CN103375156A - Crude oil recovery method - Google Patents
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Abstract
The invention discloses a crude oil recovery method. The method comprises placing a mixture in a condition which enables the heavy components of heavy oil to be under catalytic cracking for reaction, wherein reaction products serve as blending diluting oil to be injected into an oil well to recover the crude oil in the oil well, the mixture is composed of the heavy oil, catalysts and water which have a weight ratio of 1: (0.00004-0.01): (0.02-1.5). According to the crude oil recovery method, the viscosity of the heavy oil which is provided with a dynamic viscosity not less than 1000mPa*s after degassing and dewatering at a temperature of 50 DEG C can be reduced without additional hydrogen donors or oxygen donors, the catalytic viscosity reduction effects are good, and the obtained blending diluting oil can be injected into the crude oil to a certain scale to achieve diluted oil recovery. Meanwhile, the method does not require any other additives, achieves the aim of preparing the blending diluting oil in a short time and at a low temperature and a low pressure, solves the problem of thin oil scarcity of certain oil fields and is applicable to the practical application of oil fields.
Description
Technical field
The present invention relates to a kind of exploitation method of crude oil production method, particularly underground viscous crude.
Background technology
In world petroleum resource, the oil in place of viscous crude is considerably beyond the reserves of conventional crude, along with oil demand constantly increases, and the gradually minimizing of conventional crude resource, be worth so that viscous crude has had very large exploitation, the output of viscous crude also increases gradually in the world oil exploitation.But resin and asphalt content is higher so that its viscosity and freezing point are higher in the viscous crude, causes the exploitation of viscous crude and refining difficulty to become large.
Because the high viscosity of viscous crude, viscous crude is mobile variation in exploitation and the defeated process of collection, and flow resistance increases, and the long distance of the lifting of pit shaft and oil pipe is carried and all become very difficult.The main exploitation method of viscous crude comprises steam soak, steam flooding and mixes the thin oil method at present, but because the difference of viscous crude and vapour density and viscosity, reduced the sweep efficiency of steam soak, steam flooding, simultaneously the exploitation method of steam soak and steam flooding is subject to the restriction of reservoir depth and consumes energy hugely, and cost is also high; Mix the thin oil extraction system and can reduce viscosity of thickened oil and density, but some oil field is neighbouring without the thin oil source, mixes the thin oil method and implements also cumbersome.
Can carry out by the viscous crude that exploitation is obtained catalytic viscosity reduction to obtain can be used for the rare thin oil of lifting thickened oil, as proposed the method for the hydrothermal cracking viscosity reduction of viscous crude people such as eighties Canada scientist Hyne, namely in steam injection, add some catalyzer, these catalyzer can in the heavy component cracking of catalysis viscous crude under the hydrothermal condition, make the viscosity of thickened oil reduction and be easy to exploitation.They have also studied the metal ions such as nickel, molybdenum, copper, zinc, manganese and iron under simulation steam injection condition, to Canada and the reaction of heavy crude oils of Venezuela hydrothermal cracking and catalyzing.CN1915488A discloses the catalyzer that a kind of thick oil underground well aquathermolysis catalytic viscosity reduction is used, this catalyzer is made by Alusil or alumina, clay and solid super-strong acid mixing, the condition of reaction comprises that temperature is that 280 ℃, time are that 36h and pressure are high pressure, is about 60% to the viscosity break ratio of viscous crude; CN101570684A discloses a kind of catalytic thinner of the thick oil underground well hydrothermal cracking of being made by molybdenum salt, distilled water and aqueous slkali and aromatic ring acid, the condition of reaction comprises that temperature is that 180-280 ℃, time are that 24-48h and pressure are high pressure, is about 90% to the viscosity break ratio of general viscous crude and super viscous crude.More than these thick oil hydrothermal solution catalytic viscosity reductions react general reaction time long (more than the 24h), reaction pressure high (more than the 6MPa).And the disclosed viscosity reducing process of CA1195639 and CN101649734A needs very high reaction temperature (more than 370 ℃), and energy consumption is large.
US4743357 discloses a kind of employing ferrous iron or ferric oxide, sulfide and sulfate are catalyzer, under the effect of added hydrogen thick oil hydrothermal is cracked into light hydrocarbon; US5269909 discloses a kind of employing nickel, molybdenum is catalyzer, the technique of hydrothermal catalytic cracking viscous crude under the atmosphere of methane, hydrogen; CN101440275A discloses a kind of oxidative thinner for heavy oil exploitation via steam injection, this oxidative thinner with peroxide, organic acid transition metal salt, phosphate and alkaline matter as the thinner component.All need outer hydrogenation, methane etc. when coming the viscous crude catalytic viscosity reduction with above-mentioned catalyzer or thinner, perhaps need add hydrogen supply agent or oxygenate, implement relatively difficulty, and the reaction time is also longer.
