CN108203598A - A kind of technique of F- T synthesis light hydrocarbon hydrofinishing - Google Patents
A kind of technique of F- T synthesis light hydrocarbon hydrofinishing Download PDFInfo
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- CN108203598A CN108203598A CN201711348603.0A CN201711348603A CN108203598A CN 108203598 A CN108203598 A CN 108203598A CN 201711348603 A CN201711348603 A CN 201711348603A CN 108203598 A CN108203598 A CN 108203598A
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- hydrofinishing
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
- C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
- C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
- C10G45/08—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
- C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
- C10G45/12—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A kind of technique of F- T synthesis light hydrocarbon hydrofinishing is that light hydrocarbon from F- T synthesis separative element is mixed into hydrofinishing heating stove heat with circulating hydrogen hydrogenation reaction is carried out under catalyst action, reaction product enters separating at high temperature tank, gas phase out enters cryogenic separation tank after cooling from separating at high temperature tank top, hydrogen comes out from cryogenic separation tank top, and supplement fresh hydrogen, it is mixed after circulating hydrogen compressor boosts with light hydrocarbon, the high score oil come out from separating at high temperature pot bottom, it is flashed after mixing and depressurize with the low point of oil come out from cryogenic separation pot bottom, flash drum overhead discharges low molecular hydrocarbon, it is used as fuel gas, from bottom, discharge is hydrogenation products.The present invention has the advantages that efficient, flow is simple.
Description
Technical field
The present invention relates to a kind of techniques of F- T synthesis light hydrocarbon hydrofinishing.
Background technology
Oil from Fischer-Tropsch synthesis is mainly made of linear paraffin, alkene and oxygenatedchemicals, is environmental-friendly fuel oil
And chemicals.But wherein most is unsaturated hydrocarbons, there is oxygenates, to being processed further and using making for product
Into inconvenience, so suitable technique must be taken to carry out hydrofinishing to miscella, make alkene saturation, while remove in feedstock oil
Sulphur, nitrogen, oxygen compound, to improve the stability of oil product, color, smell, combustibility etc..
Oil hydrogenation technique at present has had multiple disclosed patents and technology.Such as United States Patent (USP) U.S.4,637,870
The suspension bed oil expression hydro-conversion technology of a kind of industrial phosphomolybdic acid catalyst the most announced, U.S.5,316,996gongbu
A kind of catalyst of load metal oxide as oil expression hydro-conversion, the residual oil of the high conversion of German VEBA companies exploitation
The technologies such as hot hydrogenolysis combination cracking process (VEBA-Combi-Cracking).
In the case of conventional petroleum worsening shortages, ICL for Indirect Coal Liquefaction F-T synthetic oils have caused domestic and international dependent part
The attention of door.Due to ICL for Indirect Coal Liquefaction F-T synthetic oils and traditional oil is in composition and there are larger differences in nature
It is different, therefore the processing and refining of synthetic oil and the hydrogenation process of natural oil are also very different.Chinese patent
CN1164360C, CN1597859A, CN1554728A make with regard to the preparation and application of fischer-tropsch synthesized oil product hydrogen reforming catalyst
Report, Chinese patent CN1594507A, CN1594508A, CN1594509A are directed to F- T synthesis heavy oil product hydrocracking process
It reports.Chinese patent CN200610012808.7 reports a kind of technique of hydrogenating and refining oil from Fischer-Tropsch synthesis.The invention
Using the fixed bed reactors of two series connection, pre-add hydrogen is carried out, then carry out hydrofinishing, pre-add hydrogen is catalyzed using unvulcanised state
Agent, hydrofinishing use unvulcanised state and sulphided state catalyst.
Existing oil hydrogenation technological process is complicated, equipped with oil product pre-add hydrogen and adds two reactors of hydrogen, equipment manufacturing cost is higher；
Using pre-add hydrogen and add two kinds of catalyst of hydrogen, implementation process is complicated.
Invention content
The object of the present invention is to provide a kind of efficient, the simple F- T synthesis light hydrocarbon hydrofinishing of flow techniques.
