Oil-based drilling waste resource treatment method and application thereof

Abstract

The application discloses an oil-based drilling cuttings resource processing method and application thereof, and relates to the field of oil-based drilling cuttings resource processing, and aims to realize closed-loop circulation and near-zero emission of oil-based drilling cuttings, and achieve the dual goals of harmlessness and resource utilization. The method comprises the following steps: (1) after heat desorption and pyrolysis of oil-based drilling cuttings by adopting electromagnetic + ball milling, mineral oil in the oil-based drilling cuttings is separated from solid phase in gaseous form, and oil-removed solid phase is obtained; the mineral oil gas is condensed and recovered; the non-condensable gas is used as fuel; (2) the oil-removed solid phase is ground to 200-300 meshes, and the proportion of 85% or more is obtained, then barite is extracted by adopting gravity separation + flotation, and tailings remaining after gravity separation and flotation are combined; (3) the tailings remaining after gravity separation and flotation are mixed with bauxite, and are ground to 300-400 meshes, and the proportion of 85% or more is obtained, then are mixed with solid NaOH, activated at a temperature of 550-650 DEG C for 2-3 h, added into a NaOH solution with a concentration of 5-15% after cooling to room temperature, stirred and mixed uniformly, and then added into a hydrothermal reaction kettle to carry out hydrothermal synthesis reaction, and X type molecular sieve is obtained.

Description

Technical Field

[0001] This invention relates to a method for the resource recovery of oil-based rock cuttings and its application. Background Technology

[0002] Oil-based drilling fluids are widely used in the development of unconventional oil and gas resources such as shale gas and tight gas. Composed of mineral oil, water, weighting agents, organic clay, and various oil-soluble chemical treatment agents, oil-based drilling fluids offer advantages such as resistance to high temperatures and salt-calcium erosion, improved wellbore stability, good lubrication, and minimal damage to oil and gas reservoirs. During drilling operations, oil-based drilling fluids carry drilling cuttings from the formation back to the surface, forming drilling mud. After separation by a vibrating screen and hydrocyclone, the drilling fluid is recycled, while solid cuttings remain on the surface, forming oil-bearing drilling cuttings, or oil-based cuttings for short. Their main components are mineral oil, phenols and other organic compounds, and various inorganic ores. The large amounts of mineral oil and various organic compounds in oil-based cuttings pollute soil, surface water, and groundwater, directly or indirectly causing serious harm to plants, animals, human health, and the surrounding ecological environment. It is a highly polluting solid waste, and its proper disposal is directly related to the implementation of the national energy security strategy.

[0003] In recent years, shale gas exploration and development has shown a rapid growth trend. The shale gas extraction process generates oil-based rock cuttings, which have an average oil content of approximately 25-40% and possess considerable economic value. More importantly, with increasing environmental protection efforts, developing efficient oil-based rock cuttings processing technologies to achieve environmentally friendly shale gas development has become an urgent priority.

[0004] In shale gas extraction, high-temperature thermal desorption technology is currently widely used to recover mineral oil from oil-based rock cuttings. The remaining rock cuttings and tailings are managed as general solid waste (suitable for agricultural applications, land treatment, construction, and municipal applications). However, due to differences in geographical and geological conditions, and the fact that environmental protection companies primarily focus on the recovery of high-profit mineral oil, the oil content of the remaining tailings after thermal desorption of oil-based rock cuttings at some sites is generally higher than 1%, failing to meet the requirements for further resource utilization. These tailings must be sent to hazardous waste treatment plants or co-processed in cement kilns. Some sites have adopted low-temperature extraction technology (LRET), which can reduce the oil content of the solid phase in oil-based rock cuttings to below 1%. However, this technology suffers from a high solvent loss rate, resulting in high processing costs and significant on-site operational risks. Over the next 10 years, shale gas extraction will experience rapid growth, leading to a corresponding increase in the amount of oil-based rock cuttings generated at well sites. Currently, there is no mature and comprehensive supporting technology for the proper disposal of oil-based rock cuttings. Therefore, seeking a proper integrated solution for resource and environmentally friendly treatment has become a top priority for energy extraction companies. Its market promotion and application potential is significant, with broad market prospects and major environmental significance. Summary of the Invention

[0005] In view of the deficiencies in the prior art, the present invention provides a method and application for the resource utilization of oil-based rock cuttings, so as to at least partially solve the problems existing in the prior art.

