CN115449397A - Visbreaking device and visbreaking method - Google Patents
Visbreaking device and visbreaking method Download PDFInfo
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- CN115449397A CN115449397A CN202110640182.9A CN202110640182A CN115449397A CN 115449397 A CN115449397 A CN 115449397A CN 202110640182 A CN202110640182 A CN 202110640182A CN 115449397 A CN115449397 A CN 115449397A
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
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- G01N33/28—Oils, i.e. hydrocarbon liquids
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Abstract
The invention provides a visbreaking device and a visbreaking method. The visbreaking apparatus comprises: a visbreaking unit having a feedstock oil inlet and a visbroken resid outlet; a raw oil acid value detection unit for detecting the acid value of the raw oil; and the viscosity-breaking residual oil acid value detection unit is used for detecting the acid value of the viscosity-breaking residual oil. In the case of using the visbreaking apparatus and the visbreaking method of the present invention, the degree of back-mixing of the materials in the visbreaking apparatus can be clearly reflected by the measurement of the acid values of the feedstock and the visbroken residue and the calculation of the reduction rate of the acid value. Accordingly, the structure, process, etc. of the visbreaking unit can be improved to ensure that the visbreaking is operated at high severity, and the best performance of the visbreaking process is exerted.
Description
Technical Field
The application relates to the technical field of petroleum processing, in particular to a visbreaking device and a visbreaking method.
Background
With the increasing world economy and the increasing demand of petroleum, the conventional petroleum resources cannot meet the demand of people, and the heavy crude oil becomes the main raw material in the current petroleum processing. The visbreaking has the characteristics of mature technology, less investment, easy construction, low operation cost, low requirement on raw materials and the like, and plays an important role in the heavy oil processing technology.
The visbreaking process is one of the effective ways to lighten heavy inferior oil. Visbreaking is a parallel sequential reaction process in which both cracking and condensation reactions occur. In actual production, it is desired to increase the cracking depth of the visbreaking process, but if the cracking depth is increased, the reaction temperature is increased or the reaction time is prolonged, which causes problems such as increased condensation reaction, coking, equipment blockage, and the like, and shortens the production cycle. In contrast, in the case of low reaction severity, high visbreaking efficiency cannot be obtained. In addition, the viscosity-reducing oil stability is reduced with the increase in condensation reactions, so that the fuel oil stratifies until precipitation affects product storage and transport. Therefore, the difficult problem to be solved is how to balance the relationship between the normal operation of the device and the improvement of the reaction severity for producing light oil in large quantity.
In order to reduce the viscosity of residual oil, produce light distillate as much as possible and keep good visbreaking oil stability, the key problem is how to keep materials in a visbreaking reaction tower in a horizontal plug flow state and reduce back mixing, because the materials have small reaction severity and large reaction severity along with the increase of the back mixing degree, the visbreaking reaction tower can only be operated at low severity to ensure the stability of products and the long-term operation of the device, and therefore, the back mixing degree of the materials in the visbreaking reaction tower is the most critical factor for visbreaking, namely, the back mixing degree of the materials in the visbreaking reaction tower is smaller, and the severity of visbreaking can be larger for the same material on the premise of ensuring the product quality and the long-term stable operation of the device. Therefore, how to judge and measure the relative strength of the material back-mixing in the viscosity-reducing reaction tower is particularly important, and the structure and the process which can keep or promote the material back-mixing degree in the reactor are reduced through measurement, so that the viscosity-reducing cracking is ensured to be operated under high severity, and the optimal efficiency of the viscosity-reducing cracking process is exerted.
However, the prior art methods are not effective in assessing the degree of back-mixing of the feed in the visbreaker reaction column. Therefore, there is still a need for an apparatus and method that clearly reflects the degree of material backmixing in a visbreaker reactor.
Disclosure of Invention
The present application mainly aims to provide a visbreaking apparatus and a visbreaking method, so as to solve the problem in the prior art that the degree of back-mixing of materials in a visbreaking reaction tower cannot be effectively evaluated.
In order to achieve the above object, according to one aspect of the present application, there is provided a visbreaking apparatus comprising: a visbreaking unit having a feedstock oil inlet and a visbroken resid outlet; a raw oil acid value detection unit for detecting the acid value of the raw oil; and the visbreaking residual oil acid value detection unit is used for detecting the acid value of the visbreaking residual oil.
Further, in the visbreaking device, the visbreaking unit is provided with an automatic control device, a pressure controller and a temperature controller, and the automatic control device is connected with the raw oil acid value detection unit, the visbreaking residue acid value detection unit, the pressure controller and the temperature controller; and the automatic control equipment receives the acid value of the raw oil and the acid value of the visbreaking residual oil and calculates the reduction rate of the acid value, and the automatic control equipment adjusts the pressure controller and the temperature controller of the visbreaking unit in real time according to the reduction rate of the acid value.
Further, in the above visbreaking apparatus, the visbreaking apparatus further includes a first stock oil supply unit and a second stock oil supply unit, and the stock oil inlet is connected to the first stock oil supply unit and the second stock oil supply unit, respectively; the automatic control equipment is connected with the first raw oil supply unit and the second raw oil supply unit, receives the acid value of the viscosity-breaking residual oil and the acid value of the raw oil, and adjusts the feeding amount of the first raw oil supply unit and/or the second raw oil supply unit in real time according to the reduction rate of the acid value.
Further, in the above visbreaking apparatus, the visbreaking apparatus further includes: the gas-liquid separation unit is provided with a raw material inlet and a liquid separator outlet, the liquid separator outlet is connected with the raw material oil inlet of the visbreaking unit, the gas-liquid separation unit is used for carrying out gas-liquid separation on the raw material oil to obtain a gas-state separator and a liquid-state separator, and the gas-state separator comprises water and light gas oil; and the raw oil supply unit is respectively connected with a raw material inlet of the gas-liquid separation unit and a raw oil inlet of the visbreaking unit, the visbreaking unit is provided with automatic control equipment, the automatic control equipment is connected with the raw oil acid value detection unit, the visbreaking residual oil acid value detection unit, the raw oil supply unit and the gas-liquid separation unit, the automatic control equipment receives the acid value of the visbreaking residual oil and the acid value of the raw oil and calculates the acid value reduction rate, and the feeding amount of the gas-liquid separation unit and/or the visbreaking unit and/or the temperature of the gas-liquid separation unit are adjusted in real time according to the acid value reduction rate.
Further, in the above visbreaking apparatus, the visbreaking apparatus further includes a feedstock supply unit, and the visbreaking unit further includes: a first visbreaking unit having a first feedstock inlet and a first visbroken resid outlet; the second visbreaking unit is provided with a second raw oil inlet and a second visbreaking residual oil outlet, and the raw oil supply unit is respectively connected with the first raw oil inlet and the second raw oil inlet; the viscosity-breaking residue acid value detection unit is used for detecting the acid value of the viscosity-breaking residue at the outlet of the first viscosity-breaking residue and recording the acid value as a first acid value, and is used for detecting the acid value of the viscosity-breaking residue at the outlet of the second viscosity-breaking residue and recording the acid value as a second acid value, wherein the viscosity-breaking device is provided with automatic control equipment, the automatic control equipment is connected with the raw oil supply unit, the raw oil acid value detection unit and the viscosity-breaking residue acid value detection unit, the automatic control equipment receives the first acid value, the second acid value and the acid value of the raw oil and calculates a first acid value reduction rate and a second acid value reduction rate, and the feeding amount of the first viscosity-breaking unit and/or the second viscosity-breaking unit is adjusted in real time according to the first acid value reduction rate and the second acid value reduction rate.
