Method for producing crude oil and sodium carbonate from oil-alkali paragenic ore

Abstract

The invention belongs to the technical field of mineral product processing, and discloses a method for producing crude oil and sodium carbonate from oil-alkali paragenic ore. Comprising the steps of three-phase separation, dehydration, sedimentation, cyclone separation, filtration and purification. After being treated by the treatment method disclosed by the invention, the produced petroleum and sodium carbonate both meet the quality index requirements.

Description

Technical Field

[0001] The invention belongs to the technical field of mineral processing, and in particular relates to a method for producing crude oil and soda ash from an oil-alkali symbiotic ore. Background Art

[0002] Deep trona mines are developed using water-soluble mining technology. At present, the trona brine produced by water-soluble mining technology in trona mines at home and abroad does not contain petroleum and belongs to a single trona deposit. The existing trona processing methods include evaporation and carbonization. The evaporation method can be further subdivided into monohydrate process and sesquihydrate process according to the different raw material compositions.

[0003] 1) Evaporation method: monohydrate process

[0004] The brine extracted from natural soda is refined through a filtration process and then wet decomposed. The Na2CO3 solution is evaporated and concentrated using evaporation and crystallization processes such as multiple-effect evaporators and mechanical compression heat pump evaporation crystallizers. Crystals are precipitated in the form of monohydrate (Na2CO3·H2O) at a certain temperature. The monohydrate crystals are then centrifuged, calcined and dehydrated to produce heavy soda ash (Na2CO3).

[0005] 2) Evaporation method: sesquialkali process

[0006] After the brine produced by natural alkali is refined through filtering process, it is evaporated and crystallized, and then the separated Na2CO3·NaHCO3·2H2O is calcined to produce light soda ash (Na2CO3). According to the functional requirements of the product, light soda ash (Na2CO3) can be converted into heavy soda ash (Na2CO3) through hydration process.

[0007] 3) Carbonization method: Carbonization process

[0008] The brine produced from natural alkali is refined through a filtration process and then sent to a carbonization tower at a temperature close to its saturation temperature. It comes into contact with the CO2 rising from the bottom of the tower, converting the sodium carbonate therein into sodium bicarbonate. Since sodium bicarbonate has a low solubility, crystals are precipitated. The separated sodium bicarbonate crystals are sent to a calcining furnace to be calcined into soda ash, and the resulting product is light soda ash (Na2CO3).

[0009] The above three natural soda processing technologies are all conventional natural soda ore processing methods, and are not suitable for the simultaneous production of oil and soda ash from oil-alkali co-existing ores. At the same time, since the produced fluid from oil-alkali co-existing ores contains oil, it will also have an adverse effect on the subsequent natural soda processing, not only polluting the equipment, but also causing explosion risks. Summary of the invention

[0010] In order to overcome the deficiencies of the prior art, the present invention provides a method for producing crude oil and soda ash from an oil-alkali paragenetic ore, which solves the problem of simultaneously producing crude oil and soda ash from an oil-alkali paragenetic ore.

[0011] The above object of the present invention is achieved through the following technical scheme: A method for producing crude oil and soda ash from oil-alkali paragenetic ore, the steps are as follows:

[0012] 1. Carry out three-phase separation of the produced liquid from the oil-alkali paragenetic ore: The produced liquid from the oil-alkali paragenetic ore is transported to the three-phase separator, and the oil, natural gas and brine in the oil-alkali paragenetic ore are separated into three phases. The three-phase separator is allowed to settle for 40 minutes until the oil content of the produced liquid from the oil-alkali paragenetic ore reaches ≤3000mg / L and the water content of the separated oil reaches ≤30%;

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

[0014] 3. Sedimentation treatment of the separated brine: The brine separated by the three-phase separator in step 1 and the electric dehydrator in step 2 enters the brine sedimentation tank, where it undergoes primary sedimentation treatment for 4-8 hours, and the floating oil in the brine is separated by gravity sedimentation;

[0015] 4. Brine cyclone separation: In step 3, the oily brine in the brine settling tank is lifted into the cyclone separation device by a lifting pump and cyclone separation is performed by horizontal centrifugal force;

[0016] 5. Brine filtration: The oily brine separated by the cyclone separation device in step 4 is lifted to a two-stage filter by a lifting pump, wherein the first-stage filter adopts a walnut shell filter, and the density of the walnut shell filter material is greater than or equal to 1.25g / cm 3 , bulk density 0.8-0.85g / cm 3 The particle size of walnut shell filter material is 0.6-1.2mm, and the filling height is 1.2-1.4m. Walnut shells are used to filter out the remaining oil in the brine. The secondary filter uses a double filter material filter, and the filter materials are quartz sand and magnetite filter materials. The particle size of quartz sand filter material is 0.5-0.8mm, and the particle size of magnetite filter material is 0.25-0.5mm. The double filter material filter is used to remove the remaining suspended matter in the brine.

