CN103666554A - Hydroprocessing method for producing high quality solvent oil - Google Patents
Hydroprocessing method for producing high quality solvent oil Download PDFInfo
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- CN103666554A CN103666554A CN201210326384.7A CN201210326384A CN103666554A CN 103666554 A CN103666554 A CN 103666554A CN 201210326384 A CN201210326384 A CN 201210326384A CN 103666554 A CN103666554 A CN 103666554A
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Abstract
The invention relates to a hydroprocessing method for producing high quality solvent oil. The method comprises the steps of carrying out reaction by contacting a mixture of a kerosene fraction or light diesel oil fraction raw material and hydrogen in a first reaction area with a non-noble metal hydroprocessing catalyst I; feeding the effluent in the first reaction area into a second reaction area, and contacting with hydrogen in countercurrent; sequentially carrying out aryl removing reaction in the presence of a non-noble metal hydroprocessing catalyst II and a noble metal hydroprocessing refining catalyst, wherein the reaction temperature of the second reaction area is 50-200 DEG C lower than that of the first reaction area. By using the method provided by the invention, high sulfur kerosene or light diesel oil fractions can be processed to produce a high quality solvent product with the sulfur content less than 0.5mu g/g and the aromatic hydrocarbon content less than 100mu g/g.
Description
Technical field
The invention belongs to a kind of in the situation that there is hydrogen under the method for refining hydrocarbon ils, more particularly, be a kind of method of hydrotreating of producing the food grade solvent oil that aromaticity content is extremely low.
Background technology
In the deep-processing process of petroleum refining industry, the kerosene(oil)fraction prospect that is widely used.Kerosene raffinate cut can be produced lam-oil, rocket engine fuel and all kinds of SOLVENTS oil production.The solvent oil product of solvent oil wherein, especially food grade has good price and outlet, is main point of economic increase in kerosene(oil)fraction post-treatment process.While producing solvent oil with kerosene feedstock, can virgin kerosene be carried out to deep refining processing according to the needs in market, the aromaticity content of product is reduced to below certain requirement; Then being cut into narrow fraction product adjusts and the thin rolling wet goods of aluminium product as aerosol solvent, printing ink solvent, makeup.
Traditional kerosene process for purification is clay-filtered method.But the quality product that the method obtains is low, and have that yield is low, equipment corrosion serious and produce " " shortcomings such as many, are progressively eliminated the three wastes.
What use was more at present is by Hydrofining Technology, obtains the qualified solvent oil product of aromaticity content.Main technical process has: dewaxing by molecular sieve+solvent hydrogenation, high pressure single hop deep hydrogenation etc.But, adopt above-mentioned explained hereafter solvent oil to process raw material, and be difficult to realize the food grade solvent oil production that production aromaticity content is 0.
US 5608025 discloses a kind of two-step approach aromatic saturation technique.Raw material successively, through the reactor of two series connection, does not have separation facilities between reactor.Two-stage reaction is non-precious metal catalyst.When aromatics conversion rate is greater than 50%, reaction pressure need be more than 10.0MPa.
US 5183556 discloses two sections of de-aromatics process of a kind of diesel oil concurrent-countercurrent.First paragraph adopts following current operation, adopts non-precious metal catalyst; Two sections adopt counter-current operation, adopt noble metal catalyst also can adopt non-precious metal catalyst.Can produce aromaticity content at the clean diesel product of 5 ~ 10v%.
US 5435907 discloses a kind of middle distillate deeply de-aromatizing method.Use a kind of catalyzer that activated carbon is carrier of take, process the raw material of 160 ~ 250 ℃, at 380 ℃, 10.8MPa and hydrogen to oil volume ratio are greater than under the condition of 700Nm3/m3, aromaticity content 32% can be reduced to below 10%.
EP 0699733 discloses two sections of deeply de-aromatizing operating processes of a kind of diesel oil, and two sections adopt different operational conditions.First paragraph adopts non-precious metal catalyst, at relatively high temperature, operates, and the sulphur content of raw material is reduced to below 500 μ g/g; Second segment adopts noble metal catalyst to operate at relatively low temperature, mainly completes aromatic saturation reaction.Between two-stage reaction, there is air-lift device, to remove hydrogen sulfide and the ammonia of two section feedings.Adopt this patented technology can produce the diesel product that aromaticity content is less than 20%.