According to another aspect of the present invention, there is provided a visbreaking process comprising: step S1, detecting the acid value of raw oil; s2, performing visbreaking on the raw oil to obtain visbroken produced oil, and fractionating the visbroken produced oil to obtain visbroken residual oil; and S3, detecting the acid value of the visbreaking residual oil, and calculating the reduction rate of the acid value.
Further, in the above visbreaking method, further comprising: the pressure and/or temperature of the visbreaker is adjusted based on the acid number reduction.
In the above visbreaking method, the feed oil in step S1 is a mixture of a plurality of feed oils, and the visbreaking method further comprises adjusting the composition of the feed oil based on the acid value reduction rate.
Further, in the above visbreaking process, the visbreaking process further comprises: according to the acid value reduction rate, carrying out gas-liquid separation on the hot mixture before feeding of the raw oil to obtain a gaseous separated substance and a liquid separated substance, and carrying out visbreaking on the liquid separated substance.
Further, in the above visbreaking method, the temperature of gas-liquid separation is adjusted according to the reduction rate of the acid value.
Further, in the above visbreaking process, the gaseous isolate comprises water and light gas oil.
Further, in the above visbreaking method, step S2 includes performing visbreaking on the feedstock oil under a first visbreaking condition to obtain a first visbreaking product oil, fractionating the first visbreaking product oil to obtain a first visbreaking residue, performing visbreaking on the feedstock oil under a second visbreaking condition to obtain a second visbreaking product oil, and fractionating the second visbreaking product oil to obtain a second visbreaking residue, where the first visbreaking condition is different from the second visbreaking condition; step S3 comprises the steps of detecting the acid value of the first viscosity-breaking residual oil and the acid value of the second viscosity-breaking residual oil, calculating a first acid value reduction rate according to the acid value of the raw oil and the acid value of the first viscosity-breaking residual oil, and calculating a second acid value reduction rate according to the acid value of the raw oil and the acid value of the second viscosity-breaking residual oil; and wherein the visbreaking process further comprises: and S4, selecting visbreaking conditions according to the first acid value reduction rate and the second acid value reduction rate.
Further, in the visbreaking method, the visbroken residual oil is visbroken product oil and is subjected to real boiling point distillation to obtain residual oil with the temperature of more than 430 ℃.
In the case of using the visbreaking apparatus and the visbreaking method of the present invention, the degree of back-mixing of the materials in the visbreaking apparatus can be clearly reflected by the measurement of the acid values of the feedstock and the visbroken residue and the calculation of the reduction rate of the acid value. Accordingly, the structure, process, etc. of the visbreaking unit can be improved to ensure that the visbreaking is operated at high severity, and the best performance of the visbreaking process is exerted.
Detailed Description
It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present application will be described in detail with reference to examples.
It is clear from the foregoing background that the prior art methods are not effective in assessing the degree of material backmixing in a visbreaking reactor. In view of the foregoing technical problems, the present application provides a visbreaker and a visbreaking method.
The applicant has found that the acid number of the visbroken feedstock is mainly contributed by the petroleum acids contained therein. The petroleum acid is easily decomposed above 370 ℃, if the material is not back-mixed in the visbreaking reactor, the petroleum acid of the visbreaking residual oil is easily removed under the normal visbreaking condition, but if the material is back-mixed in the visbreaking process, the retention time of part of the material in the visbreaking reactor is too short, the petroleum acid of the part of the material is not fully decomposed, and the acid value of the visbreaking residual oil is still high. Therefore, under the same visbreaking conditions, the visbroken residual oil obtained from the same high-acid visbroken raw material with different back mixing degree in the visbreaking tower has different acid value. On the basis that the acid value detection technology is relatively mature detection technology in the field, so that the measurement of the back mixing degree by using the acid value becomes particularly feasible, in an exemplary embodiment of the present application, a visbreaking apparatus is provided, which comprises a visbreaking unit, a raw oil acid value detection unit and a visbreaking residue acid value detection unit, wherein the visbreaking unit has a raw oil inlet and a visbreaking residue outlet, and the raw oil acid value detection unit is used for detecting the acid value of the raw oil and detecting the acid value of the visbreaking residue.
In the case of using the visbreaker of the present application, the acid value of the feedstock is detected by the feedstock acid value detection means before the feedstock enters the visbreaker. After entering a visbreaking device through a raw oil inlet, obtaining visbreaking generated oil through the visbreaking device, fractionating the visbreaking generated oil to obtain visbreaking residual oil and distillate oil, and performing acid value detection on the visbreaking residual oil by using a visbreaking residual oil acid value detection unit.
The raw material for the viscosity-reducing test is high-acid-value residual oil with an acid value not less than 1.0 mgkOH/g; when the visbreaking test raw material is low acid value residue with an acid value of less than 1.0mgkOH/g, a certain amount of high acid value vacuum residue is added, the acid value of the mixed raw material is adjusted to be not less than 1.0mgkOH/g, and then the raw material is used for testing.
The acid value of the raw oil in the viscosity reduction test is the acid value of residual oil with the temperature of more than 430 ℃ obtained by distilling the raw oil with a real boiling point; the acid value of the visbreaking residual oil is the acid value of residual oil with the temperature of more than 430 ℃ obtained by distilling the real boiling point of the visbreaking generated oil.
After the raw oil acid value detection unit and the viscosity breaking residual oil acid value detection unit detect the raw oil acid value and the viscosity breaking residual oil acid value, the raw oil acid value and the viscosity breaking residual oil acid value can be obtained. The acid number reduction after visbreaking of the feedstock was calculated by the following formula:
the reduction ratio of acid value = (raw oil acid value-visbreaking residue acid value)/raw oil acid value × 100% (formula 1)
Through the formula, the reduction rate of the acid value can be calculated, the device can be used for measuring the acid value reduction rate of visbreaking of the raw materials under the same operation condition in a visbreaking tower of the same visbreaking device for different raw materials, the large reduction rate of the acid value indicates that the back mixing degree of the materials in the visbreaking device (such as the visbreaking tower) is small, and on the contrary, the small reduction rate of the acid value indicates that the back mixing degree of the materials in the visbreaking device is large, the reduction rates of the acid values are close to each other, which indicates that the back mixing degrees of the two materials in the visbreaking device are equivalent, so that the acid value reduction rate of the visbreaking of the raw materials under the same operation condition in the same visbreaking device can be clearly reflected by measuring the reduction rate of the acid value of the visbreaking of the raw materials under the same operation condition in the visbreaking device for different materials.
Different from the device which can not effectively evaluate the back mixing degree of materials in the visbreaking reaction tower in the prior art, under the condition of using the device, the back mixing degree of the materials in the visbreaking reaction tower can be clearly reflected through the measurement of the acid values of the raw materials and the visbreaking residual oil and the calculation of the reduction rate of the acid values. Accordingly, the structure, process, etc. of the visbreaking unit can be improved to ensure that the visbreaking is operated at high severity, and the best performance of the visbreaking process is exerted.
In some embodiments of the present application, the visbreaking unit is equipped with an automatic control device, a pressure controller, and a temperature controller, the automatic control device is connected with the raw oil acid value detection unit, the visbreaking residue acid value detection unit, the pressure controller, and the temperature controller; and the automatic control equipment receives the acid value of the raw oil and the acid value of the visbreaking residual oil and calculates the reduction rate of the acid value, and the automatic control equipment adjusts the pressure controller and the temperature controller of the visbreaking unit in real time according to the reduction rate of the acid value. In this embodiment, the visbreaking apparatus performs the visbreaking reaction under the control of the automatic control apparatus. After the raw oil acid value and the visbroken residue acid value are measured, the reduction rate of the acid value is calculated by the formula (1). The automatic control equipment of the visbreaking equipment can adjust the temperature, the pressure, the reaction time and the like of the visbreaking equipment in real time according to the calculated reduction rate of the acid value. When the automatic control equipment detects that the reduction rate of the acid value is lower than a set value, the temperature, the pressure and the reaction time of the visbreaking unit are automatically adjusted, so that the reaction condition of the visbreaking unit is changed, and the acid value of the visbreaking residual oil generated after the reaction condition is changed is further measured to calculate the reduction rate of the acid value. In the visbreaking process, the automatic control equipment can regulate and control the conditions of visbreaking temperature, pressure, reaction time and the like so as to ensure that the acid value reduction rate is in a controllable range for visbreaking. Under the process condition of the largest acid value reduction rate, the materials in the visbreaking unit are subjected to back mixing to a smaller degree, so that the problem of excessive coking of the materials in the visbreaking unit is effectively solved.
