CN1224677C - Composite process of producing high quality diesel oil from coal liquified oil - Google Patents
Composite process of producing high quality diesel oil from coal liquified oil Download PDFInfo
- Publication number
- CN1224677C CN1224677C CN 02146386 CN02146386A CN1224677C CN 1224677 C CN1224677 C CN 1224677C CN 02146386 CN02146386 CN 02146386 CN 02146386 A CN02146386 A CN 02146386A CN 1224677 C CN1224677 C CN 1224677C
- Authority
- CN
- China
- Prior art keywords
- hydrogenation
- diesel oil
- hydrogen
- aluminum oxide
- reactor
- 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.)
- Expired - Lifetime
Links
Abstract
The present invention relates to a combined technology method for producing high-quality diesel oil by coal liquefied oil. Filtered coal liquefied oil enters a stable hydrogenation reactor with hydrogen so as to contact a hydrogenation protective agent and a hydrofining catalyst; the effluent of the stable hydrogenation reactor is extracted, so gas, naphtha fraction, diesel oil fraction and tail oil fraction are obtained; hydrogen enriched gas flow is circulated back to the stable hydrogenation reactor; the diesel oil fraction and the hydrogen obtained from a stable hydrogenation device enter a hydrogenation modification reactor of diesel oil so as to contact a hydrogenation modification catalyst; the effluent of the hydrogenation modification reactor is extracted, so naphtha fraction and diesel oil fraction are obtained; and hydrogen enriched gas flow returns to the hydrogenation modification reactor of diesel oil. The method uses the coal liquefied oil as raw materials, the cetane number of diesel oil products reach more than 45, and the sulfur content, the nitrogen content and the aromatic content can meet the standard of the oil of the second class of the world fuel specification.
Description
Technical field
The present invention relates to the method that a kind of liquid hydrocarbon that coal destruction hydrogenation is obtained carries out hydrotreatment.More particularly, be a kind of method of producing diesel oil from liquefied coal coil.
Background technology
Just having begun DCL/Direct coal liquefaction produced the liquid hydrocarbon Study on Technology as far back as 1913 in Germany, and will make the skilled industryization of gasoline with the brown coal direct liquefaction in nineteen twenty-seven.Since the world oil crisis first time took place in 1973 since; direct coal liquefaction technology is subjected to the attention of developed country; many DCL/Direct coal liquefaction technologies have been developed in succession; the IGOR technology of Germany's exploitation is online refining with liquefied coal coil; the qualified diesel product of direct production, and the liquefied coal coil of other explained hereafter will just can become the proper fuel oil production through following process.
USP4332666 has introduced a kind of method of producing diesel oil, aviation fuel and Number 2 fuel oil.The raw material of this technology is the cut that is suitable for doing hydrogen supply agent in the liquefied coal coil, and extracting goes out stable hydrocarbon as diesel oil, aviation fuel and Number 2 fuel oil from the hydrogenation resultant, and is remaining as hydrogen supply agent.But the quality of gained diesel product particularly cetane value is relatively poor.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of combined technical method of producing fine-quality diesel oil by liquefied coal coil.
Method provided by the invention comprises:
Liquefied coal coil after the filtration and hydrogen enter the stable hydrogenation reactor, contact with hydrogenation protecting agent, Hydrobon catalyst, the stable hydrogenation reactor effluent obtains gas, naphtha fraction, diesel oil distillate and tail oil cut through separation, and hydrogen rich stream loops back the stable hydrogenation reactor; The diesel oil distillate and the hydrogen that obtain from the stable hydrogenation device enter the diesel oil hydrogenation modification reactor, contact with catalyst for hydro-upgrading, separate the hydro-upgrading reactor effluent and obtain naphtha fraction, diesel oil distillate, and hydrogen rich stream returns the diesel oil hydrogenation modification reactor.
This method is raw material with the liquefied coal coil, and the cetane value of gained diesel product reaches more than 45, and sulphur, nitrogen and aromaticity content can satisfy the standard of world fuel oil standard II class oil.
Description of drawings
Accompanying drawing is a combined technical method synoptic diagram of being produced fine-quality diesel oil by liquefied coal coil provided by the invention.
Embodiment
Method provided by the invention comprises the off-line stable hydrogenation of liquefied coal coil and the deep hydrogenation upgrading of stable hydrogenation heavy distillate, describes above-mentioned two steps below respectively in detail.
