CN114989854A - Method for improving yield of light oil produced by oil shale pyrolysis - Google Patents
Method for improving yield of light oil produced by oil shale pyrolysis Download PDFInfo
- Publication number
- CN114989854A CN114989854A CN202210827680.9A CN202210827680A CN114989854A CN 114989854 A CN114989854 A CN 114989854A CN 202210827680 A CN202210827680 A CN 202210827680A CN 114989854 A CN114989854 A CN 114989854A
- Authority
- CN
- China
- Prior art keywords
- oil shale
- oil
- yield
- pyrolysis
- supercritical water
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- 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
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
- C10G1/065—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation in the presence of a solvent
-
- 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
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
- C10G1/083—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts in the presence of a solvent
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a method for improving the yield of light oil produced by oil shale pyrolysis, and belongs to the technical field of oil shale pyrolysis. In the oil shale pyrolysis process, supercritical water is continuously introduced, the supercritical water carries transition metals to enter an oil shale pore structure to cooperatively catalyze the pyrolysis of the oil shale, and a cosolvent is added in the pyrolysis process, so that the miscible phase pressure formed by the transition metals carried by the supercritical water and the oil shale is reduced, the activation energy of the pyrolysis reaction is reduced, and the mass transfer and heat transfer rate is accelerated. The supercritical water and the transition metal catalyst can promote the cracking of macromolecular heavy oil and inhibit condensation reaction, and the transition metal can provide a hydrogenation reaction active site, so that the aim of improving the yield of the oil shale pyrolysis light oil is fulfilled.
Description
Technical Field
The invention belongs to the technical field of oil shale pyrolysis, and particularly relates to a method for producing light oil by pyrolyzing oil shale.
Background
The oil shale is the most important unconventional resource in China, has wide distribution range and rich reserves, has better oil quality of the oil shale, and is an important supplementary energy source of petroleum.
Supercritical water (Tc =373.946 ℃, Pc =22.064 MPa) exhibits physical, chemical properties that are very different from normal. Has the advantages of low cost, no toxicity and no pollution. Supercritical water is generally used in three aspects of extraction, pyrolysis, oxidation and gasification. Some researches show that coal molecules in a supercritical water environment are firstly pyrolyzed to generate free radicals, and water molecules participate in the reaction, so that the generated molecular fragments can supplement hydrogen atoms and oxygen atoms in the reaction; the solvent effect of supercritical water also enables the intermediate product to be dispersed, thereby reducing the probability of formation of polycondensation reaction, reducing the coking behavior in the thermal reaction under the traditional inert atmosphere and improving the yield of light oil. The supercritical water has the advantages of low viscosity and high diffusion coefficient, and can be used as an excellent mass transfer solvent. Because of its many advantages, supercritical water is widely used in organic chemical reactions, extraction of natural organic matter, catalytic viscosity reduction of heavy oil, and hydrothermal liquefaction of biomass.
At present, in the research on the quality improvement of oil shale pyrolysis oil, the yield of the maltha Hosseipour et al, which is obtained by performing a catalytic hydrogenation experiment by using supercritical water, can reach 72%; the proportion of light oil in the pyrolysis oil obtained by injecting superheated steam into the Congestion et al to pyrolyze the oil shale reaches 72.51 percent. The yield of light oil in the above studies is not ideal enough, and there is a need for optimization and improvement of the method for pyrolyzing light oil by oil shale.
Disclosure of Invention
Based on the problems in the prior art, the invention aims to provide a method for improving the yield of light oil produced by oil shale pyrolysis.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows: a method for improving the yield of light oil produced by oil shale pyrolysis comprises the following steps:
placing a screened oil shale sample and a cosolvent into a reaction kettle, and vacuumizing the reaction kettle;
continuously introducing supercritical water dissolved with a catalyst into a reaction kettle, controlling the temperature of the reaction kettle to be 500-600 ℃, the pressure to be 23-26 MPa, and controlling the reaction time to be 1-3 h;
and step three, after the reaction is finished, cooling the reaction kettle to room temperature, and collecting the oil shale pyrolysis oil.
Further, the cosolvent in the step one is one or more of ethanol, acetic acid, ethyl acetate, isopropanol, isooctanol and acetone, and the purity is analytical purity.
Further, the catalyst in the second step is one or more of soluble acetate, sulfate and nitrate of Fe, Ni, Co, Mn and V.
