CN100510023C - Production of cleaning fuel from heavy-fraction oil - Google Patents
Production of cleaning fuel from heavy-fraction oil Download PDFInfo
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- CN100510023C CN100510023C CNB2005101300786A CN200510130078A CN100510023C CN 100510023 C CN100510023 C CN 100510023C CN B2005101300786 A CNB2005101300786 A CN B2005101300786A CN 200510130078 A CN200510130078 A CN 200510130078A CN 100510023 C CN100510023 C CN 100510023C
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Abstract
Production of clean fuel by heavy-fraction oil is carried out by hydrogenation refining for heavy-fraction oil, separating to obtain heavy material and light material, delivering heavy material to catalytic unit to be treated, and entering light material and light circulation oil of catalytic unit into reactor to hydrogenation upgrade. It's cheap, has shorter process flow path and better quality. The final products include diesel fraction, gasoline fraction and naphtha fraction to be used as catalytic reforming raw material.
Description
Technical field
The invention belongs to other step of converting of at least one hydroprocessing technique process and at least one and handle the method for hydrocarbon ils.More particularly, be a kind of heavy distillate is produced clean fuel through hydrogenation unit and catalytic cracking unit method.
Background technology
For the needs of environment protection, countries in the world have been worked out more strict fuel specification one after another, require the oil refining enterprise production performance is good, the hazardous and noxious substances quantity discharged is low eco-friendly gasoline and diesel product.China is also strict day by day to the specification of quality of gasoline and diesel oil, and the formulation of standard is with reference to " European emission standard ".The standard of carrying out in China is class Europe I at present, and gasoline and the diesel oil standard that carry out in Beijing, Shanghai and three big cities, Guangzhou are class Europe II; 2005 three big city gasoline and diesel oil standard are carried out by class Europe III.
Upgrading along with the oil fuel quality, many refineries are that the refinery of main processing means is difficult to produce qualified gasoline and diesel product with catalytic cracking unit particularly, the subject matter that gasoline products production exists is that olefin(e) centent and sulphur content are too high, the subject matter that diesel product exists is the too high and cetane value deficiency of sulphur content, and more existing at present optional technology address the above problem.Catalyzer by promoting pipe reactor, application specific aspect catalytic cracking process and add the problem that technology such as corresponding adjuvants can partly solve content of olefin in gasoline; And the problem of content of sulfur in gasoline can adopt front-end hydrogenation and two approach of back end hydrogenation to solve, front-end hydrogenation promptly is that catalytically cracked material is carried out the hydrogenation pre-treatment, can produce low-sulphur oil after being reduced to the sulphur content of catalytically cracked material to a certain degree, back end hydrogenation promptly is to adopt the method for hydrogenation optionally to remove sulphur content in the catalytic gasoline; The problem of diesel oil sulphur content can achieve the goal by the hydrofining means of routine; The problem of diesel cetane-number then can solve by the technological approaches that adopts hydro-upgrading.Yet, adopt existing technology by a plurality of explained hereafter clean fuels, its shortcoming also is conspicuous, that is exactly that Production Flow Chart is long, causes investment and production cost to increase substantially.
US5403469 discloses a kind of method of producing catalytically cracked material and intermediate oil.This method is combined hydrotreatment technology and hydrocracking technology, obtains naphtha fraction, kerosene(oil)fraction, diesel oil distillate and tail oil cut after the processing vacuum gas oil (VGO), and wherein the tail oil cut is as catalytically cracked material.This method has two different flow processs: a kind of elder generation carries out vacuum fractionation with stock oil, and the light constituent that fractionation obtains advances hydroeracking unit, and hydrotreater is advanced in the heavy constituent that fractionation obtains, and the product of two hydrogenation units advances same high-pressure separator; Isolate gas in the high-pressure separator as recycle hydrogen, liquid advances separation column; Separation column is naphtha fraction, kerosene(oil)fraction, diesel oil distillate and catalytically cracked material with the hydrogenation products fractionation.Another flow process is for carrying out hydrotreatment to stock oil earlier, the hydrotreating reactor effluent mixes in high-pressure separator with the hydrocracking reactor effluent, high-pressure separator is gas phase and liquid phase with mixture separation, gas phase is as recycle hydrogen, and liquid phase is naphtha fraction, kerosene(oil)fraction, diesel oil distillate, hydrocracking raw material and catalytically cracked material through the separation column fractionation.This method is not handled second-rate catalytic diesel oil (LCO).