Summary of the invention
The object of the invention is to provide on the basis of existing technology a kind of method of hydrotreating of producing the high-quality solvent oil that aromaticity content is extremely low.
Method provided by the invention is:
(1) after kerosene(oil)fraction or solar oil feedstock oil mix with hydrogen, its mixture enters the first reaction zone, and contact and react with non-noble metal hydrogenation processing catalyst I,
(2) effluent of the first reaction zone of step (1) gained enters second reaction zone, react with the hydrogen counter current contact that enters second reaction zone, the flow direction along the effluent of the first reaction zone, in second reaction zone, load successively non-noble metal hydrogenation and process catalyst I I and noble metal hydrogenation catalyst for refining
(3) effluent of second reaction zone, after cooling, separation, obtains hydrogen-rich gas and solvent oil product,
Wherein the temperature of reaction of second reaction zone is lower 50～200 ℃ than the temperature of reaction of the first reaction zone, preferably 80～150 ℃.
In the present invention, the boiling range of described kerosene(oil)fraction is 180～260 ℃, and the boiling range of solar oil cut is 205～350 ℃, can be kerosene(oil)fraction and the solar oil cut of different sources, is preferably virgin kerosene or straight distillation light diesel oil.
In a preferred embodiment of the present invention, described second reaction zone is fixed-bed reactor, in reactor, from up to down load successively non-noble metal hydrogenation and process catalyst I I and noble metal hydrogenation catalyst for refining, the reaction effluent of the first reactor enters fixed-bed reactor from top, hydrogen enters fixed-bed reactor from bottom, the top effluent of fixed-bed reactor is after cooling, separation, the hydrogen-rich gas obtaining recycles, and the liquid fraction of gained goes out device as hydrotreated naphtha product or boat coal blend component; The bottom effluent of fixed-bed reactor, after separation, obtains the solvent oil product that aromaticity content is extremely low.In addition, reverse-flow fixed-bed reactor have the effect of gas stripping column, can remove hydrogen sulfide and ammonia in reaction product, make the reaction effluent of the first reaction zone contact and react with noble metal hydrogenation catalyst for refining with in the very low reaction atmosphere of ammonia concentration at hydrogen sulfide, on the one hand, extend the activity stability time of noble metal hydrogenation catalyst for refining, on the other hand, be conducive to the carrying out of aromatic saturation reaction.At the top of fixed-bed reactor filling non-noble metal hydrogenation, processing catalyzer, is also the Poisoning Effect to noble metal catalyst for fear of hydrogen sulfide.
In the first reaction zone, kerosene(oil)fraction or solar oil feedstock oil-hydrogen mixture, process catalyst I with non-noble metal hydrogenation and contact, at 270～450 ℃ of temperature of reaction, hydrogen dividing potential drop 8.0～15.0MPa, hydrogen to oil volume ratio 60～1000Nm
3/ m
3, volume space velocity 1.0～3.0h
-1condition under, there is the reactions such as olefin saturation, hydrodenitrification reaction, hydrogenating desulfurization, aromatic saturation.
In second reaction zone, the reaction effluent of the first reactor is processed catalyst I I and noble metal hydrogenation catalyst for refining through non-noble metal hydrogenation successively, and with hydrogen counter current contact, at 200～320 ℃ of temperature of reaction, hydrogen dividing potential drop 8.0～15.0MPa, hydrogen to oil volume ratio 60～1000Nm
3/ m
3, volume space velocity 3.0～10.0h
-1condition under, further carry out aromatic saturation reaction and product separation.Because aromatic hydrogenation reaction exists thermodynamics equilibrium limit, high temperature can be unfavorable to aromatic hydrogenation saturated reaction.Therefore in second reaction zone, adopt relatively low temperature of reaction, be conducive to the carrying out of the hydrogenation saturated reaction of aromatic hydrocarbons.
In second reaction zone, non-noble metal hydrogenation is processed the admission space of catalyst I I and noble metal hydrogenation catalyst for refining than being 1:5 ~ 1:10.
Non-noble metal hydrogenation processes catalyst I or non-noble metal hydrogenation processing catalyst I I is loaded catalyst, and carrier is unformed aluminum oxide and/or sial, and active metal is one or more that are selected from VIB base metal and/or group VIII base metal.Wherein, group vib base metal is Mo and/or W, and group VIII base metal is Ni and/or Co.Non-noble metal hydrogenation processes catalyst I and non-noble metal hydrogenation processing catalyst I I can be identical catalyzer, can be also different catalyzer.