(1), the off-line stable hydrogenation of liquefied coal coil
Liquefied coal coil after the filtration and hydrogen are mixed into the stable hydrogenation reactor, contact with hydrogenation protecting agent, Hydrobon catalyst, and reaction conditions is: hydrogen dividing potential drop 4.0MPa～20.0MPa, 280 ℃～450 ℃ of temperature of reaction, liquid hourly space velocity 0.1h
-1～10h
-1, hydrogen-oil ratio 300v/v～2800v/v.The stable hydrogenation reactor effluent passes through high-pressure separator, light pressure separator, separation column successively, separate and obtain naphtha fraction, diesel oil distillate and tail oil cut, naphtha fraction advances reformer and produces aromatic hydrocarbons or stop bracket gasoline, all the tail oil cut is as the hydrogen supply agent of upstream gelatin liquefaction part, and diesel oil distillate is as the raw material of diesel oil hydrogenation modification reactor; Isolate light hydrocarbon gas from light pressure separator; Mix with fresh hydrogen from the isolated hydrogen rich stream of high-pressure separator, loop back the stable hydrogenation reactor.
The raw materials used liquefied coal coil of this method is the product liquid that coal obtains through direct liquefaction, and its boiling range is C
5～540 ℃ are preferably C
5～450 ℃.The liquefied coal coil cut is heavy more, and then the content of impurity such as its metal and bituminous matter is high more, and is big more to the influence in Hydrobon catalyst life-span.Nitrogen content is not more than 2.0 weight % and preferably is not more than 1.2 weight % in the raw material, and sulphur content is not more than 1.0 weight %.The raw material oil properties is largely depended in technological operation handiness of the present invention, as nitrogen content, aromaticity content, boiling range etc.Owing to contain solid particulate in the raw material, if do not remove these solid particulates, will make the reactor bed pressure drop excessive, and shorten the life-span of Hydrobon catalyst.Therefore, raw material must be earlier after filtration device filter, remove in the liquefied coal coil behind the entrained solid particle, just can enter the stable hydrogenation reactor.
Described Hydrobon catalyst can be to load on the VIB on unformed aluminum oxide or the silica-alumina supports or the non-precious metal catalyst of VIII family, and halogen atom-containing not, and preferred Hydrobon catalyst is by 2.4～6.5 weight %NiO, 24～35 weight %WO
3, 0.1～2.1 weight %MgO and surplus unformed aluminum oxide or silica-alumina supports constitute.This catalyzer has very strong hydrodenitrogenationactivity activity, and this is that the relatively low characteristics of sulphur content design at nitrogen content in the liquefied coal coil is very high.The stable hydrogenation catalyzer is halogen atom-containing not, and the water of avoiding the contained oxygen hydrogenation of halogen atom and liquefied coal coil to generate reacts, and causes equipment corrosion.Because liquefied coal coil contains a certain amount of heavy metal and C
7Insolubles, these trace heavy metals very easily are deposited on the Primary Catalysts top, cause reactor pressure reduction to occur, reduce hydrogenation unit running period, and the metal that is deposited on simultaneously on the catalyzer can cause the hydrogenation catalyst permanent deactivation, and C
7Therefore the inactivation of insolubles meeting accelerator activator in stable hydrogenation technology, has adopted the protective material technology, with having higher demetalization and taking off C
7The hydrogenation protecting agent of insolubles function is seated in the Primary Catalysts top, avoids the generation of above-mentioned phenomenon.This hydrogenation protecting agent is by 1.0～5.0 heavy %NiO, 5.5～10.0 heavy %MoO
3The γ-Al that diplopore distributes that has with surplus
2O
3Carrier is formed.This protectant specific surface ≮ 180m
2/ g, pore volume ≮ 0.6mL/g, crushing strength ≮ 12N/mm.The hydrogenation protecting agent can be used one or more, and the loadings of hydrogenation protecting agent determines that the volume ratio of hydrogenation protecting agent and Hydrobon catalyst is 0.03～0.35 by foreign matter content in the liquefied coal coil and device running period.
