrogen sulfide in naphtha and big
Part mercaptan,
(2) naphtha after (1) step alkali cleaning is washed,
(3) naphtha by (2) step through washing is contacted with modifying catalyst, in 200~500 DEG C, the item of 0.2~3.0MPa
Modification reaction is carried out under part, obtains gasoline of the sulfur content less than 10 μ g/g.
The method of the present invention first passes through whole hydrogen sulfide and most of mercaptan sulfur in alkali cleaning removal straight-run naphtha, then again
It is reacted by the modification of naphtha, is improved the octane number of naphtha, while thioether in naphtha and disulfide etc. contain
Sulphur compound occurs cracking reaction in modification reaction process and is converted to hydrogen sulfide, to further reduced the sulphur of gasoline products
Content.
Specific embodiment
The method of the present invention first passes through the hydrogen sulfide and part mercaptan sulfur in alkali cleaning removal straight-run naphtha, after washing,
So that it is carried out modification reaction, be improved the octane number of naphtha, while the thioether contained in naphtha and disulfide etc. contain
Cracking reaction occurs in upgrading processes and is converted to hydrogen sulfide and removes for sulphur compound, to obtain the extremely low higher octane of sulfur content
It is worth gasoline.The method of the present invention reacts desulfurization with modification to be carried out simultaneously, is simplified sulfur removal technology, is reduced operating cost, obtains
The research octane number (RON)s (RON) of gasoline products be increased to 90 or more, sulfur content is reduced to 10 μ g/g or less.
The method of the present invention (1) step is naphtha alkali cleaning, and alkali cleaning need to prepare inorganic alkali solution, by inorganic alkali solution and naphtha
Contact carries out alkali cleaning, and the hydrogen sulfide in naphtha and most of mercaptan is made to be dissolved in aqueous slkali and remove, the alkali cleaning removing
Most of mercaptan refers to removing C5 -The mercaptan of (carbon number is 5 and less than 5), C5 -The eluting rate of mercaptan preferably reaches 95.0m% or more,
More preferably 98m% or more, C6~C7Mercaptan can subsequent modification reaction in remove.The preferred hydroxide of the inorganic base
Sodium or potassium hydroxide, the concentration of the inorganic alkali solution preferably 5~20 mass %, more preferable 10~20 mass %.Using inorganic
Aqueous slkali carries out preferably 5~60 minutes time, 10~30 minutes more preferable of contact alkali cleaning to naphtha.
(1) sulfur-bearing straight-run naphtha can be injected a caustic treater, the inorganic alkali solution that tank is provided with, in alkali cleaning by step alkali cleaning
Naphtha is mixed with inorganic alkali solution in tank, and hybrid mode preferably stirs, through the contact of a period of time, naphtha after stirring
It is layered with inorganic alkali solution, whole hydrogen sulfide and major part mercaptan are reacted with inorganic base, generate water-soluble reaction product and molten
In aqueous slkali, naphtha is discharged from the top of caustic treater to get to the naphtha of removing hydrogen sulfide and most of mercaptan.
The method of the present invention (2) step is to wash to the naphtha after caustic wash desulfuration, to remove alkali remaining in naphtha
Liquid, after washing the amount of inorganic base contained in naphtha with metal meter contained by inorganic base less than 0.1 μ g/g, if (1) step
Alkali cleaning is carried out to naphtha using sodium hydroxide solution, then after washing, the Na content in naphtha is less than 0.1 μ g/g.It is described
Time preferably 5~100 minutes that naphtha after (1) step alkali cleaning is washed, more preferable 10~60 minutes.
(2) the alkali cleaning naphtha that (1) step obtains can be sent into a water washing tank by step, and naphtha is mixed with water in water washing tank
And after contacting a period of time, naphtha and water stratification, remaining lye is dissolved in water in naphtha, by the naphtha after washing from water
The top discharge of cleaning of evaporator is to get the naphtha for arriving removing however, residual base.
The method of the present invention (3) step be using (2) step through caustic wash desulfuration and washing after naphtha as raw material, change it
Qualitative response, reaction product are dry gas, liquefied gas and gasoline products.Since the thioether sulphur contained in naphtha after caustic wash desulfuration is changing
Hydrogen sulfide is decomposed into qualitative response, and hydrogen sulfide can be discharged with dry gas, so sulfur content is less than 10 μ g/ in obtained reformulated gasoline
g。
(3) modifying catalyst described in step preferably includes the HZSM-5 molecular sieve and 10~90 mass % of 10~90 mass %
Aluminium oxide, the more preferably aluminium oxide of the HZSM-5 molecular sieve including 20~80 mass % and 20~80 mass %.
