CN116790233A - Olefin-rich mixed drilling fluid base oil and preparation method thereof - Google Patents
Olefin-rich mixed drilling fluid base oil and preparation method thereof Download PDFInfo
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- CN116790233A CN116790233A CN202210267992.9A CN202210267992A CN116790233A CN 116790233 A CN116790233 A CN 116790233A CN 202210267992 A CN202210267992 A CN 202210267992A CN 116790233 A CN116790233 A CN 116790233A
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- olefin
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- 238000005553 drilling Methods 0.000 title claims abstract description 177
- 239000012530 fluid Substances 0.000 title claims abstract description 160
- 239000002199 base oil Substances 0.000 title claims abstract description 133
- 150000001336 alkenes Chemical class 0.000 title claims abstract description 101
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 title claims abstract description 71
- 238000002360 preparation method Methods 0.000 title claims abstract description 13
- 239000003921 oil Substances 0.000 claims abstract description 102
- 238000004821 distillation Methods 0.000 claims abstract description 50
- 150000001335 aliphatic alkanes Chemical class 0.000 claims abstract description 28
- 238000011282 treatment Methods 0.000 claims abstract description 26
- 239000002994 raw material Substances 0.000 claims abstract description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 10
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 5
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 5
- 239000011593 sulfur Substances 0.000 claims abstract description 5
- 238000005520 cutting process Methods 0.000 claims description 45
- 238000000034 method Methods 0.000 claims description 35
- 230000008569 process Effects 0.000 claims description 29
- 229910052799 carbon Inorganic materials 0.000 claims description 27
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 26
- 239000001301 oxygen Substances 0.000 claims description 26
- 229910052760 oxygen Inorganic materials 0.000 claims description 26
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 21
- GGQQNYXPYWCUHG-RMTFUQJTSA-N (3e,6e)-deca-3,6-diene Chemical compound CCC\C=C\C\C=C\CC GGQQNYXPYWCUHG-RMTFUQJTSA-N 0.000 claims description 13
- 238000009835 boiling Methods 0.000 claims description 13
- 239000000126 substance Substances 0.000 claims description 10
- 238000000638 solvent extraction Methods 0.000 claims description 6
- 238000001179 sorption measurement Methods 0.000 claims description 5
- 238000006392 deoxygenation reaction Methods 0.000 claims description 2
- 238000011085 pressure filtration Methods 0.000 abstract description 3
- 239000000047 product Substances 0.000 description 67
- 238000003786 synthesis reaction Methods 0.000 description 24
- 230000015572 biosynthetic process Effects 0.000 description 22
- 239000000203 mixture Substances 0.000 description 17
- 238000009826 distribution Methods 0.000 description 15
- 238000006317 isomerization reaction Methods 0.000 description 15
- 238000006243 chemical reaction Methods 0.000 description 14
- 150000001875 compounds Chemical class 0.000 description 14
- 239000007789 gas Substances 0.000 description 12
- 230000001276 controlling effect Effects 0.000 description 11
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 9
- 239000004711 α-olefin Substances 0.000 description 9
- 125000004432 carbon atom Chemical group C* 0.000 description 7
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 230000000704 physical effect Effects 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- MKPXGEVFQSIKGE-UHFFFAOYSA-N [Mg].[Si] Chemical compound [Mg].[Si] MKPXGEVFQSIKGE-UHFFFAOYSA-N 0.000 description 5
- 239000003463 adsorbent Substances 0.000 description 5
- 239000007864 aqueous solution Substances 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 5
- 150000002148 esters Chemical class 0.000 description 5
- 239000002002 slurry Substances 0.000 description 5
- 239000002253 acid Substances 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000003208 petroleum Substances 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 230000009467 reduction Effects 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- 238000012360 testing method Methods 0.000 description 4
- 125000000217 alkyl group Chemical group 0.000 description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000005194 fractionation Methods 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- HIXDQWDOVZUNNA-UHFFFAOYSA-N 2-(3,4-dimethoxyphenyl)-5-hydroxy-7-methoxychromen-4-one Chemical compound C=1C(OC)=CC(O)=C(C(C=2)=O)C=1OC=2C1=CC=C(OC)C(OC)=C1 HIXDQWDOVZUNNA-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 150000007513 acids Chemical class 0.000 description 2
- 150000001298 alcohols Chemical class 0.000 description 2
- 150000004996 alkyl benzenes Chemical class 0.000 description 2
- 150000001721 carbon Chemical group 0.000 description 2
- 238000004517 catalytic hydrocracking Methods 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000003995 emulsifying agent Substances 0.000 description 2
- RTZKZFJDLAIYFH-UHFFFAOYSA-N ether Substances CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- 150000002170 ethers Chemical class 0.000 description 2
- 238000004880 explosion Methods 0.000 description 2
- 238000011010 flushing procedure Methods 0.000 description 2
- 230000002706 hydrostatic effect Effects 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000003112 inhibitor Substances 0.000 description 2
- 150000002576 ketones Chemical class 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000012188 paraffin wax Substances 0.000 description 2
- 229920013639 polyalphaolefin Polymers 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 229920002994 synthetic fiber Polymers 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 241000124008 Mammalia Species 0.000 description 1
- 125000004036 acetal group Chemical group 0.000 description 1
- DHKHKXVYLBGOIT-UHFFFAOYSA-N acetaldehyde Diethyl Acetal Natural products CCOC(C)OCC DHKHKXVYLBGOIT-UHFFFAOYSA-N 0.000 description 1
- 150000001241 acetals Chemical class 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 230000000844 anti-bacterial effect Effects 0.000 description 1
- 150000001491 aromatic compounds Chemical class 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 239000003899 bactericide agent Substances 0.000 description 1
- TZCXTZWJZNENPQ-UHFFFAOYSA-L barium sulfate Chemical compound [Ba+2].[O-]S([O-])(=O)=O TZCXTZWJZNENPQ-UHFFFAOYSA-L 0.000 description 1
- 229910052601 baryte Inorganic materials 0.000 description 1
- 239000010428 baryte Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000008280 blood Substances 0.000 description 1
- 210000004369 blood Anatomy 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000004927 clay Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 239000013530 defoamer Substances 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 125000004185 ester group Chemical group 0.000 description 1
- 125000002573 ethenylidene group Chemical group [*]=C=C([H])[H] 0.000 description 1
- 125000001033 ether group Chemical group 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 239000004088 foaming agent Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000005098 hot rolling Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000009545 invasion Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000314 lubricant Substances 0.000 description 1
- 238000010907 mechanical stirring Methods 0.000 description 1