[0006] In a first aspect, the present invention provides a method for the resource recovery of oil-based rock cuttings, comprising:

[0007] (1) After the oil-based rock cuttings are thermally desorbed and thermally desorbed by electromagnetic + ball milling, the mineral oil in the oil-based rock cuttings is separated from the solid phase in gaseous form to obtain the oil-free solid phase; the mineral oil gas is recovered after condensation; the non-condensable gas is used as fuel.

[0008] (2) Grind the deoiled solid phase to 200-300 mesh with a content of more than 85%, and then extract barite by gravity separation + flotation. Combine the tailings remaining after gravity separation and flotation.

[0009] (3) The tailings remaining after gravity separation and flotation are mixed with bauxite and ground to a density of 300-400 mesh (85% or more). Then, the mixture is mixed with solid NaOH and activated at 550-650℃ for 2-3 hours. After cooling to room temperature, the mixture is added to a 5-15% NaOH solution and stirred until homogeneous. The mixture is then added to a hydrothermal reactor for hydrothermal synthesis to obtain X-type molecular sieve.

[0010] In one or more alternative embodiments, the oil-based rock cuttings are white oil-based rock cuttings or diesel-based rock cuttings.

[0011] In one or more optional embodiments, the method further includes:

[0012] (1) When processing white oil-based rock cuttings, they are directly transported to an oxygen-deficient furnace containing steel balls. When processing diesel-based rock cuttings, catalysts and viscosity reducers are added before transporting them to an oxygen-deficient furnace containing steel balls. Then, a coupled heating method of electromagnetic + ball milling is used for thermal desorption and thermal desorption. The desorbed or desorbed mineral oil leaves the furnace in gaseous form and is separated from the solid phase to obtain an oil-free solid phase. The mineral oil gas is dusted and condensed in a cyclone manner, and the desorbed mineral oil is recovered. The non-condensable gas is sent to the fuel gas pipeline network for use as fuel.

[0013] (2) After grinding the deoiled solid phase to a density of 200-300 mesh (85% or more), gravity separation is first performed, followed by flotation with mineral processing reagents to obtain barite; the tailings remaining after gravity separation and flotation are combined.

[0014] (3) The tailings remaining after gravity separation and flotation are mixed with bauxite at a SiO2 / Al2O3 molar ratio of 2.2-3.0:1 to obtain a mixed sieve. The mixed sieve is then wet-milled to a 300-400 mesh size with a content of more than 85%. It is then dried at 50-60℃ using a blower. The mixed sieve after drying through a 300-400 mesh sieve is then mixed with solid NaOH at a Na / Si molar ratio of 1.2-1.8:1. The mixture is then activated at 550-650℃ for 2-3 hours. After cooling to room temperature, it is added to a 5-15% NaOH solution. After stirring and mixing evenly, it is added to a hydrothermal reactor for hydrothermal synthesis reaction. The crystallization temperature is controlled at 120-150℃ and the reaction time is 15-18 hours. After filtration, washing, and drying, X-type molecular sieve is obtained.

[0015] In one or more alternative embodiments, the amount of catalyst added in step (1) is 3-5% of the diesel-based rock cuttings.

[0016] In one or more optional embodiments, the catalyst in step (1) is any one or more of the following composites: bauxite, natural zeolite, fly ash, and refinery waste catalyst.

[0017] In one or more alternative embodiments, the amount of viscosity reducer added in step (1) is 5-10% of the diesel-based rock cuttings.