Therefore, research is carried out the catalytic pyrolysis upgrading with the reduction viscosity of thickened oil to viscous crude at short notice and under relatively mild condition, thereby the thin oil of the rare usefulness of preparation lifting thickened oil becomes very important.
Summary of the invention
The objective of the invention is provides a kind of crude oil production method in order to overcome the deficiencies in the prior art.
To achieve these goals, the invention provides a kind of crude oil production method, the method may further comprise the steps:
(1) a kind of mixture is placed under the condition of the heavy component generation catalytic pyrolysis that makes viscous crude and react, described mixture is comprised of viscous crude, catalyzer and water, the weight ratio of described viscous crude, catalyzer and water is 1: 0.00004-0.01: 0.02-1.5, described catalyzer is one or more in the compound of iron content, cobalt, nickel, vanadium, molybdenum, manganese, copper and zinc, the condition of described reaction comprises that temperature is that 160-320 ℃, pressure are that 0.4-6MPa and time are 30-200min, and the dynamic viscosity of described viscous crude after 50 ℃ of lower degassed dehydrations is not less than 1000mPas;
(2) step (1) reaction products therefrom is rare with oil injection oil well, the crude oil in the extraction oil well as mixing.
Pass through technique scheme, need not extra hydrogen supply agent or oxygenate and can be reduced in the viscosity that 50 ℃ of dynamic viscosities after the lower degassed dehydration are not less than the viscous crude of 1000mPas, the catalytic viscosity reduction effect is better, can inject crude oil according to certain ratio with oil and realizes mixing the thin oil exploitation thereby mixing of obtaining is rare.And method of the present invention need not to add other additives, realized that under short period, lower temperature and pressure preparation mixes rare purpose with oil, solved the rare difficult problem in thin oil source, part oil field, and is easy to operate, is suitable for oil field practice application.
Other features and advantages of the present invention will partly be described in detail in the specific embodiment subsequently.
The specific embodiment
Below the specific embodiment of the present invention is elaborated.Should be understood that the specific embodiment described herein only is used for description and interpretation the present invention, is not limited to the present invention.
Oil extraction method provided by the invention may further comprise the steps:
(1) a kind of mixture is placed under the condition of the heavy component generation catalytic pyrolysis that makes viscous crude and react, described mixture is comprised of viscous crude, catalyzer and water, the weight ratio of described viscous crude, catalyzer and water is 1: 0.00004-0.01: 0.02-1.5, be preferably 1: 0.00008-0.005: 0.05-0.7, described catalyzer is one or more in the compound of iron content, cobalt, nickel, vanadium, molybdenum, manganese, copper and zinc, the condition of described reaction comprises that temperature is 160-320 ℃, is preferably 160-300 ℃; Pressure is 0.4-6MPa, is preferably 0.4-5MPa; Time is 30-200min, is preferably 45-160min; The dynamic viscosity of described viscous crude after 50 ℃ of lower degassed dehydrations is not less than 1000mPas;
(2) step (1) reaction products therefrom is rare with oil injection oil well, the crude oil in the extraction oil well as mixing.
Among the present invention, the order by merging of described viscous crude, catalyzer and water is not had particular determination, both can first catalyzer and viscous crude be mixed, add again entry; Also can first catalyzer be well dispersed in the water, contact with viscous crude again.Consider first catalyzer to be mixed with water more to be conducive to viscous crude and to mix with the even of catalyzer, and then be conducive to the carrying out of catalytic cracking reaction, under the preferable case, first catalyzer is well dispersed in the water, contact with viscous crude again.
Among the present invention, as long as with iron, cobalt, nickel, vanadium, molybdenum, manganese, in the compound of copper and zinc one or more can be realized purpose of the present invention as catalyzer, under the preferable case, described catalyzer is the oxide of iron, the oxide of cobalt, the oxide of nickel, the oxide of vanadium, the oxide of molybdenum, the oxide of manganese, the oxide of copper, the oxide of zinc, molysite, cobalt salt, nickel salt, vanadic salts, molybdenum salt, manganese salt, in mantoquita and the zinc salt one or more, more preferably iron, nickel, the sulfate of vanadium and molybdenum, nitrate, in chloride and the acylate one or more.