- 239000002480 mineral oil Substances 0.000 description 1
- 235000010446 mineral oil Nutrition 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 238000000518 rheometry Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000009738 saturating Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- -1 tackifier Substances 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- 125000000391 vinyl group Chemical group [H]C([*])=C([H])[H] 0.000 description 1
- 229920002554 vinyl polymer Polymers 0.000 description 1
- 239000001993 wax Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09K—MATERIALS FOR MISCELLANEOUS APPLICATIONS, NOT PROVIDED FOR ELSEWHERE
- C09K8/00—Compositions for drilling of boreholes or wells; Compositions for treating boreholes or wells, e.g. for completion or for remedial operations
- C09K8/02—Well-drilling compositions
- C09K8/32—Non-aqueous well-drilling compositions, e.g. oil-based
-
- 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
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages 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
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step
-
- 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
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/08—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one sorption step
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Materials Engineering (AREA)
- Lubricants (AREA)
Abstract
The invention relates to an olefin-rich mixed drilling fluid base oil, which is obtained by distillation treatment and deoxidation treatment of raw material high-temperature Fischer-Tropsch synthetic oil, wherein the initial distillation point of the drilling fluid base oil is 150-250 ℃, the final distillation point of the drilling fluid base oil is 300-400 ℃, the drilling fluid base oil comprises linear chain terminal olefin and internal olefin with 10-28 carbons and linear chain alkane and isoparaffin with 10-28 carbons, and the total mass content of the linear chain terminal olefin and the internal olefin in the drilling fluid base oil is not less than 60%; the drilling fluid base oil has sulfur and nitrogen content less than 1ppm, flash point not lower than 80deg.C, pour point not higher than-30deg.C, and kinematic viscosity at 40deg.C not higher than 2mm 2 And/s. Preparation of base oil of drilling fluid provided by the inventionThe drilling fluid has the advantages of low viscosity, high demulsification voltage, low high-temperature high-pressure filtration loss and the like. The invention also relates to a preparation method of the olefin-rich mixed drilling fluid base oil.
Description
Technical Field
The invention belongs to the technical field of synthetic base drilling fluid base oil, and particularly relates to olefin-rich mixed drilling fluid base oil derived from high-temperature Fischer-Tropsch synthetic oil and a preparation method thereof.
Background
The drilling fluid is the blood of drilling engineering, and in modern drilling technology, advanced drilling fluid technology and high-quality drilling fluid are applied to safely, high-quality and fast drilling, and also can quickly obtain good oil and gas exploration results, and effectively develop and recover oil and gas fields. Plays an important role in drilling complex stratum, ensuring underground safety, preventing chemical pollution, overcoming bottom hole temperature and the like.
The drilling fluid generally comprises more than ten components of base fluid, filtrate reducer, tackifier, emulsifier, shale inhibitor, plugging agent, viscosity reducer, corrosion inhibitor, clay, lubricant, weighting agent, bactericide, defoamer, foaming agent, flocculating agent, and stuck remover, wherein the base fluid occupies the largest volume. The types of base fluids can be classified into two main types, namely water-based drilling fluids and oil-based drilling fluids. Compared with water-based drilling fluid, the oil-based drilling fluid has the advantages of high temperature resistance, salt and calcium invasion resistance, well wall stability, good lubricity, low damage degree to oil and gas layers and the like, and has become an important means for drilling high-difficulty high-temperature deep wells, offshore drilling, high-inclination directional wells, horizontal wells, complex process wells and reservoir protection. However, the traditional white oil and mineral oil have poor biodegradability, which is easy to affect the environment, in addition, the rheological property of the drilling fluid system prepared based on diesel oil and white oil is unstable, and the phenomenon of abrupt increase of apparent viscosity sometimes occurs at low temperature, so that the pressure of a circulating pump is too high, and the normal operation of drilling operation is seriously affected, so that the biodegradable synthetic base drilling fluid with good rheological property is gradually valued.
The synthetic base drilling fluid is also called an oil-like base drilling fluid, is a water-insoluble synthetic oil-based drilling fluid, has the operation performance of the oil-based drilling fluid, and has the composition basically the same as that of the oil-based drilling fluid. The fraction contained in the synthetic base drilling fluid basically contains no aromatic compound, is basically nontoxic to mammals, and can meet the emission requirement after being used on site. More than 800 wells have been used worldwide, these being located in the gulf of mexico, the north sea, the far east, the continental europe, the south america, etc., and in countries such as australia, mexico and russia, where 90% of the gulf of mexico and the north sea are located.
The synthetic base drilling fluid has different product applications in nineties of the twentieth century internationally, and is rapidly developed under the promotion of various large oil service companies. Such as the Petrofree system from Baroid company, the Quad Drill system from Dowell company, the Bio-Drill system from Mipark company, the Novadill system from M-I company, etc.
The first generation of synthetic base drilling fluid is represented by ester group, ether group, poly alpha-olefin, acetal group and the like, and the second generation of synthetic base drilling fluid is represented by linear alpha-olefin, internal olefin, linear alkylbenzene and linear paraffin group.
Esters were the first synthetic material used first to formulate drilling fluids, successful in norway with ester-based drilling fluids, month 3 of 1990; inspired by ester-based drilling fluids, ether-based drilling fluids were developed in 1991; ether-based drilling fluids were started in the offshore fields of norway and mexico bay at 5 and 6 months, respectively, and then applied on a larger scale; at the end of 1992, acetal-based drilling fluids began to be used, but practical applications were less due to their high cost of use. In the next three years (1993-1995), foreign drilling fluid researchers developed second generation synthetic materials represented by Linear Alkylbenzene (LAB), linear Paraffin (LP), linear olefin, etc., and drilling fluid systems thereof were rapidly and widely used in north sea in the united kingdom and in the gulf of mexico. With the development of the coal-to-liquid industry, fischer-Tropsch synthetic oil has certain environmental protection advantages due to no sulfur and nitrogen impurities, is widely focused by people, and is widely applied by developing synthetic base alkane type drilling fluid base oil by energy companies represented by Shell companies.