US4780193 discloses a kind of method of hydrorefining catalyst cracking stock.This method adopts hydrorefined method to improve the quality of catalytically cracked material, and the straight-chain paraffin that consists of 30 heavy % of its raw material and 70 weighs aromatic hydrocarbons and the naphthenic hydrocarbon of %, and major part is an aromatic hydrocarbons.The temperature of reaction of hydro-refining unit is lower than 390 ℃, reaction pressure should be more than 10.0MPa, be preferably in more than the 12.0MPa, helping under the saturated processing condition of aromatic hydrocarbons, improve the cracking performance of catalytic cracking unit raw material by hydrofining, thereby improve the transformation efficiency of catalytic cracking unit, produce the high gasoline blend component of octane value.But this method is produced the gasoline that obtains, diesel product, and other is second-rate.
CN1493668A discloses a kind of middle pressure hydrocracking and catalytic cracking combined technology.This method at first enters the middle pressure hydrocracking cell processing with heavy hydrocarbon material, obtain intermediate oil and through the catalytically cracked material of hydro-upgrading, catalytically cracked material behind the hydro-upgrading enters into the catalytic cracking unit processing again and obtains main productss such as liquefied gas, gasoline fraction, LCO, then LCO is looped back the unitary hydrofining reactor of middle pressure hydrocracking, repeated hydrogenation cracking after making with extra care.This method can improve intermediate oil selectivity and quality thereof.But this method gasoline products yield is low, of poor quality.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of method of producing clean fuel by heavy distillate.
Method provided by the invention comprises:
(1) heavy distillate with enter hydrofining reactor after hydrogen mixes, contact with Hydrobon catalyst, carry out hydrogenation reaction; The reaction effluent of hydrofining reactor enters high pressure hot separator, is separated into light material I and heavier feeds I; Heavier feeds I enters thermal low-pressure separators, further is separated into light material II and heavier feeds II;
(2) light material I with enter the hydro-upgrading reactor after light cycle oil from catalytic cracking unit mixes, under the effect of catalyst for hydro-upgrading, react; The reaction effluent of hydro-upgrading reactor enters cold high pressure separator, and isolated hydrogen-rich gas recycles, and isolated liquid phase stream III enters the cold low separator with after light material II mixes, and further carries out gas-liquid separation;
(3) the isolated liquid phase stream IV of cold low separator with enter separation column after heavier feeds II mixes, obtain naphtha fraction, diesel oil distillate and tail oil cut;
(4) the tail oil cut enters catalytic cracking unit, carries out catalytic cracking reaction and obtains dry gas, liquefied gas, gasoline fraction, light cycle oil and slurry oil, and wherein light cycle oil returns and enters the hydro-upgrading reactor.
The present invention combines hydrogenation unit and catalytic cracking unit, has not only shortened work flow, has saved investment and process cost; Also can process the heavy distillate of the high nitrogen of high-sulfur, produce the diesel oil distillate and the gasoline fraction that satisfy Europe III emission standard, and the fine naphtha fraction, and naphtha fraction can be used as catalytic reforming raw material.
Description of drawings
Accompanying drawing is a method flow synoptic diagram of being produced clean fuel by heavy distillate provided by the invention.
