A method for producing crude oil and caustic soda from oil-alkali symbiotic ore

Abstract

The application belongs to the technical field of mineral processing, and discloses a method for producing crude oil and soda from oil-alkali symbiotic ore. The method comprises three-phase separation, dehydration, sedimentation, cyclone separation, filtration and purification. After the treatment method is used, the produced petroleum and soda can meet the quality index requirements.

Description

Technical Field

[0001] This invention belongs to the field of mineral processing technology, specifically relating to a method for producing crude oil and soda ash from oil-alkali symbiotic minerals. Background Technology

[0002] Deep natural soda ash deposits are developed using water-soluble extraction technology. Currently, the natural soda ash brines extracted using this technology both domestically and internationally do not contain petroleum, representing single-origin natural soda ash deposits. Existing natural soda ash processing methods include evaporation and carbonation. The evaporation method can be further subdivided into monohydrate soda ash process and sesquihydrate soda ash process, depending on the raw material composition.

[0003] 1) Evaporation method: Monohydrate alkali process

[0004] After the brine extracted from natural soda ash is refined by filtration, it undergoes wet decomposition. Using evaporation and crystallization processes such as multi-effect evaporators and mechanical compression heat pump evaporators, the Na2CO3 solution is evaporated and concentrated. At a certain temperature, it crystallizes out as soda ash monohydrate (Na2CO3·H2O). The soda ash monohydrate crystals are then separated by centrifugation and calcined to dehydrate, thus obtaining heavy soda ash (Na2CO3).

[0005] 2) Evaporation method: Sesquid alkali process

[0006] The brine extracted from natural soda ash is refined through filtration, then evaporated and crystallized. The separated Na₂CO₃·NaHCO₃·2H₂O is then calcined to produce light soda ash (Na₂CO₃). Depending on the product's functional requirements, light soda ash (Na₂CO₃) can be hydrated to produce heavy soda ash (Na₂CO₃).

[0007] 3) Carbonization method: carbonization process

[0008] After being refined by filtration, the brine extracted from natural soda ash is sent into a carbonation tower at near its saturation temperature. There, it comes into contact with CO2 rising from the bottom of the tower, causing the sodium carbonate in the brine to be converted into sodium bicarbonate. Since sodium bicarbonate has low solubility, it crystallizes out. The separated sodium bicarbonate crystals are then sent to a calcining furnace to be calcined into soda ash, yielding light soda ash (Na2CO3).

[0009] The three natural soda ash processing techniques described above are all conventional methods for processing natural soda ash ores and are not suitable for producing both petroleum and soda ash from oil-soda symbiotic ores. Furthermore, because the produced fluid from oil-soda symbiotic ores contains petroleum, it will adversely affect subsequent natural soda ash processing, not only contaminating equipment but also posing an explosion risk. Summary of the Invention

[0010] In order to overcome the shortcomings of the existing technology, the present invention provides a method for producing crude oil and soda ash from oil-alkali symbiotic minerals, which solves the problem of simultaneously producing petroleum and soda ash from oil-alkali symbiotic minerals.

[0011] The above-mentioned objective of this invention is achieved through the following technical solution: a method for producing crude oil and soda ash from an oil-alkali symbiotic mineral deposit, comprising the following steps:

[0012] 1. Three-phase separation of produced fluid from oil-alkali symbiotic minerals: The produced fluid from oil-alkali symbiotic minerals is collected and transported to a three-phase separator to separate the petroleum, natural gas, and brine in the oil-alkali symbiotic minerals. The three-phase separator is allowed to settle for 40 minutes until the oil content in the produced fluid from the oil-alkali symbiotic minerals is ≤3000mg / L and the water content of the separated petroleum is ≤30%.

[0013] 2. Further dehydration of the separated petroleum: The petroleum separated by the three-phase separator in step 1 is further dehydrated by an electrostatic dehydrator. By using the method of electric field coalescence, the water droplets in the oil are made to carry "positive and negative" charges under the influence of the electric field, collide and merge with each other, gather together, and settle and separate from the oil until the water content of the petroleum after the electrostatic dehydrator is ≤0.5%, and then enters the purified oil storage tank for storage.

[0014] 3. Separated brine settling treatment: The brine separated by the three-phase separator in step 1 and the electric dehydrator in step 2 enters the brine settling tank for primary settling treatment. The residence time in the brine settling tank is 4-8 hours, and the floating oil in the brine is separated by gravity settling.

[0015] 4. Brine hydrocyclone separation: The oily brine in the brine settling tank of step 3 is lifted by a booster pump to the hydrocyclone separator, where it is separated by horizontal centrifugal force.