The Fischer-Tropsch synthesis is a technological process for synthesizing hydrocarbon, oxygen-containing compound and water by taking synthesis gas containing hydrogen and carbon monoxide as raw materials under the reaction conditions of a catalyst, a certain temperature, a certain pressure and the like, is widely applied to petroleum substitution technologies such as coal indirect liquefaction, natural gas oil production and biomass oil production, and has important significance for relieving the dependence of national energy sources on petroleum resources. The Fischer-Tropsch synthesis can be divided into two types according to the reaction temperature and the product composition, one type is that long-chain heavy oil or Fischer-Tropsch wax is generated at low temperature (220-250 ℃), the carbon number distribution range is wider, the liquid phase product is distributed from C4 to C60 and even C100, 80-90 wt% of the liquid phase product is normal alkane, and the liquid phase product further contains a small amount of components such as isoparaffin, olefin, oxygen-containing compound and the like, and is abbreviated as low-temperature Fischer-Tropsch; and the other is to synthesize low-carbon alkane and alkene at high temperature (300-350 ℃), the carbon number distribution of the synthesized product is narrower, the synthesized product is mainly concentrated below C20, wherein the content of alkene components is more than 50wt%, and the synthesized product is high-temperature Fischer-Tropsch oil.
The low-temperature Fischer-Tropsch oil is mainly linear alkane, is a good processing raw material of the alkyl drilling fluid base oil, and can adjust the flash point range of the product by controlling the proper fraction distribution, and the higher the boiling point is, the higher the corresponding flash point is. But compared with isoparaffin, the pour point of the linear alkane is lower, and for some low-temperature areas, the linear alkane base oil cannot be directly used and has to be subjected to hydroisomerization treatment, so that the linear alkane is changed into branched isoparaffin in an isomerism mode, the pour point of the oil product is reduced, and the application range of the base oil is widened.
CN105505347a discloses a synthetic base drilling fluid base oil, which is formed by mixing a fischer-tropsch synthetic oil and a non-conventional petroleum derived fine chemical base oil, contains at least 35% by mass of a plurality of normal paraffins of 9 to 20 carbon atoms, contains at least 60% by mass of a plurality of branched or cyclic paraffins of 9 to 20 carbon atoms, and contains less than 0.5% by mass of aromatic hydrocarbons. The kinematic viscosity of the synthetic base drilling fluid base oil at 40 ℃ is 2-3 mm 2 The pour point is between-10 and-30 ℃ and the closed flash point is between 50 and 80 ℃.
CN110964564a discloses a fischer-tropsch synthesis base drilling fluid base oil and a preparation method thereof, comprising: directly carrying out cracking isomerization treatment on the Fischer-Tropsch synthesis product; directly fractionating the Fischer-Tropsch synthesis product after cracking isomerization treatment to obtain a base oil product or carrying out hydrofining treatment and then fractionating to obtain the base oil product; the isoparaffin proportion in the obtained base oil product is more than 60 weight percent. Wherein the fractionation comprises atmospheric fractionation, and the process conditions of the atmospheric fractionation are as follows: the temperature of the tower top is 100-120 ℃, the pressure of the tower top is 0.01-0.2 MPa, and the temperature of the side draw-out is 170-190 ℃ at the same line. The invention describes a processing flow for producing alkyl drilling fluid base oil from Fischer-Tropsch synthesis products after hydrocracking isomerization treatment.
CN105713661a discloses a process for preparing a base oil from a fischer-tropsch synthesis product comprising: a. cutting a Fischer-Tropsch synthesis specific fraction product into several fractions by distillation; b. carrying out isomerization treatment on one or more fractions in the obtained fractions, and controlling the isomerization degree between 50 and 100 percent by changing the reaction conditions; c. according to the application requirements of the drilling fluid, blending the obtained several distillate oils which are subjected to isomerization treatment and are not subjected to isomerization treatment according to the proportion; d. and distilling the blended product to remove the hydroisomerization byproduct low-carbon hydrocarbon, thereby obtaining a base oil sample for performance testing and commercial application.
The patents all use low-temperature Fischer-Tropsch synthetic oil to process and produce the base oil of the alkyl drilling fluid, most of the base oil needs to be subjected to an isomerization process, and the obtained base oil usually takes isoparaffin as a main component and contains a small amount of normal paraffins. The hydrocracking or hydroisomerization process is usually a high-pressure reaction process of more than 10MPa, the reaction conditions are harsh, the energy consumption of the device is high, in addition, the catalyst used in the isomerization reaction is usually a noble metal catalyst, and the production cost is high.
The prior drilling fluid base oil mainly comprising olefin components is mainly poly alpha-olefin base drilling fluid, and is derived from a mixture of linear alpha-olefin and isomers thereof or a mixture of internal olefin and internal olefin isomers generated by ethylene polymerization. The alpha-olefin product is derived from Ziegler chain growth process, the product is mainly linear alpha-olefin, the mixture of the oil products is generally high in pour point, and the mixture of the oil products is mostly treated by an isomerization process to achieve the purposes of pour point reduction and pour point reduction.
WO9521226 (A1) discloses a drilling fluid for underground oil and gas wells, the base oil of which fluid is a mixture of linear and branched olefins, most of which are linear olefins, said olefins having at least 12 carbon atoms, preferably a drilling fluid of C14 to C18 olefins, the mixture according to the invention being such that most of the olefins are linear, meaning that 50 to 100%, preferably 60 to 100%, more preferably 70 to 80% of the olefins in the mixture have no branching points along the hydrocarbon chain, and on the other hand, it is further preferred that such mixture also comprises olefins having some side chain branching, preferably branching olefins, accounting for at least 5%, preferably at least 10% of the mixture.
WO9907805 (A1) discloses a base oil mixture for the preparation of low pour point drilling fluids, the base oil consisting of mainly isomers of linear endotetradecene and isomers of linear endohexadecene, the base oil pour point being below-25 ℃, suitable for drilling in cold and offshore areas.
