CN1459489A - Method for treating heavy oil suspension bed hydrogenation tail oil by solvent extraction technology - Google Patents
Method for treating heavy oil suspension bed hydrogenation tail oil by solvent extraction technology Download PDFInfo
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- CN1459489A CN1459489A CN 02117834 CN02117834A CN1459489A CN 1459489 A CN1459489 A CN 1459489A CN 02117834 CN02117834 CN 02117834 CN 02117834 A CN02117834 A CN 02117834A CN 1459489 A CN1459489 A CN 1459489A
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- 239000003921 oil Substances 0.000 title claims abstract description 78
- 238000005516 engineering process Methods 0.000 title claims abstract description 43
- 238000000034 method Methods 0.000 title claims abstract description 41
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 31
- 239000000295 fuel oil Substances 0.000 title claims abstract description 29
- 238000000638 solvent extraction Methods 0.000 title claims abstract description 15
- 239000000725 suspension Substances 0.000 title abstract description 6
- 229910052751 metal Inorganic materials 0.000 claims abstract description 22
- 239000002184 metal Substances 0.000 claims abstract description 22
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 16
- 238000004517 catalytic hydrocracking Methods 0.000 claims abstract description 15
- 239000002904 solvent Substances 0.000 claims description 53
- 238000007667 floating Methods 0.000 claims description 30
- 239000007791 liquid phase Substances 0.000 claims description 23
- 239000012071 phase Substances 0.000 claims description 23
- 239000007789 gas Substances 0.000 claims description 18
- 238000000605 extraction Methods 0.000 claims description 16
- 239000010426 asphalt Substances 0.000 claims description 12
- 238000011084 recovery Methods 0.000 claims description 10
- 239000002994 raw material Substances 0.000 claims description 7
- 238000002156 mixing Methods 0.000 claims description 5
- 238000007670 refining Methods 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 5
- 230000008878 coupling Effects 0.000 claims description 4
- 238000010168 coupling process Methods 0.000 claims description 4
- 238000005859 coupling reaction Methods 0.000 claims description 4
- 239000012530 fluid Substances 0.000 claims description 4
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 230000006837 decompression Effects 0.000 claims description 3
- 239000007792 gaseous phase Substances 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 239000012046 mixed solvent Substances 0.000 claims description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 238000005194 fractionation Methods 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 239000005864 Sulphur Substances 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 239000000084 colloidal system Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052759 nickel Inorganic materials 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- WURBVZBTWMNKQT-UHFFFAOYSA-N 1-(4-chlorophenoxy)-3,3-dimethyl-1-(1,2,4-triazol-1-yl)butan-2-one Chemical compound C1=NC=NN1C(C(=O)C(C)(C)C)OC1=CC=C(Cl)C=C1 WURBVZBTWMNKQT-UHFFFAOYSA-N 0.000 description 2
- 238000013459 approach Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 239000002689 soil Substances 0.000 description 2
- 239000004449 solid propellant Substances 0.000 description 2
- 229910052720 vanadium Inorganic materials 0.000 description 2
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 description 1
- 241000772415 Neovison vison Species 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- BQFCCCIRTOLPEF-UHFFFAOYSA-N chembl1976978 Chemical compound CC1=CC=CC=C1N=NC1=C(O)C=CC2=CC=CC=C12 BQFCCCIRTOLPEF-UHFFFAOYSA-N 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 238000004231 fluid catalytic cracking Methods 0.000 description 1
- 239000003205 fragrance Substances 0.000 description 1
- 239000002010 green coke Substances 0.000 description 1
- PNXOJQQRXBVKEX-UHFFFAOYSA-N iron vanadium Chemical compound [V].[Fe] PNXOJQQRXBVKEX-UHFFFAOYSA-N 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000011020 pilot scale process Methods 0.000 description 1
- 230000001698 pyrogenic effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A method for treating the hydrogenated tail oil of heavy oil suspended bed by solvent extraction technique features that the heavy oil suspended bed is used as the hydrogenating part of heavy oil suspended bed, so improving the heavy oil lightening process. The method is mainly characterized in that the tail oil generated in the hydrogenation process of the heavy oil suspension bed is treated by adopting a solvent extraction technology to remove metal and carbon residue in the tail oil, so that a new way is developed for the comprehensive utilization of the hydrocracking tail oil of the heavy oil suspension bed.