Above-mentioned modifying catalyst can also further comprise rare earth oxide, it is preferable that the modifying catalyst includes
The rare earth oxide that carrier and the content calculated on the basis of carrier being carried on carrier are 0.1~5 mass %, it is described
Carrier include the HZSM-5 molecular sieve of 10~90 mass % and the aluminium oxide of 10~90 mass %, more preferably include 20~80 matter
Measure the HZSM-5 molecular sieve of % and the aluminium oxide of 20~80 mass %.The content of the rare earth oxide preferably 0.5~2 matter
Measure %.
The rare earth element is selected from least one of La, Ce, Pr, Nd and Sm, and the rare earth element is further selected from
Mischmetal.
The molar ratio preferably 10~100, more preferable 20 of the silica/alumina of HZSM-5 molecular sieve in above-mentioned catalyst
~80.
Above-mentioned catalyst the preparation method comprises the following steps: HZSM-5 molecular sieve is mixed with the precursor of aluminium oxide or aluminium oxide after, add
Enter acid solution and carry out peptization, then formed again, forming method can be extruded moulding or drips ball forming, and solid after molding is done
It is dry, roast up to catalyst.The preferred nitric acid of acid, solid drying temperature preferably 100~150 DEG C, maturing temperature after molding
It is preferred that 400~700 DEG C.
The catalyst containing rare earth oxide the preparation method comprises the following steps: with include 10~90 mass % HZSM-5 point
Son sieve and 10~90 mass % aluminium oxide catalyst, more preferably including 20~80 mass % HZSM-5 molecular sieve and 20~
The catalyst of the aluminium oxide of 80 mass % is carrier, with the solution impregnating carrier of water-solubility rare-earth element compound, then dry,
Roasting.Preferably 100~150 DEG C of the drying temperature, preferably 400~700 DEG C of maturing temperature prepare rare earth used in maceration extract
The nitrate of the preferred rare earth element of element compound.
(3) the modification reaction of naphtha described in step can carry out under conditions of facing hydrogen or non-hydrogen.When naphtha modification is anti-
When should carry out under conditions of non-hydrogen, preferably 250~450 DEG C of reaction temperature, pressure preferably 0.3~1.5MPa, material quality is empty
0.1~2.0h of speed-1, preferably 0.3~1.0h-1。
(3) when the modification of naphtha described in step reaction carries out under hydro condition, preferably 250~450 DEG C of reaction temperature, pressure
It is preferred that 0.3~1.5MPa, 0.1~2.0h of material quality air speed-1, preferably 0.3~1.0h-1, hydrogen/hydrocarbon molar ratio be 0.1~2.0,
It is preferred that 0.3~1.5.
The boiling range of straight-run naphtha of the present invention be 30~185 DEG C, preferably 35~160 DEG C, wherein sulfur content be 100~
1000 μ g/g, preferably 100~500 μ g/g.
The present invention is further illustrated below by example, but the present invention is not limited thereto.
Example 1
Prepare modifying catalyst
Taking HZSM-5 and 34 gram of boehmite powder that 80 grams of silica/alumina molar ratios are 50, (SASOL company is raw
Produce, alumina content be 75 mass %) be uniformly mixed, be added 34.2 grams of concentration be 10 mass % nitric acid solution, extruded moulding,
120 DEG C drying 24 hours, 550 DEG C roast 4 hours, obtain modifying catalyst a, wherein HZSM-5 content be 75 mass %, γ-Al2O3
Content is 25 mass %.
Example 2
Prepare modifying catalyst
Taking 100 grams of catalyst by the preparation of 1 method of example is carrier, the Ce (NO for being 3 mass % with 95 grams of concentration3)3It is water-soluble
Liquid dipping, Gu maceration extract/mass ratio is 0.95, solid is 24 hours dry in 120 DEG C after dipping, and 550 DEG C roast 4 hours, must change
Matter catalyst b, wherein the CeO calculated on the basis of carrier2Content is 1.5 mass %.
Example 3
Following instance modifies naphtha by the method for the present invention.
(1) alkali cleaning
100g straight-run naphtha A is taken, composition and property are shown in Table 1, and it is water-soluble that the NaOH that 200g concentration is 20 mass % is added
In liquid, 30 minutes are stood after mixing, two kinds of liquid layereds separate the naphtha on upper layer, the naphtha after obtaining alkali cleaning,
Sulfur-containing compound composition before alkali cleaning and after alkali cleaning in naphtha is shown in Table 2.