Further under the preferable case, described catalyzer is sulfate and/or acylate, the sulfate of molybdenum and/or the mixed catalyst of acylate that contains vanadic sulfate, iron, the sulfate of the sulfate of described vanadic sulfate, iron and/or acylate, molybdenum and/or the weight ratio of acylate are 1: 0.5-2.1: 0.7-1.1 is preferably 1: 1.0-2.1: 0.85-1.1.The present inventor finds, selects above-mentioned preferred mixed catalyst to can further improve viscosity break ratio, obtain dynamic viscosity significantly lower mix rare with oil.
The acylate of described iron can be the acylate of the various iron in the conventional catalyst of this area, is preferably carbon number at the organic carboxylate of the iron of 3-20, more preferably iron naphthenate.The acylate of described molybdenum can be the acylate of the various molybdenums in the conventional catalyst of this area, is preferably carbon number at the organic carboxylate of the molybdenum of 15-25, more preferably the oleic acid molybdenum.
Described mixed catalyst can also contain the nitrate of nickel, and the weight ratio of the nitrate of described vanadic sulfate and described nickel is 1: 2.2-2.8 is preferably 1: 2.3-2.6.
Among the present invention, described water can be in deionized water, distilled water and the salt solution one or more, and the salinity of described salt solution is less than 40000mg/L and Ca wherein
2+And Mg
2+Total concentration less than 1000mg/L.
Among the present invention, described reaction can be divided into two stages to be carried out, and comprises first stage of reaction and second stage of reaction, and it is that 160-320 ℃, pressure are that 0.4-6MPa and time are 20-60min that the condition of described first stage of reaction preferably includes temperature; It is that 160-320 ℃, time are 10-140min that the condition of described second stage of reaction preferably includes temperature, and the low 0.2-2MPa of the pressure of pressure ratio first stage of reaction of second stage of reaction, and the pressure of second stage of reaction is 0.2-4MPa.The temperature and time of described first stage of reaction and second stage of reaction can be identical or different separately, as long as in above-mentioned scope.
Described first stage of reaction and second stage of reaction can be carried out in same reactor, also can in the differential responses still, carry out, when in different reactors, carrying out, conveniently control on the one hand reaction condition, high-temperature high-voltage reaction is concentrated on the first reactor, operate the continuous processing that can improve production capacity and be conducive to realize reducing thick oil viscosity by two stills in addition, therefore preferably in the differential responses still, carry out first stage of reaction and second stage of reaction.
Among the present invention, described crude oil can be not less than for the dynamic viscosity after 50 ℃ of lower degassed dehydrations the crude oil underground viscous crude namely to be exploited of 1000mPas.The dynamic viscosity of described viscous crude after 50 ℃ of lower degassed dehydrations can be 1000-12500mPas.Can use the equipment such as gs-oil separator, settling tank and electric dehydrator that oil product to be measured is carried out degassed dehydration, dynamic viscosity records with rotation viscometer.
Among the present invention, described method can also comprise carries out catalytic pyrolysis again with step (1) reaction products therefrom, described method of carrying out again catalytic pyrolysis can be selected method well-known to those skilled in the art according to dynamic viscosity, also can select catalytic cracking method in the step of the present invention (1).Under the preferable case, described method also comprises distills step (1) reaction products therefrom, and the collection boiling range is the light ends below 300 ℃, and this light ends is rare with the oily step (2) that is used for as mixing.
Among the present invention, by step (1), the viscosity of viscous crude is reduced to below the 1000mPas usually, meets present conduct and mixes rare requirement with oil, therefore, can directly be injected in the oil well, realizes mixing the thin oil exploitation.
Among the present invention, described oil recovery can be carried out according to method well-known to those skilled in the art, for example, can the described oily well wellbore that injects of rare usefulness of mixing be contacted with crude oil by pit shaft thin oil input pipe, crude oil is mixed its viscosity of rare reduction, again by the crude oil efferent duct with Crude Oil Transportation out.
Below will describe the present invention by embodiment.In following examples, viscous crude derives from Shengli Oil Field; Dynamic viscosity is passed through rotation viscometer (Thermo Scientific companies for testing sample oil is carried out after the degassed dehydration under 50 ℃, model is HAAKE Viscotester 550, rotor is RotorMV2, rotating speed is 6r/min) dynamic viscosity that records, assay method reference standard SYT 6316-1997, the method of degassed dehydration is: the demulsifier (Shengli Chemical Company Ltd. Of Slof. that adds 15wppm in testing sample oil, SX-4056), 80 ℃ of shaking bath 12h pour out the water of sample oil bottom after processing.