The present invention is using a hydrofining reactor, using a kind of molecular sieve catalyst.Lightweight from F- T synthesis
By catalyst hydrogenation after the heating of hydrocarbon product, unsaturated hydrocarbons is converted into saturated hydrocarbons, finished product oil index meets existing oil after separation
Requirement of the product standard for the elements such as the unsaturated compounds such as aromatic hydrocarbons, system, alcohol and oxygen, sulphur, nitrogen, metal.Product oil can pass through
Distillation is cut into gasoline fraction and diesel oil distillate.
A kind of technique of F- T synthesis light hydrocarbon hydrofinishing of the present invention, includes the following steps：
Light hydrocarbon from F- T synthesis separative element enters feed surge tank, after feed pump boosts, with circulating hydrogen
It mixes, after the heat exchange of input and output material heat exchanger, stove heat is heated into hydrofinishing, enters adding equipped with catalyst from top later
Hydrogen finishing reactor carries out hydrogenation reaction under catalyst action, and reaction product comes out from hydrofining reactor bottom, into
Enter separating at high temperature tank after exchanging heat in effluent exchanger, gas phase comes out from separating at high temperature tank top, and reacted product cooler is cold
But after, into cryogenic separation tank, hydrogen comes out from cryogenic separation tank top, and supplements fresh hydrogen, boosts through circulating hydrogen compressor
It is mixed afterwards with light hydrocarbon, the high score oil come out from separating at high temperature pot bottom, the low point of oil with being come out from cryogenic separation pot bottom mixes
After merging decompression, send to flash tank, flash drum overhead discharge low molecular hydrocarbon is used as fuel gas, from bottom discharge to add
Hydrogen product.
Hydrogenation products prepared by the present invention are detached again, obtain final products.
F- T synthesis light hydrocarbon adds the reaction condition of hydrogen：Reaction temperature is 150-270 DEG C, pressure 2.0-5.0MPa, gently
Matter hydrocarbon mass space velocity is 0.5-10h-1, hydrogen to oil volume ratio 400-1000.Product oil can be cut into gasoline by distillation after separation
Fraction and diesel oil distillate.
Light hydrocarbon as described above from F- T synthesis separative element is the C5-C19 that F- T synthesis is fractionated into processing
Linear paraffin, the mixture containing a small amount of alkene and alcohol.
The temperature of separating at high temperature tank as described above is 75 DEG C -110 DEG C.
The temperature of cryogenic separation tank as described above is 45 DEG C.
Flash conditions in flash distillation as described above are 75 DEG C -110 DEG C of temperature, pressure 0.45MPa.
A kind of catalyst for fischer-tropsch synthesized oil product hydrogen saturation, it is characterised in that by nickel oxide, tungsten oxide, oxidation
Molybdenum, titanium oxide and aluminium oxide composition, weight percent are：Nickel oxide 5.0~18.0%, tungsten oxide 1.0~11.0%, oxidation
Molybdenum 0.1~8.0%, titanium oxide 1.5~19.0%, aluminium oxide 44.0~92.4%.Specific preparation method is with reference to patent
200310109729.4。
It is of the invention compared with existing, have the following advantages that：
(1) present invention carries out hydrofining technology using a fixed bed reactors, simple for process.
(2) hydrofinishing in the present invention is cheap using production domesticization molecular sieve catalyst.
(3) product oil that the present invention obtains can obtain gasoline fraction and diesel oil distillate by distillation cutting.
Description of the drawings
Fig. 1 is the process flow chart of the present invention.
Specific embodiment
Embodiment 1 --- 180 DEG C of light oil hydrogenation reactions
Hydrobon catalyst is made of nickel oxide, tungsten oxide, molybdenum oxide, titanium oxide and aluminium oxide, weight percent
It forms and is：NiO：WO3：MoO3：TiO2：Al2O3=17.5:4.9:2.1:10.5:65.0, preparation method is with reference to patent
200310109729.4 embodiment 1.
Hydrogenation conditions：Reaction temperature is 180 DEG C, pressure 3.2MPa, mass space velocity 1.0h-1, hydrogen to oil volume ratio
It is 500.Other conditions are described below.