(2) it washes
Naphtha resulting after (1) step alkali cleaning is added in 200g deionized water, is uniformly mixed, stands 30 minutes,
After two kinds of liquid are layered completely, the naphtha on upper layer is separated, wherein Na content is less than 0.1 μ g/g.
(3) it modifies
10g catalyst a is loaded in small fixed reactor, is modified using the naphtha after the washing of (2) step as raw material
Reaction, reaction carried out under conditions of non-hydrogen, control reaction temperature be 360 DEG C, reaction pressure 0.3MPa, feedstock quality
Air speed is 1.0h-1, reaction result is shown in Table 3.
Example 4
Straight-run naphtha A is modified by the method for example 3, the difference is that the concentration of NaOH used in (1) step alkali cleaning
For 15 mass %, the sulfur-containing compound composition before alkali cleaning and after alkali cleaning in naphtha is shown in Table 2, and (3) step is by stone brain after alkali cleaning, washing
Oil, which carries out under conditions of non-hydrogen modification reaction, the results are shown in Table 3.
Example 5
Straight-run naphtha A is modified by the method for example 3, the difference is that the concentration of NaOH used in (1) step alkali cleaning
For 10 mass %, the sulfur-containing compound composition before alkali cleaning and after alkali cleaning in naphtha is shown in Table 2, and (3) step is by stone brain after alkali cleaning, washing
Oil, which carries out under conditions of non-hydrogen modification reaction, the results are shown in Table 3.
Example 6
Straight-run naphtha A is modified by the method for example 3, the difference is that the concentration of NaOH used in (1) step alkali cleaning
For 15 mass %, the sulfur-containing compound composition before alkali cleaning and after alkali cleaning in naphtha is shown in Table 2, and (3) step is by stone brain after alkali cleaning, washing
Oil carries out modification reaction under hydro condition, and control reaction temperature is 360 DEG C, reaction pressure 1.0MPa, feedstock quality
Air speed is 1.0h-1, hydrogen/hydrocarbon molar ratio is 1.0, and reaction result is shown in Table 3.
Example 7
(1) alkali cleaning
100g straight-run naphtha B is taken, composition and property are shown in Table 1, and it is water-soluble that the NaOH that 200g concentration is 15 mass % is added
In liquid, 30 minutes are stood after mixing, two kinds of liquid layereds separate the naphtha on upper layer, the naphtha after obtaining alkali cleaning,
Sulfur-containing compound composition before alkali cleaning and after alkali cleaning in naphtha is shown in Table 2.
(2) it washes
Naphtha resulting after (1) step alkali cleaning is added in 200g deionized water, is uniformly mixed, stands 30 minutes,
After two kinds of liquid are layered completely, the naphtha on upper layer is separated, wherein Na content is less than 0.1 μ g/g.
(3) it modifies
10g catalyst a is loaded in small fixed reactor, is changed using the naphtha after the washing of (2) step as raw material
Qualitative response, reaction carried out under conditions of non-hydrogen, control reaction temperature be 360 DEG C, reaction pressure 0.3MPa, feedstock matter
Amount air speed is 1.0h-1, reaction result is shown in Table 3.
Example 8
Straight-run naphtha B is modified by the method for example 7, the difference is that the concentration of NaOH used in (1) step alkali cleaning
For 20 mass %, the sulfur-containing compound composition before alkali cleaning and after alkali cleaning in naphtha is shown in Table 2, and (3) step is by the stone after alkali cleaning, washing
Cerebrol, which carries out under conditions of non-hydrogen modification reaction, the results are shown in Table 3.
Example 9
Straight-run naphtha B is modified by the method for example 7, the difference is that the concentration of NaOH used in (1) step alkali cleaning
For 20 mass %, the sulfur-containing compound composition before alkali cleaning and after alkali cleaning in naphtha is shown in Table 2, and (3) step is by stone brain after alkali cleaning, washing
Oil carries out modification reaction under conditions of non-hydrogen, and modification reaction catalyst used is catalyst b, and reaction result is shown in Table 3.
Example 10
Straight-run naphtha C is modified by the method for example 7, the difference is that the concentration of NaOH used in (1) step alkali cleaning
For 20 mass %, the sulfur-containing compound composition before alkali cleaning and after alkali cleaning in naphtha is shown in Table 2, and (3) step is by stone brain after alkali cleaning, washing
Oil carries out modification reaction under conditions of non-hydrogen, and modification reaction catalyst used is catalyst b, and reaction result is shown in Table 3.