[0017] 6. Extraction of soda ash from brine: The brine filtered in step S5 is heat exchanged with high-temperature steam in heat exchanger a to 80°C and then transported to a wet decomposition tower. In the wet decomposition tower, it is heated to 100°C-115°C after heat exchange with the steam rising from heat exchanger b for wet decomposition, and NaHCO3 in the brine is decomposed into Na2CO3. Subsequently, the brine with Na2CO3 as the main component enters the MVR device to evaporate and concentrate the Na2CO3 solution. After concentration, the natural alkali content in the brine is reduced from 12% of the original water to 12% of the original water. % is increased to 24%, and the concentrated Na2CO3 solution enters a triple-effect evaporator for crystallization, wherein the first effect is at normal pressure 105°C, the second effect is at negative pressure 85°C, and the third effect is at negative pressure 65°C. When the Na2CO3 in the brine is crystallized in the form of Na2CO3·H2O, the monohydrate crystals are placed in a centrifugal dryer for centrifugal drying, and calcined in a fluidized bed dryer to remove crystal water, and heavy soda ash can be obtained. The obtained heavy soda ash is sent to the purified oil storage tank for storage or to the packaging workshop for packaging and transportation.

[0018] Compared with the prior art, the present invention has the following beneficial effects: the qualified oil index of the oil-alkali symbiotic ore produced liquid is: water content ≤0.5%; the qualified brine index of the oil-alkali symbiotic ore produced liquid is: OIL≤5mg / LSS≤5mg / L t≥80℃; the soda ash index of the oil-alkali symbiotic ore processed soda ash is: total alkali content (calculated as dry basis Na2CO3 mass fraction) ≥98%; NaCl (calculated as dry basis NaCl mass fraction) ≤1.2%; after the oil-alkali symbiotic ore produced liquid is treated by the treatment method of the present invention, the produced oil and soda ash both meet the quality index requirements. BRIEF DESCRIPTION OF THE DRAWINGS

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

[0020] Figure 1 The present invention is a flow chart of the method for producing crude oil and soda ash from oil-alkali co-existing ore.

[0021] In the figure, 1. three-phase separator; 2. electric dehydrator; 3. brine sedimentation tank; 4. lifting pump; 5. cyclone separation device; 6. walnut shell filter; 7. double filter 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 DESCRIPTION

[0022] The present invention is described in detail below by specific examples, but the protection scope of the present invention is not limited. Unless otherwise specified, the experimental methods used in the present invention are all conventional methods, and the experimental equipment, materials, reagents, etc. used can be obtained from commercial channels.

[0023] Example 1

[0024] A method for producing crude oil and soda ash from oil-alkali paragenesis ore, comprising the following steps:

[0025] 1. Carry out three-phase separation of the produced liquid from the oil-alkali paragenetic ore: The produced liquid from the oil-alkali paragenetic ore is transported to the three-phase separator, and the oil, natural gas and brine in the oil-alkali paragenetic ore are separated into three phases. The three-phase separator is allowed to settle for 40 minutes until the oil content of the produced liquid from the oil-alkali paragenetic ore reaches ≤3000mg / L and the water content of the separated oil reaches ≤30%;

[0026] 2. Further dehydration of the separated oil: The oil separated by the three-phase separator in step 1 is further dehydrated by the electric dehydrator. The water droplets in the oil are charged with "positive-negative" charges by the electric field coalescence method under the influence of the electric field, collide with each other, merge, gather together, and settle and separate from the oil until the water content of the oil treated by the electric dehydrator is ≤0.5%, and 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, and undergoes primary sedimentation treatment in the brine sedimentation tank for a residence time of 4 hours. The floating oil in the brine is separated by gravity sedimentation. After this step, the removal efficiency of the floating oil is ≥70%;

[0028] 4. Brine cyclone separation: In step 3, the oily brine in the brine settling tank is lifted to the cyclone separation device by a lifting pump, and cyclone separation is performed by horizontal centrifugal force. The oil droplet diameter is detected to be ≥50nm, and the removal efficiency of cyclone separation is 50%;

[0029] 5. Brine filtration: The oily brine separated by the cyclone separation device in step 4 is lifted to a two-stage filter by a lifting pump, wherein the first-stage filter adopts a walnut shell filter, and the density of the walnut shell filter material is greater than or equal to 1.25g / cm 3 , bulk density 0.8-0.85g / cm 3 The particle size of walnut shell filter material is 0.6-1.2mm, and the filling height is 1.2-1.4m. Walnut shells are used to filter out the remaining oil in the brine. The secondary filter uses a double filter material filter, and the filter materials are quartz sand and magnetite filter materials. The particle size of quartz sand filter material is 0.5-0.8mm, and the particle size of magnetite filter material is 0.25-0.5mm. The double filter material filter is used to remove the remaining suspended matter in the brine.