In other embodiments of the present application, the visbreaking apparatus further comprises a first stock oil supply unit and a second stock oil supply unit. The raw oil inlet is respectively connected with the first raw oil supply unit and the second raw oil supply unit; the automatic control equipment is connected with the first raw oil supply unit and the second raw oil supply unit, receives the acid value of the viscosity-breaking residual oil and the acid value of the raw oil, and adjusts the feeding amount of the first raw oil supply unit and/or the second raw oil supply unit in real time according to the reduction rate of the acid value. In this embodiment, the first stock oil supply unit and the second stock oil supply unit are both connected to the stock oil inlet of the visbreaker. The first feedstock oil and the second feedstock oil have different compositions. The raw oil acid value detection unit may detect the acid values of the first raw oil and the second raw oil entering the raw oil inlet to obtain the first raw oil acid value and the second raw oil acid value, respectively, before the raw oil enters the visbreaking apparatus, or may detect the mixed raw oil to obtain the raw oil acid value after the first raw oil and the second raw oil are mixed.
With the above visbreaking apparatus, the raw oil for visbreaking can be selected, for example, in one embodiment, the first raw oil is first fed into the visbreaking apparatus, and after the visbreaking cracking is performed in the visbreaking apparatus to generate the first visbroken residue, the acid value of the first visbroken residue is detected by the visbroken residue acid value detection unit. The feed of the first feedstock is then stopped and the visbreaker is fed using the second feedstock supply unit. After visbreaking cracking is carried out in the visbreaking device to generate a second visbroken residue, the acid value of the second visbroken residue is detected by the visbroken residue acid value detection unit. The automatic control unit receives the first raw oil acid value and the first visbreaking residue acid value and calculates the reduction rate of the first acid value according to the formula (1), and receives the second raw oil acid value and the second visbreaking residue acid value and calculates the reduction rate of the second acid value according to the formula (1). And the automatic control unit compares the reduction rate of the first acid value with the reduction rate of the second acid value, and then selects raw oil with high acid value reduction rate to feed the visbreaking device.
With the above visbreaker, the composition of the visbroken mixed feedstock can be adjusted, such as in one embodiment, the first feedstock and the second feedstock are simultaneously fed to the visbreaker. Before the mixed material enters the visbreaking device, the raw oil acid value detection unit detects the acid value of the mixed material to obtain the raw oil acid value. After the mixed raw oil is subjected to visbreaking in the visbreaking device to generate the visbroken residual oil, the acid value of the visbroken residual oil is detected by the visbroken residual oil acid value detection unit. And the automatic control unit receives the acid value of the raw material oil and the acid value of the viscosity-breaking residual oil and calculates the reduction rate of the viscosity-breaking acid value of the raw material according to the formula (1). The automatic control unit automatically adjusts the feeding amount of the first stock oil supply unit and/or the second stock oil supply unit, thereby obtaining a plurality of different acid value reduction rates. In the visbreaking process, the automatic control equipment can regulate and control the composition of the mixed raw oil fed into the visbreaking device so as to ensure that the acid value reduction rate is in a controllable range for visbreaking.
In other embodiments of the present application, the visbreaking apparatus further comprises: the gas-liquid separation unit is provided with a raw material inlet and a liquid separator outlet, the liquid separator outlet is connected with a raw material oil inlet of the visbreaking unit, the gas-liquid separation unit is used for carrying out gas-liquid separation on hot mixture before feeding of the visbreaking unit to obtain a gas-state separator and a liquid-state separator, and the gas-state separator comprises water and light gas oil; the system comprises a raw oil supply unit, a raw oil supply unit and an automatic control device, wherein the raw oil supply unit is respectively connected with a raw material inlet of a gas-liquid separation unit and a raw oil inlet of a visbreaking unit, the visbreaking unit is provided with the automatic control device, the automatic control device is connected with a raw oil acid value detection unit, a visbreaking residual oil acid value detection unit, a raw oil supply unit and the gas-liquid separation unit, the automatic control device receives the acid value of the visbreaking residual oil and the acid value of the raw oil and calculates the acid value reduction rate, and the feeding amount of the gas-liquid separation unit and/or the visbreaking unit and/or the temperature of the gas-liquid separation unit are/is adjusted in real time according to the acid value reduction rate.
In these embodiments, the visbreaking apparatus of the present application includes a visbreaking unit, a crude oil acid value detection unit, a visbroken residue acid value detection unit, a gas-liquid separation unit, and a crude oil supply unit. Wherein the raw oil supply unit is directly connected with the visbreaking unit, and can directly feed the raw oil to the visbreaking device. The feedstock supply unit may also be connected with the visbreaking unit via a gas-liquid separation unit so that the feedstock may be separated into a liquid separator and a gaseous separator including water and light gas oil after gas-liquid separation via the gas-liquid separation unit. After gas-liquid separation, the liquid isolate is fed to a visbreaking unit. Light gas oil components have been removed from the feed oil prior to visbreaking. In the subsequent visbreaking reaction, as the reaction system does not contain water and light gas oil components any more, the visbreaking reaction can be carried out at higher severity, thereby avoiding the problems of material back-mixing caused by gas phase components such as water and light gas oil and the like and excessive coking caused by partial material condensation. The stock oil acid value detection unit may detect the acid value of the stock oil supplied from the stock oil supply unit. The automatic control equipment is connected with the raw oil acid value detection unit, the viscosity breaking residual oil acid value detection unit, the raw oil supply unit and the gas-liquid separation unit, so that the process parameters such as temperature, pressure and the like of the gas-liquid separation unit can be adjusted in real time through the difference between the raw oil acid value and the viscosity breaking residual oil acid value.
In one embodiment, the acid value of the feedstock is first detected using a feedstock acid value detection unit. And then feeding the raw oil into a visbreaking device for visbreaking to obtain visbreaking product oil. And then the oil is discharged from the viscosity breaking device through a viscosity breaking residual oil outlet, and is subjected to acid value detection through a slag viscosity breaking oil acid value detection unit arranged at the viscosity breaking residual oil outlet. And (3) receiving the acid value of the raw oil and the acid value of the visbroken residual oil by automatic control equipment, and calculating the reduction rate of the visbroken acid value of the raw material according to the formula (1). When the automatic control equipment detects that the reduction rate of the visbreaking acid value of the raw material is lower than a set value, the automatic control equipment adjusts the feeding amount entering the visbreaking unit, so that part or all of the raw material oil flowing out of the raw material oil supply unit is subjected to gas-liquid separation by the gas-liquid separation unit, and then the separated liquid-state separated matter is fed into the visbreaking device. And when the feeding amount is adjusted, the automatic control equipment receives the acid value of the raw oil measured by the raw oil acid value detection unit in real time, and adjusts the proportion of the raw oil subjected to gas-liquid separation in real time by combining the acid value of the visbreaking residue measured by the visbreaking residue acid value detection unit, so that the reduction rate of the raw material visbreaking acid value after visbreaking is ensured to meet the requirement.