Further, dissolving a catalyst in ultrapure water in advance, preparing the catalyst into a supercritical state by using a steam generator, and obtaining supercritical water dissolved with the catalyst in the second step, wherein the temperature of the supercritical water is controlled to be 500-600 ℃, and the pressure is controlled to be 23-26.0 MPa.
Further, the mass ratio of the ultrapure water to the oil shale sample is (30-50): 1.
further, the mass ratio of the cosolvent to the oil shale sample is (1-3): 1.
further, the mass ratio of the catalyst to the oil shale is (0.8-1.2): 1.
further, in the step one, the oil shale is crushed and sieved to be 5-20 mm.
According to the method for improving the yield of the light oil produced by pyrolyzing the oil shale, supercritical water is utilized to cooperate with a catalyst to pyrolyze the oil shale, meanwhile, the supercritical water can carry transition metals to enter the oil shale for reaction, and a cosolvent is added in the pyrolysis process, so that the mixed phase pressure formed by the supercritical water carrying the transition metals and the oil shale is reduced, the activation energy of the pyrolysis reaction is reduced, and the pyrolysis speed is accelerated. The supercritical water synergistic catalyst can promote the cracking of macromolecular heavy oil and inhibit condensation reaction, and the transition metal can provide a hydrogenation reaction active site, so that the aim of improving the yield of the oil shale pyrolysis light oil is fulfilled. The method can lead the yield of the light oil for pyrolyzing the oil shale to reach more than 75 percent.
Drawings
FIG. 1 is a flow chart of the method for increasing the yield of light oil from oil shale pyrolysis according to the invention.
FIG. 2 is a schematic diagram of an experimental apparatus for the method for increasing yield of light oil from oil shale pyrolysis.
FIG. 3 is a bar graph comparing the yield of light oil and the improvement effect compared to the conventional dry distillation in each example.
FIG. 4 is a bar graph comparing the effect of increasing the yield of light oil obtained in example 8 with that of comparative examples 1 and 2.
In the figure: 1-a thermometer; 2-a pressure gauge; 3-supercritical water with catalyst; 4-a steam generator; 5-a reaction kettle; 6-a cosolvent; 7-oil shale sample; 8-a valve; 9-cold water bath device.
Detailed Description
Referring to fig. 1, an exemplary embodiment of the present invention provides a method for increasing yield of light oil from oil shale pyrolysis, comprising the following steps:
placing the screened oil shale sample and the cosolvent into a reaction kettle, and vacuumizing the reaction kettle.
Wherein, the cosolvent is one or more of ethanol, acetic acid, ethyl acetate, isopropanol, isooctanol and acetone, and the purity is analytical purity. The cosolvent has the function of reducing the pressure of a mixed phase formed by supercritical water carrying the transition metal catalyst and the oil shale. The cosolvent and the supercritical water are mutually soluble at a set temperature and pressure, and are promoted to form a mixed phase with the oil shale. After supercritical water, cosolvent and oil shale reach the miscible phase, can increase the contact area of reaction, reduce the activation energy of oil shale pyrolysis.
The oil shale is crushed and sieved to be 5-20 mm, for example: 5mm, 8mm, 10mm, 15mm, 20 mm.
And step two, continuously introducing supercritical water dissolved with a catalyst into a reaction kettle, controlling the temperature of the reaction kettle to be 500-600 ℃, controlling the pressure to be 23-26 MPa, and controlling the reaction time to be 1-3 h.
Wherein the catalyst is one or more of soluble acetate, sulfate and nitrate of Fe, Ni, Co, Mn and V. The catalyst can reduce the activation energy of oil shale pyrolysis, and the metal compounds can play a stable catalytic role in supercritical water and have strong catalytic effect.
In the step, a catalyst is dissolved in ultrapure water in advance, a steam generator is used for preparing the catalyst into a supercritical state, supercritical water with the catalyst dissolved in the step two is obtained, the temperature of the supercritical water is controlled to be 500-600 ℃, and the pressure is controlled to be 23-26.0 MPa.
Dissolving the catalyst in water in advance, and introducing supercritical water to the reaction kettle to catalyze the pyrolysis of the oil shale. The carrying effect of the supercritical water increases the contact area of the catalyst and the oil shale, and can better achieve the purpose of reducing the reaction activation energy.