Description
The present invention relates to a kind of method with solvent extraction technical finesse heavy oil floating bed hydrogenation tail oil, it is the integral part of heavy oil floating bed hydrogenation technology, thereby belongs to the improvement of the heavy oil hydroprocessing process process in the refining of petroleum technology.It mainly is by adopting the solvent extraction technology that the tail oil that produces in the heavy oil suspension bed hydrogenation process process is handled, remove metal and carbon residue in the tail oil, thereby opens up a new way for the comprehensive utilization of heavy oil floating bed hydrocracking tail oil.
Along with the minimizing day by day of light crude produced quantity, the increase day by day of mink cell focus produced quantities such as viscous crude adds that people increase day by day for the needs of clean fuel, and heavy-oil hydrogenation Study on Technology and development have become refining of petroleum field most important.The heavy-oil hydrogenation technology of large-scale industrial application mainly is fixed bed hydrogenation sulfur removal technology (VRDS technology) and boiling bed hydrogenation technique at present, the heavy oil that the former can only processing metal content and nitrogen content is lower, sulphur content is higher, and the latter unloads and make-up catalyst owing to will quantitatively arranging every day, thereby its running cost is than higher.The work of heavy oil floating bed hydrogenation Study on Process is more active, present stage, existing ten kinds of processes were in pilot scale and industrial demonstration unit stage, VCC (VEBA-Combi-Cracking) technology as Germany, the Micro-Cat technology of U.S. Exxon company, the HDH technology of Nei Ruina INTEVEP company of committee, Canadian CANMET technology, the SOC technology of Japan Asahi Chemical Industry Co., Ltd, Japan goes out the MRH technology of wide product company and U.S. Kai Luoge company, the Aurabon technology of American UOP company, Canadian (HC)
3Technology etc., the UPC-RSHC technology of PetroChina Company Ltd., though these technology distillate yields are all higher, the technology distillate that has (＜524 ℃ cuts) yield is up to more than 90%, but these technologies are large-scale industrial application not all, and major reason wherein is exactly that this technological process will generate a certain amount of coke.For heavy oil floating bed hydrogenation technology, because the distillate yield is up to 80～95%, the technological process green coke is inevitable, and the burnt particle that generates all is concentrated in the tail oil together with the metal catalyst and the metal component in the stock oil that add, cause tail oil character relatively poor, the content of toluene insolubles and ash content is higher, and the application of tail oil is difficulty relatively.The purpose of solvent extraction diasphaltene technology is to remove vacuum residuum bituminous matter and part colloid, this technology was in order to produce the raw material of thick oil in the past, provide carbon residue and the lower raw material of heavy metal content for catalytic cracking or hydrocracking more and more in recent years, therefore solvent deasphalting technology is an important decarburization upgrading process, because heavy metal such as nickel in the residual oil, vanadium etc. are present in the heaviest colloid and bituminous matter, therefore in solvent deasphalting process, also removed the nickel in the residual oil simultaneously, metal components such as vanadium iron claim also that sometimes solvent deasphalting process is a solvent demetallization.Metal in the deasphalted oil, carbon residue are reduced to very low, thereby can be used as oil fuel, heavy oil fluid catalytic cracking or hydrocracking blending raw material or as the pitch blending stock etc., and the de-oiled asphalt component generally can only be as solid fuel owing to contain higher metal and carbon residue.