[0030] 6. Extracting soda ash from brine: The brine filtered in step 5 is heat exchanged with high-temperature steam in heat exchanger a to 80° C. and then transported to a wet decomposition tower. After heat exchange with rising steam in the wet decomposition tower, the temperature is raised to 100° C. for wet decomposition, and NaHCO3 in the brine is decomposed into Na2CO3. Subsequently, the brine whose main component is Na2CO3 is evaporated and concentrated by MVR process. After concentration, the content of natural alkali in the brine is increased from 12% of the raw water to 24%. The concentrated Na2CO3 solution enters a triple-effect evaporator for crystallization, wherein the first effect is at normal pressure of 105° C., the second effect is at negative pressure of 85° C., and the third effect is at negative pressure of 65° C., until the Na2CO3 in the brine is crystallized in the form of Na2CO3·H2O, the monohydrate crystals are centrifugally dried and calcined to remove crystal water, and dense soda ash can be obtained. The dense soda ash is sent to a silo for storage or to a packaging workshop for packaging and transportation.

[0031] Example 2

[0032] A method for producing crude oil and soda ash from oil-alkali paragenesis ore, comprising the following steps:

[0033] 1. Carry out three-phase separation of the produced liquid from the oil-alkali paragenetic ore: The produced liquid from the oil-alkali paragenetic ore is transported to the three-phase separator, and the oil, natural gas and brine in the oil-alkali paragenetic ore are separated into three phases. The three-phase separator is allowed to settle for 40 minutes until the oil content of the produced liquid from the oil-alkali paragenetic ore reaches ≤3000mg / L and the water content of the separated oil reaches ≤30%;

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

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

[0036] 4. Brine cyclone separation: In step 3, the oily brine in the brine settling tank is lifted to the cyclone separation device by a lifting pump, and cyclone separation is performed by horizontal centrifugal force. The oil droplet diameter is ≥50nm, and the removal efficiency of cyclone separation is 90%;

[0037] 5. Brine filtration: The oily brine separated by the cyclone separation device in step 4 is lifted to a two-stage filter by a lifting pump, wherein the first-stage filter adopts a walnut shell filter, and the density of the walnut shell filter material is greater than or equal to 1.25g / cm 3, bulk density 0.8-0.85g / cm 3 The particle size of walnut shell filter material is 0.6-1.2mm, and the filling height is 1.2-1.4m. Walnut shells are used to filter out the remaining oil in the brine. The secondary filter uses a double filter material filter, and the filter materials are quartz sand and magnetite filter materials. The particle size of quartz sand filter material is 0.5-0.8mm, and the particle size of magnetite filter material is 0.25-0.5mm. The double filter material filter is used to remove the remaining suspended matter in the brine.

[0038] 6. Extracting soda ash from brine: The brine filtered in step 5 is heat exchanged with high-temperature steam in heat exchanger a to 80° C. and then transported to a wet decomposition tower. After heat exchange with rising steam in the wet decomposition tower, the temperature is raised to 115° C. for wet decomposition, and NaHCO3 in the brine is decomposed into Na2CO3. Subsequently, the brine whose main component is Na2CO3 is evaporated and concentrated by MVR process. After concentration, the content of natural alkali in the brine is increased from 12% of the raw water to 24%. The concentrated Na2CO3 solution enters a triple-effect evaporator for crystallization, wherein the first effect is at normal pressure 105° C., the second effect is at negative pressure 85° C., and the third effect is at negative pressure 65° C., until the Na2CO3 in the brine is crystallized in the form of Na2CO3·H2O, the monohydrate crystals are centrifugally dried and calcined to remove crystal water, and heavy soda ash can be obtained. The heavy soda ash is sent to a silo for storage or to a packaging workshop for packaging and transportation.

[0039] The above-described embodiments are only preferred embodiments of the present invention, but not all feasible embodiments of the present invention. For those skilled in the art, any obvious changes made thereto without departing from the principles and spirit of the present invention should be considered to be included in the scope of protection of the claims of the present invention.

