Device for reducing content of metal ions in biological heavy oil

Abstract

The utility model discloses a device for reducing the content of metal ions in biological heavy oil. An outlet of a treating agent mother liquor tank is connected to a head tank after passing through a delivery pump, the top of the tank is connected back to the treating agent mother liquor tank through a return pipe, the bottom of the tank is connected with a conical tank, a high-temperature steam heating jacket is arranged in the tank, and a water inlet valve is arranged at the top of the tank; the other path is divided into three paths after being connected with a discharge isolating valve, one path is connected with a circulating liquid tank, the other path is led to a waste liquid treatment workshop, the third path is divided into two paths, one path is connected back to the circulating liquid tank, the other path is divided into two paths after being connected with a circulating isolating valve, one path is connected to the circulating liquid tank after passing through a biological heavy oil feeding valve before treatment, and the other path is connected with a circulating pump; the circulating pump is divided into two paths, one path is connected to the top of the conical tank, the other path is connected with an inlet in the top of the flash # imgabs 0 # device, and an outlet in the bottom of the flash # imgabs 1 # device is sequentially connected with a flash discharge valve, a transition groove and a discharge pump and then is connected to a biological heavy oil finished product tank. The device solves the problem that the content of metal ions in the existing biological heavy oil obviously exceeds the standard.

Description

Technical Field

[0001] The utility model relates to the technical field of biological heavy oil production devices, in particular to a device for reducing the metal ion content in biological heavy oil. Background Art

[0002] Biodiesel production generally uses waste animal and plant oils as feedstock, which react with methanol through esterification and alcoholysis to produce crude fatty acid methyl esters (CMEs). This CME is then distilled under reduced pressure to separate into different fractions. The fraction within the S50 specification, which serves as the middle fraction for the finished biodiesel product, accounts for the vast majority, while bio-heavy oil accounts for 5%-10%, primarily used as boiler fuel. Due to the generally poor quality of the feedstock used in biodiesel production and the tendency to saponify during the alcoholysis process, the quality of the bio-heavy oil is poor. This is primarily due to the fact that metal ion content, primarily sodium, in bio-heavy oil often reaches 1000 ppm. This significantly exceeds the sodium ion content requirement of ISO 8217-2024 (en), the international standard for marine fuels. Summary of the Invention

[0003] The purpose of the utility model is to provide a device for reducing the metal ion content in biological heavy oil, so as to solve the problem that the metal ion content, mainly sodium ions, in the existing biological heavy oil obviously exceeds the standard.

[0004] To achieve the above objectives, the present invention provides a device for reducing the metal ion content in bio-heavy oil, comprising a treatment agent mother liquor tank 1, a circulating liquid tank 2, a conical tank 3, a pre-treatment bio-heavy oil tank 4, a flash evaporation device 5, a bio-heavy oil finished product tank 6, an elevated tank 7, a direct air unit 8, a transition tank 9, a water inlet valve 10, a delivery pump 11, a circulating pump 12, a discharge pump 13, a delivery pump rear valve 14, an elevated tank front valve 15, an elevated tank reflux pipe 16, an elevated tank rear valve 17, a treatment agent mother liquor feed valve 18, a water vapor inlet valve 19, a steam trap 20, a compressed air inlet valve 21, and a discharge isolation valve. 22, circulating liquid discharge valve 23, waste liquid discharge valve 24, circulating liquid tank discharge valve 25, circulating isolation valve 26, pre-processed bio-heavy oil feed valve 27, circulating pump rear valve 28, conical tank front valve 29, flash feed valve 30 and flash discharge valve 31; the outlet pipe of the treatment agent mother liquid tank 1 is connected to the delivery pump 11 and then connected to the delivery pump rear valve 14, and then connected to the top inlet of the high-level tank 7 after passing through the high-level tank front valve 15; the top of the high-level tank 7 is connected back to the treatment agent mother liquid tank 1 through the high-level tank reflux pipe 16, and the bottom of the high-level tank 7 is connected to the treatment agent mother liquid inlet through the high-level tank rear valve 17 and the treatment agent mother liquid inlet The material valve 18 is connected to the conical tank 3; a high-temperature steam heating jacket with a steam inlet valve 19 and a steam trap 20 is provided in the conical tank 3 to heat and keep the material in the tank warm. A water inlet pipe with a water inlet valve 10 is provided on the top of the conical tank 3; one outlet at the bottom of the conical tank 3 is connected to the compressed air inlet valve 21 for stirring and homogenizing operation, and the other outlet is divided into three routes after connecting to the discharge isolation valve 22. The first route is connected to the circulating liquid tank 2 after connecting to the circulating liquid discharge valve 23, the second route is connected to the waste liquid treatment workshop after connecting to the waste liquid discharge valve 24, and the third route is divided into two routes, one route passes through the circulating liquid tank The discharge valve 25 is connected back to the circulating liquid tank 2. The other path is further divided into two paths after connecting to the circulation isolation valve 26. One path is connected to the circulating liquid tank 2 after passing through the pre-treated bio-heavy oil feed valve 27, and the other path is connected to the circulation pump 12. The circulation pump 12 is divided into two paths after connecting to the circulation pump rear valve 28. One path is connected to the top of the conical tank 3 after connecting to the conical tank front valve 29, and the other path is connected to the top inlet of the flash evaporation device 5 equipped with a vacuum unit 8 after passing through the flash evaporation feed valve 30. The bottom outlet of the flash evaporation device 5 is connected to the bio-heavy oil finished product tank 6 after connecting to the flash evaporation discharge valve 31, the transition tank 9 and the discharge pump 13 in sequence.