[0018] In one or more optional embodiments, the viscosity reducer in step (1) is any one or more of quicklime, activated clay, and fly ash.

[0019] In one or more alternative embodiments, the steel balls in step (1) have a particle size of 5-50 mm.

[0020] In one or more optional embodiments, the conditions for reselection in step (2) include: the shaking table stroke is 12-15 mm, the number of strokes is 320-350 times / min, and the table surface inclination angle is 3.5-5°.

[0021] In one or more optional embodiments, the flotation method in step (2) is a closed-circuit positive flotation method consisting of 1 roughing and 5-8 cleaning; the flotation conditions include: temperature of 30-45℃, time of 40-70min, and pulp concentration of 10-20%.

[0022] In one or more optional embodiments, the mineral processing reagent in step (2) includes inhibitors, collectors, dispersants, and frothers.

[0023] In one or more optional embodiments, the inhibitor is any one or more complexes of sodium phosphate, water glass, and tannic acid.

[0024] In one or more alternative embodiments, the collector is a complex of sodium dodecyl sulfate and sodium dodecyl sulfonate in a ratio of 1:1-3.

[0025] Secondly, the present invention provides an application of the above-mentioned oil-based rock cuttings resource utilization method in the treatment of oily solid waste.

[0026] This invention first employs electromagnetic induction combined with ball milling to extract mineral oil from oil-based rock cuttings. The extracted mineral oil can be used as a base oil in drilling fluid formulation. Besides its direct effect of raising the system temperature, ball milling also achieves coarse grinding of materials (achieving a 200-300 mesh content of over 55%) and effectively prevents coking on the inner wall of the oxygen-deficient furnace. This invention then uses gravity separation combined with flotation to extract barite from oil-based rock cuttings. The extracted barite recovery rate is over 94%, and the grade is over 92%, making it suitable as a weighting agent for use in drilling fluid. The oil content of the tailings remaining after gravity separation and flotation meets the Class B treatment standard in DB51 / T2850-2021 (Standard for the Disposal of Residual Solids after Comprehensive Utilization of Oily Sludge from Natural Gas Extraction), and can be used to prepare X-type molecular sieves through alkali fusion activation and hydrothermal synthesis. This invention, based on the separation of oil and solids and the purification of the oil phase, further extracts barite from the solid phase and prepares X-type molecular sieves from the remaining tailings, realizing a closed-loop recycling and near-zero emissions of oil-based rock cuttings. It achieves the dual goals of harmlessness and resource utilization, solves the environmental problems that have plagued oil and gas field development companies, and safeguards the clean and harmless production of shale gas. Attached Figure Description

[0027] Figure 1 This is a flowchart of the oil-based rock cuttings resource utilization method provided by the present invention;

[0028] Figure 2 This is a schematic diagram of the process for the resource utilization of diesel-based rock cuttings provided in Embodiment 10 of the present invention. Detailed Implementation

[0029] The embodiments of the present invention are described in detail below: The embodiments of the present invention are implemented under the premise of the technical solution of the present invention, and detailed implementation methods and processes are given. However, the protection scope of the present invention is not limited to the following embodiments. The process parameters in the following embodiments that do not specify specific conditions are generally in accordance with conventional conditions.

[0030] The endpoints and any values ​​of the ranges disclosed in this invention are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed in this invention.

[0031] Example 1

[0032] White oil-based rock cuttings (samples taken from a shale gas drilling platform in the Changning Block of Sichuan) were transported to an oxygen-deficient furnace containing steel balls. The temperature inside the furnace was controlled at 325-345℃ using an electromagnetic + ball mill method, with a heating rate of 8℃ / min, a residence time of 45min, and a furnace cylinder rotation speed of 150r / min. The desorbed or desorbed oil left the furnace in gaseous form, and was then condensed and recovered after dust removal using a cyclone method. The separated solid phase entered the barite extraction stage.