Embodiment
Method provided by the invention is so concrete enforcement:
Heavy distillate of the present invention be vacuum gas oil, atmospheric gas oil, coker gas oil, catalysis heavy cycle oil and deasphalted oil wherein any or several and with the mixing oil of optional vacuum residuum.Its boiling range is 180～670 ℃; Sulphur content is less than 5.0 heavy %, preferably less than 4.0 heavy % in the raw material; Nitrogen content is less than 1.0 heavy %, preferably less than 0.4 heavy %.
Heavy distillate with enter hydrofining reactor after hydrogen mixes, contact with Hydrobon catalyst, at hydrogen dividing potential drop 4.0MPa～15.0MPa, 280～400 ℃ of temperature of reaction, liquid hourly space velocity 0.1～20h
-1, hydrogen to oil volume ratio 300～2000Nm
3/ m
3Reaction conditions under, carry out hydrogenating desulfurization, hydrodenitrification and aromatic hydrocarbons saturated reaction, and the mild cracking of heavy distillate reaction.Hydrobon catalyst is VIB and/or the VIII family non-precious metal catalyst that loads on unformed aluminum oxide or the silica-alumina supports.When raw material impurity content is high, an amount of protective material of need packing at the hydrofining reactor top, protective material is 0.05:1～0.5:1 with the admission space ratio of Hydrobon catalyst.Because hydrofining is strong exothermal reaction, need in the middle of reactor, to introduce cold hydrogen, control reaction temperature.
The reaction effluent of hydrofining reactor enters high pressure hot separator, under the condition of 200～370 ℃ of service temperatures, be separated into light material I and heavier feeds I, wherein light material I mainly by the lighter hydrocarbons of hydrogen, hydrogen sulfide, ammonia, C1～C4 and＜350 ℃ of hydrocarbon fractions form, heavier feeds I is mainly〉350 ℃ of hydrocarbon fractions.Heavier feeds I enters thermal low-pressure separators, further is separated into light material II and heavier feeds II, and wherein light material II is made up of hydrogen, hydrogen sulfide, ammonia, C1～C4 and a spot of＜350 a ℃ hydrocarbon fraction, and heavier feeds II is〉350 ℃ of hydrocarbon fractions.
Light material I with enter the hydro-upgrading reactor after light cycle oil from catalytic cracking unit mixes, contact with catalyst for hydro-upgrading, at hydrogen dividing potential drop 4.0MPa～15.0MPa, 280～400 ℃ of temperature of reaction, liquid hourly space velocity 0.1～20h
-1, hydrogen to oil volume ratio 300～2000Nm
3/ m
3Reaction conditions under carry out hydro-upgrading reaction, i.e. desulfurization, denitrification reaction, aromatic hydrocarbons saturated reaction, and the cracking ring-opening reaction of the polycyclic aromatic hydrocarbons of hydrogenation after saturated.The diesel oil hydrogenation modification technology is one of means that effectively improve the diesel oil distillate cetane value, and when the hydrogen dividing potential drop was the 8.0MPa left and right sides, the increase rate of diesel cetane-number generally can reach 12～15 more than the unit, and the hydrogen dividing potential drop increase rate of high hexadecane value more is big more.Catalyst for hydro-upgrading is VIB and/or the VIII family non-precious metal catalyst that loads on the molecular sieve.Can load an amount of Hydrobon catalyst in the hydro-upgrading reactor head, Hydrobon catalyst is 0.01:1～5:1 with the admission space ratio of catalyst for hydro-upgrading.Because hydrofining and hydrocracking are strong exothermal reaction, need in the middle of reactor, to introduce cold hydrogen, control reaction temperature.
The effluent of hydro-upgrading reactor enters cold high pressure separator, carries out gas-liquid separation for 25～60 ℃ in service temperature, and isolated hydrogen-rich gas recycles as recycle hydrogen; Isolated liquid phase stream III enters the cold low separator with after light material II mixes, and further carries out gas-liquid separation.The isolated liquid phase stream IV of cold low separator with enter separation column after heavier feeds II mixes, obtain naphtha fraction, diesel oil distillate and tail oil cut.