Light hydrocarbon (40 DEG C, 0.2MPa) from F- T synthesis separative element into hydrofinishing feed surge tank (40 DEG C,
0.2MPa), after feed pump boosts (40 DEG C, 3.3MPa), it after being mixed with circulating hydrogen (65 DEG C, 3.2MPa), is changed through input and output material
After the heat exchange of hot device (155 DEG C, 3.25MPa), into hydrofinishing heating furnace, be heated to reaction required temperature (180 DEG C,
3.2MPa), hydrofining reactor is entered at the top of autoreactor and carries out hydrogenation reaction.Reaction product (185 DEG C, 3.0MPa) is from anti-
Device bottom is answered to come out, enters separating at high temperature tank (85 DEG C, 2.9MPa) after input and output material heat exchanger and raw material heat exchange.Gas phase is from high temperature
It comes out at the top of knockout drum, after reacted product cooler cooling, into cryogenic separation tank (45 DEG C, 2.8MPa), recycle hydrogen is from low
It comes out at the top of warm knockout drum, after supplementing fresh hydrogen, is followed after being mixed after circulating hydrogen compressor boosts (65 DEG C, 3.3MPa) with raw material
Ring uses.Hydrofinishing separating at high temperature pot bottom is high score oil, after low with cryogenic separation pot bottom point of oil is mixed and depressurized, is sent
To flash tank.Discharge low molecular hydrocarbon is sent to torch at the top of flash tank (85 DEG C, 0.45MPa), bottom for hydrogenated products send to point
From unit.
Light hydrocarbon adds hydrogen feed composition table
| Serial number | Component | It forms (w%) |
| 1 | C1-C4 | 0 |
| 2 | C5-C9 | 28.84 |
| 3 | C10-C14 | 32.79 |
| 4 | C15-C19 | 36.38 |
| 5 | Alkene | 2.21 |
| 6 | Alcohol | 0.17 |
Light hydrocarbon hydrogenated products composition -1
| Serial number | Component | It forms (w%) |
| 1 | C1-C4 | 0 |
| 2 | C5-C9 | 29.80 |
| 34 | C10-C14 | 33.37 |
| 5 | C15-C19 | 36.83 |
| 6 | Alkene | 0 |
| 7 | Alcohol | 0 |
Embodiment 2 --- 210 DEG C of oily hydrogenation reactions
Hydrobon catalyst is made of nickel oxide, tungsten oxide, molybdenum oxide, titanium oxide and aluminium oxide, weight percent
It forms and is：NiO：WO3：MoO3：TiO2：Al2O3=12.0:4.0:8.0:16.0：60.0, preparation method is with reference to patent
200310109729.4 embodiment 2.
Hydrogenation conditions：Reaction temperature is 210 DEG C, pressure 4.0MPa, mass space velocity 2.0h-1, hydrogen to oil volume ratio
It is 700.Raw material is formed with embodiment 1.Other conditions are described below.
Light hydrocarbon (40 DEG C, 0.2MPa) from F- T synthesis separative element into hydrofinishing feed surge tank (40 DEG C,
0.2MPa), after feed pump boosts (40 DEG C, 4.3MPa), it after being mixed with circulating hydrogen (65 DEG C, 4.2MPa), is changed through input and output material
After the heat exchange of hot device (180 DEG C, 4.25MPa), into hydrofinishing heating furnace, be heated to reaction required temperature (210 DEG C,
4.2MPa), hydrofining reactor is entered at the top of autoreactor and carries out hydrogenation reaction.Reaction product (215 DEG C, 4.0MPa) is from anti-
Device bottom is answered to come out, enters separating at high temperature tank (95 DEG C, 3.9MPa) after input and output material heat exchanger and raw material heat exchange.Gas phase is from high temperature
It comes out at the top of knockout drum, after reacted product cooler cooling, into cryogenic separation tank (45 DEG C, 3.8MPa), recycle hydrogen is from low
It comes out at the top of warm knockout drum, after supplementing fresh hydrogen, is followed after being mixed after circulating hydrogen compressor boosts (65 DEG C, 4.3MPa) with raw material
Ring uses.Hydrofinishing separating at high temperature pot bottom is high score oil, after low with cryogenic separation pot bottom point of oil is mixed and depressurized, is sent
To flash tank.Discharge low molecular hydrocarbon is sent to torch at the top of flash tank (95 DEG C, 0.45MPa), bottom for hydrogenated products send to point
From unit.