The purpose of this utility model combines original solvent deasphalting technology and heavy oil floating bed hydrogenation technology (being called for short UPC-RSHC technology) exactly and has proposed a kind of method of utilizing solvent extraction technical finesse heavy oil floating bed hydrogenation tail oil.Thereby it has mainly constituted complete suspension bed hydrogenation process (UPC-RSHC technology) having carried out some improvement aspect solvent that is adopted and the extraction process.It is mainly by at online solvent tower and the solvent recovery tower of having used of the product separate part of heavy oil floating bed hydrogenation technology, in solvent tower, used low molecular varsol, thereby carbon residue and metal content in the UPC-RSHC technological process tail oil are reduced greatly, for hydrogenation tail oil utilize again and the recovery of metal catalyst provides new approach.Treatment process proposed by the invention is to be exclusively used in to handle heavy crude and viscous crude residual oil or special thick, high viscous crude, comprises the tail oil of the heavy oil floating bed hydrocracking technology of the viscous crude residual oil (for example Liaohe River viscous crude, xinjiang viscous crude oil and isolated island viscous crude etc.) that contains low-sulfur, high-sulfur, high metal (nickel, calcium, vanadium etc.), high carbon residue, high viscosity, high nitrogen and special thick, high viscous crude (for example Liaohe River, Xinjiang spy's viscous crude etc.) and various sulphur content.It mainly is the tail oil that adopts in the technical finesse heavy oil floating bed hydrocracking technology of solvent extraction, and make tail oil remove metal and part carbon residue, the solvent that its technical essential adopted is the low molecular varsol of C4～C10 or their mixed solvent or light naphthar, extraction temperature is 80～250 ℃, the mass ratio of solvent and tail oil is 2～6: 1, and working pressure is 0.1～2.0Mpa.
This method mainly is solvent tower of coupling in the tail oil separation system of above-mentioned technology, and concrete technical process is to realize by following scheme:
(1) stock oil enters the floating bed hydrocracking reactor, the gaseous phase materials that comes out from the floating bed hydrogenation reactor head enters high pressure hot separator and further is separated into gas phase and liquid phase, after merging, the liquid phase stream that comes out from the floating bed hydrocracking reactor bottom and the liquid phase stream of high pressure hot separator enter thermal low-pressure separators, under low pressure be separated into gas phase and liquid phase again, gas phase enters the low pressure oil aspiration and receives treatment system, and liquid phase enters atmospheric flash tower and flashes off gas phase and liquid phase;
(2) go online refining reaction device and refined products separation system after the gas phase merging that the gas phase of atmospheric flash tower and high pressure hot separator come out, the liquid phase separated into two parts that atmospheric flash tower comes out, mixing reenters light liquid that suspension bed (3) comes out from the extraction tower top mutually to a part behind oily process furnace as circulation tail oil and fresh feed, be deasphalted oil solution, enter solvent recovery tower, solvent comes out to recycle from the top, and the deasphalted oil of coming out at the bottom of the tower enters vacuum still and further is separated into wax slop and decompression tail oil carrying device respectively;
(4) the heavy-fluid phase of coming out from extraction tower bottom, promptly de-oiled asphalt solution enters another solvent recovery tower, and the solvent recirculation of coming out from the top is used, and the de-oiled asphalt carrying device that comes out at the bottom of the tower is as the raw material that reclaims catalyzer.