Liquefied coal coil off-line stable hydrogenation is meant that the stable hydrogenation device is not serially connected with coal liquification device, have independent raw material supply system and product gathering system, hydrogenation unit is shutting down voluntarily, the hydrogenation unit shutting down does not influence other device running, and the hydrogenation unit running is not subjected to the influence of other device running status yet.Adopt the off-line hydrogenation can avoid the influence of the water vapour that is rich in the liquefied coal coil, CO in the upstream gelatin liquefaction part gas phase to hydrogenation catalyst
xCan not enter the stable hydrogenation device, reduce by CO
xHydrogenation generates CH
4The meaningless hydrogen consumption that causes.The off-line hydrogenation technique can be avoided the influence of gelatin liquefaction part unplanned shutdown to the stable hydrogenation device.If adopt online hydrogenation technique, when gelatin liquefaction partly went wrong and causes hydrogenation unit to stop in emergency, when temperature of reactor drops to below 100 ℃, the water in the gas phase can be absorbed by catalyzer, cause the catalyzer mechanical property to descend, have a strong impact on catalyst life.
Not good enough for preventing coal liquefaction system separating device separating effect, cause carrying secretly in the liquefied coal coil gelatin liquefaction process catalyst system therefor, before stable hydrogenation device feedstock pump, install filtration unit additional, filter out the solid particulate in the liquefied coal coil, prevent the too fast inactivation of hydrogenation catalyst, improve the hydrogenation catalyst life-span, prolong stable hydrogenation device running period.
(2), the hydro-upgrading of diesel oil distillate
The diesel oil distillate of stable hydrogenation device gained enters the diesel oil hydrogenation modification reactor and contacts with hydrogen, catalyst for hydro-upgrading, at hydrogen dividing potential drop 6.0～20.0MPa, 280～450 ℃ of temperature of reaction, liquid hourly space velocity 0.1～20h
-1, hydrogen-oil ratio 400～3000v/v condition under react, the separating reaction effluent obtains naphtha fraction, diesel oil distillate, hydrogen rich stream returns the diesel oil hydrogenation modification reactor.
The composition of described catalyst for hydro-upgrading is that the metal with VIII family, group vib in the periodic table of elements is an active ingredient, is carrier with aluminum oxide and zeolite.Specifically, this hydrogenation catalyst contains a kind of carrier and the molybdenum and/or tungsten and nickel and/or the cobalt that load on this carrier.Preferred catalyzer is composed as follows: in oxide compound and with the catalyzer total amount is benchmark, and the content of molybdenum and/or tungsten is 10～35 heavy % preferred 18～32 heavy % in this hydrogenation catalyst, and the content of nickel and/or cobalt is 1～15 heavy % preferred 3～12 heavy %.Described carrier is made up of aluminum oxide and zeolite, the weight ratio of aluminum oxide and zeolite be 90: 10～50: 50 preferred 90: 10～60: 40.Described aluminum oxide is the aluminum oxide that is composited according to 75: 25～50: 50 weight ratio by little porous aluminum oxide and macroporous aluminium oxide, to be diameter account for the aluminum oxide of total pore volume more than 95% less than the pore volume in 80 holes to wherein little porous aluminum oxide, and macroporous aluminium oxide is that the pore volume in diameter 60～600 holes accounts for the aluminum oxide of total pore volume more than 70%.Described zeolite is selected from one or more in faujusite, mordenite, erionite zeolite, zeolite L, omega zeolite, ZSM-4 zeolite, the Beta zeolite, preferred y-type zeolite, particularly preferred zeolite is that total acid content is 0.02 to less than 0.5 mmole/gram, the y-type zeolite of preferred 0.05～0.2 mmole/gram.
Why the present invention selected diesel oil hydrogenation modification in second step, be to loop back the gelatin liquefaction part as hydrogen supply agent because of tail oil cut in the stable hydrogenation product among the present invention, what need further processing is diesel oil distillate, and aromaticity content height, the cetane value of this diesel oil distillate are low, the utilization diesel oil hydrogenation modification is processed this diesel oil distillate, can reduce the aromaticity content of diesel oil distillate, and reach the purpose that reduces diesel oil distillate density and improve the diesel oil distillate cetane value by appropriate open loop, and the yield that keeps diesel product is more than 95 heavy %.Second step was adopted diesel oil hydrogenation modification, made that the flow process of liquefied coal coil processing upgrading is comparatively simple, and hydrogenation upgrading part is only established stable hydrogenation and two reactors of diesel oil hydrogenation modification, and investment and process cost have decline by a relatively large margin.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed, but does not therefore limit the present invention.
Accompanying drawing is the combined technical method schematic flow sheet by liquefied coal coil production fine-quality diesel oil provided by the invention, has omitted the equipment of many necessity among the figure, as pump, air cooler and valve etc.