Embodiment 1
First the agent of 1.08g Catalyzed by Nickel Sulfate is added in the 2.16g deionized water, again this mixture and 108g viscous crude (dynamic viscosity after 50 ℃ of lower degassed dehydrations is 2310mPas) are added in the 300mL reactor, reactant is heated to 160 ℃, keep reaction pressure at 6MPa, stirring reaction 200min.Recording the dynamic viscosity of reaction afterproduct oil after 50 ℃ of lower degassed dehydrations is 821mPas, and it is rare with oil injection oil well, the crude oil in the extraction oil well as mixing.
Embodiment 2
First the 0.01g ferrous sulfate catalyst is added in the 375g deionized water, again this mixture and 250g viscous crude (dynamic viscosity after 50 ℃ of lower degassed dehydrations is 2310mPas) are added in the 1L reactor, reactant is heated to 320 ℃, keep reaction pressure at 0.4MPa, stirring reaction 30min.Recording the dynamic viscosity of reaction afterproduct oil after 50 ℃ of lower degassed dehydrations is 847mPas, and it is rare with oil injection oil well, the crude oil in the extraction oil well as mixing.
Embodiment 3
First 0.25g ferrous sulfate, 0.12g vanadic sulfate and 0.13g molybdenum trisulfate catalyzer are added in the 28.8g deionized water, again this mixture and 120.1g viscous crude (dynamic viscosity after 50 ℃ of lower degassed dehydrations is 3470mPas) are added in the 300mL reactor, reactant is heated to 265 ℃, keep reaction pressure at 4MPa, stirring reaction 100min.Recording the dynamic viscosity of reaction afterproduct oil after 50 ℃ of lower degassed dehydrations is 283mPas, and it is rare with oil injection oil well, the crude oil in the extraction oil well as mixing.
Embodiment 4
Method according to embodiment 3 is carried out oil extraction, and different is that as catalyzer, recording the dynamic viscosity of reaction afterproduct oil after 50 ℃ of lower degassed dehydrations is 775mPas with " 0.12g vanadic sulfate ".
Embodiment 5
Method according to embodiment 3 is carried out oil extraction, and different is that as catalyzer, recording the dynamic viscosity of reaction afterproduct oil after 50 ℃ of lower degassed dehydrations is 459mPas with " 0.25g ferrous sulfate and 0.12g vanadic sulfate ".
Embodiment 6
First 0.25g nickel nitrate, 0.10g vanadic sulfate, 0.08g oleic acid molybdenum and 0.06g iron naphthenate catalyzer are added in the 26.3g distilled water, again this mixture and 110.3g viscous crude (dynamic viscosity after 50 ℃ of lower degassed dehydrations is 7650mPas) are added in the 300mL reactor, reactant is heated to 200 ℃, keep reaction pressure at 2.2MPa, stirring reaction 120min.Recording the dynamic viscosity of reaction afterproduct oil after 50 ℃ of lower degassed dehydrations is 735mPas, and it is rare with oil injection oil well, the crude oil in the extraction oil well as mixing.
Embodiment 7
Method according to embodiment 6 is carried out oil extraction, different is, as catalyzer, recording the dynamic viscosity of reaction afterproduct oil after 50 ℃ of lower degassed dehydrations is 860mPas with " 0.06g frerrous chloride, 0.25g nickel chloride, 0.08g ammonium molybdate and 0.10 citric acid vanadium ".
Embodiment 8
First 0.08g ferrous nitrate catalyzer is added in the 52.1g distilled water, again this mixture and 96.6g viscous crude (dynamic viscosity after 50 ℃ of lower degassed dehydrations is 2685mPas) are added in the 300mL reactor, reactant is heated to 180 ℃, keep reaction pressure at 1.2MPa, stirring reaction 90min, recording the dynamic viscosity of reaction afterproduct oil after 50 ℃ of lower degassed dehydrations is 985mPas, temperature with reactor is increased to 320 ℃ again, the collection boiling range is the light ends below 300 ℃, recording the dynamic viscosity of this light ends after 50 ℃ of lower degassed dehydrations is 26.8mPas, it is rare with oil injection oil well, the crude oil in the extraction oil well as mixing.