Accompanying drawing is process flow sheet of the present invention:
The drawing of accompanying drawing is described as follows:
Low divide (K-3) of the hot high score of 1--floating bed hydrogenation reactor (K-1) 2--(K-2) 3---heat
4--atmospheric flash tower (K-4) 5--solvent tower (k-5)
6--deasphalted oil solvent recovery tower (K-6) 7--de-oiled asphalt solvent recovery tower (K-7)
8---vacuum fractionation tower (K-8)
Below in conjunction with accompanying drawing and specific embodiment in detail technical characterstic of the present invention and effect are described in detail:
In the process that reality is implemented, planner of the present invention is designed to solvent tower online among the UCP-RSHC technical process, and its logistics derives from the normal pressure of product separate part or the tail oil at the bottom of the vacuum fractionation tower.The operational condition of agent extraction tower is: extraction temperature is 80～250 ℃, the solvent that is adopted is the low molecular varsol of C4～C10 or their mixed solvent or light naphthar, solvent ratio is 2～6: 1 (mass ratio of solvent and tail oil), and working pressure is 0.1～2.0Mpa.The concrete technical process of implementing is: solvent tower of coupling behind the normal pressure of floating bed hydrocracking process unit or vacuum fractionation tower, and extraction tower is divided into two sections, and hypomere is the extracting section, and epimere is a settling section; The hydrogenation tail oil that comes out at the bottom of normal pressure or the vacuum fractionation tower enters from the extraction tower middle part, a certain proportion of circulating solvent enters from the bottom from extraction tower, the two is reverse contact in extraction tower, and under stirring, rotating disk carries out extracting, the heavy-fluid that heavy colloid in the tail oil and bituminous matter and partial solvent form (raffinate or de-oiled asphalt phase) is mutually extracted out to sedimentation at the bottom of the tower and at the bottom of tower, obtains de-oiled asphalt after reclaiming solvent; The light liquid that deasphalted oil and solvent form (extracting solution or diasphaltene oil phase) mutually enters settling section through riser pipe, ejects the extracting solution that comes from extraction tower and enters and obtain deasphalted oil after an atmospheric flash tower steams solvent, and the solvent cycle that steams is used.Deasphalted oil is owing to only contain lower metal and carbon residue, thereby can be used as mediation pitch and pyrogenic raw material, if sulphur content is not high, oil then can also act as a fuel, de-oiled asphalt can be mixed in the coal dust as solid fuel owing to contain higher metal and carbon residue.Like this, during the device operation, the circulating hydrogen that derives from the stock oil and the fresh hydrogen of stock oil process furnace and derive from the hydrogen process furnace enters floating bed hydrogenation reactor K-1, the gaseous phase materials that comes out from the K-1 top enters high pressure hot separator K-2 and further is separated into gas phase and liquid phase, enter light pressure separator K-3 after the liquid phase stream that comes out from K-1 bottom and the liquid phase stream merging of K-2, under low pressure be separated into gas phase and liquid phase again, gas phase enters the low pressure oil aspiration and receives treatment system, liquid phase enters atmospheric flash tower K-4 and flashes off gas phase and liquid phase, the gas phase that the gas phase of K-4 and K-2 come out merges online refining reaction device in back and refined products separation system, the liquid phase separated into two parts that K-4 comes out, the a part of mixing with fresh feed as the circulation tail oil reenters floating bed hydrogenation reactor K-1 behind oily process furnace, remainder and the extracting in extraction tower K-5 of a certain proportion of solvent, the light liquid phase of coming out from the K-5 top (deasphalted oil solution) enters solvent recovery tower K-6, solvent comes out to recycle from the K-6 top, and the deasphalted oil of coming out from the K-6 bottom enters vacuum still K-8 and further is separated into wax slop and decompression tail oil difference carrying device; The heavy-fluid phase (de-oiled asphalt solution) of coming out from K-5 bottom enters another solvent recovery tower K-7, and the solvent recirculation of coming out from the K-7 top is used, and the de-oiled asphalt carrying device that comes out from the K-7 bottom is as the raw material that reclaims catalyzer.
Embodiment adopts the solvent extraction technology to handle its result such as table 1 to the tail oil in the normal slag floating bed hydrocracking technology of Kelamayi, Xinjiang.
Although what the present invention adopted is that the solvent extraction technology removes metal and the carbon residue in the hydrogenation of residual oil suspended bed tail oil, compares with existing solvent de-asphalting process, have its outstanding characteristics in:
(1) generally the solvent molecule amount more used than conventional solvent de-asphalting process is big for the solvent that adopts of technology.