[0033] After removing mineral oil, the solid phase is ground to a particle size of 200-300 mesh (over 85%). First, barite is coarsely extracted using gravity separation. The shaking table has a stroke of 12 mm, a stroke rate of 330 times / min, and a table inclination angle of 3.5°. The concentrate obtained after shaking table gravity separation has a grade in the range of 65-70%. The tailings are then sent to the molecular sieve preparation stage. The barite concentrate obtained from the shaking table was added to a flotation system containing mineral processing reagents such as inhibitors (1 part sodium phosphate: 1-2 parts water glass, dosage 800-1200 g / t), collectors (sodium dodecyl sulfate: sodium dodecyl sulfonate in a 1:1-3 ratio, dosage 350-450 g / t), dispersants (sodium pyrophosphate, sodium hexametaphosphate, and water glass in a mass ratio of 1-2:1-3:1, dosage 0.25-1%), and frothers (pine oil 5-15 g / t). The flotation method was a closed-circuit positive flotation with 1 rougher and 6 cleaner stages. The flotation temperature was controlled at 35℃, the total flotation time was 50 min, and the pulp concentration was 15.5%. After flotation, the barite recovery rate was 95%, and the grade was above 95%. The tailings were then used for molecular sieve preparation.

[0034] The tailings remaining after gravity separation and flotation were mixed with bauxite at a SiO2 / Al2O3 molar ratio of 2.5:1 and wet-milled using a ball mill to a density of 300-400 mesh (over 85%). The mixture was then dried using a blower at 50-60℃ for 20-24 hours. The dried and sieved mixture was then mixed with solid NaOH at a Na / Si molar ratio of 1.2-1.8:1 and activated at 550-650℃ for 2-3 hours. After cooling to room temperature, the mixture was added to a 9% NaOH solution and stirred until homogeneous. The mixture was then added to a hydrothermal reactor, crystallized at 125℃ for 16 hours, and the final product (X-type molecular sieve) was obtained after filtration, washing, and drying.

[0035] Table 1 shows a comparison of the physical properties of the prepared X-type molecular sieve and coal-based activated carbon. As can be seen from Table 1, the X-type molecular sieve prepared using the method described in this invention is in the mesoporous range, and its physical properties are superior to those of commercially available coal-based activated carbon (coal-based columnar activated carbon, Liyang Zhouyuan Environmental Protection Materials Co., Ltd.).

[0036] Table 1 Comparison of physical properties of X-type molecular sieves and coal-based activated carbon

[0037] project Specific surface area / m 3 • g]] Pore volume / cm 3 • g]] Average pore size / nm X-type molecular sieve 985.4 0.75 1.3 Coal-based activated carbon 918.2 0.48 1.8

[0038] Using benzene as the target VOCs, the adsorption performance of two adsorbents, X-type molecular sieve and coal-based activated carbon, was further compared. The results are shown in Table 2. It can be seen that the saturated adsorption capacity of the X-type molecular sieve prepared using the technology described in this invention is greater than that of coal-based activated carbon, its breakthrough time is longer, and its saturation time is slightly longer, indicating good potential for practical application.

[0039] Table 2. Comparison of adsorption characteristics between X-type molecular sieves and coal-based activated carbon

[0040]

[0041] Example 2

[0042] In this embodiment, the object being processed is white oil-based rock fragments, and the processing method is the same as in Example 1. The difference from Example 1 is that the inhibitor in the flotation process is a mixture of water glass and tannic acid in a mass ratio of 1-2:1. After flotation, the recovery rate of barite is 95%, and the grade is 92%.

[0043] Example 3

[0044] In this embodiment, the object being processed is white oil-based rock fragments, and the processing method is the same as in Example 1. The difference from Example 1 is that the inhibitor in the flotation process is a mixture of sodium phosphate and tannic acid in a mass ratio of 1:1-3. After flotation, the recovery rate of barite is 96%, and the grade is 95%.