Preferred non-noble metal hydrogenation is processed catalyst I or non-noble metal hydrogenation, and to process catalyst I I be that to take composite alumina and composite oxygen SiClx be carrier, it consists of: in oxide compound and take catalyzer total amount as benchmark, the content of nickel and/or cobalt is 2～8 heavy %, molybdenum and tungsten sum are 12～45 heavy %, and surplus is carrier.
Described noble metal hydrogenation catalyst for refining is loaded catalyst, carrier is heat-resistant inorganic oxide, load hydrogenation activity component, described hydrogenation activity component concentration, in oxide compound, be 0.01～15 heavy %, be selected from least one platinum, palladium precious metal or itself and the group that formed by molybdenum, nickel, vanadium, cobalt, tungsten in the mixture of one or more metals.Preferred hydrogenation activity component is a kind of combination in nickel-platinum, nickel-palladium, nickel-platinum-palladium, platinum-palladium.
When described hydrogenation active metals component is selected from the nickel, platinum of group VIII and/or metallic palladium component, in metal and take catalyzer as benchmark, the content of described group VIII metal is preferably 0.1～7 % by weight, more preferably 0.1～5 % by weight.While containing platinum and palladium in described hydrogenation active metals component, Pd/(Pt+Pd wherein) weight ratio is 0.3～1.0, preferably 0.5～0.8.
The optional self-alumina of described carrier, silicon oxide, titanium oxide, magnesium oxide, silica-alumina, aluminum oxide-magnesium oxide, silicon oxide-magnesium oxide, silicon oxide-zirconium white, silicon oxide-Thorotrast, silicon oxide-beryllium oxide, silicon oxide-titanium oxide, silicon oxide-zirconium white, oxidation titania-zirconia, silica-alumina-Thorotrast, silica-alumina-titanium oxide, silica-alumina-magnesium oxide, silica-alumina-zirconium white, natural zeolite, one or more in clay.Preferred aluminum oxide and/or silica-alumina wherein.
Described noble metal hydrogenation catalyst for refining can also contain selectable adjuvant component, is one or more in boron, fluorine, chlorine and phosphorus, take catalyzer as benchmark, and the content of adjuvant component is 0.1%～5.0 % by weight.
The invention has the advantages that:
1, use method provided by the invention, can process kerosene or the solar oil cut of high sulfur-bearing, produce sulphur content and be less than 0.5 μ g/g, aromaticity content is less than the high-quality solvent product of 100 μ g/g, and quality product reaches the requirement of food grade solvent oil.
2, in the present invention, the first reaction zone at high temperature operates, and most sulfide and nitride in raw material is removed, simultaneously saturated part aromatic hydrocarbons; In the present invention, second reaction zone adopts adverse current bed bioreactor, adopted the good noble metal catalyst of part aromatic saturation performance, and under the operational condition of aromatic hydrogenation, reacts being conducive to, and can obtain better aromatic saturation effect.In addition, at the top of the adverse current bed bioreactor of second reaction zone filling non-noble metal hydrogenation, process catalyzer, avoided high density H
2the influence of S to noble metal catalyst, the life cycle that has extended noble metal hydrogenation catalyst for refining.
3, compare with two-stage hydrogenation, the high pressure air lift facility in the middle of having omitted, reduces equipment cost.
Accompanying drawing explanation
Accompanying drawing is the hydroprocessing process schematic flow sheet of production high-quality solvent oil provided by the invention.
Embodiment
Below by accompanying drawing, method provided by the invention is illustrated further, but not thereby limiting the invention.