Flow process is described in detail as follows: liquefied coal coil is after pipeline 1 enters strainer 3 filtrations; boost to reaction pressure by feedstock pump (not marking among the figure); after mixing from the hydrogen-rich gas of pipeline 5,6 successively; through interchanger 4 heat exchange; again after process furnace 7 heating; enter stable hydrogenation reactor 9, contact, remove impurity such as metal in the stock oil, sulphur and nitrogen with hydrogenation protecting agent, Hydrobon catalyst bed.Because hydrofining is strong exothermal reaction, need in the middle of reactor, to introduce cold hydrogen, control reaction temperature.The effluent of stable hydrogenation reactor 9 is successively behind pipeline 8, interchanger 4, enter high-pressure separator 10, in high-pressure separator, be separated into two bursts of logistics, one is a hydrogen-rich stream, wherein be mainly hydrogen, also comprise partial vulcanization hydrogen, ammonia, hydrogen-rich stream after pipeline 5 is through recycle compressors (not marking among the figure) compression with mix from the fresh hydrogen of pipeline 2, behind pipeline 6, interchanger 4, process furnace 7, loop back reactor 9 successively; Another burst logistics enters light pressure separator 12 through pipeline 11, the lighter hydrocarbons that remove are through pipeline 13 caterpillars, light pressure separator bottom effluent enters fractionating column system 15 through pipeline 14, the naphtha fraction that fractionates out is through pipeline 16 caterpillars, diesel oil distillate enters the diesel oil hydrogenation modification device through pipeline 17, the tail oil cut goes out the stable hydrogenation device through pipeline 18, loops back coal liquefaction system and does hydrogen supply agent.
Diesel oil distillate from pipeline 18 advances surge tank 19, boost to reaction pressure by another feedstock pump (not marking among the figure) then, mix with the hydrogen-rich gas from pipeline 27,20 successively, after interchanger 21 heat exchange, after pipeline 22 enters process furnace 23 heating, enter diesel oil hydrogenation modification reactor 24 again, by contacting with the catalyst for hydro-upgrading bed, further remove impurity such as sulphur and nitrogen, saturated aromatic hydrocarbons wherein, and part open loop.Though ring-opening reaction is thermopositive reaction, hydrofining is strong exothermal reaction, so from total thermopositive reaction that is seen as, need to introduce cold hydrogen, control reaction temperature in the middle of reactor.The effluent of reactor 24 is successively behind pipeline 25, interchanger 21, enter high-pressure separator 26, in high-pressure separator, be separated into two bursts of logistics, one is a hydrogen-rich stream, wherein be mainly hydrogen, also comprise partial vulcanization hydrogen, ammonia and because the light hydrocarbon that cracking produces, hydrogen-rich stream is after pipeline 27 is through recycle compressors (not marking among the figure) compression, with mix from the fresh hydrogen of pipeline 2, loop back reactor 24 through pipeline 20, interchanger 21, pipeline 22, process furnace 23 successively; Another burst logistics enters light pressure separator 29 through pipeline 28, the lighter hydrocarbons that remove are through pipeline 30 caterpillars, light pressure separator bottom effluent enters fractionating column system 32 through pipeline 31, and the naphtha fraction that fractionates out, diesel oil distillate are respectively through pipeline 33,34 caterpillars.
Method advantage provided by the invention is:
1, because the Hydrobon catalyst of stable hydrogenation halogen atom-containing not, the water of avoiding the contained oxygen hydrogenation of halogen atom and liquefied coal coil to generate reacts and the equipment corrosion that causes.
2, because the raw material of stable hydrogenation is removed solid particulate earlier after filtration, avoid the reactor bed pressure drop excessive, thereby prolonged the life-span of Hydrobon catalyst.
3, adopt the off-line stable hydrogenation can avoid that contained a large amount of water vapour reduce the hydrogen consumption, and can avoid the influence of gelatin liquefaction part unplanned shutdown to the stable hydrogenation device the influence of hydrogenation catalyst in the liquefied coal coil.
4, the flow process of this method is simple, only need establish stable hydrogenation and two reactors of diesel oil hydrogenation modification, and investment and process cost have decline by a relatively large margin.
5, the cetane value of this method gained diesel product reaches more than 45, and sulphur, nitrogen and aromaticity content can satisfy the standard of world fuel oil standard II class oil.