Embodiment 9
First 0.1g nickel nitrate catalyzer is added in the 25.6g salt solution salinity 12400mg/L of salt solution, wherein Ca
2+, Mg
2+The total concentration of two kinds of ions is less than 600mg/L, again this mixture and 147.5g viscous crude (dynamic viscosity after 50 ℃ of lower degassed dehydrations is 3825mPas) are added in the 300mL reactor, reactant is heated to 220 ℃, keep reaction pressure at 3MPa, stirring reaction 70min, recording the dynamic viscosity of reaction afterproduct oil after 50 ℃ of lower degassed dehydrations is 990mPas, temperature with reactor is increased to 320 ℃ again, the collection boiling range is the light ends below 300 ℃, recording the dynamic viscosity of this light ends after 50 ℃ of lower degassed dehydrations is 25.3mPas, it is rare with oil injection oil well, the crude oil in the extraction oil well as mixing.
Embodiment 10
First with the 0.15g frerrous chloride, 0.09g nickel chloride, 0.04g ammonium molybdate, 0.03 the citric acid vanadium catalyst adds in the 12.7g deionized water, again this mixture and 113.5g viscous crude (dynamic viscosity after 50 ℃ of lower degassed dehydrations is 5643mPas) are added in the 300mL reactor, reactant is heated to 250 ℃, keep reaction pressure at 3.5MPa, stirring reaction 100min, recording the dynamic viscosity of reaction afterproduct oil after 50 ℃ of lower degassed dehydrations is 982mPas, temperature with reactor is increased to 320 ℃ again, the collection boiling range is the light ends below 300 ℃, recording the dynamic viscosity of this light ends after 50 ℃ of lower degassed dehydrations is 28.7mPas, it is rare with oil injection oil well, the crude oil in the extraction oil well as mixing.
Embodiment 11
First with the 0.15g frerrous chloride, 0.09g nickel chloride, 0.04g ammonium molybdate and 0.03 citric acid vanadium catalyst add in the 12.7g deionized water, again this mixture and 113.5g viscous crude (dynamic viscosity after 50 ℃ of lower degassed dehydrations is 5852mPas) are added in the 300mL reactor, temperature in the control reactor is 320 ℃, pressure is 0.4MPa, stirring reaction 50min, product is moved in another 300mL reactor, the temperature of controlling in this reactor is 280 ℃, pressure is 0.2MPa, stirring reaction 50min, recording the dynamic viscosity of reaction afterproduct oil after 50 ℃ of lower degassed dehydrations is 978mPas, temperature with reactor is increased to 320 ℃ again, the collection boiling range is the light ends below 300 ℃, recording the dynamic viscosity of this light ends after 50 ℃ of lower degassed dehydrations is 24.6mPas, it is rare with oil injection oil well, the crude oil in the extraction oil well as mixing.
Embodiment 12
Method according to embodiment 11 is carried out oil extraction, different is: the temperature of control in the reactor is that 160 ℃, pressure are 6MPa, stirring reaction 20min, after moving into product in another 300mL reactor, controlling temperature in this reactor and be 160 ℃, pressure is 4MPa, stirring reaction 140min, recording the dynamic viscosity of reaction afterproduct oil after 50 ℃ of lower degassed dehydrations is 955mPas, recording the dynamic viscosity of light ends after 50 ℃ of lower degassed dehydrations is 24.2mPas.
Embodiment 13
Method according to embodiment 11 is carried out oil extraction, different is: the temperature of control in the reactor is that 200 ℃, pressure are 4MPa, stirring reaction 60min, product is moved in another 300mL reactor, controlling temperature in this reactor and be 320 ℃, pressure is 2.5MPa, stirring reaction 10min, recording the dynamic viscosity of reaction afterproduct oil after 50 ℃ of lower degassed dehydrations is 878mPas, recording the dynamic viscosity of light ends after 50 ℃ of lower degassed dehydrations is 23.7mPas.
As can be seen from the above embodiments, the present invention need not extra hydrogen supply agent or oxygenate and obtained mixing rare oil of using under relatively mild condition, and easy to operate, the reaction time is short, and energy consumption is low, has guaranteed again to mix rare with oily quality simultaneously.When using the preferred mixed catalyst of the present invention, can obtain dynamic viscosity lower mix rare with oil.Thereby can solve to a certain extent the rare difficult problem in thin oil source, part oil field, promote to mix the application of thin oil exploitation method in the oil field.
More than describe preferred embodiment of the present invention in detail; but the present invention is not limited to the detail in the above-mentioned embodiment, in technical conceive scope of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.