[0045] Example 4

[0046] In this embodiment, the object being processed is white oil-based rock fragments, and the processing method is the same as in Example 1. The difference from Example 1 is that the inhibitor in the flotation stage is water glass. After flotation, the recovery rate of barite is 94%, and the grade is 92%.

[0047] Example 5

[0048] In this embodiment, the object being processed is white oil-based rock fragments, and the processing method is the same as in Example 1. The difference from Example 1 is that the inhibitor in the flotation process is a mixture of sodium phosphate, water glass, and tannic acid in a mass ratio of 1:1-2:1-3. After flotation, the recovery rate of barite is 96%, and the grade is 97%.

[0049] Example 6

[0050] In this embodiment, the object being processed is white oil-based rock fragments, and the processing method is the same as in Example 1. The difference from Example 1 is that the dispersant in the flotation stage is a mixture of sodium pyrophosphate and sodium hexametaphosphate in a mass ratio of 1:1-2. After flotation, the recovery rate of barite is 94%, and the grade is 93%.

[0051] Example 7

[0052] In this embodiment, the object being processed is white oil-based rock fragments, and the processing method is the same as in Example 1. The difference from Example 1 is that the dispersant in the flotation stage is a mixture of sodium pyrophosphate and water glass in a mass ratio of 1-3:1. After flotation, the recovery rate of barite is 95%, and the grade is 94%.

[0053] Example 8

[0054] In this embodiment, the object being processed is white oil-based rock fragments, and the processing method is the same as in Example 1. The difference from Example 1 is that the dispersant in the flotation stage is sodium pyrophosphate. After flotation, the recovery rate of barite is 94%, and the grade is 92%.

[0055] Example 9

[0056] In this embodiment, the object being processed is white oil-based rock fragments. The processing method is the same as in Example 1. The difference from Example 5 is that the dispersant in the flotation stage is a mixture of sodium pyrophosphate and water glass in a mass ratio of 1-3:1. After flotation, the recovery rate of barite is 97%, and the grade is 95%.

[0057] Example 10

[0058] Diesel bedrock cuttings (sample taken from a shale gas drilling platform in the Weiyuan Block of Sichuan) were mixed evenly with catalyst (a mixture of bauxite, natural zeolite, fly ash, and refinery waste catalyst in a mass ratio of 1:1-2:1:1, with an addition ratio of 3-5%) and viscosity reducer (quicklime, activated clay, and fly ash in a mass ratio of 1-2:1-3:1, with an addition ratio of 5-10%) and transported to an oxygen-deficient furnace containing steel balls. The temperature inside the furnace was controlled at 275-350℃ using an electromagnetic + ball mill method, with a heating rate of 5-10℃ / min, a residence time of 30-60min, and a furnace cylinder rotation speed of 100-200r / min. The desorbed or precipitated oil left the furnace in gaseous form, was dusted and condensed for recovery using a cyclone method, and the solid phase after desorption entered the barite extraction stage.

[0059] The solid phase minerals, after the removal of mineral oil, are ground to a particle size of 200-300 mesh (85% or more). First, barite is coarsely extracted using gravity separation. The shaking table has a stroke of 12-15 mm, a stroke rate of 320-350 times / min, and a table inclination angle of 3.5-5°. The concentrate obtained from the shaking table gravity separation has a grade in the range of 65-78%. The resulting tailings are then used in the molecular sieve preparation stage.

[0060] The barite concentrate obtained from the shaking table was added to a flotation system containing mineral processing reagents including: inhibitor (sodium phosphate, water glass, and tannic acid in a mass ratio of 1:1-2:1-3, dosage 800-1200 g / t), collector (sodium dodecyl sulfate and sodium dodecyl sulfonate in a mass ratio of 1:1-3, dosage 350-450 g / t), dispersant (sodium pyrophosphate, sodium hexametaphosphate, and water glass in a mass ratio of 1-2:1-3:1, dosage 0.25%-1%), and frother (pine oil 5-15 g / t). The flotation method was a closed-circuit positive flotation with 1 rougher and 8 cleaner stages. The flotation temperature was controlled at 45℃, the total flotation time was 60 min, and the pulp concentration was 10-20%. After flotation, the barite recovery rate was 95%, and the grade was 96%. The tailings were then used for molecular sieve preparation.