(2) another characteristics of this technology are need to not operate under higher pressure, and operating pressure is similar to normal pressure.
(3) because the molecular weight of solvent for use is bigger, thereby the yield of deasphalted oil is higher, generally about 90%, deasphalted oil Tenor is lower, and the removal efficiency of metal is generally more than 98%, and the bitum removal efficiency of normal heptane is also higher, the carbon residue ratio Difficulty removes, and its removal efficiency generally only has about 30%. Compared with prior art, the utlity model has following advantage:
(1) this technology mainly is in order to remove metal and the part carbon residue in the hydrogenation of residual oil suspended bed tail oil, thereby in the metal removal oil Tenor is very low, and total metal contents in soil is not higher than 50PPm, for can obtaining the floating bed hydrogenation tail oil of comparison high-quality, for The commercial Application of heavy oil floating bed hydrocracking technology (UPC-RSHC) provides strong assurance.
(2) working pressure approaches normal pressure, and technical process is simple, can be coupling in the hydrogenation of residual oil suspended bed process unit, and the Installed capital cost of device is low.
Depitching oil properties and composition after the normal slag floating bed hydrogenation tail oil in table 1 Kelamayi is processed with solvent
| Solvent | Tail oil | Solvent orange 2 A | Solvent B | Solvent C | Solvent D |
| Yield, m% | ---- | 97.0 | 92.0 | 86.4 | 88.2 |
| Carbon residue, m% carbon residue removal efficiency, % | 9.18 | 9.53 ---- | 5.85 36.3 | 5.77 37.1 | 6.33 31.0 |
| Total metal contents in soil, the total metal removal rate of PPm Fe Ni Ca, % | 4288 2640 972 676 | 56.8 11.7 9.9 35.2 98.7 | 36.3 17.0 7.3 12.0 99.2 | 26.6 14.7 2.3 9.6 99.4 | 29.8 10.9 3.6 15.3 99.3 |
| Four components form, and the saturated branch fragrance of m% divides gum asphalt | 55.78 20.19 15.61 5.32 | 57.56 20.84 16.11 5.49 | 58.21 22.60 18.44 0.75 | 58.56 22.38 17.20 1.86 | 56.17 22.87 18.38 2.58 |
Claims (2)
1. use the method for solvent extraction technical finesse heavy oil floating bed hydrogenation tail oil, it mainly is the tail oil that adopts in the technical finesse heavy oil floating bed hydrocracking technology of solvent extraction, and make tail oil remove metal and part carbon residue, it is characterized in that the solvent that is adopted is the low molecular varsol of C4～C10 or their mixed solvent or light naphthar, extraction temperature is 80～250 ℃, the mass ratio of solvent and tail oil is 2～6: 1, and working pressure is 0.1～2.0Mpa.