The temperature of the supercritical water is controlled to be 500-600 ℃, the pressure is 23-26 MPa, and the temperature is the same as or similar to the temperature controlled by the reaction kettle. And continuously introducing supercritical water in the controlled reaction time to maintain the temperature and the pressure in the reaction kettle. Supercritical water can promote the cracking of macromolecular heavy oil and inhibit condensation reaction. Too high supercritical water temperature can lead to further cracking of small molecule compounds, resulting in increased gas phase products, thereby reducing the yield of light oil.
And step three, after the reaction is finished, cooling the reaction kettle to room temperature, and collecting the oil shale pyrolysis oil. Then, the component analysis was performed to calculate the yield of light oil.
The light oil of the invention refers to a hydrocarbon mixture with a boiling point of less than 260 ℃. In order to fully exert the functions of the supercritical water, the cosolvent and the catalyst, the mass ratio of the ultrapure water to the oil shale sample is (30-50): 1, the mass ratio of the cosolvent to the oil shale sample is (1-3): 1, the mass ratio of the catalyst to the oil shale is (0.8-1.2): 1.
in the oil shale pyrolysis process, supercritical water is continuously introduced, the supercritical water carries transition metals to enter an oil shale pore structure to cooperatively catalyze the pyrolysis of the oil shale, and a cosolvent is added in the pyrolysis process, so that the miscible phase pressure formed by the transition metals carried by the supercritical water and the oil shale is reduced, the activation energy of the pyrolysis reaction is reduced, and the mass transfer and heat transfer rate is accelerated. The supercritical water and the transition metal catalyst can promote the cracking of macromolecular heavy oil and inhibit condensation reaction, and the transition metal can provide a hydrogenation reaction active site, so that the aim of improving the yield of the oil shale pyrolysis light oil is fulfilled. The invention provides reference for the theory of oil shale pyrolysis heavy oil lightening.
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail below with reference to some specific embodiments. The examples and comparative examples described herein are intended to illustrate the invention and are not intended to limit the invention.
The oil shale sample employed in the examples below was gibbosa oil shale. For the sake of convenience of calculation, the mass of the oil shale samples used in the experiment was 100 g.
Calculation formula of light oil yield:
light oil yield = W Pyrolytic light oil / W Pyrolysis oil
In the formula, W Pyrolytic light oil Denotes the mass of light oil in the pyrolysis oil, W Pyrolysis oil Representing the total mass of pyrolysis oil.
The yield of light oil obtained by ordinary dry distillation is 60%.
Referring to fig. 2, the oil shale pyrolysis apparatus employed in the following examples includes a steam generator 4, a reaction kettle 5, and a cold water bath device 9, which are connected in order by pipes. The steam generator 4 and the reaction kettle 5 are respectively provided with a thermometer 1 and a pressure gauge 2. The catalyst is dissolved in ultrapure water in advance, supercritical water 3 with the catalyst is prepared in a steam generator 4, and an oil shale sample 7 and a cosolvent 6 are placed in a reaction kettle 5. The cold water bath device 9 is used for collecting the oil shale pyrolysis oil.
The claimed solution is further illustrated by the following examples. However, the examples and comparative examples are intended to illustrate the embodiments of the present invention without departing from the scope of the subject matter of the present invention, and the scope of the present invention is not limited by the examples. Unless otherwise specifically indicated, the materials and reagents used in the present invention are available from commercial products in the art.
Example 1
Crushing and screening oil shale into 5mm, weighing 100g of oil shale sample and 100g of acetone, placing the oil shale sample and the acetone into a reaction kettle, and vacuumizing the reaction kettle;
80g of catalyst C 4 H 6 CoO 4 ·4(H 2 O) is dissolved in 3000g of ultrapure water, and is prepared into a supercritical state by a steam generator to form supercritical water with a catalyst, the temperature is controlled at 500 ℃, the pressure is controlled at 23MPa, and the supercritical water is introduced into a reaction kettle to react for 1 hour;
and after the reaction is finished, cooling the reaction kettle to room temperature, collecting the oil shale pyrolysis oil, performing component analysis, and calculating the yield of the light oil. As a result, the yield of light oil was 78%. Compared with the common dry distillation, the yield is improved by 30 percent.