Need to prove in addition, each concrete technical characterictic described in the above-mentioned specific embodiment in reconcilable situation, can make up by any suitable mode, for fear of unnecessary repetition, the present invention is to the no longer separately explanation of various possible combinations.
In addition, also can carry out any combination between the various embodiment of the present invention, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (10)
1. crude oil production method, the method may further comprise the steps:
(1) a kind of mixture is placed under the condition of the heavy component generation catalytic pyrolysis that makes viscous crude and react, described mixture is comprised of viscous crude, catalyzer and water, the weight ratio of described viscous crude, catalyzer and water is 1: 0.00004-0.01: 0.02-1.5, described catalyzer is one or more in the compound of iron content, cobalt, nickel, vanadium, molybdenum, manganese, copper and zinc, the condition of described reaction comprises that temperature is that 160-320 ℃, pressure are that 0.4-6MPa and time are 30-200min, and the dynamic viscosity of described viscous crude after 50 ℃ of lower degassed dehydrations is not less than 1000mPas;
(2) step (1) reaction products therefrom is rare with oil injection oil well, the crude oil in the extraction oil well as mixing.
2. method according to claim 1, wherein, the weight ratio of described viscous crude, catalyzer and water is 1: 0.00008-0.005: 0.05-0.7.
3. method according to claim 1 and 2, wherein, described catalyzer is one or more in oxide, molysite, cobalt salt, nickel salt, vanadic salts, molybdenum salt, manganese salt, mantoquita and the zinc salt of oxide, zinc of oxide, the copper of oxide, the manganese of oxide, the molybdenum of oxide, the vanadium of oxide, the nickel of oxide, the cobalt of iron.
4. the described method of any one according to claim 1-3, wherein, described catalyzer is one or more in sulfate, nitrate, chloride and the acylate of iron, nickel, vanadium and molybdenum.
5. the described method of any one according to claim 1-4, wherein, described catalyzer is sulfate and/or acylate, the sulfate of molybdenum and/or the mixed catalyst of acylate that contains vanadic sulfate, iron, and the sulfate of the sulfate of described vanadic sulfate, iron and/or acylate, molybdenum and/or the weight ratio of acylate are 1: 0.5-2.1: 0.7-1.1.
6. method according to claim 5, wherein, described mixed catalyst also contains the nitrate of nickel, and the weight ratio of the nitrate of described vanadic sulfate and described nickel is 1: 2.2-2.8.
7. method according to claim 1 and 2, wherein, described water is one or more in deionized water, distilled water and the salt solution, the salinity of described salt solution is less than 40000mg/L and Ca wherein
2+And Mg
2+Total concentration less than 1000mg/L.
8. method according to claim 1, wherein, the condition of described reaction comprises that temperature is that 160-300 ℃, pressure are that 0.4-5MPa and time are 45-160min.
9. method according to claim 1, wherein, described reaction comprises first stage of reaction and second stage of reaction, the condition of described first stage of reaction comprises that temperature is that 160-320 ℃, pressure are that 0.4-6MPa and time are 20-60min; The condition of described second stage of reaction comprises that temperature is that 160-320 ℃, time are 10-140min, and the low 0.2-2MPa of the pressure of pressure ratio first stage of reaction of second stage of reaction.
10. method according to claim 1, wherein, described method also comprises distills step (1) reaction products therefrom, collects boiling range and be the light ends below 300 ℃, and with this light ends as mix rare with oil for step (2).
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| CN104565824A (en) * | 2014-12-22 | 2015-04-29 | 山东东明石化集团有限公司 | Long-distance pipeline normal-temperature Merey crude oil mixing and conveying method |
| CN104565824B (en) * | 2014-12-22 | 2016-03-02 | 山东东明石化集团有限公司 | A kind of long-distance pipe normal temperature mixes the method for the auspicious crude oil of defeated agate |
| CN112324409A (en) * | 2020-12-31 | 2021-02-05 | 西南石油大学 | Method for producing solvent in situ in oil layer to recover thick oil |
| US11391128B1 (en) | 2020-12-31 | 2022-07-19 | Southwest Petroleum University | Method for producing heavy oil by generating solvents in situ in the reservoir |
| CN115895628A (en) * | 2021-08-26 | 2023-04-04 | 中国石油化工股份有限公司 | Thick oil viscosity reducer and preparation method and application thereof |
| CN115895628B (en) * | 2021-08-26 | 2024-05-28 | 中国石油化工股份有限公司 | Thickened oil viscosity reducer and preparation method and application thereof |
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