Claims

1. A method for producing crude oil and soda ash from oil-alkali paragenesis ore, characterized in that: Here are the steps: S1. Separate the produced liquid from the oil-alkali symbiotic ore into three phases; S2. The separated oil is further dehydrated; S3. Separated brine sedimentation treatment; S4. Brine cyclone separation; S5. Brine filtration; S6. Extracting soda ash from brine.

2. The method for producing crude oil and soda ash from oil-alkali paragenesis ore according to claim 1, characterized in that: Step S1 specifically comprises: collecting and transporting the produced liquid of the oil-alkali paragenetic ore to a three-phase separator (1), performing three-phase separation of the oil, natural gas and brine in the oil-alkali paragenetic ore, and allowing the three-phase separator (1) to settle for 40 minutes until the oil content of the produced liquid of the oil-alkali paragenetic ore reaches ≤3000 mg / L and the water content of the separated oil reaches ≤30%.

3. The method for producing crude oil and soda ash from oil-alkali paragenesis ore according to claim 1, characterized in that: Step S2 specifically comprises: the oil separated by the three-phase separator (1) in step S1 is further dehydrated by the electric dehydrator (2), and the water droplets in the oil are charged with positive and negative charges under the influence of the electric field by using the electric field agglomeration method, so that the water droplets collide with each other, merge, gather together, and settle and separate from the oil, until the water content of the oil treated by the electric dehydrator (2) is ≤0.5%, and enters the purified oil storage tank (15) for storage.

4. The method for producing crude oil and soda ash from oil-alkali paragenesis ore according to claim 1, characterized in that: Step S3 specifically comprises: the brine separated by the three-phase separator (1) in step S1 and the electric dehydrator (2) in step S2 enters the brine settling tank (3), undergoes primary sedimentation treatment in the brine settling tank (3), and stays there for 4-8 hours, and separates the floating oil in the brine by gravity sedimentation.

5. The method for producing crude oil and soda ash from oil-alkali paragenesis ore according to claim 1, characterized in that: Step S4 is specifically as follows: the oily brine in the brine settling tank (3) of step S3 is lifted into the cyclone separation device (5) by the lifting pump (4), and cyclone separation is performed by horizontal centrifugal force.

6. The method for producing crude oil and soda ash from oil-alkali paragenesis ore according to claim 1, characterized in that: Step S5 specifically comprises: the oily brine separated by the cyclone separation device (5) in step S4 is lifted to a two-stage filter by a lifting pump (4), wherein the first-stage filter is a walnut shell filter (6), and the density of the walnut shell filter material is greater than or equal to 1.25 g / cm 3 , bulk density 0.8-0.85g / cm 3 The particle size of the walnut shell filter material is 0.6-1.2mm, and the filling height is 1.2-1.4m. The walnut shell is used to filter out the remaining petroleum in the brine; the secondary filter adopts a double filter material filter (7), and the filter materials are quartz sand and magnetite filter materials respectively. The particle size of the quartz sand filter material is 0.5-0.8mm, and the particle size of the magnetite filter material is 0.25-0.5mm. The double filter material filter (7) is used to remove the remaining suspended matter in the brine.

7. The method for producing crude oil and soda ash from oil-alkali paragenesis ore according to claim 1, characterized in that: Step S6 specifically comprises: the brine filtered in step S5 is heat exchanged with high-temperature steam in heat exchanger a (8) to 80°C and then transported to a wet decomposition tower (9). In the wet decomposition tower (9), the brine is heated to 100°C-115°C after heat exchange with steam rising from heat exchanger b (10) to perform wet decomposition, thereby decomposing NaHCO3 in the brine into Na2CO3. Subsequently, the brine whose main component is Na2CO3 enters an MVR device (11) to evaporate and concentrate the Na2CO3 solution. After concentration, the content of natural soda in the brine is increased from 12% of the original water to 24%. The concentrated Na2CO3 solution enters a three-effect evaporator (12) for crystallization, wherein the first effect is at normal pressure of 105°C, the second effect is at negative pressure of 85°C, and the third effect is at negative pressure of 65°C. After the Na2CO3 in the brine is crystallized in the form of Na2CO3·H2O, the monohydrate soda crystals are placed in a centrifugal dryer (13) for centrifugal drying, and calcined in a fluidized bed dryer (14) to remove crystal water, thereby obtaining heavy soda ash.

8. The method for producing crude oil and soda ash from oil-alkali paragenesis ore according to claim 7, characterized in that: The heavy soda ash obtained in step S6 is sent to the purified oil storage tank (15) for storage or to the packaging workshop for packaging and shipment.

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