In another embodiment, the hot mixture prior to feeding the visbreaking unit is first fed to a gas-liquid separation unit where the hot mixture is separated into a liquid fraction and a gaseous fraction comprising water and light gas oil. The liquid isolate is then fed to a visbreaking unit for visbreaking to obtain a visbroken product oil. And after the viscosity-breaking residual oil is discharged from a viscosity-breaking residual oil outlet, detecting the acid value of the viscosity-breaking residual oil by a viscosity-breaking residual oil acid value detection unit, and detecting the acid value of the raw oil by a raw oil acid value detection unit. And (3) receiving the acid value of the raw oil and the acid value of the viscosity-breaking residual oil by automatic control equipment, and calculating the reduction rate of the acid values by the formula (1). When the automatic control device detects that the reduction rate of the acid value is lower than the set value, the temperature and pressure of the gas-liquid separation unit are automatically adjusted, thereby adjusting the amounts of water and light gas oil separated from the feed stream. In the visbreaking process, the automatic control equipment can regulate and control the temperature and pressure conditions of visbreaking so as to ensure that the reduction rate of the acid value is in a controllable range for visbreaking.
In other embodiments herein, the visbreaker further comprises a feedstock supply unit, and the visbreaker unit further comprises a first visbreaking unit and a second visbreaking unit, wherein the first visbreaking unit has a first feedstock inlet and a first visbroken resid outlet; the second visbreaking unit has a second feed oil inlet and a second visbroken resid outlet. The raw oil supply unit is respectively connected with the first raw oil inlet and the second raw oil inlet; the viscosity-breaking residue acid value detection unit is used for detecting the acid value of the viscosity-breaking residue at the outlet of the first viscosity-breaking residue and recording the acid value as a first acid value, and is used for detecting the acid value of the viscosity-breaking residue at the outlet of the second viscosity-breaking residue and recording the acid value as a second acid value, wherein the viscosity-breaking device is provided with automatic control equipment, the automatic control equipment is connected with the raw oil supply unit, the raw oil acid value detection unit and the viscosity-breaking residue acid value detection unit, the automatic control equipment receives the first acid value, the second acid value and the acid value of the raw oil and calculates a first acid value reduction rate and a second acid value reduction rate, and the feeding amount of the first viscosity-breaking unit and/or the second viscosity-breaking unit is adjusted in real time according to the first acid value reduction rate and the second acid value reduction rate.
In some embodiments, the raw oil acid value detection unit is first used to detect the acid value of the raw oil supplied from the raw oil supply unit. And then feeding the raw oil to a first viscosity breaking unit and a second viscosity breaking unit respectively through a first raw oil inlet and a second raw oil inlet. After visbreaking in the first and second visbreaking units, respectively, a first and second visbroken resid are obtained. And then leading the first viscosity breaking residual oil and the second viscosity breaking residual oil out of the first viscosity breaking unit and the second viscosity breaking unit from a first viscosity breaking residual oil outlet and a second viscosity breaking residual oil outlet respectively. In this example, the first visbreaking unit differs from the second visbreaking unit in the number of trays, the opening ratio of the trays, and the like. After the obtained first viscosity-breaking residue and the second viscosity-breaking residue are led out, a viscosity-breaking residue acid number detection unit is used for respectively detecting the acidity of the first viscosity-breaking residue and recording the acidity as a first acid number, and the acidity of the second viscosity-breaking residue and recording the acidity as a second acid number. The first acid value reduction rate and the second acid value reduction rate were calculated using the formula 1 described above, respectively. When the first acid number reduction is compared with the second acid number reduction, a large acid number reduction indicates a lesser degree of back-mixing of the same feedstock in the visbreaking unit, and the visbreaking unit is therefore more suitable for this feedstock. In some embodiments, the automated control apparatus will automatically adjust the supply of feedstock to the first and second visbreaking units based on the comparison of the first and second acid value reduction rates, thereby selecting a visbreaking unit that is more appropriate for the feedstock used.
In another exemplary embodiment of the present application, there is provided a visbreaking method, comprising: step S1, detecting the acid value of raw oil; step S2, performing visbreaking on the raw oil to obtain visbroken generated oil, and fractionating the visbroken generated oil to obtain visbroken residual oil; and S3, detecting the acid value of the visbreaking residual oil, and calculating the reduction rate of the acid value.
Unlike the prior art methods, when the method of the present application is used, the acid value of the feedstock is detected before the feedstock is visbroken, and the acid value of the visbroken residue produced is also detected after the feedstock is visbroken and fractionated. After acid number detection, the acid number reduction after visbreaking of the feedstock can be calculated by the following formula:
acid value reduction rate = (raw oil acid value-visbroken residue acid value)/raw oil acid value × 100% (formula 1)
Through the formula, the reduction rate of the acid value can be calculated, experience shows that the reduction rate of the acid value is large, the back mixing degree of the materials in the visbreaking device (such as a visbreaking tower) is small, on the contrary, the reduction rate of the acid value is small, the back mixing degree of the materials in the visbreaking device is large, the reduction rate of the acid value is close, the back mixing degree of the two materials in the visbreaking device is equivalent, and the reduction rate can clearly reflect the back mixing degree of the materials of different materials in the same visbreaking device
In further embodiments, the visbreaking process of the present application further comprises adjusting the pressure, temperature, and/or reaction time of the visbreaking unit based on the acid number reduction rate. After the reduction rate of the acid value is calculated by the formula (1), the pressure, temperature and/or reaction time of the visbreaker may be adjusted individually or simultaneously. The raw oil acid value and the residual oil acid value were measured at different pressures, temperatures and/or reaction times, and the reduction rate of the acid value was calculated. During the visbreaking process, the temperature, pressure and/or reaction time conditions of visbreaking can be regulated and controlled to ensure that the acid value reduction rate is in a controllable range for visbreaking. Under the process condition of the largest acid value reduction rate, the materials in the visbreaking unit are subjected to back mixing to a smaller degree, so that the problem of excessive coking of the materials in the visbreaking unit is effectively solved.
In some embodiments of the present application, the feedstock of step S1 is a mixture of a plurality of feedstocks, and the visbreaking process of the present application further comprises adjusting the composition of the feedstocks based on the acid number reduction rate. In one embodiment, the first feedstock oil and the second feedstock oil can be mixed prior to undergoing the visbreaking reaction, and the mixture can be subjected to the visbreaking reaction. And (4) carrying out acid value detection on the separated residual oil to obtain the residual oil acid value. The reduction rate of the acid value is calculated by mixing the acid value of the raw oil with the acid value of the residual oil. And adjusting the ratio of the first raw oil to the second raw oil to obtain a plurality of groups of different reduction rates of the acid value. In the visbreaking process, the composition of the raw oil mixture subjected to visbreaking can be regulated and controlled to ensure that the acid value reduction rate is in a controllable range for visbreaking.
In other embodiments herein, the visbreaking process comprises subjecting a hot pre-feed mixture of feedstock oil to gas-liquid separation to obtain a gaseous fraction and a liquid fraction, and subjecting the liquid fraction to visbreaking, based on the acid number reduction rate.
After the acid value of the feedstock oil and the acid value of the residue oil are measured, the hot mixture before the feedstock oil is fed may be first subjected to gas-liquid separation before the feedstock oil is subjected to visbreaking, based on the acid value reduction rate. Since water and light gas oil in the hot mix will cause severe back mixing in the visbreaking reaction, it is necessary to remove the water and light gas oil from the hot mix. In one embodiment, part or all of the hot mixture may be subjected to gas-liquid separation based on the reduction rate of the acid value. In some embodiments, after gas-liquid separation, the liquid isolate is subjected to visbreaking. In other examples, after gas-liquid separation, a portion of the feed oil that has not been subjected to gas-liquid separation is mixed with a liquid separator, and the mixture is subjected to visbreaking. And carrying out gas-liquid separation on the raw oil with different proportions, measuring the acid value and calculating the reduction rate for multiple times, and obtaining the raw oil proportion with proper back mixing degree according to the comparison of the reduction rate.