[0005] The device for reducing the metal ion content in bio-heavy oil of the utility model has the following technical features and beneficial effects:

[0006] 1. After treatment by the above device, the content of metal ions, mainly sodium ions, in bio-heavy oil can be reduced to below 50ppm, meeting the requirements for metal ion content in the international standard for marine fuel - ISO_8217_2024(en).

[0007] 2. The mother liquor of the treatment agent can be quickly diluted and replenished. The diluted liquid can be reused many times until it loses its efficacy and is then discharged to the waste liquid treatment workshop. Resources are comprehensively and efficiently utilized, saving production costs.

[0008] 3. Conical tank 3 integrates steam jacket heating, air pressure stirring, pump circulation stirring, feeding and discharging and other functions in one, with free switching and flexible process adjustment to ensure qualified treatment before discharge. BRIEF DESCRIPTION OF THE DRAWINGS

[0009] Figure 1 This is a schematic diagram of the structure of a device for reducing the metal ion content in biological heavy oil according to the present invention.

[0010] Figure numerals: treatment agent mother liquor tank 1, circulating liquid tank 2, conical tank 3, pre-treatment bio-heavy oil tank 4, flash evaporation device 5, bio-heavy oil finished product tank 6, elevated tank 7, direct air unit 8, transition tank 9, water inlet valve 10, delivery pump 11, circulating pump 12, discharge pump 13, delivery pump rear valve 14, elevated tank front valve 15, elevated tank reflux pipe 16, elevated tank rear valve 17, treatment agent mother liquor feed valve 18, water vapor inlet valve 19, steam trap 20, compressed air inlet valve 21, discharge isolation valve 22, circulating liquid discharge valve 23, waste liquid discharge valve 24, circulating liquid tank discharge valve 25, circulation isolation valve 26, pre-treatment bio-heavy oil feed valve 27, circulating pump rear valve 28, conical tank front valve 29, flash evaporation feed valve 30, flash evaporation discharge valve 31. DETAILED DESCRIPTION

[0011] The specific implementation of the device for reducing the metal ion content in bio-heavy oil according to the present invention will be further described in detail below with reference to the accompanying drawings.