Light hydrocarbon hydrogenated products composition -2
| Serial number | Component | It forms (w%) |
| 1 | C1-C4 | 0.12 |
| 2 | C5-C9 | 29.87 |
| 34 | C10-C14 | 33.57 |
| 5 | C15-C19 | 36.44 |
| 6 | Alkene | 0 |
| 7 | Alcohol | 0 |
Embodiment 3 --- 250 DEG C of oily hydrogenation reactions
Hydrobon catalyst is made of nickel oxide, tungsten oxide, molybdenum oxide, titanium oxide and aluminium oxide, weight percent
It forms and is：NiO：WO3：MoO3：TiO2：Al2O3=5.0:6.0:6.5:7.5：70.0, preparation method is with reference to patent
200310109729.4 embodiment 5.
Hydrogenation conditions：Reaction temperature is 250 DEG C, pressure 5.0MPa, mass space velocity 4h-1, hydrogen to oil volume ratio is
900.Raw material is formed with embodiment 1.Other conditions are described below.
Light hydrocarbon (40 DEG C, 0.2MPa) from separative element into hydrofinishing feed surge tank (40 DEG C, 0.2MPa),
After feed pump boosts (40 DEG C, 5.3MPa), after being mixed with circulating hydrogen (65 DEG C, 5.2MPa), exchange heat through input and output material heat exchanger
(215 DEG C, 5.25MPa) afterwards into hydrofinishing heating furnace, is heated to reaction required temperature (250 DEG C, 5.2MPa), autoreaction
Enter hydrofining reactor at the top of device and carry out hydrogenation reaction.Reaction product (254 DEG C, 5.0MPa) comes out from reactor bottom,
Enter separating at high temperature tank (105 DEG C, 4.9MPa) after input and output material heat exchanger and raw material heat exchange.Gas phase goes out from separating at high temperature tank top
Come, after the cooling of reacted product cooler, into cryogenic separation tank (45 DEG C, 4.8MPa), recycle hydrogen is from cryogenic separation tank top
Out, it after supplementing fresh hydrogen, is used after circulating hydrogen compressor boosts (65 DEG C, 5.3MPa) with raw material mixing Posterior circle.Add hydrogen
Refined separating at high temperature pot bottom is high score oil, after low with cryogenic separation pot bottom point of oil is mixed and depressurized, is sent to flash tank.It dodges
Discharge low molecular hydrocarbon is sent to torch at the top of steaming pot (105 DEG C, 0.45MPa), and bottom is sent for hydrogenated products to separative element.
Product form see the table below：
Light hydrocarbon hydrogenated products composition -3
| Serial number | Component | It forms (w%) |
| 1 | C1-C4 | 0.19 |
| 2 | C5-C9 | 30.61 |
| 34 | C10-C14 | 33.25 |
| 5 | C15-C19 | 35.95 |
| 6 | Alkene | 0 |
| 7 | Alcohol | 0 |
As above, light oil adds the alkene saturation factor of hydrogen and dealcoholysis rate reachable 100%.
Claims (7)
1. a kind of technique of F- T synthesis light hydrocarbon hydrofinishing, it is characterised in that include the following steps：
Light hydrocarbon from F- T synthesis separative element enters feed surge tank, after feed pump boosts, is mixed with circulating hydrogen,
After the heat exchange of input and output material heat exchanger, stove heat is heated into hydrofinishing, enters equipped with catalyst plus hydrogen essence from top later
Reactor processed carries out hydrogenation reaction under catalyst action, and reaction product comes out from hydrofining reactor bottom, in input and output material
Entering separating at high temperature tank after exchanging heat in heat exchanger, gas phase comes out from separating at high temperature tank top, after reacted product cooler cooling,
Into cryogenic separation tank, hydrogen comes out from cryogenic separation tank top, and supplements fresh hydrogen, after circulating hydrogen compressor boosts and light
Matter hydrocarbon mixes, and the high score oil come out from separating at high temperature pot bottom is mixed and subtracted with the low point of oil come out from cryogenic separation pot bottom
After pressure, send to flash tank, flash drum overhead discharge low molecular hydrocarbon is used as fuel gas, and from bottom, discharge is hydrogenation products.