2. the method with solvent extraction technical finesse heavy oil floating bed hydrogenation tail oil according to claim 1, the method that it is characterized in that the tail oil in the described employing solvent extraction technical finesse floating bed hydrocracking technology mainly is solvent tower of coupling in the tail oil separation system of above-mentioned technology, and concrete technical process is to realize by following scheme:
(1) stock oil enters the floating bed hydrocracking reactor, the gaseous phase materials that comes out from the floating bed hydrogenation reactor head enters high pressure hot separator and further is separated into gas phase and liquid phase, after merging, the liquid phase stream that comes out from the floating bed hydrocracking reactor bottom and the liquid phase stream of high pressure hot separator enter thermal low-pressure separators, under low pressure be separated into gas phase and liquid phase again, gas phase enters the low pressure oil aspiration and receives treatment system, and liquid phase enters atmospheric flash tower and flashes off gas phase and liquid phase;
(2) go online refining reaction device and refined products separation system after the gas phase merging that the gas phase of atmospheric flash tower and high pressure hot separator come out, the liquid phase separated into two parts that atmospheric flash tower comes out, the a part of mixing with fresh feed as the circulation tail oil reenters the floating bed hydrogenation reactor, remainder and the extracting in extraction tower of a certain proportion of solvent behind oily process furnace;
(3) the light liquid phase of coming out from the extraction tower top, promptly deasphalted oil solution enters solvent recovery tower, and solvent comes out to recycle from the top, and the deasphalted oil of coming out at the bottom of the tower enters vacuum still and further is separated into wax slop and decompression tail oil carrying device respectively;
(4) the heavy-fluid phase of coming out from extraction tower bottom, promptly de-oiled asphalt solution enters another solvent recovery tower, and the solvent recirculation of coming out from the top is used, and the de-oiled asphalt carrying device that comes out at the bottom of the tower is as the raw material that reclaims catalyzer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02117834 CN1209446C (en) | 2002-05-23 | 2002-05-23 | Method for treating heavy oil suspension bed hydrogenation tail oil by solvent extraction technology |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02117834 CN1209446C (en) | 2002-05-23 | 2002-05-23 | Method for treating heavy oil suspension bed hydrogenation tail oil by solvent extraction technology |
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| Publication Number | Publication Date |
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| CN1459489A true CN1459489A (en) | 2003-12-03 |
| CN1209446C CN1209446C (en) | 2005-07-06 |
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| CN 02117834 Expired - Fee Related CN1209446C (en) | 2002-05-23 | 2002-05-23 | Method for treating heavy oil suspension bed hydrogenation tail oil by solvent extraction technology |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102260527A (en) * | 2011-06-29 | 2011-11-30 | 中国石油大学(华东) | New catalytic hydroprocessing thermal cracking-hydrotreating process of high-sulfur high-acid inferior heavy oil |
| CN102309949A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Suspension bed hydrogenation reactor with high pressure separator and process |
| CN103540358A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Residual oil conversion-aromatic hydrocarbon extraction combined process |
| CN109609185A (en) * | 2018-12-23 | 2019-04-12 | 洛阳瑞华新能源技术发展有限公司 | Content of wax oil plant adds hydrogen, adds the combined method of hydrogen, catalyst circulation containing oil of dreg |
| CN114149825A (en) * | 2021-12-20 | 2022-03-08 | 陕西精益化工有限公司 | Process for processing and utilizing hydrogenated tail oil of coal tar |
-
2002
- 2002-05-23 CN CN 02117834 patent/CN1209446C/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102309949A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Suspension bed hydrogenation reactor with high pressure separator and process |
| CN102309949B (en) * | 2010-07-07 | 2013-07-24 | 中国石油化工股份有限公司 | Suspension bed hydrogenation reactor with high pressure separator and process |
| CN102260527A (en) * | 2011-06-29 | 2011-11-30 | 中国石油大学(华东) | New catalytic hydroprocessing thermal cracking-hydrotreating process of high-sulfur high-acid inferior heavy oil |
| CN102260527B (en) * | 2011-06-29 | 2014-05-28 | 中国石油大学(华东) | New catalytic hydroprocessing thermal cracking-hydrotreating process of high-sulfur high-acid inferior heavy oil |
| CN103540358A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Residual oil conversion-aromatic hydrocarbon extraction combined process |
| CN103540358B (en) * | 2012-07-12 | 2016-05-11 | 中国石油天然气股份有限公司 | Residual oil conversion-aromatic hydrocarbon extraction combined process |
| CN109609185A (en) * | 2018-12-23 | 2019-04-12 | 洛阳瑞华新能源技术发展有限公司 | Content of wax oil plant adds hydrogen, adds the combined method of hydrogen, catalyst circulation containing oil of dreg |
| CN114149825A (en) * | 2021-12-20 | 2022-03-08 | 陕西精益化工有限公司 | Process for processing and utilizing hydrogenated tail oil of coal tar |
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| Publication number | Publication date |
|---|---|
| CN1209446C (en) | 2005-07-06 |
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