The tail oil cut enters catalytic cracking unit, a reactor that comprises two reaction zones is arranged in the catalytic cracking unit, the tail oil cut enters behind the reactor in the presence of water vapor to contact with the catalytic cracking catalyst of heat and carries out primary first-order equation and secondary reaction, reaction conditions is: the temperature of first reaction zone is 540～580 ℃, and the temperature of second reaction zone is that 495～510 ℃, total residence time are 3～10 seconds.Reaction product isolated, reclaimable catalyst enters revivifier through stripping, recycles after burning; Separating obtained liquid product obtains dry gas, liquefied gas, gasoline fraction, light cycle oil and slurry oil, and wherein light cycle oil returns the hydro-upgrading reactor.
It is to produce one of operational path of low-sulphur oil that catalytically cracked material is carried out the hydrogenation pre-treatment.By hydrofining the sulphur content of catalytically cracked material is descended, thereby the sulphur content that makes the catalytic cracking production gasoline fraction reach " European emission standard " to the sulphur content requirement in the III gasoline less than 150ppm.The preferred catalytic cracking unit of the present invention is the catalytic cracking technology of voluminous isoparaffin, under can the prerequisite that the gasoline fraction octane value becomes substantially in keeping product, reduce its olefin(e) centent significantly, reach " European emission standard " the requirement of III content of olefin in gasoline.
In addition, aromatic hydrocarbons and alkene by containing in the saturated raw material of hydrofining energy improve the hydrogen richness of catalytically cracked material, thereby reduce the growing amount of coke in the catalytic cracking process effectively, can improve the yield of gasoline and light cycle oil.Because the sulphur and the nitrogen content of catalytically cracked material are lower,, produce the contained SO of flue gas in the catalyst regeneration process again so generate the sulphur and the nitrogen content of coke on the cracking catalyst surface also lower
xAnd NO
xCan significantly descend, reduce pollution environment.
Advantage of the present invention is:
1, the present invention is integrated into two relatively independent operating units with three kinds of different technology of catalytic cracking of the pre-treatment of catalytically cracked material hydrogenation, diesel oil hydrogenation modification and voluminous isoparaffin, be hydrogenation unit and catalytic cracking unit, shorten the work flow of producing clean fuel by heavy distillate greatly, saved investment and process cost.
2, because separating the LCO that produces with catalytic cracking unit with the diesel oil distillate that generates in the catalytically cracked material unifining process, the high pressure hot separator that the present invention adopts is mixed into hydro-upgrading unit, thereby high potential temperature and high pressure position in the raw material hydrogenation pretreatment technology flow process have been made full use of, greatly reduce energy consumption, and improved diesel yield.
3, the present invention can produce simultaneously and obtain high clean gasoline cut of yield and clean diesel cut, it all can meet " European emission standard " III generic request, while by-product virtue potential content height, sulphur, nitrogen content all satisfy the naphtha fraction of catalysis CONTINUOUS REFORMER charging requirement.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed.