2. a kind of technique of F- T synthesis light hydrocarbon hydrofinishing as described in claim 1, it is characterised in that F- T synthesis is light
Matter hydrocarbon adds the reaction condition of hydrogen：Reaction temperature is 150-270 DEG C, pressure 2.0-5.0MPa, and light hydrocarbon mass space velocity is 0.5-
10h-1, hydrogen to oil volume ratio 400-1000.
3. a kind of technique of F- T synthesis light hydrocarbon hydrofinishing as described in claim 1, it is characterised in that described comes from
The light hydrocarbon of F- T synthesis separative element is the linear paraffin for the C5-C19 that F- T synthesis is fractionated into processing, containing a small amount of alkene and alcohol
Mixture.
A kind of 4. technique of F- T synthesis light hydrocarbon hydrofinishing as described in claim 1, it is characterised in that the high temperature
The temperature of knockout drum is 75 DEG C -110 DEG C.
A kind of 5. technique of F- T synthesis light hydrocarbon hydrofinishing as described in claim 1, it is characterised in that the low temperature
The temperature of knockout drum is 45 DEG C.
A kind of 6. technique of F- T synthesis light hydrocarbon hydrofinishing as described in claim 1, it is characterised in that the flash distillation
In flash conditions for 75 DEG C -110 DEG C of temperature, pressure 0.45MPa.
7. a kind of technique of F- T synthesis light hydrocarbon hydrofinishing as described in claim 1, it is characterised in that catalyst is by oxygen
Changing nickel, tungsten oxide, molybdenum oxide, titanium oxide and aluminium oxide composition, weight percent is：Nickel oxide 5.0~18.0%, tungsten oxide
1.0~11.0%, molybdenum oxide 0.1~8.0%, titanium oxide 1.5~19.0%, aluminium oxide 44.0~92.4%.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114426529A (en) * | 2021-12-31 | 2022-05-03 | 大连理工大学 | High-selectivity production process for preparing succinic anhydride by maleic anhydride liquid-phase hydrogenation |
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| CN1554728A (en) * | 2003-12-26 | 2004-12-15 | 中国科学院山西煤炭化学研究所 | Catalyst for fischer-tropsch synthesized oil product hydrogen saturation and its preparing method and use |
| CN102746895A (en) * | 2011-04-19 | 2012-10-24 | 中科合成油技术有限公司 | Single-reactor hydrogenation technology of Fischer-Tropsch synthetic full fraction products |
| CN103146426A (en) * | 2013-03-20 | 2013-06-12 | 中科合成油工程有限公司 | Method of converting fischer-tropsch synthesis products into naphtha, diesel and liquefied petroleum gas |
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2017
- 2017-12-15 CN CN201711348603.0A patent/CN108203598A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1554728A (en) * | 2003-12-26 | 2004-12-15 | 中国科学院山西煤炭化学研究所 | Catalyst for fischer-tropsch synthesized oil product hydrogen saturation and its preparing method and use |
| CN102746895A (en) * | 2011-04-19 | 2012-10-24 | 中科合成油技术有限公司 | Single-reactor hydrogenation technology of Fischer-Tropsch synthetic full fraction products |
| CN103146426A (en) * | 2013-03-20 | 2013-06-12 | 中科合成油工程有限公司 | Method of converting fischer-tropsch synthesis products into naphtha, diesel and liquefied petroleum gas |
Non-Patent Citations (1)
| Title |
|---|
| 李增杰等: "费托合成油品加氢精制的工艺条件及产品分析", 《石油化工应用》 * |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114426529A (en) * | 2021-12-31 | 2022-05-03 | 大连理工大学 | High-selectivity production process for preparing succinic anhydride by maleic anhydride liquid-phase hydrogenation |
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