Drilling fluid base oils, which typically comprise linear alpha olefins, internal olefins, and the like as the major components, have excellent viscosity properties and a relatively high flash point, but have a relatively high pour point, and typically require isomerization to reduce the pour point of the oil. WO0132590 (A3) discloses a process for isomerising a mixture of linear alpha-olefins of vinyl and vinylidene groups of 10 to 35 carbon atoms, at least 70% by weight of the mixture after isomerisation being di-or tri-substituted internal olefins; at least 20% by weight of the total amount of internal olefins which are trisubstituted; of the disubstituted internal olefins, at least 20 weight percent of the product mixture is a disubstituted internal olefin having a double bond at the fourth or higher numbered carbon atom position and wherein less than 50 weight percent is a disubstituted internal olefin having a double bond at the second or third numbered carbon atom position. Also disclosed is a reverse phase drilling fluid comprising at least about 50% by volume base oil, wherein at least about 25% by volume, more preferably 75% by volume of the base oil content of the drilling fluid is the above isomerized mixture.
In the above patents, the base oil mainly comprising saturated alkane components or the base oil mainly comprising olefin components such as alpha-olefin, internal olefin and the like mostly needs to be treated by hydroisomerization process to achieve the purposes of pour point reduction and pour point reduction.
Disclosure of Invention
Based on the above, the invention aims to provide an olefin-rich mixed drilling fluid base oil derived from Fischer-Tropsch synthetic oil and a preparation method thereof. The olefin-rich mixed drilling fluid base oil provided by the invention simultaneously contains olefin and alkane components, has the performance characteristics of olefin groups and alkane base drilling fluid base oil, does not need to be subjected to isomerization or hydrogenation treatment, has high olefin content, has low viscosity, is favorable for improving the actual drilling rate, has flexible regulation and control of performance indexes, and has wide product application range.
The invention provides an olefin-rich mixed drilling fluid base oil, which is prepared by distilling and deoxidizing raw material high-temperature Fischer-Tropsch synthetic oil, wherein the initial distillation point of the drilling fluid base oil is 150-250 ℃, the final distillation point of the drilling fluid base oil is 300-400 ℃, the drilling fluid base oil comprises 10-28 carbon linear-end olefins and internal olefins and 10-28 carbon linear-end paraffins and isoparaffins, and the total mass content of the linear-end olefins and the internal olefins in the drilling fluid base oil is more than or equal to 60%; the drilling fluid base oil has a sulfur and nitrogen content less than1ppm, flash point not lower than 80 ℃, pour point not higher than-30 ℃, and kinematic viscosity at 40 ℃ not higher than 2mm 2 /s。
Specifically, the high temperature Fischer-Tropsch oil contains a large amount of olefins, accounting for more than 50% of the total amount of hydrocarbons, wherein alpha-olefins are used as main components, and other parts of internal olefins and alkanes are used. The high temperature Fischer-Tropsch oil is prepared by Fischer-Tropsch synthesis of low-carbon alkane and alkene at high temperature (300-350 ℃), the carbon number distribution of the synthesized product is narrower, and the synthesized product is mainly concentrated below C20, wherein the content of the alkene component is more than 50 wt%.
In addition, CO and H 2 In the Fischer-Tropsch synthesis reaction process, the generation of oxygen-containing compounds is difficult to avoid, and particularly the content of the oxygen-containing compounds in high-temperature Fischer-Tropsch oil can be up to more than 10 weight percent, and the oxygen-containing compounds comprise different types such as alcohols, ethers, acids, ketones, esters and the like. The existence of the oxygen-containing compound can aggravate the taste of the oil product, the pungent smell is easy to exist in the use process, the light stability and the heat stability of the product can be influenced, in addition, the existence of the acid substance is extremely easy to cause metal corrosion of a drill rod, equipment and the like, the safety of the use process is influenced, and the removal of the oxygen-containing compound is necessary before the next processing process is carried out. Moreover, the high temperature Fischer-Tropsch synthesis oil contains a large amount of olefin, and the conventional hydrofining means is not applicable because olefin saturation is unavoidable while removing the oxygen-containing compound. Non-hydro means are typically employed, and relatively effective treatments include solvent extraction, physical adsorption and chemical removal.
The olefin-rich mixed drilling fluid base oil disclosed by the invention is preferable in that the initial boiling point of the drilling fluid base oil is 170-200 ℃ and the final boiling point of the drilling fluid base oil is 300-350 ℃.
The olefin-rich mixed drilling fluid base oil of the invention, wherein the drilling fluid base oil preferably has 12-24 carbon linear terminal olefin and internal olefin and 12-24 carbon linear alkane and isoparaffin.
The olefin-rich mixed drilling fluid base oil disclosed by the invention is preferable, wherein the mass content of the linear-chain end olefin with 12-24 carbon atoms and the internal olefin in the drilling fluid base oil is more than or equal to 60%.
The olefin-rich mixed drilling fluid base oil disclosed by the invention is preferable, wherein the mass content of the linear alkane with 12-24 carbon atoms in the drilling fluid base oil is not less than 10%.
The olefin-rich mixed drilling fluid base oil disclosed by the invention is preferable, wherein the mass content of isoparaffin with 12-24 carbon atoms in the drilling fluid base oil is not less than 10%.
The mass content of oxygen element in the drilling fluid base oil is preferably not higher than 1.5%, and preferably not higher than 1%.
The olefin-rich mixed drilling fluid base oil according to the present invention, wherein preferably, the deoxidizing treatment comprises at least one of a solvent extraction method, a physical adsorption method and a chemical removal method.
The invention relates to a preparation method of an olefin-rich mixed drilling fluid base oil, which preferably comprises the following steps: and (3) performing primary fraction cutting on the high-temperature Fischer-Tropsch synthetic oil, performing deoxidation treatment on the primary cut distillate oil, wherein the mass content of oxygen elements is not higher than 1%, and performing secondary fraction cutting on the deoxidized primary cut distillate oil again to obtain the olefin-rich mixed drilling fluid base oil with an initial distillation point of 150-250 ℃, preferably 170-200 ℃, and a final distillation point of 300-400 ℃, preferably 300-350 ℃.
The preparation method of the present invention, wherein the primary cut distillate preferably has an initial boiling point of 150 to 250 ℃, preferably 170 to 200 ℃, and a final boiling point of 300 to 400 ℃, preferably 300 to 350 ℃.