Accompanying drawing is a method flow synoptic diagram of being produced clean fuel by heavy distillate provided by the invention.Omitted equipment such as process furnace, pump and interchanger among the figure, but this is known to those of ordinary skills.Flow process is described in detail as follows: from the heavy distillate of pipeline 1 after feedstock pump 2 boosts, mix with hydrogen stream through pipeline 3 from pipeline 36, enter hydrofining reactor 4 then, under the Hydrobon catalyst effect, carry out hydrogenating desulfurization, hydrodenitrification and aromatic hydrocarbons saturated reaction, and a small amount of cracking reaction.Its reaction effluent enters high pressure hot separator 6 through pipeline 5, is separated into light material I and heavier feeds I in high pressure hot separator 6, and light material I is extracted out through pipeline 8 by the top of high pressure hot separator 6; Heavier feeds I enters thermal low-pressure separators 9 by the bottom of high pressure hot separator 6 after pipeline 7 is extracted out; Further be separated into light material II and heavier feeds II at this, light material II is extracted out through pipeline 10 by thermal low-pressure separators 9 tops, and heavier feeds II is extracted out through pipeline 11 by thermal low-pressure separators 9 bottoms.From the light material I of pipeline 8 with after light cycle oil from pipeline 30 mixes, enter hydro-upgrading reactor 13 through pipeline 12, by contacting with the catalyst for hydro-upgrading bed, further remove impurity such as sulphur and nitrogen in the stock oil, saturated aromatic hydrocarbons, and the polycyclic aromatic hydrocarbons after saturated carried out the cracking open loop.The reaction effluent of hydro-upgrading reactor 13 enters cold high pressure separator 15 through pipeline 14 and carries out gas-liquid separation, isolated hydrogen rich stream mixes with new hydrogen from pipeline 35 behind pipeline 32, circulating hydrogen compressor 33, pipeline 34 successively, mixes hydrogen stream and mixes with heavy distillate from pipeline 3 through pipeline 36.Cold high pressure separator 15 isolated liquid phase stream III extract out through pipeline 16, mix after pipeline 17 enters cold low separator 18 with light material II from pipeline 10.Mixture further carries out gas-liquid separation in cold low separator 18, isolated gaseous stream is through pipeline 19 withdrawing devices; Isolated liquid phase stream IV is extracted out through pipeline 20 by cold low separator 18 bottoms, after heavier feeds II from pipeline 11 mixes, enters separation column 22 through pipeline 21.The naphtha fraction that fractionates out in separation column 22, diesel oil distillate and tail oil cut are extracted out through pipeline 23,24 and 25 respectively.The tail oil cut enters catalytic cracking unit 26 through pipeline 25, carries out catalytic cracking reaction, and the dry gas that catalytic cracking unit 26 is produced, liquefied gas, gasoline fraction, light cycle oil and slurry oil are extracted out through pipeline 27,28,29,30,31 respectively.Light cycle oil through pipeline 30 with enter hydro-upgrading reactor 13 after light material I from pipeline 8 mixes.
The following examples will give further instruction to method provided by the invention, but not thereby limiting the invention.
The trade names of the Hydrobon catalyst that uses among the embodiment are RN-32V, and the trade names of catalyst for hydro-upgrading are RIC-1, are China PetroChemical Corporation's Chang Ling catalyst plant production.The trade names of catalytic cracking catalyst are CR002, are China PetroChemical Corporation's Zhou village catalyst plant production.
Embodiment
Present embodiment is a stock oil with a kind of heavy distillate, and its feedstock property is as shown in table 1, and the sulphur content of this stock oil is the high-sulfur heavy distillate of poor quality up to 3.1 heavy % as shown in Table 1.According to method provided by the present invention stock oil is handled, successively through obtaining naphtha fraction, products such as gasoline fraction and diesel oil distillate behind hydrogenation unit and the catalytic cracking unit.The operational condition of hydrogenation unit is as shown in table 2, and the operational condition of catalytic cracking unit is as shown in table 3, from table 2 and table 3 as can be seen, the comparatively demulcent reaction conditions that present embodiment all adopts, wherein the reaction pressure of hydrogenation unit only is 10.0MPa.The yield of each cut is as shown in table 4, and the character of gasoline fraction, diesel oil distillate and naphtha fraction is listed in table 5, table 6 and the table 7 respectively.By table 4 as seen, the yield of gasoline fraction and diesel oil distillate is respectively 46.1 heavy % and 30.5 heavy %; By table 5 as seen, the sulphur content of gasoline fraction only is 120ppm, and olefin(e) centent only is 16ppm; By table 6 as seen, the sulphur content of diesel oil distillate is less than 10ppm, and cetane value is 51.8, and polycyclic aromatic hydrocarbon content only is 5.0 heavy %.Therefore adopt the inventive method to produce and obtain high gasoline fraction of yield and diesel oil distillate, and their character all can satisfy " European emission standard " III number specification of quality to gasoline and diesel oil.In addition, by table 7 as seen, the arene underwater content of the naphtha fraction of by-product is up to 65 heavy %, and therefore sulphur content and nitrogen content can be used as the fine catalytic reforming raw material all less than 0.5ppm.