Comparative example 1
10g catalyst a is loaded in small fixed reactor, by straight-run naphtha raw material A without alkali cleaning and washing,
It is sent directly into reactor, control reaction feed mass space velocity is 1.0h-1, reacted under conditions of non-hydrogen, reaction temperature 360
DEG C, pressure 0.3MPa, reaction result is shown in Table 3.
Comparative example 2
10g catalyst a is loaded in small fixed reactor, by straight-run naphtha raw material B without alkali cleaning and washing,
It is sent directly into reactor, control reaction feed mass space velocity is 1.0h-1, reacted under conditions of non-hydrogen, reaction temperature 360
DEG C, pressure 0.3MPa, reaction result is shown in Table 3.
Comparative example 3
10g catalyst b is loaded in small fixed reactor, by straight-run naphtha raw material C without alkali cleaning and washing,
It is sent directly into reactor, control reaction feed mass space velocity is 1.0h-1, reacted under conditions of non-hydrogen, reaction temperature 360
DEG C, pressure 0.3MPa, reaction result is shown in Table 3.
Table 1
Table 2
Table 3
Claims (14)
1. a kind of method by sulfur-bearing straight-run naphtha production low-sulphur oil, includes the following steps:
(1) sulfur-bearing straight-run naphtha is contacted with inorganic alkali solution and carries out alkali cleaning, remove the hydrogen sulfide and major part in naphtha
Mercaptan,
(2) naphtha after (1) step alkali cleaning is washed,
(3) naphtha by (2) step through washing is contacted with modifying catalyst, under conditions of 200~500 DEG C, 0.2~3.0MPa
Modification reaction is carried out, gasoline of the sulfur content less than 10 μ g/g is obtained.
2. according to the method for claim 1, it is characterised in that (1) inorganic base described in step is sodium hydroxide or hydroxide
Potassium, the concentration of the inorganic alkali solution are 5~20 mass %.
3. according to the method for claim 1, it is characterised in that (1) step with inorganic alkali solution to naphtha carry out alkali cleaning when
Between be 5~60 minutes.
4. according to the method for claim 1, it is characterised in that (2) after step washing inorganic base contained in naphtha amount with
Metal meter contained by inorganic base is less than 0.1 μ g/g.
5. according to the method for claim 4, it is characterised in that (2) after step washing inorganic base contained in naphtha amount with
Na content meter is less than 0.1 μ g/g.
6. according to the method for claim 1, it is characterised in that (2) step washes the naphtha after (1) step alkali cleaning
Time is 5~100 minutes.
7. according to the method for claim 1, it is characterised in that (3) modifying catalyst described in step includes 10~90 mass %
The aluminium oxide of HZSM-5 molecular sieve and 10~90 mass %.
8. according to the method for claim 1, it is characterised in that (3) modifying catalyst described in step includes carrier and is carried on load
The oxide for the rare earth element that the content calculated on the basis of carrier on body is 0.1~5 mass %, the carrier include 10
The aluminium oxide of the HZSM-5 molecular sieve of~90 mass % and 10~90 mass %.
9. according to method described in claim 7 or 8, it is characterised in that the silica/alumina of the HZSM-5 molecular sieve
Molar ratio be 10~100.
10. according to the method for claim 8, it is characterised in that the rare earth element is in La, Ce, Pr, Nd and Sm
At least one.
11. according to the method for claim 10, it is characterised in that the rare earth element is selected from mischmetal.
12. according to the method for claim 1, it is characterised in that (3) step naphtha modification reaction under conditions of non-hydrogen into
Row, reaction temperature are 250~450 DEG C, and pressure is 0.3~1.5MPa, and material quality air speed is 0.1~2.0h-1。
13. according to the method for claim 1, it is characterised in that (3) step naphtha modification reaction under hydro condition carry out,
Reaction temperature is 250~450 DEG C, and pressure is 0.3~1.5MPa, and material quality air speed is 0.1~2.0h-1, hydrogen/hydrocarbon molar ratio is
0.1~2.0.
14. according to the method for claim 1, it is characterised in that the boiling range of the straight-run naphtha is 30~185 DEG C, wherein
Sulfur content is 100~1000 μ g/g.
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| CN109385305B (en) | 2022-08-09 |
| PH12018000210A1 (en) | 2019-02-18 |
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