Example 2
Crushing and screening oil shale into 20mm, weighing 100g of oil shale sample and 200g of ethanol, placing the oil shale sample and the ethanol in a reaction kettle, and vacuumizing the reaction kettle;
100g of catalyst NiSO 4 Dissolving in 4000g of ultrapure water, preparing the ultrapure water into a supercritical state by using a steam generator to obtain supercritical water with a catalyst, controlling the temperature to be 550 ℃ and the pressure to be 24MPa, introducing the supercritical water into a reaction kettle, and reacting for 2 hours;
and after the reaction is finished, cooling the reaction kettle to room temperature, collecting the oil shale pyrolysis oil, performing component analysis, and calculating the yield of the light oil. As a result, the yield of light oil was 82%. Compared with the common dry distillation, the yield is improved by 37 percent.
Example 3
Crushing and screening oil shale into 15mm, weighing 100g of oil shale sample and 200g of ethyl acetate, placing the oil shale sample and the ethyl acetate into a reaction kettle, and vacuumizing the reaction kettle;
120g of catalyst Fe 2 (SO 4 ) 3 Dissolving in 5000g of ultrapure water, preparing the ultrapure water into a supercritical state by using a steam generator to obtain supercritical water with a catalyst, controlling the temperature to be 550 ℃ and the pressure to be 26MPa, introducing the supercritical water into a reaction kettle, and reacting for 3 hours;
and after the reaction is finished, cooling the reaction kettle to room temperature, collecting the oil shale pyrolysis oil, performing component analysis, and calculating the yield of the light oil. As a result, the yield of light oil was 86%. Compared with common dry distillation, the yield is improved by 43 percent.
Example 4
Crushing and screening the oil shale into 15mm, weighing 100g of oil shale sample and 100g of ethyl acetate, placing the oil shale sample and the ethyl acetate in a reaction kettle, and vacuumizing the reaction kettle;
80g of Catalyst (CH) 3 COO) 2 Dissolving Ni in 4000g of ultrapure water, preparing the Ni into a supercritical state by using a steam generator to obtain supercritical water with a catalyst, controlling the temperature to be 500 ℃ and the pressure to be 24MPa, introducing the supercritical water into a reaction kettle, and reacting for 1 hour;
and after the reaction is finished, cooling the reaction kettle to room temperature, collecting the oil shale pyrolysis oil, performing component analysis, and calculating the yield of the light oil. As a result, the yield of light oil was 75%. Compared with common dry distillation, the yield is improved by 25 percent.
Example 5
Crushing and screening oil shale into 15mm, weighing 100g of oil shale sample and 200g of ethanol, placing the oil shale sample and the ethanol in a reaction kettle, and vacuumizing the reaction kettle;
80g of catalyst VSO 4 ·7H 2 Dissolving O in 3000g of ultrapure water, preparing the O into a supercritical state by using a steam generator to obtain supercritical water with a catalyst, controlling the temperature to be 600 ℃ and the pressure to be 24MPa, introducing the supercritical water into a reaction kettle, and reacting for 3 hours;
and after the reaction is finished, cooling the reaction kettle to room temperature, collecting the oil shale pyrolysis oil, performing component analysis, and calculating the yield of the light oil. As a result, the yield of light oil was 85%. Compared with the common dry distillation, the yield is improved by 42 percent.
Example 6
Crushing and screening the oil shale into 15mm, weighing 100g of oil shale sample and 300g of acetone, placing the oil shale sample and the acetone into a reaction kettle, and vacuumizing the reaction kettle;
100g of catalyst C 4 H 6 CoO 4 ·4(H 2 O) is dissolved in 4000g of ultrapure water, the supercritical water is prepared into a supercritical state by a steam generator to form supercritical water with a catalyst, the temperature is controlled to be 550 ℃, the pressure is controlled to be 25MPa, and the supercritical water is introduced into a reaction kettle to react for 2 hours;
and after the reaction is finished, cooling the reaction kettle to room temperature, collecting the oil shale pyrolysis oil, performing component analysis, and calculating the yield of the light oil. As a result, the yield of light oil was 83%. Compared with the common dry distillation, the yield is improved by 38 percent.
Example 7
Crushing and screening the oil shale into 15mm, weighing 100g of oil shale sample and 300g of ethanol, placing the oil shale sample and the ethanol in a reaction kettle, and vacuumizing the reaction kettle;
120g of catalyst VSO 4 ·7H 2 Dissolving O in 5000g of ultrapure water, preparing the O into a supercritical state by using a steam generator to obtain supercritical water with a catalyst, controlling the temperature to be 500 ℃ and the pressure to be 26MPa, introducing the O into a reaction kettle, and reacting for 3 hours;
and after the reaction is finished, cooling the reaction kettle to room temperature, collecting the oil shale pyrolysis oil, performing component analysis, and calculating the yield of the light oil. As a result, the yield of light oil was 87%. Compared with common dry distillation, the yield is improved by 45%.