In a further embodiment, the visbreaking process of the present application comprises adjusting the temperature of the gas-liquid separation based on the reduction in acid number. In the example in which the entire hot mixture is subjected to gas-liquid separation using gas-liquid separation, the temperature of the gas-liquid separation may be adjusted in accordance with the acid value reduction rate. Gas-liquid separation is carried out at varying temperatures to obtain liquid isolates of different compositions. After visbreaking of the liquid isolate, a residual oil is obtained. And detecting the acid value of the residual oil, and calculating the reduction rate of the acid value by combining the acid value of the raw oil. The operations of temperature change, gas-liquid separation and visbreaking were repeated to obtain a plurality of values of the reduction rate of the acid value. And selecting the gas-liquid separation temperature at which the acid value reduction rate is maximum, carrying out gas-liquid separation, and then carrying out visbreaking. Under the process condition of the largest acid value reduction rate, the materials in the visbreaking unit are subjected to back mixing to a smaller degree, so that the problem of excessive coking of the materials in the visbreaking unit is effectively solved.
In a further embodiment of the present application, the gaseous separation comprises water and light gas oil. Since gas-liquid separation separates a gaseous separation comprising water and light gas oil from the feed oil, light gas oil and water components have been removed from the feed oil prior to visbreaking. In the subsequent visbreaking reaction, as the reaction system does not contain light gas oil and water components, the visbreaking reaction can be carried out at higher severity, and the problem of excessive coking caused by material back-mixing and material transition reaction condensation due to the existence of water and the light gas oil components is avoided. Therefore, in the visbreaking reaction, more severe reaction conditions can be adopted, so that the reacted heavy fuel oil component is subjected to visbreaking sufficiently, and the yield of the product light distillate oil is improved.
In some embodiments of the present application, step S2 comprises visbreaking the feedstock under first visbreaking conditions to obtain a first visbroken product oil, fractionating the first visbroken product oil to obtain a first visbroken residuum, and visbreaking the feedstock under second visbroken conditions to obtain a second visbroken product oil, fractionating the second visbroken product oil to obtain a second visbroken residuum, wherein the first visbroken conditions are different from the second visbroken conditions. And the step S3 comprises the steps of detecting the acid value of the first viscosity-breaking residual oil and the acid value of the second viscosity-breaking residual oil, calculating a first acid value reduction rate according to the acid value of the raw oil and the acid value of the first viscosity-breaking residual oil, and calculating a second acid value reduction rate according to the acid value of the raw oil and the acid value of the second viscosity-breaking residual oil. And the visbreaking process further comprises: and S4, selecting a visbreaking device according to the first acid value reduction rate and the second acid value reduction rate.
In the above examples, the acid values of the visbroken residues obtained were different due to the different visbreaking conditions. The first acid value reduction rate and the second acid value reduction rate were calculated by the previously described formula 1, respectively. When the first acid number reduction is compared with the second acid number reduction, a large acid number reduction indicates that the same feedstock is less back-mixed under the visbreaking conditions, and thus the visbreaking conditions are more suitable for such a feedstock. In this embodiment, the visbreaking conditions include the visbreaking equipment used and the process conditions such as time, temperature and pressure for visbreaking.
In a preferred embodiment, the residue obtained after visbreaking is a residue obtained with a true boiling point distillation cut at 410 ℃ to 430 ℃ and the acid value of the residue obtained at said cut enables better back-mixing during reactive visbreaking, preferably the residue is a residue obtained by cutting at 430 ℃.
In a further example, when the acid value of the feedstock oil is 1mgKOH/g or less, it is necessary to adjust the acid value of the feedstock oil to more than 1mgKOH/g using a feedstock oil or a residual oil having a high acid value.
The present application is described in further detail below with reference to specific examples, which should not be construed as limiting the scope of the present application as claimed.
Example 1
The feedstock a and the feedstock B were used as feedstocks, and the visbreaking reaction was performed under the same visbreaking conditions.
The raw oil A is Liaohe super heavy oil, wherein the density of the raw oil at 20 ℃ is 1004.6kg/m 3 The kinematic viscosity at 100 ℃ is 905.6mm 2 (ii)/s, residual carbon is 13.72wt%, andthe content of distillate below 165 ℃ in the raw oil is 0.01wt%, and the content of distillate (residual oil) above 350 ℃ is 91.1%. And the yield of the residual oil at the temperature of more than 430 ℃ is 75.03wt%.
The raw material B is vacuum residue, wherein the density of the raw material oil at 20 ℃ is 986.2kg/m 3 The kinematic viscosity at 100 ℃ is 556.8mm 2 The carbon residue was 11.77wt% and the residue yield above 430 ℃ was 99.32wt%.
First, the acid value of the feedstock a was measured by a feedstock acid value measuring unit, and the acid value of the feedstock a was 7.34mgKOH/g.
The raw oil A and water are mixed to form a mixture, wherein the weight ratio of water to raw oil is 0.5. The mixture was fed to a heating furnace (heating unit) to be heated, wherein the outlet temperature of the heating furnace was 435 ℃. And feeding the heated material into the visbreaking tower through a raw oil inlet arranged at the bottom of the visbreaking tower for visbreaking. The pressure of the visbreaking tower is 1.0MPa, and the retention time of the materials in the visbreaking device is 50 minutes. After undergoing the visbreaking treatment, the visbroken produced oil is discharged through an outlet provided at the bottom of the visbreaking column. Then, the visbreaking product oil is fractionated through a fractionating tower, wherein the visbreaking residual oil of the fraction higher than 430 ℃ is obtained at the bottom outlet of the fractionating tower.
The acid value of the viscosity-breaking residual oil is 3.2mgKOH/g detected by a viscosity-breaking residual oil acid value detection unit.
The acid value of feedstock oil B was measured by a unit for measuring the acid value of feedstock oil B, and the acid value of feedstock oil B was 1.56mgKOH/g.
And mixing the raw oil B with water to form a mixture, wherein the weight ratio of water to the raw oil is 0.5. The mixture was fed to a heating furnace (heating unit) for heating, wherein the outlet temperature of the heating furnace was 435 ℃. The heated material is fed into the visbreaking tower through a raw oil inlet arranged at the bottom of the visbreaking tower to be subjected to visbreaking. The pressure of the visbreaking tower is 1.0MPa, and the retention time of the materials in the visbreaking device is 50 minutes. After undergoing the visbreaking treatment, the visbroken product oil is discharged through an outlet provided at the bottom of the visbreaking tower. Then, the visbroken oil is fractionated in a fractionating tower, wherein the visbroken residual oil with the temperature of more than 430 ℃ is obtained at the bottom outlet of the fractionating tower.
The acid value of the visbreaking residue is 0.18mgKOH/g detected by the visbreaking residue acid value detection unit.
The acid value reduction ratios of the feedstock a and the feedstock B were calculated from the reduction ratio of acid value = (feedstock acid value-visbroken residue acid value)/feedstock acid value × 100%.
The rate of decrease in the visbroken acid value of the raw material a was = (7.34-3.20)/7.34 × 100% =56.4%.
The rate of decrease in the visbroken acid value of the raw material B was = (1.56-0.18)/1.56 × 100% =88.5%.
Because the rate of reducing the visbreaking acid value of the raw material A is lower than that of the raw material B, the raw material oil B has smaller back mixing degree than the raw material oil A under the same visbreaking condition in the same visbreaking tower, and the materials react more uniformly in the visbreaking reaction tower.