Specifically, key physical parameters of the drilling fluid base oil include flash point, pour point, density, kinematic viscosity and the like, and the low physical parameter index has important influence on the performance and safety of the base oil. In the drilling process, the drilling fluid needs to keep good rheological property, the viscosity needs to be kept in a moderate range, the higher the viscosity is, the worse the rheological property is, the pressure fluctuation is easy to generate, the circulating pressure consumption is large, the drilling speed is reduced, the drilling sticking is easy to cause, and the drilling fluid is not easy to maintain; too low viscosity, poor carrying and suspending capabilities, poor well flushing effect and easy drill sticking caused by heavy spar and drilling cuttings sedimentation. The pour point mainly influences the use of drilling fluid in a low-temperature environment, the lower the pour point is, the wider the application range is, the flash point mainly influences the safety of the use process, the lower the drilling fluid is, the temperature is increased by about 4 ℃, for some ultra-deep wells, the temperature is even more than 200 ℃, the oil product combustion, explosion and the like are easily caused in the construction engineering due to the fact that the flash point is too low, and safety accidents occur, so that the flash point is required to be as high as possible; in the drilling process, the drilling fluid is required to have a certain density, the hydrostatic column pressure of the drilling fluid in the well is regulated, the stability of the well wall is maintained, and the heavy spar is usually required to be added for regulation, so that the dosage of the heavy spar can be reduced by increasing the density of the base oil, and the precipitation and separation caused by excessive addition of the heavy spar are avoided.
The distribution of the base oil fraction of the drilling fluid plays a decisive role on the physical parameters, and in general, the higher the molecular weight of the oil product is, the higher the carbon number is, and the flash point, the pour point, the density and the viscosity all tend to be increased. The flash point is mainly related to the initial point, the higher the initial point is, the larger the flash point is, the pour point is mainly related to the final point, and the higher the final point is, because the carbon number distribution of the Fischer-Tropsch synthetic oil is in a normal distribution shape and the distribution range is wider, the excessive light component and the excessive heavy component are required to be cut off, the relatively concentrated carbon number distribution is obtained, and the product index is controllable. The invention mainly solves the problem that the carbon number is concentrated by a rectification cutting mode, utilizes the boiling point difference between different fractions to separate light and heavy components, mainly controls the initial distillation point and the final distillation point of the oil product in the separation process, and controls the initial distillation point range of the oil product to be 150-250 ℃ and the final distillation point range to be 300-400 ℃ after separation. The range of the initial fraction of the oil product obtained by further optimizing cutting and separating is controlled to be 170-200 ℃ and the range of the final distillation point is controlled to be 300-350 ℃.
The beneficial effects of the invention are as follows:
(1) The drilling fluid base oil provided by the invention contains olefin and alkane components, the performance characteristics of olefin-based and alkane-based drilling fluid base oil are considered, the isomerization process treatment is not needed, the viscosity of the base oil is low, the improvement of the actual drilling rate is facilitated, the performance index can be flexibly regulated and controlled, and the application range of the product is wide.
(2) The drilling fluid prepared from the drilling fluid base oil provided by the invention has the advantages of low viscosity, high demulsification voltage, low high-temperature high-pressure filtration loss and the like.
Detailed Description
The following describes embodiments of the present invention in detail: the present example is carried out on the premise of the technical scheme of the present invention, and detailed implementation modes and processes are given, but the protection scope of the present invention is not limited to the following examples, and the experimental methods of specific conditions are not noted in the following examples, and generally, the% is weight% according to conventional conditions.
The invention provides an olefin-rich mixed drilling fluid base oil, which is obtained by distillation and deoxidation of raw material high-temperature Fischer-Tropsch synthetic oil, wherein the initial distillation point of the drilling fluid base oil is 150-250 ℃, the final distillation point is 300-400 ℃, the drilling fluid base oil comprises 10-28 carbon linear terminal olefin and internal olefin and 10-28 carbon linear alkane and isoparaffin, and the total mass content of the linear terminal olefin and the internal olefin in the drilling fluid base oil is more than or equal to 60%; the drilling fluid base oil has sulfur and nitrogen content less than 1ppm, flash point not lower than 80deg.C, pour point not higher than-30deg.C, and kinematic viscosity at 40deg.C not higher than 2mm 2 /s。
Specifically, the high temperature Fischer-Tropsch oil contains a large amount of olefins, accounting for more than 50% of the total amount of hydrocarbons, wherein alpha-olefins are used as main components, and other parts of internal olefins and alkanes are used. The high temperature Fischer-Tropsch oil is prepared by Fischer-Tropsch synthesis of low-carbon alkane and alkene at high temperature (300-350 ℃), the carbon number distribution of the synthesized product is narrower, and the synthesized product is mainly concentrated below C20, wherein the content of the alkene component is more than 50 wt%.
In addition, CO and H 2 In the Fischer-Tropsch synthesis reaction process, the generation of oxygen-containing compounds is difficult to avoid, and particularly the content of the oxygen-containing compounds in high-temperature Fischer-Tropsch oil can be up to more than 10 weight percent, and the oxygen-containing compounds comprise different types such as alcohols, ethers, acids, ketones, esters and the like. The existence of the oxygen-containing compound can aggravate the taste of the oil product, the pungent smell is easy to exist in the use process, the light stability and the heat stability of the product can be influenced, in addition, the existence of the acid substance is extremely easy to cause metal corrosion of a drill rod, equipment and the like, the safety of the use process is influenced, and the removal of the oxygen-containing compound is necessary before the next processing process is carried out. Furthermore, the high temperature Fischer-Tropsch synthesis oil product containsConventional hydrofinishing means, which remove oxygenates while inevitably saturating the olefin with large amounts of olefin, is not well suited. Non-hydro means are typically employed, and relatively effective treatments include solvent extraction, physical adsorption and chemical removal.
In some embodiments, it is preferred that the drilling fluid base oil has an initial boiling point of 170 to 200 ℃ and a final boiling point of 300 to 350 ℃.
In some embodiments, it is preferred that the drilling fluid base oil has linear terminal and internal olefins of 12 to 24 carbons and linear and isoparaffins of 12 to 24 carbons.
In some embodiments, it is preferred that the drilling fluid base oil has a mass content of linear end olefins and internal olefins of 12 to 24 carbons of 60% or more.
In some embodiments, it is preferred that the drilling fluid base oil has a linear alkane content of from 12 to 24 carbons of not less than 10% by mass.