Table 1
| Analysis project | Analytical results |
| Density (20 ℃), g/cm 3 | 0.9235 |
| Carbon residue, heavy % | 0.23 |
| Sulphur content, heavy % | 3.1 |
| Nitrogen content, heavy % | 0.09 |
| Hydrogen richness, heavy % | 11.61 |
| Group composition, heavy % | |
| Stable hydrocarbon | 56.0 |
| Aromatic hydrocarbons | 39.8 |
| Colloid+bituminous matter | 4.2 |
| Boiling range (ASTM D1160), ℃ | |
| 50％ | 446 |
| 95％ | 528 |
| Do | 560 |
Table 2
| Reaction conditions | Hydrofining reactor | The hydro-upgrading reactor |
| The hydrogen dividing potential drop, MPa | 10.0 | 9.8 |
| Temperature of reaction, ℃ | 360 | 350 |
| Volume space velocity, h -1 | 2.0 | 1.5 |
| Hydrogen to oil volume ratio, Nm 3/m 3 | 500 | 700 |
| High pressure hot separator | Cold high pressure separator | |
| Service temperature, ℃ | 360 | 55 |
Table 3
| Reaction conditions | Catalyst cracker |
| The primary first-order equation temperature, ℃ | 550 |
| The secondary reaction temperature, ℃ | 510 |
| Total reaction time, second | 4 |
| Reaction pressure, MPa | 0.15 |
| Regeneration temperature, ℃ | 695 |
| Recycle ratio | 0.15 |
Table 4
| Yield (to stock oil), heavy % | |
| Dry gas | 1.3 |
| Liquefied gas | 12.6 |
| Naphtha fraction | 2.6 |
| Gasoline fraction | 46.1 |
| Diesel oil distillate | 30.5 |
| Slurry oil | 4.9 |
| Coke | 1.5 |
Table 5
| Gasoline fraction character | |
| Density (20 ℃), g/cm 3 | 0.742 |
| Sulphur content, ppm | 120 |
| Nitrogen content, |
8 |
| Olefin(e) centent, heavy % | 16 |
| Aromaticity content, heavy % | 24 |
| RON | 90 |
| MON | 79 |
| Boiling range ASTM D-86, ℃ | |
| Initial boiling point | 42 |
| Do | 185 |
Table 6
| Diesel oil distillate character | |
| Density (20 ℃), g/cm 3 | 0.842 |
| Sulphur content, ppm | <10 |
| Aromaticity content, heavy % | 19.4 |
| Polycyclic aromatic hydrocarbon content, heavy % | 5.0 |
| Cetane value | 51.8 |
| Boiling range ASTM D-86, ℃ | |
| Initial boiling point | 195 |
| Do | 360 |
Table 7
| Naphtha fraction character | |
| Density (20 ℃), g/cm 3 | 0.738 |
| Sulphur content, ppm | <0.5 |
| Nitrogen content, ppm | <0.5 |
| Arene underwater content, heavy % | 65 |
| Boiling range ASTM D-86, ℃ | |
| Initial boiling point | 42 |
| Do | 155 |
Claims (5)
1, a kind of method of producing clean fuel by heavy distillate comprises the following steps:
(1) heavy distillate with enter hydrofining reactor after hydrogen mixes, contact with Hydrobon catalyst, carry out hydrogenation reaction; The reaction effluent of hydrofining reactor enters high pressure hot separator, is separated into light material I and heavier feeds I; Heavier feeds I enters thermal low-pressure separators, further is separated into light material II and heavier feeds II;
(2) light material I with enter the hydro-upgrading reactor after light cycle oil from catalytic cracking unit mixes, under the effect of catalyst for hydro-upgrading, react; The reaction effluent of hydro-upgrading reactor enters cold high pressure separator, and isolated hydrogen-rich gas recycles, and isolated liquid phase stream III enters the cold low separator with after light material II mixes, and further carries out gas-liquid separation;
(3) the isolated liquid phase stream IV of cold low separator with enter separation column after heavier feeds II mixes, obtain naphtha fraction, diesel oil distillate and tail oil cut;
(4) the tail oil cut enters catalytic cracking unit, carries out catalytic cracking reaction and obtains dry gas, liquefied gas, gasoline fraction, light cycle oil and slurry oil, and wherein light cycle oil returns and enters the hydro-upgrading reactor.
