TH94974B - How to deal with low-quality refined oil. - Google Patents

Abstract

------15/03/2566------(OCR) This invention relates to a method for processing inferior distillate oil. Such inferior distillate oil is separated into light distillate and heavy distillate oil. The heavy distillate oil is cracked using hydrogen, and the resulting substance is mixed with the light distillate oil and distilled using hydrogen. This application method can be used to produce high-yield, high-quality heavy naphtha and clean diesel fuel. Furthermore, the method involves a simple processing procedure and uses minimal energy. ------------ DC60 This invention relates to a method for processing inferior distillate oil. Such inferior distillate oil is separated into light distillate and heavy distillate oil. The heavy distillate oil is cracked using hydrogen, and the resulting substance is mixed with the light distillate oil and distilled using hydrogen. This application method can be used to produce high-yield, high-quality heavy naphtha and clean diesel fuel. Furthermore, the method involves a simple processing procedure and uses minimal energy.

Claims (14)

------15/03/2566------(OCR) 1. Method for processing inferior distillate oil, which includes: a. Separating the inferior distillate oil into light distillate with a final boiling point of 180-310 °C and heavy distillate with a final boiling point of 380-460 °C; b. Feeding the heavy distillate from step (a) into the hydrogen cracking area for hydrogen cracking with a hydrogen cracking catalyst; c. Mixing the hydrogen cracking agent from step (b) with the light distillate from step (a) and feeding the mixture into the hydrogen cracking area for hydrogen desulfurization, hydrogen nitrogen removal, and hydrogen saturation with a hydrogen cracking catalyst. The light distillate is then heated to a desired temperature at the inlet of the hydrogen cracking area by mixing it with the hydrogen cracking agent. and d. The hydrogen distillation product in step (c) is fed into a separator to separate the gas and liquid, where the resulting liquid phase is fed into a separation system to produce light naphtha, heavy naphtha and diesel oil.2. The method under claim 1 is characterized by the fact that the light distillation oil in step (3) has a final boiling point of 210-290 °C.3. The method under claim 1, characterized in step (b), the hydrogen cracking region is controlled under hydrogen partial pressure conditions of 3.0-20.0 MPa, reaction temperature of 300-440 °C, liquid hourly volumespace velocity of 0.1-10.0/hr, and hydrogen/oil volume ratio of 100:1-3000:14. The method under claim 1, characterized in step (b), the hydrogen cracking region is controlled under hydrogen partial pressure conditions of 5.0-16.0 MPa, reaction temperature of 350-420 °C, liquid hourly volumespace velocity of 0.2-5.0/hr. and a hydrogen/oil volume ratio of 500:1 -2000:15. Method according to claim 1 with the characteristic that in step (c) the hydrogen distillation area is controlled under conditions of hydrogen partial pressure 3.0-20.0 MPa, reaction temperature 280-400 °C, liquid volume feed rate 0.1-10.0 hrs/ and a hydrogen/oil volume ratio of 100:1-3000:16. Method according to claim 1 with the characteristic that in step (c) the hydrogen distillation area is controlled under conditions of hydrogen partial pressure 5.0-16.0 MPa, reaction temperature 300-370 °C, liquid volume feed rate 0.4-5.0 hrs/ and a hydrogen/oil volume ratio of 200:1-1500:17. The method under Reputation 1 is characterized by the pre-hydrogenation treated region being placed before the hydrogenation cracking region in step (b)8. The method under Reputation 7 is characterized by the volume ratio of the catalyst in the pre-hydrogenation treated region to the catalyst in the hydrogenation cracking region being in the range of 2:1 to 1:59. The method under Reputation 1 is characterized by the hydrogenation cracking catalyst being used in the hydrogenation cracking region, where the hydrogenation cracking catalyst is composed of an active cracking component including a molecular sieve of type H or an acidic amorphous alumina-silica, and an active component in 10. Hydrogenation involving one or more selectable compounds from W, Mo, Ni, and Co. 11. Method under claim 7 or 8 characterized by the use of a hydrogenated refining catalyst, including W, Mo, Ni, or Co as the active component, in the pre-hydrogenation treatment region. 