In some embodiments, it is preferred that the 12 to 24 carbon isoparaffin mass content in the drilling fluid base oil is not less than 10%.
In some embodiments, it is preferred that the drilling fluid base oil has an elemental oxygen content of no greater than 1.5% by mass, preferably no greater than 1%.
In some embodiments, it is preferred that the deoxygenation treatment comprises at least one of solvent extraction, physical adsorption, and chemical removal.
The invention provides a preparation method of an olefin-rich mixed drilling fluid base oil, which comprises the following steps: and (3) performing primary fraction cutting on the high-temperature Fischer-Tropsch synthetic oil, performing deoxidation treatment on the primary cut distillate oil, wherein the mass content of oxygen elements is not higher than 1%, and performing secondary fraction cutting on the deoxidized primary cut distillate oil again to obtain the olefin-rich mixed drilling fluid base oil with an initial distillation point of 150-250 ℃, preferably 170-200 ℃, and a final distillation point of 300-400 ℃, preferably 300-350 ℃.
In some embodiments, it is preferred that the primary cut distillate has an initial point of 150 to 250 ℃, preferably 170 to 200 ℃, and a final point of 300 to 400 ℃, preferably 300 to 350 ℃.
Specifically, key physical parameters of the drilling fluid base oil include flash point, pour point, density, kinematic viscosity and the like, and the low physical parameter index has important influence on the performance and safety of the base oil. In the drilling process, the drilling fluid needs to keep good rheological property, the viscosity needs to be kept in a moderate range, the higher the viscosity is, the worse the rheological property is, the pressure fluctuation is easy to generate, the circulating pressure consumption is large, the drilling speed is reduced, the drilling sticking is easy to cause, and the drilling fluid is not easy to maintain; too low viscosity, poor carrying and suspending capabilities, poor well flushing effect and easy drill sticking caused by heavy spar and drilling cuttings sedimentation. The pour point mainly influences the use of drilling fluid in a low-temperature environment, the lower the pour point is, the wider the application range is, the flash point mainly influences the safety of the use process, the lower the drilling fluid is, the temperature is increased by about 4 ℃, for some ultra-deep wells, the temperature is even more than 200 ℃, the oil product combustion, explosion and the like are easily caused in the construction engineering due to the fact that the flash point is too low, and safety accidents occur, so that the flash point is required to be as high as possible; in the drilling process, the drilling fluid is required to have a certain density, the hydrostatic column pressure of the drilling fluid in the well is regulated, the stability of the well wall is maintained, and the heavy spar is usually required to be added for regulation, so that the dosage of the heavy spar can be reduced by increasing the density of the base oil, and the precipitation and separation caused by excessive addition of the heavy spar are avoided.
The distribution of the base oil fraction of the drilling fluid plays a decisive role on the physical parameters, and in general, the higher the molecular weight of the oil product is, the higher the carbon number is, and the flash point, the pour point, the density and the viscosity all tend to be increased. The flash point is mainly related to the initial point, the higher the initial point is, the larger the flash point is, the pour point is mainly related to the final point, and the higher the final point is, because the carbon number distribution of the Fischer-Tropsch synthetic oil is in a normal distribution shape and the distribution range is wider, the excessive light component and the excessive heavy component are required to be cut off, the relatively concentrated carbon number distribution is obtained, and the product index is controllable. The invention mainly solves the problem that the carbon number is concentrated by a rectification cutting mode, utilizes the boiling point difference between different fractions to separate light and heavy components, mainly controls the initial distillation point and the final distillation point of the oil product in the separation process, and controls the initial distillation point range of the oil product to be 150-250 ℃ and the final distillation point range to be 300-400 ℃ after separation. The range of the initial fraction of the oil product obtained by further optimizing cutting and separating is controlled to be 170-200 ℃ and the range of the final distillation point is controlled to be 300-350 ℃.
Test method
The composition of the base oil is measured by adopting a Japanese electronic gas chromatograph-time-of-flight mass spectrometer, the mass content of oxygen element is measured by adopting an EA 2400 instrument of Perkinelmer company, the closed flash point is measured by adopting GB/T261-2008, the pour point is measured by adopting GB/T3535-2006, and the kinematic viscosity is measured by adopting GB/30015-2014.
Raw materials and sources of reagents
Silicon magnesium adsorbent, hu test of national medicine, FCP 60-100 mesh.
Example 1:
certain high temperature Fischer-Tropsch synthesis slurry bed reactor is prepared with H 2 The synthetic gas with the ratio of/CO of 2:1 is used as a raw material, the operating temperature of the device is 320 ℃, the reaction pressure is 3MPa, the product at the outlet of the reactor, namely high-temperature Fischer-Tropsch oil, is collected, the product is added into a 5L rectifying tower to carry out one-time fraction cutting, the theoretical plate number of the rectifying tower is 25, the fraction smaller than 170 ℃ is cut off by utilizing normal pressure rectification, then the vacuum degree is controlled to be 50mmHg, the fraction larger than 320 ℃ is cut off, and the oil with the initial distillation point of 170 ℃ and the final distillation point of 320 ℃ is obtained. The obtained distillate oil is deoxidized by using a silicon-magnesium adsorbent under the following treatment conditions: the temperature is 25 ℃, the pressure is 0.1MPa, the volume ratio of the distillate oil to the silicon-magnesium adsorbent is 400:1, and the oxygen content after the distillate oil is deoxidized is 0.42wt%. And (3) carrying out secondary fraction cutting on the deoxidized distillate oil again through a rectifying tower, wherein the cutting conditions are the same as those of the primary fraction cutting, and controlling the cutting temperature of the distillate to obtain an oil product with an initial distillation point of 170 ℃ and a final distillation point of 320 ℃, namely the olefin-rich mixed drilling fluid base oil. The total mass content of the linear end alkene and the internal alkene of 12-24 carbons in the obtained base oil is 64.3%, the mass content of the linear alkane is 14.2%, and the mass content of the isoparaffin is 16.4%. Physical properties of the drilling fluid base oil are shown in table 1.