The method of hydrotreating technical process of production high-quality solvent oil provided by the invention is described in detail as follows: new hydrogen enters make-up hydrogen compressor 19 and boosts by pipeline 11 with after recycle hydrogen from circulating hydrogen compressor 20 mixes, be divided into two-way, mix with fresh feed oil through pipeline 2 on one tunnel, and another road enters the second reactor 15 through pipeline 4 from the second reactor 15 bottoms.Fresh feed oil from pipeline 1 mixes with the hydrogen from pipeline 2, and mixing raw material enters the first reactor 14 and carries out hydrotreatment reaction.The first reactor effluent of gained enters the second reactor 15 through pipeline 3 from the top of the second reactor, with the hydrogen counter current contact from pipeline 4, at non-noble metal hydrogenation, process under the effect of catalyst I I and noble metal hydrogenation catalyst for refining successively, further remove the aromatic hydrocarbons in product.The second hydrogenator 15 top materials are delivered to high-pressure separator 16 through pipeline 5, and separating obtained hydrogen-rich gas enters circulating hydrogen compressor 20 through pipeline 7, and separating obtained liquid product is extracted out through pipeline 8, as hydrotreated naphtha component.The second reactor 15 bottom materials enter high-pressure separator 17 through pipeline 6, separating obtained gas is extracted out through pipeline 10, separating obtained liquid stream enters separation column 18 and cuts, and isolates lightnaphtha and extracts out through pipeline 12, isolates heavy naptha and extracts out through pipeline 13.
The following examples will be further described method provided by the invention, but not thereby limiting the invention.
Non-noble metal hydrogenation processing catalyst I and non-noble metal hydrogenation processing catalyst I I used in embodiment are Cat-A, and noble metal hydrogenation catalyst for refining is Cat-B, and the trade names of Cat-A are RS-1000, and by Sinopec catalyzer, branch office produces.The carrier of Cat-B is silica-alumina, take carrier as benchmark, and the content of its silicon oxide is 25 % by weight, and the specific surface area of carrier is 218m
2/ g, pore volume is 0.45ml/g; Active metal is Pt, Pd and Ni, take catalyzer as whole, and the content of Pt is 0.09 heavy %, and the content of Pd is 0.06 heavy %, and the content of Ni is 6 heavy %.
In embodiment, stock oil A used is a kind of virgin kerosene, and stock oil B is a kind of straight distillation light diesel oil.The main character of various raw materials is as shown in table 1.
Aromatic hydrocarbons bioassay standard is SH/T 0415-92.
Embodiment 1
First stock oil A fully mixes with hydrogen, enters the first reaction zone, under higher temperature of reaction, contacts carry out deep hydrodesulfurizationof reaction, denitrification reaction and the reaction of part aromatic saturation with non-noble metal hydrogenation processing catalyst I (Cat-A); Resultant of reaction enters second reaction zone, at non-noble metal hydrogenation, process catalyst I I(Cat-A) and the effect of noble metal hydrogenation catalyst for refining (Cat-B) under, with hydrogen counter current contact, proceed the reaction of degree of depth aromatic saturation, non-noble metal hydrogenation is processed the admission space of catalyst I I and noble metal hydrogenation catalyst for refining than being 1:7, meanwhile, the second reactor has the effect of gas stripping column, can remove hydrogen sulfide and ammonia in raw material.Top, second reaction zone resultant of reaction is through cooling after separated, and the hydrogen-rich gas of gained is recycle hydrogen, and the liquid fraction of gained goes out device as hydrotreated naphtha product or boat coal blend component; Bottoms directly enters fractionating system, isolates the solvent oil product of each fraction section.The reaction conditions of the present embodiment is as shown in table 2, and product main character is as shown in table 3, and as can be seen from Table 3, the aromaticity content of product is approximately 0, is the product index that meets food grade solvent oil.
First stock oil A fully mixes with hydrogen, enters the first reaction zone, contacts carry out deep hydrodesulfurizationof reaction, denitrification reaction and the reaction of part aromatic saturation under higher temperature of reaction with non-noble metal hydrogenation processing catalyst I (Cat-A); Resultant of reaction enters second reaction zone, at non-noble metal hydrogenation, process catalyst I I(Cat-A) and the effect of noble metal hydrogenation catalyst for refining (Cat-B) under, with hydrogen counter current contact, proceed the reaction of degree of depth aromatic saturation, non-noble metal hydrogenation is processed the admission space of catalyst I I and noble metal hydrogenation catalyst for refining than being 1:5.Meanwhile, the second reactor has the effect of gas stripping column, can remove hydrogen sulfide and ammonia in raw material.Top, second reaction zone resultant of reaction is through cooling, and the hydrogen-rich gas of gained is recycle hydrogen, and the liquid fraction of gained goes out device as hydrotreated naphtha product or boat coal blend component; Bottoms directly enters fractionating system, isolates the solvent oil product of each fraction section.The reaction conditions of the present embodiment is as shown in table 2, and product main character is as shown in table 3, and as can be seen from Table 3, the aromaticity content of product is 30 μ g/g, is the product of high-quality solvent oil.