[0012] Figure 1As shown, the device for reducing the metal ion content in bio-heavy oil of the present invention comprises a treatment agent mother liquor tank 1, a circulating liquid tank 2, a conical tank 3, a pre-treated bio-heavy oil tank 4, a flash evaporation device 5, a bio-heavy oil finished product tank 6, an elevated tank 7, a direct air unit 8, a transition tank 9, a water inlet valve 10, a delivery pump 11, a circulating pump 12, a discharge pump 13, a delivery pump rear valve 14, an elevated tank front valve 15, an elevated tank reflux pipe 16, an elevated tank rear valve 17, a treatment agent mother liquor feed valve 18, a water vapor inlet valve 19, a steam trap 20, a compressed air inlet valve 21, a discharge isolation valve 22, a circulating Circulating liquid discharge valve 23, waste liquid discharge valve 24, circulating liquid tank discharge valve 25, circulating isolation valve 26, pre-processed bio-heavy oil feed valve 27, circulating pump rear valve 28, conical tank front valve 29, flash feed valve 30 and flash discharge valve 31; the outlet pipe of the treatment agent mother liquid tank 1 is connected to the delivery pump 11 and then connected to the delivery pump rear valve 14, and then connected to the top inlet of the high-level tank 7 after passing through the high-level tank front valve 15; the top of the high-level tank 7 is connected back to the treatment agent mother liquid tank 1 through the high-level tank reflux pipe 16, and the bottom of the high-level tank 7 is connected to the treatment agent mother liquid tank 1 through the high-level tank rear valve 17 and the treatment agent mother liquid feed valve 1 8 is then connected to the conical tank 3; a high-temperature steam heating jacket with a steam inlet valve 19 and a steam trap 20 is provided in the conical tank 3 to heat and keep the material in the tank warm. A water inlet pipe with a water inlet valve 10 is provided on the top of the conical tank 3; one outlet at the bottom of the conical tank 3 is connected to the compressed air inlet valve 21 for stirring and homogenizing operation, and the other outlet is divided into three routes after connecting to the discharge isolation valve 22. The first route is connected to the circulating liquid tank 2 after connecting to the circulating liquid discharge valve 23, the second route is connected to the waste liquid treatment workshop after connecting to the waste liquid discharge valve 24, and the third route is divided into two routes, one route is discharged through the circulating liquid tank Valve 25 is connected back to the circulating liquid tank 2. The other path is further divided into two paths after connecting to the circulating isolation valve 26. One path passes through the pre-processed bio-heavy oil feed valve 27 and is connected to the circulating liquid tank 2, and the other path is connected to the circulating pump 12. The circulating pump 12 is divided into two paths after being connected to the circulating pump rear valve 28. One path is connected to the top of the conical tank 3 after connecting to the conical tank front valve 29, and the other path is connected to the top inlet of the flash evaporation device 5 equipped with a vacuum unit 8 after passing through the flash evaporation feed valve 30. The bottom outlet of the flash evaporation device 5 is connected to the bio-heavy oil finished product tank 6 after being connected to the flash evaporation discharge valve 31, the transition tank 9 and the discharge pump 13 in sequence.

[0013] The specific operating steps of the device for reducing the metal ion content in bio-heavy oil of the utility model are as follows:

[0014] 1. Bio-heavy oil feeding: Close the treatment agent mother liquor feed valve 18, water inlet valve 10, compressed air inlet valve 21, discharge isolation valve 22, circulation isolation valve 26, and flash feed valve 30. Open the pre-treated bio-heavy oil feed valve 27, the circulation pump rear valve 28, and the conical tank front valve 29. Start the circulation pump 12 to pump the material in the pre-treated bio-heavy oil tank 4 into the conical tank 3. After the feeding is completed, close the pre-treated bio-heavy oil feed valve 27 and the conical tank front valve 29.

[0015] 2. Process water feeding: Open the water inlet valve 10 and feed water into the conical tank 3 according to the process requirements. After checking the steam trap 20 and confirming that it is in normal state, open the steam inlet valve 19 for heating.

[0016] 3. Feeding the treatment agent mother liquor: open the rear valve 14 of the delivery pump and the front valve 15 of the header tank, close the rear valve 17 of the header tank and the treatment agent mother liquor feed valve 18, start the delivery pump 11 to quantitatively pump the treatment agent mother liquor to the header tank 7, then stop the delivery pump 11 and close the front valve 15 of the header tank; open the compressed air inlet valve 21 to stir the material in the conical tank 3, open the rear valve 17 of the header tank and the treatment agent mother liquor feed valve 18, and slowly add the treatment agent mother liquor in the header tank 7 into the conical tank 3.

[0017] 4. Reaction control: Maintain the temperature in the conical tank 3 at 70-80°C. After reacting for 2-4 hours depending on the material, close the compressed air inlet valve 21 to stop stirring, and keep it warm and let it stand for 3-5 hours until the treatment agent aqueous solution settles to the bottom and separates into layers.

[0018] 5. Liquid separation operation: Close the waste liquid discharge valve 24, the circulating liquid tank discharge valve 25, and the circulating isolation valve 26. Open the discharge isolation valve 22 and the circulating liquid discharge valve 23 to discharge the treatment agent aqueous solution at the bottom of the conical tank 3 into the circulating liquid tank 2. During the discharge process, pay attention to the discharge port of the circulating liquid discharge valve 23. Close the circulating liquid discharge valve 23 if bio-heavy oil flows out.

[0019] 6. Flash Distillation Operation: After the flash evaporation device 5 is ready, start the vacuum unit 8, check and confirm that the circulating liquid discharge valve 23, waste liquid discharge valve 24, circulating liquid tank discharge valve 25, pre-processed bio-heavy oil feed valve 27, and conical tank front valve 29 are in the closed state. Open the circulation isolation valve 26, circulation pump rear valve 28, and flash evaporation feed valve 30, and pump the remaining bio-heavy oil after liquid separation in the conical tank 3 to the flash evaporation device 5 for flash evaporation to remove moisture. After the flash evaporation process is adjusted to meet the requirements, open the flash evaporation discharge valve 31 to allow the material to flow to the transition tank 9 for the flashed bio-heavy oil. After cooling, it is pumped to the bio-heavy oil finished product tank 6 via the discharge pump 13.