Example 2
The feed oil A was used as the feed oil, and the visbreaking reaction was carried out under different visbreaking conditions (method 1 and method 2).
The raw oil A is Liaohe super heavy oil, wherein the density of the raw oil at 20 ℃ is 1004.6kg/m 3 The kinematic viscosity at 100 ℃ is 905.6mm 2 The carbon residue was 13.72wt%, and the content of a fraction at less than 165 ℃ in the feed oil was 0.01wt%, and the content of a fraction (residual oil) at more than 350 ℃ was 91.1%. And the yield of the residual oil at the temperature of more than 430 ℃ is 75.03wt%.
The method comprises the following steps:
first, the acid value of the stock oil A was measured by using a stock oil acid value measuring unit, and the acid value of the stock oil A was 7.34mgKOH/g.
The raw oil A and water are mixed to form a mixture, wherein the weight ratio of water to raw oil is 0.5. The mixture was fed to a heating furnace (heating unit) for heating, wherein the outlet temperature of the heating furnace was 435 ℃. The heated material is fed into the visbreaking tower through a raw oil inlet arranged at the bottom of the visbreaking tower to be subjected to visbreaking. The pressure of the visbreaking tower is 1.0MPa, and the retention time of the materials in the visbreaking device is 50 minutes. After undergoing the visbreaking treatment, the visbroken produced oil is discharged through an outlet provided at the bottom of the visbreaking column. Then, the visbreaking product oil is fractionated through a fractionating tower, wherein the visbreaking residual oil of the fraction higher than 430 ℃ is obtained at the bottom outlet of the fractionating tower.
The acid value of the visbreaking residue is 3.20mgKOH/g detected by the visbreaking residue acid value detection unit. The viscosity-reduced oil was determined to have a toluene insoluble (coke) content of 0.58 wt.%.
The method 2 comprises the following steps:
first, the acid value of the stock oil A was measured by using a stock oil acid value measuring unit, and the acid value of the stock oil A was 7.34mgKOH/g.
The raw oil A and water are mixed to form a mixture, wherein the weight ratio of water to raw oil is 0.5. Feeding the mixture into a heating furnace (heating unit) for heating, introducing the heated material into a gas-liquid separation tank (gas-liquid separation unit), separating water and light gas oil from an outlet at the top of the gas-liquid separation tank, and condensing to obtain the light gas oil, wherein the temperature of a liquid phase part is 435 ℃. Feeding the liquid phase part obtained by gas-liquid separation into a visbreaking tower through a raw oil inlet arranged at the bottom of the visbreaking tower for visbreaking. The pressure of the visbreaking tower is 1.0MPa, and the retention time of the materials in the visbreaking device is 50 minutes. After undergoing the visbreaking treatment, the visbroken produced oil is discharged through an outlet provided at the bottom of the visbreaking column. Then, the visbreaking product oil is fractionated through a fractionating tower, wherein the visbreaking residual oil of the fraction higher than 430 ℃ is obtained at the bottom outlet of the fractionating tower.
The acid value of the visbreaking residue is 0.28mgKOH/g detected by the visbreaking residue acid value detection unit. The toluene insoluble (coke) content of the visbreaking oil and light gas oil mixture was determined to be 0.17wt%.
The acid value reduction rate of the visbroken residue was obtained by the method 1 and the method 2 through the calculation of the reduction rate of the acid value = (raw oil acid value-visbroken residue acid value)/raw oil acid value × 100%.
Method 1 the rate of decrease in the visbreaking acid value was = (7.34-3.20)/7.34 × 100% =55.85%.
Method 2 the visbreaking acid value reduction rate was = (7.38-0.28)/7.34 × 100% =96.7%.
Since the visbreaking acid number reduction rate of method 1 is lower than the visbreaking acid number reduction rate of method 2, method 2 has a smaller degree of back-mixing than method 1 and the material reacts more uniformly in the visbreaking reaction tower under the same visbreaking conditions used in the same visbreaking tower.
As can be seen from the comparison of the toluene insoluble (coke) content of the visbroken product oil and the toluene insoluble (coke) content of the light gas oil mixed oil in the two processes, the toluene insoluble (coke) content of the visbroken product is obviously reduced in the method 2 compared with the method 1, the backswing degree is smaller, and the material reacts more uniformly in the visbroken reaction tower.
Example 3
The feedstock B was used as feedstock and the visbreaking reaction was carried out under different visbreaking conditions (method 1 and method 2).
The raw oil B is a vacuum residue, wherein the density of the raw oil at 20 ℃ is 986.2kg/m 3 The kinematic viscosity at 100 ℃ is 556.8mm 2 The carbon residue was 11.77wt% and the residue yield above 430 ℃ was 99.32wt%.
The method comprises the following steps:
first, the acid value of the feedstock oil B was measured by a feedstock oil acid value measuring means, and the acid value of the feedstock oil B was 1.56mgKOH/g.
And (3) forming a mixture by mixing the raw oil B and water, wherein the weight ratio of water to the raw oil is 0.5. The mixture was fed to a heating furnace (heating unit) for heating, wherein the outlet temperature of the heating furnace was 435 ℃. And feeding the heated material into the visbreaking tower through a raw oil inlet arranged at the bottom of the visbreaking tower for visbreaking. The pressure of the visbreaking tower is 1.0MPa, and the retention time of the materials in the visbreaking device is 50 minutes. After undergoing the visbreaking treatment, the visbroken product oil is discharged through an outlet provided at the bottom of the visbreaking tower. Then, the visbreaking product oil is fractionated through a fractionating tower, wherein the visbreaking residual oil of the fraction higher than 430 ℃ is obtained at the bottom outlet of the fractionating tower.
The acid value of the visbreaking residue is 0.18mgKOH/g detected by the visbreaking residue acid value detection unit.
The method 2 comprises the following steps:
first, the acid value of the feedstock oil B was measured by a feedstock oil acid value measuring means, and the acid value of the feedstock oil B was 1.56mgKOH/g.
And mixing the raw oil B with water to form a mixture, wherein the weight ratio of water to the raw oil is 0.5. Feeding the mixture into a heating furnace (heating unit) for heating, guiding the heated material into a gas-liquid separation tank (gas-liquid separation unit), separating water and light gas oil from an outlet at the top of the gas-liquid separation tank, and condensing to obtain light gas oil; the temperature of the liquid phase part was 435 ℃. Feeding the liquid phase part obtained by gas-liquid separation into a visbreaking tower through a raw oil inlet arranged at the bottom of the visbreaking tower for visbreaking. The pressure of the visbreaking tower is 1.0MPa, and the retention time of the materials in the visbreaking device is 50 minutes. After undergoing the visbreaking treatment, the visbroken product oil is discharged through an outlet provided at the bottom of the visbreaking tower. Then, the visbroken oil is fractionated in a fractionating tower, wherein the visbroken residual oil with the temperature of more than 430 ℃ is obtained at the bottom outlet of the fractionating tower.
The acid value of the visbreaking residue is 0.04mgKOH/g detected by the visbreaking residue acid value detection unit.
The acid value reduction rate of the visbroken residue was obtained by the method 1 and the method 2 through the calculation of the reduction rate of the acid value = (raw oil acid value-visbroken residue acid value)/raw oil acid value × 100%.
Method 1 the rate of decrease in the visbroken acid value was = (1.56-0.18)/1.56 × 100% =88.5%.
Method 2 the rate of decrease in the visbreaking acid value was = (1.56-0.04)/1.56 × 100% =97.4%.
Since the visbreaking acid number reduction rate of method 1 is lower than the visbreaking acid number reduction rate of method 2, method 2 has a smaller degree of back-mixing than method 1 and the material reacts more uniformly in the visbreaking reaction tower under the same visbreaking conditions used in the same visbreaking tower.