[0016] 5. Brine Filtration: The oily brine separated by the hydrocyclone separator in step 4 is pumped to a two-stage filter. The first-stage filter uses a walnut shell filter with a walnut shell filter media density greater than or equal to 1.25 g / cm³. 3 Bulk density 0.8-0.85 g / cm³ 3 The first stage uses walnut shell filter media with a particle size of 0.6-1.2mm and a filling height of 1.2-1.4m to remove residual petroleum from the brine. The second stage uses a dual-media filter with quartz sand and magnetite filter media respectively. The quartz sand filter media has a particle size of 0.5-0.8mm, and the magnetite filter media has a particle size of 0.25-0.5mm. The dual-media filter media removes residual suspended solids from the brine.

[0017] 6. Extraction of soda ash from brine: After filtration in step S5, the brine is heated to 80°C by heat exchanger a and high-temperature steam, and then sent to a wet decomposition tower. Inside the wet decomposition tower, it is heated to 100°C-115°C by heat exchanger b and steam rising from heat exchanger b, resulting in wet decomposition of NaHCO3 into Na2CO3. The brine, whose main component is Na2CO3, then enters an MVR device for evaporation and concentration of the Na2CO3 solution. After concentration, the natural soda ash content in the brine is reduced from 1% of the original brine. The concentration of Na2CO3 solution is increased from 2% to 24%. The concentrated Na2CO3 solution is then fed into a triple-effect evaporator for crystallization. The first effect is at atmospheric pressure (105℃), the second effect at negative pressure (85℃), and the third effect at negative pressure (65℃). Once the Na2CO3 in the brine crystallizes out as Na2CO3·H2O, the monohydrate alkali crystals are then centrifuged and dried. Finally, the water of crystallization is removed by calcination in a fluidized bed dryer, thus producing heavy soda ash. The resulting heavy soda ash is then stored in a silo or packaged and shipped out.

[0018] The beneficial effects of this invention compared with the prior art are as follows: For the production of qualified petroleum from oil-alkali symbiotic mineral produced fluid: water content ≤ 0.5%; For the separation of qualified brine from oil-alkali symbiotic mineral produced fluid: OIL ≤ 5 mg / L, S ≤ 5 mg / L, t ≥ 80℃; For the processing of soda ash from oil-alkali symbiotic minerals: total alkali content (based on dry basis Na2CO3 mass fraction) ≥ 98%; NaCl (based on dry basis NaCl mass fraction) ≤ 1.2%; After treatment by the method described in this invention, the petroleum and soda ash produced from the oil-alkali symbiotic mineral produced fluid both meet the quality requirements. Attached Figure Description

[0019] The present invention will be further described below with reference to the accompanying drawings and specific embodiments.

[0020] Figure 1 This is a flowchart of the method for producing crude oil and soda ash from an oil-alkali symbiotic mineral according to the present invention.

[0021] In the diagram: 1. Three-phase separator; 2. Electrostatic dehydrator; 3. Brine settling tank; 4. Booster pump; 5. Cyclone separator; 6. Walnut shell filter; 7. Dual-media filter; 8. Heat exchanger a; 9. Wet decomposition tower; 10. Heat exchanger b; 11. MVR device; 12. Triple-effect evaporator; 13. Centrifugal dryer; 14. Fluidized bed dryer; 15. Purified oil storage tank. Detailed Implementation

[0022] The present invention is described in detail below through specific embodiments, but this does not limit the scope of protection of the present invention. Unless otherwise specified, the experimental methods used in the present invention are all conventional methods, and the experimental equipment, materials, reagents, etc. used can all be obtained commercially.

[0023] Example 1

[0024] A method for producing crude oil and soda ash from an oil-alkali symbiotic mineral deposit includes the following steps:

[0025] 1. Three-phase separation of produced fluid from oil-alkali symbiotic minerals: The produced fluid from oil-alkali symbiotic minerals is collected and transported to a three-phase separator to separate the petroleum, natural gas, and brine in the oil-alkali symbiotic minerals. The three-phase separator is allowed to settle for 40 minutes until the oil content in the produced fluid from the oil-alkali symbiotic minerals is ≤3000mg / L and the water content of the separated petroleum is ≤30%.

[0026] 2. Further dehydration of the separated petroleum: The petroleum separated by the three-phase separator in step 1 is further dehydrated by an electrostatic dehydrator. By using the method of electric field coalescence, the water droplets in the oil are made to carry "positive and negative" charges under the influence of the electric field, collide and merge with each other, gather together, and settle and separate from the oil until the water content of the petroleum after the electrostatic dehydrator is ≤0.5%, and then enters the purified oil storage tank for storage.

[0027] 3. Separated brine sedimentation treatment: The brine separated by the three-phase separator in step 1 and the electric dehydrator in step 2 enters the brine sedimentation tank for primary sedimentation treatment. The residence time is 4 hours. The floating oil in the brine is separated by gravity sedimentation. After this step, the removal efficiency of floating oil is ≥70%.