[0020] 7. Reuse of treatment agent dilution and replenishment of mother liquor: If the used treatment agent dilution in the circulating liquid tank 2 still has some efficacy after testing, it shall be processed as follows:

[0021] (1) Perform the bio-heavy oil feeding operation according to the above step 1.

[0022] (2) Close the discharge isolation valve 22, the pre-treatment bio-heavy oil feed valve 27, and the flash feed valve 30; open the circulating liquid tank discharge valve 25, the circulating isolation valve 26, the circulating pump rear valve 28, and the conical tank front valve 29; start the circulating pump 12 to pump the liquid back into the conical tank 3; and then follow the above steps 3 and 2 to replenish a certain amount of treatment agent mother liquor and water.

[0023] (3) The subsequent operations are carried out in the same manner as steps 4, 5, and 6 above.

[0024] If the test shows that the drug has no efficacy, the operation of discharging the spent treatment agent waste liquid is carried out: when the treatment agent dilution liquid becomes ineffective after multiple uses, it is discharged to the transition tank of the sewage treatment station for treatment by closing the circulating liquid discharge valve 23 and opening the waste liquid discharge valve 24 in the liquid separation operation step of the above step 5.

Claims

1. A device for reducing the metal ion content in bio-heavy oil, characterized by: The invention comprises a treatment agent mother liquid tank (1), a circulating liquid tank (2), a conical tank (3), a pre-treatment bio-heavy oil tank (4), a flash evaporation device (5), a bio-heavy oil finished product tank (6), an elevated tank (7), a direct air unit (8), a transition tank (9), a water inlet valve (10), a delivery pump (11), a circulating pump (12), a discharge pump (13), a delivery pump rear valve (14), an elevated tank front valve (15), an elevated tank reflux pipe (16), an elevated tank rear valve (17), a treatment agent mother liquid feed valve (18), a water vapor inlet valve (19), a steam trap (20), a compressed air inlet valve (21), a discharge isolation valve (22), and a circulating liquid discharge valve (23). , waste liquid discharge valve (24), circulating liquid tank discharge valve (25), circulating isolation valve (26), pre-processed bio-heavy oil feed valve (27), circulating pump rear valve (28), conical tank front valve (29), flash feed valve (30) and flash discharge valve (31); the outlet pipe of the treatment agent mother liquid tank (1) is connected to the delivery pump (11) and then connected to the delivery pump rear valve (14), and then connected to the top inlet of the high-level tank (7) after passing through the high-level tank front valve (15); the top of the high-level tank (7) is connected back to the treatment agent mother liquid tank (1) through the high-level tank reflux pipe (16), and the bottom of the high-level tank (7) is connected to the treatment agent mother liquid tank (1) through the high-level tank rear valve (17) and the treatment agent mother liquid feed valve (1 8) is connected to the conical tank (3); the conical tank (3) is provided with a high-temperature steam heating jacket with a steam inlet valve (19) and a steam trap (20) to heat and keep the material in the tank warm. The top of the conical tank (3) is provided with a water inlet pipe with a water inlet valve (10); one of the outlets at the bottom of the conical tank (3) is connected to the compressed air inlet valve (21) for stirring and homogenizing operation, and the other is divided into three routes after connecting to the discharge isolation valve (22). The first route is connected to the circulating liquid discharge valve (23) and then connected to the circulating liquid tank (2). The second route is connected to the waste liquid discharge valve (24) and then leads to the waste liquid treatment workshop. The third route is further divided into two routes, one of which passes through the circulating liquid tank discharge valve (25). The first path is connected to the circulating liquid tank (2), and the second path is further divided into two paths after being connected to the circulating isolation valve (26). One path is connected to the circulating liquid tank (2) after passing through the pre-processed bio-heavy oil feed valve (27), and the other path is connected to the circulating pump (12). The circulating pump (12) is divided into two paths after being connected to the circulating pump rear valve (28). One path is connected to the top of the conical tank (3) after being connected to the conical tank front valve (29), and the other path is connected to the top inlet of the flash evaporation device (5) equipped with a vacuum unit (8) after passing through the flash evaporation feed valve (30). The bottom outlet of the flash evaporation device (5) is connected to the bio-heavy oil finished product tank (6) after being connected to the flash evaporation discharge valve (31), the transition tank (9) and the discharge pump (13) in sequence.

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