Example 4
The feedstock oils B and C were used as feedstock oils, and the visbreaking reaction was performed under the same visbreaking conditions.
The raw material B is vacuum residue, wherein the density of the raw material oil at 20 ℃ is 986.2kg/m 3 The kinematic viscosity at 100 ℃ is 556.8mm 2 The carbon residue was 11.77wt% and the residue yield above 430 ℃ was 99.32wt%.
The raw material C is vacuum residue, wherein the density of the raw material oil at 20 ℃ is 932.6kg/m 3 A kinematic viscosity at 100 ℃ of 234.2mm 2 The carbon residue was 6.59% by weight.
First, the acid value of the feedstock oil B was measured by a feedstock oil acid value measuring means, and the acid value of the feedstock oil B was 1.56mgKOH/g.
And mixing the raw oil B with water to form a mixture, wherein the weight ratio of water to the raw oil is 0.5. The mixture was fed to a heating furnace (heating unit) to be heated, wherein the outlet temperature of the heating furnace was 435 ℃. And feeding the heated material into the visbreaking tower through a raw oil inlet arranged at the bottom of the visbreaking tower for visbreaking. The pressure of the visbreaking tower is 1.0MPa, and the retention time of the materials in the visbreaking device is 50 minutes. After undergoing the visbreaking treatment, the visbroken produced oil is discharged through an outlet provided at the bottom of the visbreaking column. Then, the visbreaking product oil is fractionated through a fractionating tower, wherein the visbreaking residual oil of the fraction higher than 430 ℃ is obtained at the bottom outlet of the fractionating tower.
The acid value of the visbreaking residue is detected to be 0.33mgKOH/g by a visbreaking residue acid value detection unit.
The acid value of the feedstock C was measured by using a feedstock acid value measuring unit, and the acid value of the feedstock C was 0.25mgKOH/g.Since the acid value of the feedstock oil C is 1mgKOH/g or less, a vacuum residue D having a feedstock oil density of 1062.9kg/m at 20 ℃ is added to the feedstock oil C 3 The kinematic viscosity at 100 ℃ is 1234.8mm 2 (s), the carbon residue was 16.36% by weight, and the acid value was 12.5mgKOH/g. The mixture of the raw oil C and D is the mixed high-acid residual oil. And (3) detecting the acid value of the mixed high-acid residual oil by using a raw oil acid value detection unit, wherein the acid value of the obtained mixed high-acid residual oil is 2.2mgKOH/g.
And mixing the mixed high-acid residual oil and water to form a mixture, wherein the weight ratio of the water to the raw oil is 0.5. The mixture was fed to a heating furnace (heating unit) to be heated, wherein the outlet temperature of the heating furnace was 435 ℃. And feeding the heated material into the visbreaking tower through a raw oil inlet arranged at the bottom of the visbreaking tower for visbreaking. The pressure of the visbreaking tower is 1.0MPa, and the retention time of the materials in the visbreaking device is 50 minutes. After undergoing the visbreaking treatment, the visbroken produced oil is discharged through an outlet provided at the bottom of the visbreaking column. Then, the visbroken oil is fractionated in a fractionating tower, wherein the visbroken residual oil with the temperature of more than 430 ℃ is obtained at the bottom outlet of the fractionating tower.
The acid value of the visbreaking residue is 0.95mgKOH/g detected by the visbreaking residue acid value detection unit.
The acid value reduction ratios of the feedstock a and the feedstock B were calculated from the reduction ratio of acid value = (feedstock acid value-visbroken residue acid value)/feedstock acid value × 100%.
The rate of decrease in the visbroken acid value of the raw material B was = (1.56-0.33)/1.56 × 100% =78.8%.
The reduction rate of the viscosity breaking acid value of the mixed high-acid residual oil is = (2.2-0.95)/2.2 multiplied by 100% =56.8%.
Because the visbreaking acid value reduction rate of the mixed high-acid residual oil is lower than that of the raw material B, the raw material oil B has smaller back mixing degree than the mixed high-acid residual oil under the same visbreaking condition in the same visbreaking tower, and the materials react more uniformly in the visbreaking reaction tower.
Example 5
The feedstock B was used as feedstock and the visbreaking reactions were carried out in separate visbreaking units (unit 1 and unit 2), wherein unit 1 corresponds to method 1 and unit 2 corresponds to method 2.
The raw material B is vacuum residue, wherein the density of the raw material oil at 20 ℃ is 986.2kg/m 3 The kinematic viscosity at 100 ℃ is 556.8mm 2 The carbon residue was 11.77wt% and the residue yield above 430 ℃ was 99.32wt%.
The method comprises the following steps:
first, the acid value of feedstock B was measured by a feedstock acid value measuring unit, and the acid value of feedstock B was 1.56mgKOH/g.
And (3) forming a mixture by mixing the raw oil B and water, wherein the weight ratio of water to the raw oil is 0.5. The mixture was fed to a heating furnace (heating unit) for heating, wherein the outlet temperature of the heating furnace was 435 ℃. The heated material is fed into the visbreaking tower 1 through a raw oil inlet arranged at the bottom of the visbreaking tower 1 for visbreaking. The pressure of the visbreaking tower 1 is 1.0MPa, the retention time of materials in the visbreaking device is 50 minutes, three sieve plates are arranged in the visbreaking tower 1, and the aperture ratio of each sieve plate is 10%. After the visbreaking treatment, the visbroken product oil is discharged through an outlet provided at the bottom of the visbreaking tower 1. Then, the visbroken oil is fractionated in a fractionating tower, wherein the visbroken residual oil with the temperature of more than 430 ℃ is obtained at the bottom outlet of the fractionating tower.
The acid value of the viscosity-breaking residual oil is 0.83mgKOH/g detected by a viscosity-breaking residual oil acid value detection unit.
The method 2 comprises the following steps:
first, the acid value of the feedstock oil B was measured by a feedstock oil acid value measuring means, and the acid value of the feedstock oil B was 1.56mgKOH/g.
And mixing the raw oil B with water to form a mixture, wherein the weight ratio of water to the raw oil is 0.5. The mixture was fed to a heating furnace (heating unit) for heating, wherein the outlet temperature of the heating furnace was 435 ℃. The heated material is fed into the visbreaking tower 2 for visbreaking through a raw oil inlet arranged at the bottom of the visbreaking tower 2. The pressure of the visbreaking tower 2 is 1.0MPa, the retention time of materials in the visbreaking device is 50 minutes, six sieve plates are arranged in the visbreaking tower 2, and the opening rates of the sieve plates of the visbreaking tower are 10%, 12%, 15%, 16%, 18% and 20% from bottom to top in sequence. After the visbreaking treatment is performed, the visbroken produced oil is discharged through an outlet provided at the bottom of the visbreaking tower 2. Then, the visbreaking product oil is fractionated through a fractionating tower, wherein the visbreaking residual oil of the fraction higher than 430 ℃ is obtained at the bottom outlet of the fractionating tower.
The acid value of the visbreaking residue is 0.42mgKOH/g detected by the visbreaking residue acid value detection unit.
The acid value reduction rate of the visbroken residue was obtained by the method 1 and the method 2 through the calculation of the reduction rate of the acid value = (raw oil acid value-visbroken residue acid value)/raw oil acid value × 100%.
Method 1 the rate of decrease in the visbroken acid value was = (1.56-0.83)/1.56 × 100% =46.8%.
Method 2 the rate of decrease in the visbreaking acid value was = (1.56-0.42)/1.56 × 100% =73.1%.