[0028] 4. Brine hydrocyclone separation: The oily brine in the brine settling tank in step 3 is lifted by a booster pump to the hydrocyclone separator, where it is separated by horizontal centrifugal force. The oil droplet diameter is ≥50nm, and the removal efficiency of the hydrocyclone separation is 50%.

[0029] 5. Brine Filtration: The oily brine separated by the hydrocyclone separator in step 4 is pumped to a two-stage filter. The first-stage filter uses a walnut shell filter with a walnut shell filter media density greater than or equal to 1.25 g / cm³. 3 Bulk density 0.8-0.85 g / cm³ 3 The first stage uses walnut shell filter media with a particle size of 0.6-1.2mm and a filling height of 1.2-1.4m to remove residual petroleum from the brine. The second stage uses a dual-media filter with quartz sand and magnetite filter media respectively. The quartz sand filter media has a particle size of 0.5-0.8mm, and the magnetite filter media has a particle size of 0.25-0.5mm. The dual-media filter media removes residual suspended solids from the brine.

[0030] 6. Extraction of Soda Ash from Brine: After filtration in step 5, the brine is heated to 80°C by heat exchanger a and high-temperature steam, and then sent to a wet decomposition tower. In the wet decomposition tower, it is heated to 100°C by heat exchange with rising steam to decompose NaHCO3 in the brine into Na2CO3. Subsequently, the brine, whose main component is Na2CO3, is concentrated by evaporation using the MVR process. After concentration, the natural alkali content in the brine increases from 12% to 24%. The concentrated Na2CO3 solution enters a triple-effect evaporator for crystallization, with the first effect at atmospheric pressure (105°C), the second effect at negative pressure (85°C), and the third effect at negative pressure (65°C). When the Na2CO3 in the brine crystallizes out as Na2CO3·H2O, the monohydrate alkali crystal is then centrifuged, dried, and calcined to remove the water of crystallization, thus obtaining heavy soda ash. The heavy soda ash is then sent to a storage silo or to a packaging workshop for packaging and shipment.

[0031] Example 2

[0032] A method for producing crude oil and soda ash from an oil-alkali symbiotic mineral deposit includes the following steps:

[0033] 1. Three-phase separation of produced fluid from oil-alkali symbiotic minerals: The produced fluid from oil-alkali symbiotic minerals is collected and transported to a three-phase separator to separate the petroleum, natural gas, and brine in the oil-alkali symbiotic minerals. The three-phase separator is allowed to settle for 40 minutes until the oil content in the produced fluid from the oil-alkali symbiotic minerals is ≤3000mg / L and the water content of the separated petroleum is ≤30%.

[0034] 2. Further dehydration of the separated petroleum: The petroleum separated by the three-phase separator in step 1 is further dehydrated by an electrostatic dehydrator. By using the method of electric field coalescence, the water droplets in the oil are made to carry "positive and negative" charges under the influence of the electric field, collide and merge with each other, gather together, and settle and separate from the oil until the water content of the petroleum after the electrostatic dehydrator is ≤0.5%, and then enters the purified oil storage tank for storage.

[0035] 3. Separated brine sedimentation treatment: The brine separated by the three-phase separator in step 1 and the electric dehydrator in step 2 enters the brine sedimentation tank for primary sedimentation treatment. The residence time is 8 hours. The floating oil in the brine is separated by gravity sedimentation. After this step, the removal efficiency of floating oil is ≥70%.

[0036] 4. Brine hydrocyclone separation: The oily brine in the brine settling tank in step 3 is lifted by a booster pump to the hydrocyclone separator, where it is separated by horizontal centrifugal force. The oil droplet diameter is ≥50nm, and the removal efficiency of the hydrocyclone separation is 90%.

[0037] 5. Brine Filtration: The oily brine separated by the hydrocyclone separator in step 4 is pumped to a two-stage filter. The first-stage filter uses a walnut shell filter with a walnut shell filter media density greater than or equal to 1.25 g / cm³. 3Bulk density 0.8-0.85 g / cm³ 3 The first stage uses walnut shell filter media with a particle size of 0.6-1.2mm and a filling height of 1.2-1.4m to remove residual petroleum from the brine. The second stage uses a dual-media filter with quartz sand and magnetite filter media respectively. The quartz sand filter media has a particle size of 0.5-0.8mm, and the magnetite filter media has a particle size of 0.25-0.5mm. The dual-media filter media removes residual suspended solids from the brine.