Example 2:
certain high temperature Fischer-Tropsch synthesis slurry bed reactor is prepared with H 2 The synthesis gas with the ratio of/CO of 2:1 is taken as a raw material, the operating temperature of the device is 320 ℃, the reaction pressure is 3MPa, and the reaction is collectedAnd adding the product at the outlet of the reactor, namely the high-temperature Fischer-Tropsch oil, into a 5L rectifying tower for one-time distillate cutting, wherein the theoretical plate number of the rectifying tower is 25, cutting off the distillate at the temperature of less than 170 ℃ by utilizing normal pressure rectification, controlling the vacuum degree to be 20mmHg, cutting off the distillate at the temperature of more than 330 ℃ to obtain the oil product with the initial distillation point of 170 ℃ and the final distillation point of 330 ℃. The obtained distillate oil is deoxidized by a chemical removal method, and the treatment conditions are as follows: adding distillate oil into a three-neck flask with a mechanical stirring device, adding aqueous solution prepared by methanol and sodium hydroxide (the preparation method is that 10% of methanol aqueous solution and 25% of sodium hydroxide aqueous solution are prepared according to the volume ratio of 1:3), stirring for 4 hours at the rotating speed of 800r/min, standing for layering, taking an upper oil phase into a new three-neck flask, adding desalted water with equal mass, starting stirring for a certain time, standing for layering, wherein the upper layer is the distillate oil after deoxidation refining, and the oxygen content of the distillate oil after deoxidation is 0.38wt%. And (3) carrying out secondary fraction cutting on the deoxidized distillate oil again through a rectifying tower, wherein the cutting conditions are the same as those of the primary cutting, and controlling the cutting temperature of the distillate to obtain an oil product with an initial distillation point of 170 ℃ and a final distillation point of 330 ℃, namely the olefin-rich mixed drilling fluid base oil. The mass content of the linear chain end alkene and the internal alkene of 12-24 carbons in the obtained base oil is 70.0%, the mass content of the linear chain alkane is 12.9%, and the mass content of the isoparaffin is 13.1%. Physical properties of the drilling fluid base oil are shown in table 1.
Example 3:
certain high temperature Fischer-Tropsch synthesis slurry bed reactor is prepared with H 2 The synthetic gas with the ratio of/CO of 2:1 is used as a raw material, the operating temperature of the device is 320 ℃, the reaction pressure is 3MPa, the outlet product of the reactor is collected, the oil product is added into a 5L rectifying tower kettle for one-time fraction cutting, the theoretical plate number of the rectifying tower is 25, the fraction with the temperature less than 200 ℃ is cut off by utilizing normal pressure rectification, then the vacuum degree is controlled to be 20mmHg, the fraction with the temperature greater than 310 ℃ is cut off, and the oil product with the initial distillation point of 200 ℃ and the final distillation point of 310 ℃ is obtained. The obtained distillate oil is deoxidized by chemical removal method under the same conditions as in example 2, stirring for 4 hr at 800r/min, standing until the solution is layered, adding upper oil phase into new three-neck flask, adding desalted water with equal mass, and stirringAfter stirring for a certain time, standing until the solution is layered, wherein the upper layer is the distillate oil after deoxidation and refining, and the oxygen content of the distillate oil after deoxidation is 0.32 weight percent. And (3) carrying out secondary fraction cutting on the deoxidized distillate oil again through a rectifying tower, wherein the cutting conditions are the same as those of the primary cutting, and controlling the cutting temperature of the distillate to obtain an oil product with an initial distillation point of 200 ℃ and a final distillation point of 310 ℃, namely the olefin-rich mixed drilling fluid base oil. The total mass content of the linear-chain terminal olefin and the internal olefin of 12-24 carbons in the obtained base oil is 66.2%, the mass content of the linear-chain alkane is 13.6%, and the mass content of the isoparaffin is 15.3%. Physical properties of the drilling fluid base oil are shown in table 1.
Example 4:
certain high temperature Fischer-Tropsch synthesis slurry bed reactor is prepared with H 2 The synthetic gas with the ratio of/CO of 2:1 is used as a raw material, the operating temperature of the device is 320 ℃, the reaction pressure is 3MPa, the outlet product of the reactor is collected, the oil product is added into a 5L rectifying tower kettle for one-time fraction cutting, the theoretical plate number of the rectifying tower is 25, the fraction with the temperature less than 180 ℃ is cut off by utilizing normal pressure rectification, then the vacuum degree is controlled to be 50mmHg, the fraction with the temperature greater than 300 ℃ is cut off, and the oil product with the initial distillation point of 180 ℃ and the final distillation point of 300 ℃ is obtained. The obtained distillate oil is deoxidized by using a silicon-magnesium adsorbent under the following treatment conditions: the temperature is 25 ℃, the pressure is 0.1MPa, the volume ratio of the distillate oil to the silicon-magnesium adsorbent is 400:1, and the oxygen content after the distillate oil is deoxidized is 0.48wt%. And (3) carrying out secondary fraction cutting on the deoxidized distillate oil again through a rectifying tower, wherein the cutting conditions are the same as those of the primary cutting, and controlling the cutting temperature of the distillate to obtain an oil product with an initial distillation point of 170 ℃ and a final distillation point of 320 ℃, namely the olefin-rich mixed drilling fluid base oil. The total mass content of the linear end alkene and the internal alkene of 12-24 carbons in the obtained base oil is 72.5%, the mass content of the linear alkane is 10.8%, and the mass content of the isoparaffin is 11.7%. Physical properties of the drilling fluid base oil are shown in table 1.
Example 5:
certain high temperature Fischer-Tropsch synthesis slurry bed reactor is prepared with H 2 The synthesis gas with the ratio of/CO of 2:1 is taken as a raw material, the operating temperature of the device is 320 ℃, the reaction pressure is 3MPa, the product at the outlet of the reactor is collected, the oil product is added into a 5L rectifying tower kettle for one-time fraction cutting, and the theoretical plate of the rectifying tower is a theoretical plateAnd cutting off the fraction with the temperature of less than 190 ℃ by using normal pressure rectification, then controlling the vacuum degree to be 10mmHg, and cutting off the fraction with the temperature of more than 350 ℃ to obtain the oil product with the initial distillation point of 190 ℃ and the final distillation point of 350 ℃. The obtained distillate oil is deoxidized by using a solvent extraction rectification method, and is repeatedly extracted by taking an aqueous solution containing 95wt% of methanol as an extracting agent to remove oxygen-containing compounds in the distillate oil, wherein the oxygen content of the distillate oil after deoxidization is 0.46wt%. And (3) carrying out secondary fraction cutting on the deoxidized distillate oil again through a rectifying tower, wherein the cutting conditions are the same as the primary cutting conditions, controlling the cutting temperature of the distillate to obtain an oil product with an initial distillation point of 190 ℃ and a final distillation point of 350 ℃, namely the olefin-rich mixed drilling fluid base oil. The total mass content of the linear chain end alkene and the internal alkene of 12-24 carbons in the obtained base oil is 73.6%, the mass content of the linear chain alkane is 10.1%, and the mass content of the isoparaffin is 12.2%. Physical properties of the drilling fluid base oil are shown in table 1.