Since the visbreaking acid number reduction rate of method 1 is lower than the visbreaking acid number reduction rate of method 2, method 2 has a smaller degree of back-mixing than method 1 and the material reacts more uniformly in the visbreaking reaction tower under the same visbreaking conditions used in the same visbreaking tower.
From the above description, it can be seen that the above-described embodiments of the present application achieve the following technical effects:
in the case of using the visbreaker and the visbreaking method of the present application, the degree of back-mixing of the materials in the visbreaker can be clearly reflected by the measurement of the acid values of the feedstock and the produced residue and the calculation of the reduction rate of the acid values. And based on the acid value reduction rate, the structure and process parameters of the visbreaking tower can be adjusted to ensure that the visbreaking is operated at high severity, so as to exert the best efficiency of the visbreaking process.
The above description is only a preferred embodiment of the present application and is not intended to limit the present application, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present application shall be included in the protection scope of the present application.
Claims (13)
1. A visbreaking apparatus, comprising:
a visbreaking unit having a feedstock oil inlet and a visbroken resid outlet;
a raw oil acid value detection unit for detecting the acid value of the raw oil; and
and the viscosity-breaking residual oil acid value detection unit is used for detecting the acid value of the viscosity-breaking residual oil.
2. The visbreaking apparatus according to claim 1, wherein the visbreaking unit is equipped with an automatic control device, a pressure controller and a temperature controller, the automatic control device is connected with the raw oil acid value detection unit, the visbroken residue acid value detection unit, the pressure controller and the temperature controller; and the automatic control equipment receives the acid value of the raw oil and the acid value of the visbreaking residual oil and calculates the reduction rate of the acid value, and the automatic control equipment adjusts the pressure controller and the temperature controller of the visbreaking unit in real time according to the reduction rate of the acid value.
3. The visbreaking apparatus according to claim 2, further comprising a first stock oil supply unit and a second stock oil supply unit, the stock oil inlet being connected to the first stock oil supply unit and the second stock oil supply unit, respectively; the automatic control equipment is connected with the first raw oil supply unit and the second raw oil supply unit, receives the acid value of the visbroken residual oil and the acid value of the raw oil, and adjusts the feeding amount of the first raw oil supply unit and/or the second raw oil supply unit in real time according to the reduction rate of the acid value.
4. The visbreaking apparatus of claim 1, further comprising:
the gas-liquid separation unit is provided with a raw material inlet and a liquid separator outlet, the liquid separator outlet is connected with the raw material oil inlet of the visbreaking unit, the gas-liquid separation unit is used for carrying out gas-liquid separation on the raw material oil to obtain a gaseous separator and a liquid separator, and the gaseous separator comprises water and light gas oil;
a stock oil supply unit connected to the stock inlet of the gas-liquid separation unit and the stock oil inlet of the visbreaking unit, respectively,
the visbreaking unit is provided with an automatic control device, the automatic control device is connected with the raw oil acid value detection unit, the visbreaking residual oil acid value detection unit, the raw oil supply unit and the gas-liquid separation unit, the automatic control device receives the acid value of the visbreaking residual oil and the acid value of the raw oil, calculates the reduction rate of the acid value, and adjusts the feeding amount of the gas-liquid separation unit and/or the visbreaking unit and/or the temperature of the gas-liquid separation unit in real time according to the reduction rate of the acid value.
5. The visbreaking apparatus according to claim 1, further comprising a feedstock supply unit, the visbreaking unit further comprising:
a first visbreaking unit having a first feedstock inlet and a first visbroken resid outlet;
the second visbreaking unit is provided with a second raw oil inlet and a second visbreaking residual oil outlet, and the raw oil supply unit is respectively connected with the first raw oil inlet and the second raw oil inlet;
the viscosity breaking residual oil acid value detection unit is used for detecting the acid value of the viscosity breaking residual oil at the first viscosity breaking residual oil outlet and recording the acid value as a first acid value, and is used for detecting the acid value of the viscosity breaking residual oil at the second viscosity breaking residual oil outlet and recording the acid value as a second acid value,
the visbreaking device is provided with an automatic control device, the automatic control device is connected with the raw oil supply unit, the raw oil acid value detection unit and the visbreaking residual oil acid value detection unit, the automatic control device receives the first acid value, the second acid value and the acid value of the raw oil, calculates a first acid value reduction rate and a second acid value reduction rate, and adjusts the feeding amount of the first visbreaking unit and/or the second visbreaking unit in real time according to the first acid value reduction rate and the second acid value reduction rate.
6. A visbreaking process comprising:
step S1, detecting the acid value of raw oil;
s2, performing visbreaking on the raw oil to obtain visbroken generated oil, and fractionating the visbroken generated oil to obtain visbroken residual oil; and
and S3, detecting the acid value of the visbreaking residual oil, and calculating the reduction rate of the acid value.
7. The visbreaking process of claim 6, further comprising:
adjusting the pressure and/or temperature of the visbreaking based on the acid number reduction rate.
8. The visbreaking method according to claim 6, wherein the feedstock in step S1 is a mixture of a plurality of feedstocks, and the visbreaking method further comprises adjusting the composition of the feedstock based on the acid value reduction rate.
9. The visbreaking process of claim 6, further comprising:
according to the acid value reduction rate, carrying out gas-liquid separation on the hot mixture before feeding of the raw oil to obtain a gaseous separated substance and a liquid separated substance, and carrying out visbreaking on the liquid separated substance.
10. The visbreaking process according to claim 9, wherein the temperature of the gas-liquid separation is adjusted according to the acid value reduction rate.
11. The visbreaking process of claim 9, wherein the gaseous separation comprises water and light gas oil.
12. The visbreaking process of claim 6,
the step S2 includes performing visbreaking on the raw oil under a first visbreaking condition to obtain a first visbreaking product oil, fractionating the first visbreaking product oil to obtain a first visbreaking residue, performing visbreaking on the raw oil under a second visbreaking condition to obtain a second visbreaking product oil, and fractionating the second visbreaking product oil to obtain a second visbreaking residue, wherein the first visbreaking condition is different from the second visbreaking condition;
the step S3 includes detecting an acid value of the first visbroken residue and an acid value of the second visbroken residue, calculating a first acid value reduction rate from the acid value of the feedstock oil and the acid value of the first visbroken residue, and calculating a second acid value reduction rate from the acid value of the feedstock oil and the acid value of the second visbroken residue;
and wherein the visbreaking process further comprises: and S4, selecting visbreaking conditions according to the first acid value reduction rate and the second acid value reduction rate.
13. A visbreaking process according to claim 6, wherein the visbroken resid is subjected to a real boiling distillation of the visbroken product oil to yield a resid greater than 430 ℃.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1200139A (en) * | 1995-10-20 | 1998-11-25 | 埃克森研究工程公司 | Viscosity reduction by heat soak-induced naphthenic acid decomposition in hydrocarbon oils |
| CN1814704A (en) * | 2005-01-31 | 2006-08-09 | 中国石油化工股份有限公司 | Method for deeply removing petroleum acids from acid-contained raw oil |
| CN206184388U (en) * | 2016-11-01 | 2017-05-24 | 中石化广州工程有限公司 | Raw oil proportion blending feeding system |
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2021
- 2021-06-08 CN CN202110640182.9A patent/CN115449397A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1200139A (en) * | 1995-10-20 | 1998-11-25 | 埃克森研究工程公司 | Viscosity reduction by heat soak-induced naphthenic acid decomposition in hydrocarbon oils |
| CN1814704A (en) * | 2005-01-31 | 2006-08-09 | 中国石油化工股份有限公司 | Method for deeply removing petroleum acids from acid-contained raw oil |
| CN206184388U (en) * | 2016-11-01 | 2017-05-24 | 中石化广州工程有限公司 | Raw oil proportion blending feeding system |
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