12. Method under claim 1 characterized by the use of a coke-containing refined oil or a catalytic cracking refined oil. 13. Method under claim 1 characterized by the use of a hydrogenated cracking catalyst, including H-type beta zeolites, in the hydrogenated cracking region. The method under claim 12 is characterized by the inclusion of a hydrogenated cracking catalyst containing 0.5% by weight–40.0% by weight of H-type beta zeolite, with less than 0.15% by weight of Na2O in the H-type beta zeolite, and a molar ratio of SiO2/A12O3 in the range of 30–300.14. The method under claim 12 is characterized by the inclusion of a hydrogenated cracking catalyst containing 1.0% by weight–19.0% by weight of H-type beta zeolite, and a molar ratio of SiO2/A12O3 in the H-type beta zeolite in the range of 70–170. ------------ ------10/10/2560------(OCR) Page 1 of 3 pages. Claim 1. Method for handling low-quality refined oils comprising: a. Separating the low-quality refined oils into light refined oils. a. Feeding the light distillate from step (a) into the hydrogen cracking area for hydrogen-catalyzed cracking; c. Mixing the hydrogen-catalyzed cracking agent from step (b) with the light distillate from step (a) and feeding the mixture into the hydrogen-catalyzed cracking area for hydrogen-catalyzed desulfurization, hydrogen-catalyzed nitrogen removal, and hydrogen-catalyzed saturation, where the light distillate reaches the desired temperature at the inlet of the hydrogen-catalyzed cracking area while being mixed with the hydrogen-catalyzed cracking agent; and d. Feeding the hydrogen-catalyzed cracking product from step (c) into a separator for gas and liquid separation, where the resulting liquid phase is fed into the separation system. 1. To produce light naphtha, heavy naphtha and diesel fuel. 2. Method according to claim 1 by analyzing the properties that the light oil from the distillation in step (a) has a final boiling point of 210-290°C. 3. Method according to claim 1 by analyzing the properties that in step (b), the hydrogen cracking region is controlled under hydrogen partial pressure conditions of 3.0-20.0 MPa, reaction temperature of 300-440°C, liquid frothing rate of 0.1 - 10.0 hrs-1 and hydrogen/oil volume ratio of 100:1-3000:1. 4. Method according to claim 1 by analyzing the properties that in step (b), the hydrogen cracking region is controlled under hydrogen partial pressure conditions. 5.0-16.0 MPa, page 2 of 3. The reaction temperature is 350-420°C, the liquid feeding rate per hour is 0.2 - 5.0 hrs-1, and the hydrogen/oil volume ratio is 500:1 -2000:1. 5. Method according to claim 1 by analyzing the properties that in step (c), the distillation area occurs using hydrogen under hydrogen partial pressure conditions of 3.0 - 20.0 MPa, the reaction temperature is 280-400°C, the liquid feeding rate per hour is 0.1 - 10.0 hrs-1, and the hydrogen/oil volume ratio is 100:1 -3000:1. 6. Method according to claim 1 by analyzing the properties that in step (c), the distillation area occurs by... Hydrogen is used under conditions of hydrogen partial pressure 5.0-16.0 MPa, reaction temperature 300-370°C, liquid feed rate per hour 0.4 - 5.0 h-1, and hydrogen/water volume ratio 200:1 - 1500:1. 7. Method according to claim 1, by analyzing the properties, the pre-hydrogenation treatment region is placed before the hydrogen cracking region in step (b). 8. Method according to claim 7, by analyzing the properties, the volume ratio of the catalyst in the pre-hydrogenation treatment region to the catalyst in the hydrogen cracking region is in the range of 2:1 to 1:5. 9. Method according to claim 1, by analyzing the properties, the hydrogen cracking catalyst is used in the hydrogen cracking region, where the said catalyst consists of 10. Method according to claim 7 or 8, analyzing the properties of the hydrogenation catalyst, including W, Mo, Ni, or Co as the active component, which includes one or more selected components from W, Mo, Ni, and Co. 11. Method according to claim 1, analyzing the properties of the low-quality distillate, including coke or catalytic cracking distillate. 