The following examples will give further instruction to present method, but therefore not limit present method.
Liquefied coal coil A, B used among the embodiment are all through filtering, the used Hydrobon catalyst trade names of stable hydrogenation are RCT-1, hydrogenation protecting agent trade names are RG-10A/RG-10B, produce by Sinopec Chang Ling catalyst plant, the volume ratio of RG-10A/RG-10B and RCT-1 is 0.2; The trade names of the catalyst for hydro-upgrading that diesel oil hydrogenation modification is used are RIC-1, produce by Sinopec Chang Ling catalyst plant.Test is carried out on medium-sized fixed bed hydrogenation device.
Embodiment 1
Liquefied coal coil A and hydrogen after the filtration enter the stable hydrogenation reactor, contact with hydrogenation protecting agent RG-10A/RG-10B, Hydrobon catalyst RCT-1, the stable hydrogenation reactor effluent obtains gas, naphtha fraction, diesel oil distillate and tail oil cut through separation, and hydrogen rich stream loops back the stable hydrogenation reactor; The diesel oil distillate and the hydrogen that obtain from the stable hydrogenation reactor enter the hydro-upgrading reactor that catalyst for hydro-upgrading RIC-1 is housed, separate the hydro-upgrading reactor effluent and obtain naphtha fraction, diesel oil distillate, hydrogen rich stream returns the deep hydrogenation reforming reactor.
Stock oil character, processing condition and diesel product character are listed in table 1, table 2 and table 3 respectively.By table as seen, the density of liquefied coal coil is not too high, and processing condition are not harsh, the sulphur of product diesel oil distillate and the content of nitrogen are very low, and aromaticity content is lower, have reached the index request of " world's fuel oil standard " II class diesel oil, its cetane value surpasses 45, is qualified diesel product.
Embodiment 2
The flow process of this embodiment is substantially the same manner as Example 1, and stock oil is changed to liquefied coal coil B.Stock oil character, processing condition and diesel product character are listed in table 1, table 2 and table 3 respectively.By table as seen, the density of liquefied coal coil is near 1, and the processing condition of hydrogenation upgrading are comparatively harsh, the sulphur of product diesel oil distillate and the content of nitrogen are very low, and aromaticity content is lower, have reached the index request of " world's fuel oil standard " II class diesel oil, its cetane value surpasses 45, is qualified diesel product.
Table 1
| Embodiment 1 | Embodiment 2 | |
| Stock oil | Liquefied coal coil A | Liquefied coal coil B |
| Density (20 ℃), g/cm 3 | 0.920 | 0.9912 |
| S, heavy % | 0.19 | 0.16 |
| N, heavy % | 0.41 | 0.56 |
| Total aromaticity content, heavy % | 71.5 | 72.3 |
| Polycyclic aromatic hydrocarbon content, heavy % | 43.5 | 52.1 |
| Boiling range (ASTMD-1160), ℃ | ||
| Initial boiling point/10% | 124/176 | 170/268 |
| 50％/90％ | 302/370 | 379/419 |
| Do | 393 | 445 |
Table 2
| Embodiment 1 | Embodiment 2 | |
| The stable hydrogenation processing condition | ||
| Temperature of reaction, ℃ | 340 | 350 |
| The hydrogen dividing potential drop, MPa | 14.0 | 14.0 |
| Volume space velocity, h -1 | 1.0 | 1.0 |
| Hydrogen-oil ratio, v/v | 1200 | 1200 |
| The hydrogenation modifying process condition | ||
| Temperature of reaction, ℃ | 350 | 350 |
| The hydrogen dividing potential drop, MPa | 14.0 | 14.0 |
| Volume space velocity, h -1 | 1.0 | 0.75 |
| Hydrogen-oil ratio, v/v | 900 | 900 |
Table 3
| Embodiment 1 | Embodiment 2 | |
| Density (20 ℃), g/cm 3 | 0.8650 | 0.8774 |
| S，ppm | ＜10 | ＜10 |
| Total aromaticity content, heavy % | 13.6 | 14.2 |
| Polycyclic aromatic hydrocarbon content, heavy % | 2.4 | 2.9 |
| Boiling range (ASTM D-86), ℃ | ||
| Initial boiling point | 184 | 187 |
| 50％ | 267 | 277 |
| 90％ | 361 | 353 |
| Cetane value | 46.2 | 47.3 |
Claims (12)