Example 8
Crushing and screening the oil shale into 15mm, weighing 100g of oil shale sample and 300g of ethanol, placing the oil shale sample and the ethanol in a reaction kettle, and vacuumizing the reaction kettle;
120g of catalyst C 4 H 6 CoO 4 ·4(H 2 O) is dissolved in 5000g of ultrapure water, the supercritical water with the catalyst is prepared by a steam generator to be supercritical water, the temperature is controlled to be 600 ℃, the pressure is controlled to be 26MPa, the supercritical water is introduced into a reaction kettle, and the reaction is carried out for 3 hours;
and after the reaction is finished, cooling the reaction kettle to room temperature, collecting the oil shale pyrolysis oil, performing component analysis, and calculating the yield of the light oil. As a result, the yield of light oil was 90%. Compared with common dry distillation, the yield is improved by 50%.
The light oil yield vs. ratio for examples 1-8 is shown in FIG. 3. FIG. 3 also shows the upgrading effect of examples 1-8 relative to conventional dry distillation.
Comparative example 1
No cosolvent is added, the rest reaction conditions are the same as those in the example 8, the yield of the light oil is 68 percent, and is improved by 13 percent compared with the common dry distillation. The light oil yield is improved by 32% compared with the condition after adding the cosolvent. It can be seen that the presence of the co-solvent greatly exerts the solvating effect of supercritical water, and the reduction of miscible pressure greatly promotes the pyrolysis of oil shale.
Comparative example 2
The introduced supercritical water does not carry a catalyst, and the rest reaction conditions are the same as those in the example 8, so that the yield of the light oil is 65 percent, which is improved by 8 percent compared with the common dry distillation. The yield of light oil after supercritical water carrying the catalyst is improved by 38 percent compared with the condition. Therefore, the supercritical water synergistic catalyst has a remarkable catalytic effect in the pyrolysis of the oil shale.
The light oil yields for example 8 and comparative examples 1 and 2 are shown in fig. 4.
Claims (8)
1. A method for improving the yield of light oil produced by oil shale pyrolysis is characterized by comprising the following steps: the method comprises the following steps:
placing a screened oil shale sample and a cosolvent into a reaction kettle, and vacuumizing the reaction kettle;
continuously introducing supercritical water dissolved with a catalyst into a reaction kettle, controlling the temperature of the reaction kettle to be 500-600 ℃, the pressure to be 23-26 MPa, and controlling the reaction time to be 1-3 h;
and step three, after the reaction is finished, cooling the reaction kettle to room temperature, and collecting the oil shale pyrolysis oil.
2. The method for improving the yield of light oil from oil shale pyrolysis according to claim 1, wherein: the cosolvent in the step one is one or more of ethanol, acetic acid, ethyl acetate, isopropanol, isooctanol and acetone, and the purity is analytical purity.
3. The method for improving the yield of light oil from oil shale pyrolysis according to claim 1 or 2, wherein: the catalyst in the second step is one or more of soluble acetate, sulfate and nitrate of Fe, Ni, Co, Mn and V.
4. The method for improving the yield of light oil from oil shale pyrolysis according to claim 3, wherein: and (3) dissolving a catalyst in ultrapure water in advance, and preparing the catalyst into a supercritical state by using a steam generator to obtain supercritical water dissolved with the catalyst in the second step, wherein the temperature of the supercritical water is controlled to be 500-600 ℃, and the pressure is controlled to be 23-26.0 MPa.
5. The method for improving the yield of light oil from oil shale pyrolysis according to claim 4, wherein: the mass ratio of the ultrapure water to the oil shale sample is (30-50): 1.
6. the method for improving the yield of light oil from oil shale pyrolysis according to claim 1 or 5, wherein: the mass ratio of the cosolvent to the oil shale sample is (1-3): 1.
7. the method for improving the yield of light oil from oil shale pyrolysis according to claim 6, wherein: the mass ratio of the catalyst to the oil shale is (0.8-1.2): 1.