[0061] The tailings remaining after gravity separation and flotation are mixed with bauxite at a SiO2 / Al2O3 molar ratio of 2.2-3.0, and then wet-milled using a ball mill to achieve a 300-400 mesh content of over 85%. The mixture is then dried using a blower at 50-60℃ for 20-24 hours. The dried and sieved mixture is then mixed with solid NaOH at a Na / Si molar ratio of 1.2-1.8:1, and activated at 550-650℃ for 2-3 hours. After cooling to room temperature, the mixture is added to a 5-15% NaOH solution, stirred until homogeneous, and then added to a hydrothermal reactor. The crystallization temperature is 120-150℃, and the reaction time is controlled at 15-18 hours. After filtration, washing, and drying, X-type molecular sieve is obtained.

[0062] Table 3 shows a comparison of the physical properties of the prepared X-type molecular sieve and coal-based activated carbon. It can be seen that the X-type molecular sieve prepared using the technology described in this invention is in the mesoporous range, and its physical properties are superior to those of commercially available coal-based activated carbon.

[0063] Table 3 Comparison of physical properties of X-type molecular sieves and coal-based activated carbon

[0064] project <![CDATA[Specific surface area / m 3 ·g]]> <![CDATA[Pore volume / cm 3 ·g]]> Average pore size / nm X-type molecular sieve 991.6 0.85 1.5 Coal-based activated carbon 918.2 0.48 1.8

[0065] Using benzene as the target VOCs, the adsorption performance of two adsorbents, X-type molecular sieve and coal-based activated carbon, was further compared. The results are shown in Table 4. It can be seen that the saturated adsorption capacity of the X-type molecular sieve prepared using the technology described in this invention is greater than that of coal-based activated carbon, its breakthrough time is longer, and its saturation time is slightly longer, indicating good potential for practical application.

[0066] Table 4. Comparison of adsorption characteristics between X-type molecular sieves and coal-based activated carbon

[0067]

[0068] Example 11

[0069] In this embodiment, the object being processed is diesel-based rock cuttings. The processing method is the same as in Example 10. The difference from Example 10 is that the catalyst used in the thermal desorption process is a mixture of bauxite, natural zeolite, and fly ash in a mass ratio of 1:1 to 2:1. The oil content of the tailings of the oil-based rock cuttings after thermal desorption is 0.6%.

[0070] Example 12

[0071] In this embodiment, the object being processed is diesel-based rock cuttings. The processing method is the same as in Example 10. The difference from Example 10 is that the catalyst used in the thermal desorption process is a mixture of bauxite and natural zeolite in a mass ratio of 1:1-2. The oil content of the tailings of the oil-based rock cuttings after thermal desorption is 1.2%.

[0072] Example 13

[0073] In this embodiment, the object being processed is diesel-based rock cuttings, and the processing method is the same as in Example 10. The difference from Example 10 is that the catalyst used in the thermal desorption process is bauxite, and the oil content of the tailings of the oil-based rock cuttings after thermal desorption is 1.4%.

[0074] Example 14

[0075] In this embodiment, the object being processed is diesel-based rock cuttings. The processing method is the same as in Example 10. The difference from Example 10 is that the catalyst used in the thermal desorption process is a mixture of bauxite and refinery waste catalyst at a mass ratio of 1:1. The oil content of the tailings of the oil-based rock cuttings after thermal desorption is 1%.

[0076] Example 15

[0077] In this embodiment, the object being processed is diesel-based rock cuttings. The processing method is the same as in Example 10. The difference from Example 10 is that the catalyst used in the thermal desorption process is a mixture of bauxite and refinery waste catalyst at a mass ratio of 1:1-2. The oil content of the tailings of the oil-based rock cuttings after thermal desorption is 0.8%.