1, a kind of combined technical method of producing fine-quality diesel oil by liquefied coal coil; liquefied coal coil after it is characterized in that filtering and hydrogen enter the stable hydrogenation reactor; contact with hydrogenation protecting agent, Hydrobon catalyst; the reaction conditions of stable hydrogenation is: hydrogen dividing potential drop 4.0MPa～20.0MPa; 280 ℃～450 ℃ of temperature of reaction, liquid hourly space velocity 0.1h
-1～10h
-1, hydrogen-oil ratio 300v/v～2800v/v, the stable hydrogenation reactor effluent obtains gas, naphtha fraction, diesel oil distillate and tail oil cut through separation, and hydrogen rich stream loops back the stable hydrogenation reactor; The diesel oil distillate and the hydrogen that obtain from the stable hydrogenation device enter the diesel oil hydrogenation modification reactor, contact with catalyst for hydro-upgrading, the reaction conditions of diesel oil hydrogenation modification is: hydrogen dividing potential drop 6.0～20.0MPa, 280～450 ℃ of temperature of reaction, liquid hourly space velocity 0.1～20h
-1, hydrogen-oil ratio 400～3000v/v, separate the hydro-upgrading reactor effluent and obtain naphtha fraction, diesel oil distillate, hydrogen rich stream returns the diesel oil hydrogenation modification reactor.
2, according to the method for claim 1, it is characterized in that described liquefied coal coil is the product liquid that coal obtains through direct liquefaction, its boiling range is C
5～540 ℃.
3, according to the method for claim 1, it is characterized in that the used Hydrobon catalyst of stable hydrogenation is to load on the VIB on unformed aluminum oxide or the silica-alumina supports or the non-precious metal catalyst of VIII family, and halogen atom-containing not.
4,, it is characterized in that the used Hydrobon catalyst of stable hydrogenation is by 2.4～6.5 weight %NiO, 24～35 weight %WO according to the method for claim 3
3, 0.1～2.1 weight %MgO and surplus unformed aluminum oxide or silica-alumina supports constitute.
5,, it is characterized in that the used hydrogenation protecting agent of stable hydrogenation is by 1.0～5.0 heavy %NiO, 5.5～10.0 heavy %MoO according to the method for claim 1
3The γ-Al that diplopore distributes that has with surplus
2O
3Carrier is formed.
6, according to the method one of in the claim 1,3,4,5, the volume ratio that it is characterized in that described hydrogenation protecting agent and Hydrobon catalyst is 0.03～0.35.
7, according to the method for claim 1, it is characterized in that described catalyst for hydro-upgrading is an active ingredient with the metal of VIII family, group vib in the periodic table of elements, be carrier with the mixture of aluminum oxide and zeolite.
8, method according to claim 1, it is characterized in that described hydrogenation catalyst contains a kind of carrier and the molybdenum and/or tungsten and nickel and/or the cobalt that load on this carrier, described carrier is made up of aluminum oxide and zeolite, the weight ratio of aluminum oxide and zeolite is 90: 10～50: 50, described aluminum oxide is the aluminum oxide that is composited according to 75: 25～50: 50 weight ratio by little porous aluminum oxide and macroporous aluminium oxide, to be diameter account for the aluminum oxide of total pore volume more than 95% less than the pore volume in 80 holes to wherein little porous aluminum oxide, and macroporous aluminium oxide is that the pore volume in diameter 60～600 holes accounts for the aluminum oxide of total pore volume more than 70%.
9, method according to claim 8 is characterized in that in oxide compound and is benchmark with the catalyzer total amount that the content of molybdenum and/or tungsten is 10～35 heavy %, and the content of nickel and/or cobalt is 1～15 heavy %.
10, method according to claim 9, the content that it is characterized in that molybdenum and/or tungsten are 18～32 heavy %, and the content of nickel and/or cobalt is 3～12 heavy %.
11, method according to claim 8, the weight ratio that it is characterized in that described aluminum oxide and zeolite is 90: 10～60: 40.