Comparative example 1:
low-temperature Fischer-Tropsch synthesis fixed bed reaction device using H 2 The synthesis gas with the ratio of/CO of 2:1 is taken as a raw material, the operating temperature of the device is 220 ℃, the reaction pressure is 2.5MPa, the product at the outlet of the reactor is collected, and the reaction temperature is 320 ℃, the pressure is 7MPa, and the space velocity is 2h -1 Hydroisomerization is carried out under the process condition of hydrogen-oil ratio of 500, and the petroleum PIC-812 hydroisomerization catalyst is used in the catalyst. Then cutting the distillate by a rectifying tower, cutting the distillate at the temperature of less than 200 ℃ by utilizing normal pressure rectification, cutting the distillate at the temperature of more than 330 ℃ by controlling the vacuum degree to be 20mmHg, controlling the initial distillation point to be 200 ℃ and the final distillation point to be 330 ℃, and finally obtaining the alkane type drilling fluid base oil with the isoparaffin accounting for 80 wt%.
Test example 1
The invention relates to an olefin-rich mixed drilling fluid base oil from Fischer-Tropsch synthetic oil, which is prepared into an oil-based drilling fluid for testing the drilling fluid according to the following formula: 240ml of the olefin-rich mixed base oil obtained in each example or the alkane type drilling fluid base oil obtained in the comparative example, 8% of an emulsifier, 2.5% of organic soil, 60ml of 20% CaCl 2 Aqueous solution, 2% cao, 4% fluid loss additive, 666g barite (tarabite), oil to water ratio 4:1.the performance index of the drilling fluid is shown in table 2.
Table 1 physical properties index of drilling fluid base oil
Table 2 performance index of drilling fluid
As can be seen from Table 1, the drilling fluid base oil provided by the embodiments of the invention comprises olefin and alkane components, the performance characteristics of olefin-based and alkane-based drilling fluid base oil are considered, the isomerization process treatment is not needed, the viscosity of the base oil is low, the improvement of the actual drilling rate is facilitated, the performance index can be flexibly regulated and controlled, and the application range of the product is wide.
In Table 2, the rheology and breaking voltage were measured at 65℃and the high temperature and high pressure fluid loss was measured after 16 hours of hot rolling at 150 ℃. As can be seen from Table 2, the drilling fluid prepared by using the drilling fluid base oil provided by the invention has the advantages of low viscosity, high demulsification voltage, low high-temperature high-pressure filtration loss and the like.
Of course, the present invention is capable of other various embodiments and its several details are capable of modification and variation in light of the present invention by one skilled in the art without departing from the spirit and scope of the invention.
Claims (10)
1. The drilling fluid base oil is prepared from raw material high-temperature Fischer-Tropsch synthetic oil through distillation treatment and deoxidation treatment, wherein the initial distillation point of the drilling fluid base oil is 150-250 ℃, the final distillation point of the drilling fluid base oil is 300-400 ℃, the drilling fluid base oil comprises 10-28 carbon linear-end olefins and internal olefins and 10-28 carbon linear-end paraffins and isoparaffins, and the total mass content of the linear-end olefins and the internal olefins in the drilling fluid base oil is more than or equal to 60%; the drilling fluid foundationThe oil has sulfur and nitrogen contents of less than 1ppm, flash point of no less than 80deg.C, pour point of no more than-30deg.C, and kinematic viscosity at 40deg.C of no more than 2mm 2 /s。
2. The olefin-rich mixed drilling fluid base oil according to claim 1, wherein the initial boiling point of the drilling fluid base oil is 170-200 ℃ and the final boiling point is 300-350 ℃.
3. The olefin-rich mixed drilling fluid base oil of claim 1, wherein the drilling fluid base oil has linear terminal and internal olefins of 12 to 24 carbons and linear and isoparaffins of 12 to 24 carbons.
4. The olefin-rich mixed drilling fluid base oil according to claim 1, wherein the total mass content of the linear terminal olefin and the internal olefin of 12 to 24 carbons in the drilling fluid base oil is 60% or more.
5. The olefin-rich mixed drilling fluid base oil according to claim 1, wherein the mass content of the linear alkane of 12 to 24 carbons in the drilling fluid base oil is not less than 10%.
6. The olefin-rich mixed drilling fluid base oil according to claim 1, wherein the mass content of isoparaffin of 12-24 carbons in the drilling fluid base oil is not less than 10%.
7. The olefin-rich mixed drilling fluid base oil according to claim 1, wherein the mass content of oxygen element in the drilling fluid base oil is not higher than 1.5%, preferably not higher than 1%.
8. The olefin-rich mixed drilling fluid base oil of claim 1, wherein the deoxygenation treatment comprises at least one of solvent extraction, physical adsorption, and chemical removal.
9. The preparation method of the olefin-rich mixed drilling fluid base oil is characterized by comprising the following steps of: and (3) performing primary fraction cutting on the high-temperature Fischer-Tropsch synthetic oil, performing deoxidization treatment on the obtained primary cut distillate, wherein the mass content of oxygen elements is not higher than 1.5%, preferably not higher than 1.0%, and performing secondary fraction cutting on the deoxidized primary cut distillate again to obtain the olefin-rich mixed drilling fluid base oil with the initial distillation point of 150-250 ℃, preferably 170-200 ℃ and the final distillation point of 300-400 ℃, preferably 300-350 ℃.
10. The process according to claim 9, wherein the primary cut distillate has a primary boiling point of 150 to 250 ℃, preferably 170 to 200 ℃, and a final boiling point of 300 to 400 ℃, preferably 300 to 350 ℃.
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