[0038] 6. Extraction of Soda Ash from Brine: After filtration in step 5, the brine is heated to 80°C by heat exchanger a and high-temperature steam, and then sent to a wet decomposition tower. In the wet decomposition tower, it is heated to 115°C by heat exchange with rising steam to decompose NaHCO3 in the brine into Na2CO3. Subsequently, the brine, whose main component is Na2CO3, is concentrated by evaporation using the MVR process. After concentration, the natural alkali content in the brine increases from 12% to 24%. The concentrated Na2CO3 solution enters a triple-effect evaporator for crystallization, with the first effect at atmospheric pressure (105°C), the second effect at negative pressure (85°C), and the third effect at negative pressure (65°C). When the Na2CO3 in the brine crystallizes out as Na2CO3·H2O, the monohydrate alkali crystal is then centrifuged, dried, and calcined to remove the water of crystallization, thus obtaining heavy soda ash. The heavy soda ash is then sent to a storage silo or to a packaging workshop for packaging and shipment.

[0039] The embodiments described above are merely preferred embodiments of the present invention, and not all feasible embodiments of the present invention. Any obvious modifications made by those skilled in the art without departing from the principles and spirit of the present invention should be considered to be included within the scope of protection of the claims of the present invention.

Claims

1. A method for producing crude oil and soda ash from an oil-alkali symbiotic mineral, characterized in that, The steps are as follows: S1. Three-phase separation of oil-alkali symbiotic mineral produced fluid: The oil-alkali symbiotic mineral produced fluid is collected and transported to a three-phase separator (1) to separate the petroleum, natural gas and brine in the oil-alkali symbiotic mineral. The three-phase separator (1) settles for 40 minutes until the oil-alkali symbiotic mineral produced fluid has an oil content of ≤3000mg / L and the separated petroleum has a water content of ≤30%. S2. Further dehydration of the separated petroleum: The petroleum separated by the three-phase separator (1) in step S1 is further dehydrated by the electric dehydrator (2). By using the method of electric field coalescence, the water droplets in the oil are made to carry "positive and negative" charges under the influence of the electric field, collide and merge with each other, gather together, and settle and separate from the oil until the petroleum after being treated by the electric dehydrator (2) has a water content of ≤0.5% and enters the purified oil storage tank (15) for storage. S3. Separated brine sedimentation treatment: The brine separated by the three-phase separator (1) in step S1 and the electric dehydrator (2) in step S2 enters the brine sedimentation tank (3) and undergoes primary sedimentation treatment in the brine sedimentation tank (3) for a residence time of 4-8 hours. The floating oil in the brine is separated by gravity sedimentation. S4. Brine hydrocyclone separation: The oily brine in the brine settling tank (3) in step S3 is lifted by the lift pump (4) to the hydrocyclone separator (5) and separated by horizontal centrifugal force; S5. Brine Filtration: The oily brine separated by the hydrocyclone separator (5) in step S4 is pumped by the booster pump (4) to a two-stage filter. The first-stage filter is a walnut shell filter (6) with a walnut shell filter media density greater than or equal to 1.25 g / cm³. 3 Bulk density 0.8-0.85 g / cm³ 3 The walnut shell filter media has a particle size of 0.6-1.2mm and a filling height of 1.2-1.4m. The walnut shell filter media is used to remove the residual petroleum in the brine. The secondary filter adopts a dual-media filter (7), with quartz sand and magnetite filter media respectively. The quartz sand filter media has a particle size of 0.5-0.8mm and the magnetite filter media has a particle size of 0.25-0.5mm. The dual-media filter (7) is used to remove the residual suspended matter in the brine. S6. Extraction of soda ash from brine: After filtration in step S5, the brine is heated to 80°C by heat exchanger a (8) and high-temperature steam, and then sent to a wet decomposition tower (9). In the wet decomposition tower (9), the brine is heated to 100°C-115°C by heat exchanger b (10) with rising steam, and then wet decomposition is performed to decompose NaHCO3 in the brine into Na2CO3. Subsequently, the brine with Na2CO3 as the main component enters the MVR device (11) to evaporate and concentrate the Na2CO3 solution. After concentration, the natural alkali content in the brine increases from 12% to 24% of the original water. The concentrated Na2CO3 solution enters a triple-effect evaporator (12) for crystallization, with the first effect at atmospheric pressure of 105℃, the second effect at negative pressure of 85℃, and the third effect at negative pressure of 65℃. After the Na2CO3 in the brine crystallizes out in the form of Na2CO3•H2O, the monohydrate alkali crystal is placed in a centrifugal dryer (13) for centrifugal drying and then calcined in a fluidized bed dryer (14) to remove the water of crystallization, thus obtaining heavy soda ash.

2. The method for producing crude oil and soda ash from oil-alkali symbiotic minerals according to claim 1, characterized in that, The heavy soda ash obtained in step S6 is sent to a storage silo or to a packaging workshop for packaging and shipment.

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