12, according to Claim 8 or 11 described methods, it is characterized in that described zeolite is a y-type zeolite.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02146386 CN1224677C (en) | 2002-10-30 | 2002-10-30 | Composite process of producing high quality diesel oil from coal liquified oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02146386 CN1224677C (en) | 2002-10-30 | 2002-10-30 | Composite process of producing high quality diesel oil from coal liquified oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1493663A CN1493663A (en) | 2004-05-05 |
| CN1224677C true CN1224677C (en) | 2005-10-26 |
Family
ID=34232713
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 02146386 Expired - Lifetime CN1224677C (en) | 2002-10-30 | 2002-10-30 | Composite process of producing high quality diesel oil from coal liquified oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1224677C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20110129895A (en) * | 2009-02-13 | 2011-12-02 | 포마갈스키 | Conveyor facility with a passive vehicle hitched to lateral traction ropes |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100389169C (en) * | 2005-07-15 | 2008-05-21 | 中国石油化工股份有限公司 | Production of high-bioctyl-value diesel oil by coal liquification |
| CN100419044C (en) * | 2005-07-15 | 2008-09-17 | 中国石油化工股份有限公司 | Production of large-specific-weight aircraft liquid petroleum oil at maximum from coal liquefied oil |
| CN101173190B (en) * | 2007-10-22 | 2012-03-28 | 中国石油集团工程设计有限责任公司抚顺分公司 | Feito synthetic oil processing line |
| CN101144032B (en) * | 2007-10-23 | 2011-09-07 | 神华集团有限责任公司 | Preparation method for cleaning diesel oil |
| CN103059934B (en) * | 2011-10-19 | 2015-11-25 | 中国石油化工股份有限公司 | A kind of hydro-upgrading pour-point depressing method taking into account diesel product quality |
-
2002
- 2002-10-30 CN CN 02146386 patent/CN1224677C/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20110129895A (en) * | 2009-02-13 | 2011-12-02 | 포마갈스키 | Conveyor facility with a passive vehicle hitched to lateral traction ropes |
| KR101713349B1 (en) * | 2009-02-13 | 2017-03-07 | 포마 | Transport installation with a passive carrier vehicle hitched to lateral hauling ropes |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1493663A (en) | 2004-05-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| RU2430957C2 (en) | Procedure and installation for conversion of heavy oil fractions in boiling layer by integrated production of middle distallate with extremly low sulphur contents | |
| CN101210198B (en) | Hydrogenation method for producing high grade diesel oil and high grade reforming raw material | |
| CN100590182C (en) | Method for producing cleaning oil from coal-tar oil | |
| CN101107060A (en) | Hydrocracking method of heavy feedstocks with improved hydrogen processing | |
| CN1162516C (en) | Process for greatly preparing hihg-quality diesel oil or jet fuel from liquefied coil oil | |
| CN102453543B (en) | Combined process of hydrotreatment and catalytic cracking for residuum | |
| CN100478426C (en) | Process of desulfurizing and eliminating aromatic hydrocarbons deeply for diesel oil | |
| CN103305269A (en) | Method for producing gasoline and diesel by directly hydrogenating medium and low temperature coal tar | |
| CN1173012C (en) | Method of desulfurizing and dearomatizing diesel oil deeply | |
| CN100389169C (en) | Production of high-bioctyl-value diesel oil by coal liquification | |
| CN1224677C (en) | Composite process of producing high quality diesel oil from coal liquified oil | |
| CN1100122C (en) | Process for hydrogenating poor-quality raw material for catalytic cracking | |
| CN109988609B (en) | Flexible shale oil hydrocracking process | |
| CN1132913C (en) | Process for preparing jet fuel and/or diesel oil or tail oil | |
| CN1912062A (en) | Hydrogenation method for producing catalytic reforming raw material | |
| CN1216967C (en) | Hydrogenation cracking method for maximally producing intermediate distillate | |
| CN109777501B (en) | Refinery gas combined processing method | |
| US20020008050A1 (en) | Medium-pressure hydrocracking process | |
| CN100510022C (en) | Low-hydrogenloss hydrogenation of high-output qulified diesel oil | |
| CN1141362C (en) | Stable hydrogenation process for liquefied coal coil | |
| CN100419044C (en) | Production of large-specific-weight aircraft liquid petroleum oil at maximum from coal liquefied oil | |
| CN1261544C (en) | Medium pressure hydrogenation method for maximumly producing high quality diesel fuel | |
| CN1266256C (en) | Improved hydrocracking process | |
| CN100378201C (en) | Stabilized hydrogenation of coal liquefied oil | |
| CN109777499B (en) | Refinery gas combined processing technology |
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 |
Granted publication date: 20051026 |
|
| CX01 | Expiry of patent term |