Table 1 stock oil character
| Stock oil numbering | A | B |
| Type of feed | Virgin kerosene | Straight distillation light diesel oil |
| Density (20 ℃), g/cm 3 | 0.805 | 0.823 |
| Sulphur content, μ g/g | 550 | 650 |
| Nitrogen content, μ g/g | 4.2 | 28 |
| Bromine valency, gBr/100g | 0.6 | 2.2 |
| Aromatic hydrocarbons, heavy % | 12.0 | 17.5 |
| Boiling range ASTM D-1160, ℃ | ||
| IBP | 185 | 208 |
| 10% | 208 | 228 |
| 50% | 225 | 275 |
| 90% | 243 | 303 |
| FBP | 255 | 333 |
Table 2 operational condition
| Numbering | Embodiment 1 | |
| Stock oil | A | B |
| The first hydroconversion reaction zone | ||
| Hydrogen dividing potential drop, MPa | 10.0 | 12.0 |
| Temperature of reaction, ℃ | 300 | 320 |
| Volume space velocity during liquid, h -1 | 3.0 | 2.0 |
| Hydrogen to oil volume ratio, Nm 3/m 3 | 100 | 500 |
| The second hydroconversion reaction zone | ||
| Hydrogen dividing potential drop, MPa | 9.0 | 10.0 |
| Temperature of reaction, ℃ | 200 | 220 |
| Volume space velocity during liquid, h -1 | 1.5 | 1.3 |
| Hydrogen to oil volume ratio, Nm 3/m 3 | 100 | 300 |
Table 3 main products character
| Numbering | Embodiment 1 | |
| Sulphur content, μ g/g | <0.1 | <0.5 |
| Nitrogen content, μ g/g | <0.1 | <0.5 |
| Bromine valency, gBr/100g | <0.1 | <0.5 |
| Aromatic hydrocarbons, μ g/g | 0 | 30 |
| Boiling range scope ASTM D-1160, ℃ | 210～230 | 245～280 |
Claims (12)
1. produce a hydroprocessing process for high-quality solvent oil,
(1) kerosene(oil)fraction or solar oil feedstock oil mix with hydrogen, and its mixture enters the first reaction zone, and contact and react with non-noble metal hydrogenation processing catalyst I,
(2) effluent of the first reaction zone of step (1) gained enters second reaction zone, react with the hydrogen counter current contact that enters second reaction zone, the flow direction along the effluent of the first reaction zone, in second reaction zone, load successively non-noble metal hydrogenation and process catalyst I I and noble metal hydrogenation catalyst for refining
(3) effluent of second reaction zone, after cooling, separation, obtains hydrogen-rich gas and solvent oil product,
Wherein the temperature of reaction of second reaction zone is lower 50～200 ℃ than the temperature of reaction of the first reaction zone.
2. in accordance with the method for claim 1, it is characterized in that, the temperature of reaction of second reaction zone is lower 80～150 ℃ than the temperature of reaction of the first reaction zone.
3. in accordance with the method for claim 1, it is characterized in that, described second reaction zone is fixed-bed reactor, in reactor, from up to down load successively non-noble metal hydrogenation and process catalyst I I and noble metal hydrogenation catalyst for refining, the reaction effluent of the first reactor enters fixed-bed reactor from top, hydrogen enters fixed-bed reactor from bottom, the top effluent of fixed-bed reactor is through cooling, after separation, the hydrogen-rich gas obtaining recycles, the bottom effluent of fixed-bed reactor is after separation, obtain the solvent oil product that aromaticity content is extremely low.
4. in accordance with the method for claim 1, it is characterized in that the reaction conditions of the first reaction zone: 270～450 ℃ of temperature of reaction, hydrogen dividing potential drop 8.0～15.0MPa, hydrogen to oil volume ratio 60～1000Nm
3/ m
3, volume space velocity 1.0～3.0h
-1.
5. in accordance with the method for claim 1, it is characterized in that the reaction conditions of second reaction zone: 200～320 ℃ of temperature of reaction, hydrogen dividing potential drop 8.0～15.0MPa, hydrogen to oil volume ratio 60～1000Nm
3/ m
3, volume space velocity 3.0～10.0h
-1.