2, in accordance with the method for claim 1, it is characterized in that described heavy distillate is the mixing oil of any or several and optional vacuum residuum in vacuum gas oil, atmospheric gas oil, coker gas oil, catalysis heavy cycle oil and the deasphalted oil.
3, in accordance with the method for claim 1, the reaction conditions that it is characterized in that described hydrofining reactor and hydro-upgrading reactor is: hydrogen dividing potential drop 4.0MPa～15.0MPa, 280～400 ℃ of temperature of reaction, volume space velocity 0.1～20h
-1, hydrogen to oil volume ratio 300～2000Nm
3/ m
3
4, in accordance with the method for claim 1, the service temperature that it is characterized in that described high pressure hot separator is: 200～370 ℃; The service temperature of cold high pressure separator is 25～60 ℃.
5, in accordance with the method for claim 1, it is characterized in that a reactor that comprises two reaction zones is arranged in the described catalytic cracking unit, the tail oil cut enters behind the reactor in the presence of water vapor to contact with the catalytic cracking catalyst of heat and carries out primary first-order equation and secondary reaction, reaction conditions is: the temperature of first reaction zone is 540～580 ℃, and the temperature of second reaction zone is that 495～510 ℃, total residence time are 3～10 seconds.
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|---|---|---|---|
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Families Citing this family (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101434865B (en) * | 2007-11-15 | 2012-12-26 | 中国石油化工股份有限公司 | Heavy distillate hydrogenation and catalytic cracking combined method |
| KR101589565B1 (en) * | 2007-12-20 | 2016-01-28 | 차이나 페트로리움 앤드 케미컬 코포레이션 | An improved combined process of hydrotreating and catalytic cracking of hydrocarbon oils |
| GB0812699D0 (en) * | 2008-07-11 | 2008-08-20 | Johnson Matthey Plc | Apparatus and process for treating offshore natural gas |
| CN103773472B (en) * | 2012-10-24 | 2015-08-12 | 中国石油化工股份有限公司 | A kind of method improving hydrotreater oil-water separation |
| CN103789022B (en) * | 2012-11-03 | 2015-07-22 | 中国石油化工股份有限公司 | Hydrogenation process |
| CN105316039A (en) * | 2014-07-07 | 2016-02-10 | 中石化洛阳工程有限公司 | Hydrogenation technology |
| CN105713662B (en) * | 2016-01-27 | 2017-12-19 | 北京宝聚能源科技有限公司 | A kind of group technology of hydrotreating and catalytic cracking |
| CN107619680B (en) * | 2017-10-17 | 2023-08-08 | 正和集团股份有限公司 | System and process for naphtha direct-supply reforming device of diesel hydrogenation device |
| CN109988615B (en) * | 2017-12-29 | 2021-07-09 | 中国石油化工股份有限公司 | Flexible wax oil hydrotreating process |
| CN109988646B (en) * | 2017-12-29 | 2022-07-12 | 中国石油化工股份有限公司 | Wax oil hydrotreating and hydrofining combined process |
| CN109988602A (en) * | 2017-12-29 | 2019-07-09 | 中国石油化工股份有限公司 | A kind of flexible wax oil hydrogenation treatment process |
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