[0078] Example 16

[0079] In this embodiment, the object being processed is diesel-based rock cuttings. The processing method is the same as in Example 10. The difference from Example 10 is that the viscosity reducer used in the thermal desorption process is a mixture of quicklime and activated clay in a mass ratio of 1:1-3. The oil content of the tailings of the oil-based rock cuttings after thermal desorption is 1%.

[0080] Example 17

[0081] In this embodiment, the object being processed is diesel-based rock cuttings. The processing method is the same as in Example 10. The difference from Example 10 is that the viscosity reducer used in the thermal desorption process is a mixture of quicklime and fly ash in a mass ratio of 1-2:1. The oil content of the tailings of the oil-based rock cuttings after thermal desorption is 1.3%.

[0082] Example 18

[0083] In this embodiment, the object being processed is diesel-based rock cuttings. The processing method is the same as in Example 10. The difference from Example 10 is that the viscosity reducer used in the thermal desorption process is a mixture of activated clay and fly ash in a mass ratio of 1-3:1. The oil content of the tailings of the oil-based rock cuttings after thermal desorption is 0.9%.

[0084] Example 19

[0085] In this embodiment, the object being processed is diesel bedrock cuttings, and the processing method is the same as in Example 10. The difference from Example 10 is that the inhibitor in the flotation process is a mixture of water glass and tannic acid in a mass ratio of 1-2:1. After flotation, the recovery rate of barite is 94%, and the grade is 93%.

[0086] Example 20

[0087] In this embodiment, the object being processed is diesel bedrock cuttings. The processing method is the same as in Example 10. The difference from Example 1 is that the inhibitor in the flotation process is a mixture of sodium phosphate and tannic acid in a mass ratio of 1:1-3. After flotation, the recovery rate of barite is 97%, and the grade is 95%.

[0088] Example 21

[0089] In this embodiment, the object being processed is diesel bedrock cuttings, and the processing method is the same as in Example 10. The difference from Example 1 is that the inhibitor in the flotation stage is water glass. After flotation, the recovery rate of barite is 94%, and the grade is 92%.

[0090] Example 22

[0091] In this embodiment, the object being processed is diesel bedrock cuttings. The processing method is the same as in Example 10. The difference from Example 1 is that the inhibitor in the flotation process is a mixture of sodium phosphate, water glass, and tannic acid in a mass ratio of 1:1-2:1-3. After flotation, the recovery rate of barite is 95%, and the grade is 97%.

[0092] Example 23

[0093] In this embodiment, the object being processed is diesel bedrock cuttings, and the processing method is the same as in Example 10. The difference from Example 1 is that the dispersant in the flotation stage is a mixture of sodium pyrophosphate and sodium hexametaphosphate in a mass ratio of 1:1-2. After flotation, the recovery rate of barite is 94%, and the grade is 94%.

[0094] Example 24

[0095] In this embodiment, the object being processed is diesel bedrock cuttings. The processing method is the same as in Example 10. The difference from Example 1 is that the dispersant in the flotation stage is a mixture of sodium pyrophosphate and water glass in a mass ratio of 1-3:1. After flotation, the recovery rate of barite is 95%, and the grade is 96%.

[0096] Example 25

[0097] In this embodiment, the object being processed is diesel bedrock cuttings, and the processing method is the same as in Example 10. The difference from Example 1 is that the dispersant in the flotation stage is sodium pyrophosphate. After flotation, the recovery rate of barite is 95%, and the grade is 92%.

[0098] Example 26

[0099] In this embodiment, the object being processed is diesel bedrock cuttings. The processing method is the same as in Example 10. The difference from Example 5 is that the dispersant in the flotation stage is a mixture of sodium pyrophosphate and water glass in a mass ratio of 1-3:1. After flotation, the recovery rate of barite is 97%, and the grade is 96%.