8. the method for increasing the yield of light oil from oil shale pyrolysis according to claim 1, 2, 4, 5 or 7, characterized in that: in the first step, the oil shale is crushed and sieved to be 5-20 mm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210827680.9A CN114989854B (en) | 2022-07-14 | 2022-07-14 | Method for improving yield of light oil produced by oil shale pyrolysis |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210827680.9A CN114989854B (en) | 2022-07-14 | 2022-07-14 | Method for improving yield of light oil produced by oil shale pyrolysis |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN114989854A true CN114989854A (en) | 2022-09-02 |
| CN114989854B CN114989854B (en) | 2022-11-01 |
Family
ID=83020937
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210827680.9A Active CN114989854B (en) | 2022-07-14 | 2022-07-14 | Method for improving yield of light oil produced by oil shale pyrolysis |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114989854B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116333771A (en) * | 2023-05-10 | 2023-06-27 | 中国矿业大学 | Device and method for improving light oil yield of oil shale |
Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1688672A (en) * | 2002-09-19 | 2005-10-26 | 约翰·S·伦德尔 | Supercritical hydro extraction of kerogen and aqueous extraction of alumina and soda ash with a residue for portland cement production |
| CN101421488A (en) * | 2006-02-16 | 2009-04-29 | 雪佛龙美国公司 | Kerogen extraction from subterranean oil shale resources |
| US20090166262A1 (en) * | 2007-12-28 | 2009-07-02 | Chevron U.S.A. Inc. | Simultaneous metal, sulfur and nitrogen removal using supercritical water |
| CN101565631A (en) * | 2009-06-02 | 2009-10-28 | 华东理工大学 | Method for directly liquefying coal in CO and H2O system |
| US9051521B2 (en) * | 2010-12-23 | 2015-06-09 | Stephen Lee Yarbro | Using supercritical fluids to refine hydrocarbons |
| CN105441103A (en) * | 2016-01-06 | 2016-03-30 | 昆明理工大学 | Subcritical or supercritical water electrochemistry reinforced liquid phase catalytic biomass pyrolysis method |
| CN107178350A (en) * | 2016-03-09 | 2017-09-19 | 中国石油化工股份有限公司 | A kind of method of hydro carbons in in-situ extraction oil shale |
| CN107418608A (en) * | 2017-05-08 | 2017-12-01 | 太原理工大学 | The preparation method of the application of semicoke, hydrocarbon compound or hydrocarbon derivative |
| US20180265792A1 (en) * | 2017-03-14 | 2018-09-20 | Saudi Arabian Oil Company | Integrated supercritical water and steam cracking process |
| CN111788283A (en) * | 2018-02-26 | 2020-10-16 | 沙特阿拉伯石油公司 | Conversion process using supercritical water |
| US11034897B1 (en) * | 2020-04-30 | 2021-06-15 | Saudi Arabian Oil Company | Scheme for supercritical water process for heavy oil upgrading |
| CN113926379A (en) * | 2021-12-15 | 2022-01-14 | 太原理工大学 | Hydrogen production method by supercritical water oxygen oil production by long-distance multi-stage heating of pilot-scale organic rock |
-
2022
- 2022-07-14 CN CN202210827680.9A patent/CN114989854B/en active Active
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1688672A (en) * | 2002-09-19 | 2005-10-26 | 约翰·S·伦德尔 | Supercritical hydro extraction of kerogen and aqueous extraction of alumina and soda ash with a residue for portland cement production |
| CN101421488A (en) * | 2006-02-16 | 2009-04-29 | 雪佛龙美国公司 | Kerogen extraction from subterranean oil shale resources |
| US20090166262A1 (en) * | 2007-12-28 | 2009-07-02 | Chevron U.S.A. Inc. | Simultaneous metal, sulfur and nitrogen removal using supercritical water |
| CN101565631A (en) * | 2009-06-02 | 2009-10-28 | 华东理工大学 | Method for directly liquefying coal in CO and H2O system |
| US9051521B2 (en) * | 2010-12-23 | 2015-06-09 | Stephen Lee Yarbro | Using supercritical fluids to refine hydrocarbons |
| CN105441103A (en) * | 2016-01-06 | 2016-03-30 | 昆明理工大学 | Subcritical or supercritical water electrochemistry reinforced liquid phase catalytic biomass pyrolysis method |
| CN107178350A (en) * | 2016-03-09 | 2017-09-19 | 中国石油化工股份有限公司 | A kind of method of hydro carbons in in-situ extraction oil shale |
| US20180265792A1 (en) * | 2017-03-14 | 2018-09-20 | Saudi Arabian Oil Company | Integrated supercritical water and steam cracking process |