6. according to the method described in claim 1 or 3, it is characterized in that, in second reaction zone, non-noble metal hydrogenation is processed the admission space of catalyst I I and noble metal hydrogenation catalyst for refining than being 1:5 ~ 1:10.
7. in accordance with the method for claim 1, it is characterized in that, non-noble metal hydrogenation processes catalyst I or non-noble metal hydrogenation processing catalyst I I is loaded catalyst, carrier is unformed aluminum oxide and/or sial, and active metal is one or more that are selected from VIB base metal and/or group VIII base metal.
8. in accordance with the method for claim 7, it is characterized in that, non-noble metal hydrogenation is processed catalyst I or non-noble metal hydrogenation, and to process catalyst I I be that to take composite alumina and composite oxygen SiClx be carrier, it consists of: in oxide compound and take catalyzer total amount as benchmark, the content of nickel and/or cobalt is 2～8 heavy %, molybdenum and tungsten sum are 12～45 heavy %, and surplus is carrier.
9. in accordance with the method for claim 1, it is characterized in that, described precious metal catalyst for refining is loaded catalyst, carrier is heat-resistant inorganic oxide, load hydrogenation activity component, described hydrogenation activity component concentration, in oxide compound, be 0.01～15 heavy %, be selected from least one platinum, palladium precious metal or itself and the group that formed by molybdenum, nickel, vanadium, cobalt, tungsten in the mixture of one or more metals.
10. in accordance with the method for claim 9, it is characterized in that, described hydrogenation active metals component is selected from nickel, platinum and/or the metallic palladium component of group VIII, and in metal and take catalyzer as benchmark, the content of described group VIII metal is 0.1～7 % by weight.
11. according to the method described in claim 9 or 10, it is characterized in that, contains platinum and palladium, wherein Pd/(Pt+Pd in described hydrogenation active metals component) weight ratio be 0.3～1.0.
12. in accordance with the method for claim 1, it is characterized in that, the boiling range of described kerosene(oil)fraction is: 180 ~ 260 ℃ is virgin kerosene cut; The boiling range of described solar oil cut is: 205 ~ 350 ℃ is straight distillation light diesel oil cut.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109423328A (en) * | 2017-08-24 | 2019-03-05 | 中国石油化工股份有限公司 | A kind of method of solvent oil hydrogenation Porous deproteinized bone |
| CN111378502A (en) * | 2018-12-31 | 2020-07-07 | 中国石油化工股份有限公司 | Method for producing aromatic hydrocarbon solvent oil by hydrogenating C9 aromatic hydrocarbon fraction cracked by ethylene |
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| CN1267709A (en) * | 1999-03-19 | 2000-09-27 | 中国石油化工集团公司 | Two-stage fraction oil hydrogenating and arene eliminating process |
| CN1488713A (en) * | 2002-10-10 | 2004-04-14 | 中国石油化工股份有限公司 | Hydrocarbon hdyrotreating method |
| CN102443431A (en) * | 2010-10-13 | 2012-05-09 | 天津河清化学工业有限公司 | Naphtha hydrorefining dearomatization method |
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| CN1157847A (en) * | 1996-12-26 | 1997-08-27 | 南京兴达石油化工科技工贸公司 | Method for producing special kerosene type solvent naphtha |
| CN1267709A (en) * | 1999-03-19 | 2000-09-27 | 中国石油化工集团公司 | Two-stage fraction oil hydrogenating and arene eliminating process |
| CN1488713A (en) * | 2002-10-10 | 2004-04-14 | 中国石油化工股份有限公司 | Hydrocarbon hdyrotreating method |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109423328A (en) * | 2017-08-24 | 2019-03-05 | 中国石油化工股份有限公司 | A kind of method of solvent oil hydrogenation Porous deproteinized bone |
| CN111378502A (en) * | 2018-12-31 | 2020-07-07 | 中国石油化工股份有限公司 | Method for producing aromatic hydrocarbon solvent oil by hydrogenating C9 aromatic hydrocarbon fraction cracked by ethylene |
| CN111378502B (en) * | 2018-12-31 | 2021-12-07 | 中国石油化工股份有限公司 | Method for producing aromatic hydrocarbon solvent oil by hydrogenating C9 aromatic hydrocarbon fraction cracked by ethylene |
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