1. The method for handling the quality refined oil of this invention consists of: a. Separating the quality refined oil into light refined oil, which has a final boiling point of 180-310 °C, preferably 210-290 °C, and heavy refined oil, which has a final boiling point of 380-460 °C; b. Feeding the heavy refined oil from step (a) into the hydrogen cracking area with a hydrogen cracking catalyst; c. Mixing the product from step (b) with the light refined oil from step (a) and feeding the mixture into the hydrogen cracking area for hydrogen desulfurization, hydrogen denitrogenation, and hydrogen saturation with a catalyst, where the light refined oil is at the desired temperature at the inlet of the hydrogen cracking area while being mixed with the hydrogen cracking product; and d. Feeding the product from the hydrogen cracking area in step (c) into a separator for gas and liquid separation, where the resulting liquid phase is fed into the separation system. To produce light naphtha, heavy naphtha, and diesel fuel. 2. By method according to claim 1, the properties of the oil from the light distillation in step (a) are analyzed, and it has a final boiling point of 210-290 °C. 3. Method according to claim 1 by analyzing the properties that in step (b), the hydrogen cracking area is controlled under hydrogen partial pressure conditions of 3.0-20.0 MPa, reaction temperature of 300-400 °C, liquid feed rate per hour of 0.1 - 10.0 hrs-1 and hydrogen/oil volume ratio of 500:1 - 2000:1. 4. Method according to claim 1 by analyzing the properties that in step (b), the hydrogen cracking area is controlled under hydrogen partial pressure conditions of 5.0-16.0 MPa, reaction temperature of 300-400 °C, liquid feed rate per hour of 0.2 - 5.0 hrs-1 and hydrogen/oil volume ratio of 500:1 - 2000:1. 5. Method according to claim 1 by analyzing the properties that in step (c), the hydrogen cracking area is controlled under hydrogen partial pressure conditions of 3.0-20.0 MPa, reaction temperature of 280-400 °C, liquid feed rate per hour of 0.1 - 10.0 hrs-1 and hydrogen/oil volume ratio of 100:1 - 3000:1. 6. Method according to claim 1 by analyzing the properties that in step (c) the hydrogen cracking area is controlled under hydrogen partial pressure conditions of 5.0 -16.0 MPa, reaction temperature of 280-400 °C, liquid feed rate per hour of 0.4 - 5.0 hrs-1 and hydrogen/oil volume ratio of 200:1 - 1500:1. 7. The method under Claim 1, by analyzing the properties of the pre-hydrogenation treatment region to the catalyst in the hydrogenation fracture region, shows a ratio between 2:1 and 1:5. 8. The method under claim 7, by analyzing the properties, shows that the volume ratio of the catalyst in the pre-hydrogenation treatment region to the catalyst in the hydrogenation cracking region is in the range of 2:1 to 1:5. 9. The method under Claim 1, by analyzing the properties of the hydrogenation catalyst used in the hydrogenation region, where the catalyst consists of an active cracking component including a desiccant of type H or acidic amorphous alumina-silica, and an active hydrogenation component including one or more of the selected compounds from W, Mo, Ni, and Co. 10. The method under claim 7 or 8 involves analyzing the properties of the hydrogen-based distillation catalyst, including W, Mo, Ni, or Co, as the active component, to determine which is used in the pre-hydrogenation treatment region. 11. The method under Claim 1 involves analyzing the properties to determine whether the low-quality refined oil consists of coke-based refined oil or catalytic cracked refined oil. 12. The method under Claim 1, by analyzing the properties of the hydrogenated cracking catalyst consisting of (formula) H-type zeolite, will be used in the hydrogenated cracking region. 13. The method under claim 12, by analyzing the properties of the hydrogen-based cracking catalyst, consists of (formula) type H zeolites in amounts of 0.5 - 40.0% by weight, with Na2O present in amounts less than 0.15% by weight of the (formula) type H zeolites, and the molar ratio of SiO2/Al2O3 is in the range of 30-300. 14. The method under claim 12, by analyzing the properties of the hydrogen-based cracking catalyst, involves the inclusion of 1.0-19.0% by weight of (formula) H-type zeolites, where the molar ratio of SiaO2/Al2O3 in these (formula) H-type zeolites is in the range of 70-170.