[0100] Although specific embodiments of the invention have been described in detail, those skilled in the art will understand that various modifications and substitutions can be made to those details based on all the teachings disclosed, and all such changes are within the scope of protection of this invention. The full scope of this invention is given by the appended claims and any equivalents thereof.

Claims

1. A method for the resource utilization of oil-based rock cuttings, characterized in that, The oil-based rock cuttings are white oil-based rock cuttings or diesel oil-based rock cuttings; the method includes: (1) When processing white oil-based rock cuttings, they are directly transported to an oxygen-deficient furnace containing steel balls. When processing diesel-based rock cuttings, catalysts and viscosity reducers are added before transporting them to an oxygen-deficient furnace containing steel balls. Then, a coupled heating method of electromagnetic + ball milling is used for thermal desorption and thermal desorption. The desorbed or desorbed mineral oil leaves the furnace in gaseous form and is separated from the solid phase to obtain an oil-free solid phase. The mineral oil gas is dusted and condensed in a cyclone manner, and the desorbed mineral oil is recovered. The non-condensable gas is sent to the fuel gas pipeline network for use as fuel. (2) After grinding the deoiled solid phase to a density of 200-300 mesh (85% or more), gravity separation is first performed, followed by flotation with mineral processing reagents to obtain barite; the tailings remaining after gravity separation and flotation are combined. (3) The tailings remaining after gravity separation and flotation are mixed with bauxite at a SiO2 / Al2O3 molar ratio of 2.2-3.0:1 to obtain a mixed sieve. The mixed sieve is then wet-milled to a 300-400 mesh size with a content of more than 85%. It is then dried at 50-60℃ using a blower. The mixed sieve after drying through a 300-400 mesh sieve is then mixed with solid NaOH at a Na / Si molar ratio of 1.2-1.8:

1. The mixture is then activated at 550-650℃ for 2-3 hours. After cooling to room temperature, it is added to a 5-15% NaOH solution. After stirring and mixing evenly, it is added to a hydrothermal reactor for hydrothermal synthesis reaction. The crystallization temperature is controlled at 120-150℃ and the reaction time is 15-18 hours. After filtration, washing, and drying, X-type molecular sieve is obtained.

2. The method as described in claim 1, characterized in that, The amount of catalyst added in step (1) is 3-5% of the diesel-based rock cuttings.

3. The method as described in claim 1, characterized in that, The catalyst mentioned in step (1) is any one or more of the following composite materials: bauxite, natural zeolite, fly ash, and waste catalyst from refineries.

4. The method as described in claim 1, characterized in that, The amount of viscosity reducer added in step (1) is 5-10% of the diesel-based rock cuttings.

5. The method as described in claim 1, characterized in that, The viscosity reducer mentioned in step (1) is any one or more of quicklime, activated clay, and fly ash.

6. The method as described in claim 1, characterized in that, The size of the steel balls mentioned in step (1) is 5-50 mm.

7. The method as described in claim 1, characterized in that, The conditions for reselection in step (2) include: the stroke of the shaking table is 12-15 mm, the number of strokes is 320-350 times / min, and the tilt angle of the table surface is 3.5-5°.

8. The method as described in claim 1, characterized in that, The flotation method described in step (2) is a closed-circuit positive flotation method consisting of 1 roughing and 5-8 cleaning; the flotation conditions include: temperature of 30-45℃, time of 40-70min, and pulp concentration of 10-20%.

9. The method as described in claim 1, characterized in that, The mineral processing reagents mentioned in step (2) include inhibitors, collectors, dispersants, and frothers.

10. The method as described in claim 9, characterized in that, The inhibitor is any one or more of sodium phosphate, water glass, and tannic acid in combination.

11. The method as described in claim 9, characterized in that, The collector is a complex of sodium dodecyl sulfate and sodium dodecyl sulfonate in a ratio of 1:1-3.

12. The application of the oil-based rock cuttings resource utilization method according to any one of claims 1 to 11 in the treatment of oily solid waste.

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