| CN107418608A (en) * | 2017-05-08 | 2017-12-01 | 太原理工大学 | The preparation method of the application of semicoke, hydrocarbon compound or hydrocarbon derivative |
| CN111788283A (en) * | 2018-02-26 | 2020-10-16 | 沙特阿拉伯石油公司 | Conversion process using supercritical water |
| US11034897B1 (en) * | 2020-04-30 | 2021-06-15 | Saudi Arabian Oil Company | Scheme for supercritical water process for heavy oil upgrading |
| CN113926379A (en) * | 2021-12-15 | 2022-01-14 | 太原理工大学 | Hydrogen production method by supercritical water oxygen oil production by long-distance multi-stage heating of pilot-scale organic rock |
Non-Patent Citations (1)
| Title |
|---|
| 李宇航等: "油页岩勘探开发现状及进展", 《CT理论与应用研究》 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116333771A (en) * | 2023-05-10 | 2023-06-27 | 中国矿业大学 | Device and method for improving light oil yield of oil shale |
| CN116333771B (en) * | 2023-05-10 | 2023-10-20 | 中国矿业大学 | Device and method for improving light oil yield of oil shale |
Also Published As
| Publication number | Publication date |
|---|---|
| CN114989854B (en) | 2022-11-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Yuan et al. | Comparative study on pyrolysis of lignocellulosic and algal biomass using a thermogravimetric and a fixed-bed reactor | |
| Teh et al. | Dilute sulfuric acid hydrolysis of red macroalgae Eucheuma denticulatum with microwave-assisted heating for biochar production and sugar recovery | |
| Xu et al. | Catalytic pyrolysis and liquefaction behavior of microalgae for bio-oil production | |
| Wang et al. | Mechanism study on cellulose pyrolysis using thermogravimetric analysis coupled with infrared spectroscopy | |
| Wang et al. | Oriented valorization of cellulose and xylan into anhydrosugars by using low-temperature pyrolysis | |
| CN114989854B (en) | Method for improving yield of light oil produced by oil shale pyrolysis | |
| Fan et al. | Microwave-enhanced formation of glucose from cellulosic waste | |
| CN111363572B (en) | Method for co-producing gas-liquid fuel, chemicals and carbon materials by catalytic pyrolysis of biomass | |
| Liu et al. | The kinetics model and pyrolysis behavior of the aqueous fraction of bio-oil | |
| Donar et al. | Catalytic effect of tin oxide nanoparticles on cellulose pyrolysis | |
| Kim et al. | Investigation into role of CO2 in two-stage pyrolysis of spent coffee grounds | |
| Qiao et al. | Highly efficient microwave driven assisted hydrolysis of cellulose to sugar with the utilization of ZrO2 to inhibit recrystallization of cellulose | |
| Cen et al. | Biomass pyrolysis polygeneration with bio-oil recycling: Co-pyrolysis of heavy bio-oil and pine wood leached with light bio-oil for product upgradation | |
| CN110272762B (en) | CO (carbon monoxide)2Method for gasifying sludge by synergistic action with subcritical/supercritical water | |
| Zhang et al. | Influence of typical pretreatment on cotton stalk conversion activity and bio-oil property during low temperature (180–220℃) hydrothermal process | |
| Li et al. | Preparing levoglucosan derived from waste material by pyrolysis | |
| Wu et al. | Catalytic hydropyrolysis of biomass over NiMo bimetallic carbon-based catalysts | |
| Rao et al. | A new strategy of preparing high-value products by co-pyrolysis of bamboo and ZIF-8 | |
| Xu et al. | Influence of pre-treatment on torrefaction of Phyllostachys edulis | |
| CN109851689B (en) | Method for preparing levoglucosan by using agricultural and forestry waste | |
| CN102897714A (en) | Method for increasing yield of hydrogen in gas production process by using biomass | |
| CN110205159B (en) | Method for directionally preparing high-quality oil by reforming tar and molten salt and product | |
| CN111876180A (en) | Method for preparing nitrogen-containing chemical product by catalytic pyrolysis of nitrogen-doped deoxygenated biomass | |
| Fan et al. | In-situ catalytic pyrolysis of cellulose with lithium-ion battery ternary cathodes and ex-situ upgrading over Ru/HZSM-5 for bio-aromatics | |
| Zhang et al. | EXPERIMENTAL STUDY ON BIO-OIL PYROLYSIS/GASIFICATION. |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |