CN114749108A

CN114749108A - Online loading and unloading method and system for catalyst for fluidized bed residual oil hydrogenation process

Info

Publication number: CN114749108A
Application number: CN202210353001.9A
Authority: CN
Inventors: 程燕侠; 刁望升; 刘建平; 张松; 郑鑫; 严吉国; 潘佳田
Original assignee: Shenghong Refining And Chemical Lianyungang Co ltd
Current assignee: Shenghong Refining And Chemical Lianyungang Co ltd
Priority date: 2022-04-06
Filing date: 2022-04-06
Publication date: 2022-07-15
Anticipated expiration: 2042-04-06
Also published as: CN114749108B

Abstract

The invention discloses an on-line loading and unloading method and system for a catalyst for a fluidized bed residual oil hydrogenation process. The method comprises the following steps: adding the used catalyst in the second reactor into the first reactor, allowing the catalyst to participate in residual oil hydrogenation reaction, discharging the catalyst after the catalyst is partially deactivated, and adding new catalyst into the second reactor. The system comprises a first reactor, a second reactor, a loading and unloading tank and a delivery oil storage tank, wherein the bottom of the first reactor and the bottom of the second reactor are communicated with the loading and unloading tank through pipelines, the loading and unloading tank is communicated with the top of the first reactor and the top of the second reactor through pipelines, the delivery oil storage tank is communicated with the loading and unloading tank through a delivery oil inlet pipe, and the delivery oil inlet pipe is provided with a delivery oil heater. The invention solves the problem of coking caused by overhigh conversion rate due to overhigh activity of the catalyst at the bottom of the first reactor by changing the loading and unloading mode of the catalyst, and simultaneously reduces the loss of new catalyst of the second reactor.

Description

Online loading and unloading method and system for catalyst for fluidized bed residual oil hydrogenation process

Technical Field

The invention relates to the technical field of chemical production, in particular to an on-line loading and unloading method and system for a catalyst for a boiling bed residual oil hydrogenation process.

Background

At present, the boiling bed residual oil hydrogenation technology is generally adopted to realize the lightening of the residual oil. The process generally uses nickel-vanadium metal, nickel-molybdenum metal or nickel-cobalt metal and the like as catalysts to enable raw oil to be subjected to hydrocracking reaction in a first reactor and a second reactor in sequence. In this process, the activity of the catalyst in the first and second reactors needs to be ensured by adding fresh catalyst and discharging the used catalyst every day, the discharging agent containing spent catalyst, coke, residual oil, etc. During the operation of the system, the contents of nickel-vanadium metal, nickel-molybdenum metal or nickel-cobalt metal and the like in the used catalyst need to be sampled and analyzed every day to monitor the activity of the catalyst.

At present, the loading and unloading modes of the built and under-built catalyst on-line loading and unloading system are generally carried out by adopting the following modes: firstly, adding new catalyst into a second reactor; secondly, discharging the used catalyst in the second reactor; then, adding the catalyst discharged from the second reactor into the first reactor; finally, the spent catalyst in the first reactor is discharged (as shown in FIG. 1).

However, the catalyst on-line loading method has the following defects:

(1) the activity of the catalyst in the second reactor is easy to reduce: in the reaction process, new catalyst needs to be added into the first reactor and the second reactor every day, and used catalyst (hereinafter referred to as adding and discharging agent) needs to be discharged, the activity of the catalyst in the second reactor is obviously reduced along with the accumulation of time, the reaction degree is insufficient due to the reduction of the activity of the catalyst at the same temperature, and finally the yield of a target product is reduced, and the economic benefit is reduced. To ensure a stable product yield, the degree of reaction is generally increased by increasing the reaction temperature. However, this will inevitably increase the operational difficulty and risk of the device, and at the same time will increase the labor cost and material cost, which is not easy to pay.

(2) It is easy to cause excessive increase of catalyst activity in the first reactor, which is not favorable for temperature control: the daily loading and unloading time is 2-3 months. Typically, after three months of operation, the nuclear level gauge at the bottom of the first reactor showed a density value of more than 1200kg/m³Even up to 1500kg/m³(as shown in FIG. 2), this indicates that coking has occurred in the first reactor bottoms, i.e., the catalyst in the first reactor is too active. Excessive increase in catalyst activity tends to drive the reaction products towards two polarizations: gas phase products are increased, liquid phase products are reduced, and the reaction depth is increased. So that macromolecular substances such as asphalt in the raw oil are condensed to form coke, and the long-period operation of the device is influenced.

(3) The side reaction is more: the catalyst activity in the two reactors progressively moves away from the target value after each addition of agent, differentiating more and more as the catalyst activity in the second reactor decreases and the activity in the first reactor increases. The same frequency of adding and removing the catalyst cannot improve the activity of the respective catalyst, and finally, the stability is difficult to maintain, side reactions are inevitably increased, and the economic benefit is seriously influenced.

(4) Cause waste of catalyst and reduction of environmental protection: when about 200 tons of catalyst are stably contained in each reactor, calculated in 8400 hours (i.e., 350 days) per year of operation, and 7 tons of fresh catalyst and used catalyst are discharged each day (here, only used catalyst, waste oil, etc., are excluded), the amount of catalyst wasted per year is m (kg) ═ 7000 × 7/207 ═ 7/207 ═ 350 ═ 3001.25 (kg). The catalyst is usually added and discharged by using conveying oil as a conveying carrier of the catalyst in the whole process of adding and discharging the agent. In order to ensure the smoothness of the conveying pipeline, reduce the adhesion of catalyst powder on the pipe wall of the conveying pipeline and ensure that the added new catalyst can smoothly reach the second reactor, a large amount of conveying oil with the temperature of 230-260 ℃ is usually conveyed into the second reactor. However, the average temperature of the material in the second reactor was 428-440 ℃ and the temperature difference between the transported oil and the material reached 168-210 ℃. The transport oil fed into the second reactor reduces the average temperature of the material in the second reactor, inevitably has a negative effect on the properties and yield of the target product, causes production fluctuations, and also increases the operational difficulty and the risk of operating the apparatus.

(5) Long-cycle operation of the device is affected: the added fresh catalyst is usually weighed by a catalyst metering tank and transferred to a loading and unloading tank, and after being mixed with transfer oil in the loading and unloading tank, the fresh catalyst is transferred to a second reactor together with the transfer oil. However, in the process of transferring the new catalyst from the catalyst metering tank to the charge-discharge tank, abrasion of the catalyst is inevitably caused, and the generated powder enters the charge-discharge tank and cannot be removed in time. When new catalyst is added into the second reactor, the catalyst powder can gradually cause the pressure difference of a catalyst bed layer in the second reactor to increase, and simultaneously, the catalyst powder can be combined with substances such as colloid, asphalt and the like in raw oil to generate coking substances more easily, so that the long-period operation of the device is influenced.

Disclosure of Invention

In view of the defects of the prior art, the invention aims to provide an on-line loading and unloading method and system for a catalyst for an ebullated bed residual oil hydrogenation process, so as to solve the technical problems of unstable catalyst activity, coking and production fluctuation caused by the production of transport oil entering a second reactor due to the fact that the activity of the catalyst in the second reactor is reduced and the activity of the catalyst in a first reactor is excessively increased.

In a first aspect, the present invention provides an on-line loading and unloading method for a catalyst for an ebullated-bed residue hydrogenation process, which is performed in an on-line loading and unloading system for a catalyst for an ebullated-bed residue hydrogenation process, the system comprising a first reactor and a second reactor, wherein the first reactor and the second reactor are ebullated-bed hydrogenation reactors, and the method comprises the following steps: adding the used catalyst in the second reactor into the first reactor, allowing the catalyst entering the first reactor to participate in residual oil hydrogenation, discharging the catalyst after the catalyst loses activity, and adding new catalyst into the second reactor.

Optionally, the system further comprises a charge-discharge tank, and charging the spent catalyst in the second reactor into the first reactor comprises the steps of: the method comprises the steps of taking conveying oil as a carrier, enabling the catalyst used in the second reactor to enter the loading and unloading tank along with the conveying oil by adjusting the pressure difference between the second reactor and the loading and unloading tank, and enabling the catalyst in the loading and unloading tank to enter the first reactor along with the conveying oil by adjusting the pressure difference between the loading and unloading tank and the first reactor.

Optionally, the internal pressure of the second reactor is at least 0.2MPa higher than the internal pressure of the charge-discharge tank.

Optionally, the internal pressure of the loading and unloading tank is at least 0.2MPa higher than the internal pressure of the first reactor.

Optionally, the flow rate of the conveying oil is 5-15m during the process that the catalyst enters the first reactor³H, preferably 5 to 10m³/h。

Optionally, the temperature of the transportation oil during the catalyst entering the first reactor is 350-.

Optionally, the system further comprises a charge-discharge tank, and discharging the catalyst in the first reactor comprises the following steps: the transportation oil is used as a carrier, and the catalyst in the first reactor enters the loading and unloading tank along with the transportation oil by adjusting the pressure difference between the first reactor and the loading and unloading tank.

Optionally, the internal pressure of the first reactor during the discharge of the catalyst from the first reactor is at least 0.2MPa higher than the internal pressure of the charge-discharge tank.

Optionally, the addition of fresh catalyst to the second reactor comprises the steps of: and adding new catalyst and conveying oil into the loading and unloading tank, and adjusting the pressure difference between the loading and unloading tank and the second reactor to ensure that the new catalyst in the loading and unloading tank enters the second reactor along with the conveying oil.

Optionally, during the addition of fresh catalyst to the second reactor, the internal pressure of the second reactor is at least 0.2MPa lower than the internal pressure of the charge-discharge tank.

Optionally, the flow rate of the conveying oil is 5-15m during the process of adding the new catalyst into the second reactor³H, preferably 5 to 10m³/h。

Optionally, the temperature of the transportation oil during the process of adding the new catalyst into the second reactor is 350-.

Optionally, the catalyst on-line loading and unloading method further comprises the following steps: and (3) regenerating the catalyst discharged from the first reactor to obtain a regenerated catalyst, and adding the regenerated catalyst into the second reactor.

In another aspect, the present invention also provides an online loading and unloading system for catalyst, which comprises:

including first reactor, second reactor, add and unload jar and transport oil storage jar, add and unload the place that the jar was mixed for carrying oil and catalyst, it is provided with the waste oil export, and first reactor bottom and second reactor bottom all are linked together through pipeline and adding the jar of unloading, add and unload the jar and be linked together through pipeline and first reactor top and second reactor top, carry oil storage jar and advance oil pipe intercommunication through carrying oil add and unload the jar, it is provided with the transport oil heater on advancing oil pipe to carry oil.

According to the system, the oil conveying heater is additionally arranged, so that the oil conveying can be heated to 350-440 ℃, the temperature difference between the oil conveying entering the first reactor and/or the second reactor and the materials in the reactors is reduced, and the adverse effects of overlarge temperature difference on the properties of the target product and the yield of the target product are further reduced.

Optionally, the first reactor and the second reactor are both provided with a temperature regulation assembly and a hydrogen inlet pipeline.

Optionally, the loading and unloading tank is provided with a hydrogen gas inlet pipeline and a pressure relief valve.

Optionally, the loading and unloading tank is provided with a flare pipeline, and the flare pipeline is communicated with a flare system.

Optionally, the transfer oil heater communicates with a conduit between the bottom of the first reactor and the loading and unloading tank.

Optionally, the transfer oil heater communicates with a conduit between the bottom of the second reactor and the loading and unloading tank.

The pipeline between the bottom of the first reactor and/or the bottom of the second reactor and the loading and unloading tank is communicated with the oil conveying heater, so that the heated oil conveying heater can preheat and flush the pipeline between the bottom of the first reactor and/or the bottom of the second reactor and the loading and unloading tank, the temperature difference between the pipeline and the catalyst in the unloading process is prevented from being too large to reduce the temperature of the catalyst, and the problem that the property and yield of a target product are negatively influenced by the excessive temperature difference between the oil conveying heater and the catalyst and the materials inside the first reactor and/or the second reactor in the subsequent operation process is further avoided.

Optionally, the transfer oil heater communicates with a conduit between the top of the first reactor and the loading and unloading tank.

Optionally, the transferred oil heater communicates with a conduit between the top of the second reactor and the charge-discharge tank.

Through will carry the pipeline between oil heater intercommunication first reactor top and/or second reactor top and the loading and unloading jar, can make the transport oil after the heating preheat, wash the pipeline between first reactor top and/or second reactor top and the loading and unloading jar, avoid adding the reduction that the temperature difference is too big between agent in-process pipeline and the catalyst causes the catalyst temperature, and then further avoid getting into the transport oil in first reactor and/or the second reactor, the too big problem that produces negative effects to the nature and the yield of target product of the difference in temperature between catalyst and the inside material.

Optionally, the oil conveying and feeding pipe is communicated with the upper part or the middle part of the loading and unloading tank.

Through will carry oil to advance the upper portion or the middle part of oil pipe intercommunication loading and unloading jar, can make and carry oil to get into from upper portion or middle part in the loading and unloading jar to top-down sprays under the action of gravity, thereby wash loading and unloading jar and loading and unloading the catalyst that the jar was loaded, in order to avoid loading and unloading the impurity in the jar and loading and unloading the catalyst on adnexed impurity get into first reactor and/or second reactor in follow-up operation process, and then cause negative effects to production.

Optionally, the bottom of the loading and unloading tank is provided with a level detector.

Optionally, the bottom of the loading and unloading tank is provided with a densimeter.

Optionally, a densitometer is arranged at the bottom of the first reactor.

Optionally, the bottom of the second reactor is provided with a densitometer.

The density of the materials at the bottoms of the first reactor and the second reactor can be monitored by the densimeter, so that whether coking occurs or not can be timely known, and corresponding measures can be taken.

Optionally, the online catalyst loading and unloading system further comprises a waste oil filter, the waste oil filter is communicated with the waste oil outlet of the loading and unloading tank and the delivery oil storage tank through a pipeline, and a waste oil tank is arranged on the pipeline communicating the waste oil filter with the delivery oil storage tank.

Optionally, the online catalyst loading and unloading system further comprises a new catalyst storage tank, the new catalyst storage tank is communicated with the loading and unloading tank through a pipeline, and a catalyst metering tank is arranged on the pipeline communicating the new catalyst storage tank with the loading and unloading tank.

Optionally, the catalyst metering tank is provided with a pressure relief valve, a flare conduit and an exhaust conduit, the flare exhaust conduit being in communication with a flare system.

Optionally, the catalyst metering tank is provided with a shielding gas inlet conduit. The protective gas can be introduced into the catalyst measuring tank through the protective gas inlet pipeline, and then the air in the catalyst measuring tank can be removed.

Optionally, the online loading and unloading system for the catalyst further comprises a regenerated catalyst storage tank, and the regenerated catalyst storage tank is communicated with the loading and unloading tank through a pipeline.

Optionally, the on-line catalyst loading and unloading system further comprises a spent catalyst tank communicating with a conduit between the loading and unloading tank and the top of the first reactor and/or the top of the second reactor.

Optionally, the spent catalyst tank is provided with a gas outlet, an exhaust pipeline and a flare pipeline, the gas outlet is communicated with the flare pipeline, and the flare pipeline is communicated with a flare system.

As mentioned above, the catalyst on-line loading and unloading method and system of the invention ensure the stability of the activity of the catalyst in the first reactor and the second reactor by changing the daily loading and unloading agent mode and adding the oil transfer heat exchanger and the waste oil filter. Simultaneously, reduced the influence of loading and unloading agent process to material temperature in first reactor and the second reactor, still solved the coking problem, provide reliable assurance for the long period operation of device, specifically:

(1) the catalyst loading and unloading mode is changed from adding the agent first and then unloading the agent into adding the agent first and then unloading the agent, so that the stability of the activity of the catalyst in the first reactor and the second reactor is ensured, and meanwhile, the coking problem caused by excessive increase of the activity of the catalyst in the first reactor is avoided.

(2) By additionally arranging the oil conveying heater, the oil conveying heater can heat the oil conveying heater to 350-440 ℃, so that the temperature difference between the oil conveying heater entering the first reactor and/or the second reactor and the materials in the reactors is reduced, and the adverse effects of overlarge temperature difference on the properties of the target product and the yield of the target product are further avoided.

(3) By additionally arranging the waste oil filter, the catalyst powder can be retained in the waste oil filter, and the catalyst powder is prevented from entering the first reactor and the second reactor along with the conveying oil in the subsequent operation process and further being combined with substances such as colloid, asphalt and the like contained in the raw oil in the first reactor and the second reactor to generate coking.

Drawings

FIG. 1 is a schematic diagram of an on-line loading and unloading method of a conventional catalyst;

FIG. 2 is a graph showing the density of the bottom of the first reactor after three months of operation in the on-line loading and unloading manner of the conventional catalyst, wherein the density is 1310kg/m³And 1507kg/m³Are respectively a distanceThe density values of materials at 50% of the tangent height and 60% of the tangent height of the lower tangent of the first reactor;

FIG. 3 is a schematic view of the structure of the catalyst in-line loading and unloading system of example 1;

FIG. 4 shows the on-line loading and unloading manner of the catalyst of example 2;

FIG. 5 shows the density values of the bottom material of the first reactor after three months of operation according to the catalyst in-line loading and unloading method of example 2, wherein 849kg/m ³And 869kg/m³The density values of the materials at 50% tangential height and 60% tangential height from the lower tangent of the first reactor are respectively.

Reference numerals

The device comprises a first hoisting device 1, a second hoisting device 2, a new catalyst storage tank 3, a regenerated catalyst storage tank 4, a catalyst metering tank 5, a conveying oil storage tank 6, a conveying oil pump 7, a conveying oil heater 8, a loading and unloading tank 9, a first reactor 10, a second reactor 11, a waste catalyst tank 12, a waste oil filter 13, a waste oil tank 14, a waste oil pump 15, a densimeter DI, weighing components W1, W2, W3 and W4, a temperature adjusting component TC and an LI liquidometer.

Detailed Description

The following embodiments of the present invention are provided by way of specific examples, and other advantages and effects of the present invention will be readily apparent to those skilled in the art from the disclosure herein. The invention is capable of other and different embodiments and of being practiced or of being carried out in various ways, and its several details are capable of modification in various respects, all without departing from the spirit and scope of the present invention.

The invention provides an on-line loading and unloading method of a catalyst for a boiling bed residual oil hydrogenation process, which is carried out in an on-line loading and unloading system of the catalyst for the boiling bed residual oil hydrogenation process, wherein the system comprises a first reactor, a second reactor and a loading and unloading tank, the first reactor and the second reactor are both boiling bed hydrogenation reactors, and the method comprises the following steps:

Adjusting the internal pressure of the second reactor and the loading and unloading tank by using the conveying oil as a carrierMaking the internal pressure of the second reactor at least 0.2MPa higher than that of the loading and unloading tank, then making the used catalyst in the second reactor enter the loading and unloading tank together with the conveying oil, then making the internal pressure of the loading and unloading tank at least 0.2MPa higher than that of the first reactor by regulating the pressures of the loading and unloading tank and the first reactor, and further making the catalyst in the loading and unloading tank at 350-440 deg.C and 5-15m flow rate³H, conveying oil into the first reactor; the catalyst entering the first reactor participates in residual oil hydrogenation reaction, after the activity of the catalyst is partially lost, the pressure difference between the first reactor and the loading and unloading tank is adjusted, so that the internal pressure of the first reactor is at least 0.2MPa higher than that of the loading and unloading tank, and the catalyst in the first reactor enters the loading and unloading tank along with the conveying oil;

then adding new catalyst and conveying oil into the loading and unloading tank, adjusting the pressure of the loading and unloading tank and the second reactor to make the internal pressure of the second reactor at least lower than the internal pressure of the loading and unloading tank by 0.2MPa, and further making the new catalyst in the loading and unloading tank follow the temperature of 350- ³The/h of the transport oil are passed together into the second reactor.

The present invention will be described in detail below with reference to specific exemplary embodiments. It is also to be understood that the following examples are illustrative of the present invention and are not to be construed as limiting the scope of the invention, and that insubstantial modifications and adaptations of the invention as described above will now occur to those skilled in the art. The specific process parameters and the like of the following examples are also merely one example of suitable ranges, i.e., those skilled in the art can select the appropriate ranges through the description herein, and are not limited to the specific values exemplified below.

Example 1

Fig. 1 shows the catalyst on-line loading and unloading system of the present embodiment, which is used for discharging the used catalyst in the first reactor 10 and the second reactor 11 and adding new catalyst to the second reactor 11 in order to ensure the activity of the catalyst in the ebullated bed residue hydrogenation process.

As shown in fig. 1, the catalyst on-line loading and unloading system of the embodiment includes:

the system comprises a first reactor 10, a second reactor 11, a first hoisting device 1, a second hoisting device 2, a new catalyst storage tank 3, a regenerated catalyst storage tank 4, a catalyst metering tank 5, a loading and unloading tank 9, a waste catalyst tank 12 and a conveying oil storage tank 6.

The first reactor 10 and the second reactor 11 are used as reaction vessels for crude oil such as residual oil of heavy crude oil. When the raw oil such as the residual oil of heavy crude oil is treated, the raw oil such as the residual oil of heavy crude oil, hydrogen and a catalyst (usually nickel-vanadium metal, nickel-molybdenum metal or nickel-cobalt metal) are added into a first reactor 10, after a reaction for a period of time, the material in the first reactor 10 is added into a second reactor 11 for continuous reaction, and particularly, the material is transferred through a pipeline between the top of the first reactor 10 and the bottom 11 of the second reactor, so that the material is reacted completely. In the reaction process, the liquid reactant (the heavy component which is not evaporated in the raw oil) and the hydrogen-rich gas are lifted upwards and are in a fluidized state, so that the raw oil, the catalyst and the hydrogen enter the first reactor 10 and the second reactor 11 to be fully contacted, and then the hydrogenation reaction is completed, thereby improving the quality of the raw oil. In this process, the catalytic activity of the catalyst gradually decreases as the reaction proceeds. The first reactor 10 and the second reactor 11 both use ebullated-bed hydrogenation reactors, which are prior art and will not be described herein.

The first reactor 10 and the second reactor 11 are provided with a temperature regulating assembly, a hydrogen inlet pipeline (not shown), a densimeter and a reactant outlet, and the hydrogen inlet pipeline is provided with a switch valve. The temperature of the materials in the first reactor 10 and the second reactor 11 can be adjusted by the temperature adjusting assembly, and then the reaction temperature is controlled. The densimeter is used for monitoring the density of the materials at the bottom of the first reactor 10 and the second reactor 11, and then timely knowing whether the coking phenomenon occurs, so that corresponding measures are taken. In this embodiment, the first reactor 10 and the second reactor 11 both have cylindrical tubular structures.

The bottom of the first reactor 10 and the bottom of the second reactor 11 are communicated with the first end of the charging and discharging tank 9 through a discharging agent pipeline, the used catalyst in the first reactor 10 and the second reactor 11 can be conveyed to the charging and discharging tank 9 through the discharging agent pipeline, and the discharging agent pipeline is provided with a switch valve.

The top of the first reactor 10 and the top of the second reactor 11 are both communicated with the second end of the charging and discharging tank 9 through a chemical adding pipeline, and a switch valve is arranged on the chemical adding pipeline. The used catalyst in the charge-discharge tank 9 can be transported into the first reactor 10 through the dosing pipe between the first reactor 10 and the charge-discharge tank 9, and the new catalyst in the charge-discharge tank 9 can be transported into the second reactor 11 through the dosing pipe between the second reactor 11 and the second end of the charge-discharge tank 9.

The first and second lifting devices 1 and 2 are used for adding new catalyst and regenerated catalyst to the new catalyst storage tank 3 and the regenerated catalyst storage tank 4, respectively.

The new catalyst storage tank 3 and the regenerated catalyst storage tank 4 are both located above the catalyst metering tank 5, and are respectively used for storing new catalyst and regenerated catalyst, and are both provided with weighing components W1 and W2. The new catalyst storage tank 3 and the regenerated catalyst storage tank 4 are both communicated with a first end of a catalyst metering tank 5 through pipelines. And switching valves are arranged on a pipeline between the new catalyst storage tank 3 and the catalyst metering tank 5 and a pipeline between the regenerated catalyst storage tank 4 and the catalyst metering tank 5. The new catalyst and the regenerated catalyst in the new catalyst storage tank 3 and the regenerated catalyst storage tank 4 can be respectively conveyed to the catalyst metering tank 5 under the action of gravity through pipelines between the new catalyst storage tank 3 and the regenerated catalyst storage tank 4 and the catalyst metering tank 5.

The catalyst metering tank 5 is located above the charge-discharge tank 9, and is used for weighing and metering the catalyst filled in the catalyst metering tank, so as to monitor the amount of the catalyst. The second end of the catalyst metering tank 5 is communicated with a catalyst feed inlet of the loading and unloading tank 9 through a pipeline. A switch valve is arranged on a pipeline between the catalyst metering tank 5 and the loading and unloading tank 9. The catalyst after being weighed and measured can be conveyed to the loading and unloading tank 9 under the action of gravity through a pipeline between the catalyst metering tank 5 and the loading and unloading tank 9.

The catalyst metering tank 5 is provided with a protective gas inlet pipeline, a weighing component W3, a pressure release valve (not shown), a torch pipeline and an exhaust pipeline, and the torch pipeline is communicated with a torch system. Protective gas (such as nitrogen) can be introduced into the catalyst metering tank 5 through a protective gas inlet pipe, and then the air in the catalyst metering tank 5 is replaced. The weighing unit W3 can weigh the catalyst measuring tank 5, thereby monitoring the amount of catalyst filled in the catalyst measuring tank 5.

The charge-discharge tank 9 is a place where oil and catalyst are transferred to be mixed. The transportation oil is used as the transportation carrier of the catalyst, the catalyst is transferred among containers along with the transportation oil in the loading and unloading process, and the transportation oil can adopt wax oil and the like. The first end of the loading and unloading tank 9 is communicated with the delivery oil storage tank 6 through a delivery oil inlet pipe, and the second end of the loading and unloading tank is communicated with the delivery oil storage tank 6 through a delivery oil inlet pipe. The first end refers to the upper or middle portion of the loading and unloading tank and the second end refers to the lower portion of the loading and unloading tank. The oil conveying pipe is provided with an oil conveying pump 7 (not shown) and a switch valve. Through the first end, can make in carrying oil to get into loading and unloading jar 9 from upper portion or middle part, the transport oil that gets into in loading and unloading jar 9 sprays downwards at the action of gravity to play infiltration, dust removal and preheating effect to loading and unloading jar 9 and the inside catalyst that loads thereof, thereby get rid of impurity in loading and unloading jar 9 and the adnexed impurity on the inside catalyst that loads, avoid impurity to get into in first reactor 10 and/or second reactor 11 in follow-up operation process, and then cause negative effects to production. Through the second end, the conveying oil can enter the loading and unloading tank 9 from the lower part, and the conveying oil entering the loading and unloading tank 9 from the lower part is in reverse contact with the catalyst entering the loading and unloading tank 9 from the catalyst metering tank 5, so that the catalyst is flushed, and impurities attached to the catalyst are removed; in the process, the conveying oil and the catalyst are in sufficient heat transfer, so that the catalyst is preheated.

The second end of the loading and unloading tank 9 is communicated with the first end of the waste catalyst tank 12 through a pipeline, and a switch valve is arranged on the pipeline communicating the waste catalyst tank 12 with the loading and unloading tank 9. The spent catalyst deactivated in the loading and unloading tank 9 can be transferred into the spent catalyst tank 12 through a pipe between the loading and unloading tank 9 and the spent catalyst tank 12.

The loading and unloading tank 9 is provided with a hydrogen inlet pipeline (not shown), a pressure release valve (not shown), a material level detector DI, a liquid level meter LI, an exhaust pipeline (not shown) and a torch pipeline, wherein the first end of the loading and unloading tank is provided with an overflow port, the second end of the loading and unloading tank is provided with a waste oil outlet, the exhaust pipeline and the torch pipeline are both provided with switch valves, and the torch pipeline is communicated with a torch system.

The level detector DI can monitor the level change of the material in the loading/unloading tank 9, and thereby know the amount of the catalyst or the liquid remaining in the loading/unloading tank 9. The level detector DI employs a nuclear level gauge, which is prior art and will not be described herein.

The spent catalyst pot 12 is for storing spent catalyst of which activity is lost, and is provided with a gas outlet, a flare pipe, a shielding gas inlet pipe, and a weighing assembly W4. The gas outlet is communicated with a torch pipeline, the torch pipeline is provided with a switch valve which is communicated with a torch system, and the protective gas inlet pipeline is provided with a switch valve. Protective gas (such as nitrogen) can be introduced into the waste catalyst tank 12 through the protective gas inlet pipeline, and then oil gas in the waste catalyst tank 12 is replaced. A first end of the spent catalyst tank 12 is provided with a diesel inlet.

The catalyst on-line loading and unloading system of the embodiment further comprises a delivery oil heater 8, wherein the delivery oil heater 8 is positioned on a delivery oil inlet pipe, a switch valve and a delivery oil pump 7 are arranged on the delivery oil inlet pipe between the delivery oil heater 8 and the delivery oil storage tank 6, and a switch valve is arranged on the delivery oil inlet pipe between the delivery oil heater 8 and the loading and unloading tank 9. The oil delivery heater 8 may be an oil tank heater, which is a conventional technique and will not be described herein.

The delivery oil heater 8 is communicated with the agent discharging pipeline between the first end of the loading and unloading tank 9 and the positions A and B. And a switching valve is arranged on a pipeline between the conveying oil heater 8 and the position A and/or the position B. Through the pipelines between the conveying oil heater 8 and the position A and/or the position B, heated conveying oil can be preheated and flushed through the agent unloading pipelines between the loading and unloading tank 9 and the position A and/or the position B, the temperature difference between the catalyst and the agent unloading pipelines in the agent unloading process is prevented from being too large to cause the reduction of the temperature of the catalyst, the temperature difference between the catalyst entering the first reactor 10 and/or the second reactor 11 and materials in the subsequent operation process is further prevented from being too large, the reaction temperature of the materials in the reactors is reduced, and the property and the yield of target products are further influenced.

The conveying oil heater 8 is communicated with a feeding and discharging tank 9, and a dosing pipeline is arranged between the second end of the feeding and discharging tank and the top of the first reactor 10 and the top of the second reactor 11, and a switch valve is arranged on each dosing pipeline between the conveying oil heater 8 and the top of the first reactor 10 and between the conveying oil heater and the top of the second reactor 11. In the same way, by means of the additive pipeline between the oil delivery heater 8 and the top of the first reactor 10 and the top of the second reactor 11, heated delivery oil can be preheated and the additive pipeline at the section is washed, the temperature difference between the catalyst and the additive unloading pipeline in the additive process is prevented from being too large to reduce the temperature of the catalyst, the temperature difference between the catalyst entering the first reactor 10 and/or the second reactor 11 and the material is prevented from being too large, the reaction temperature of the material in the reactors is reduced, and the property and the yield of the target product are influenced.

The catalyst on-line loading and unloading system of the embodiment can heat the conveying oil from the conveying oil storage tank 6 to 350-.

The catalyst in-line loading and unloading system of the present embodiment further includes a waste oil filter 13 and a waste oil tank 14.

The waste oil filter 13 is provided with a filter assembly (not shown), which may be a screen or the like. The first end of the waste oil filter 13 is communicated with the overflow port of the loading and unloading tank 9 and the waste oil outlet through pipelines, and the second end of the waste oil filter is communicated with the waste oil tank 14 through a pipeline. Switch valves are arranged on the pipelines between the overflow port and the waste oil outlet and the waste oil filter 13, and switch valves are arranged on the pipelines between the waste oil filter 13 and the waste oil tank 14. The excess delivery oil in the loading and unloading tank 9 can be conveyed to the waste oil filter 13 through the overflow port and the pipeline between the waste oil outlet and the waste oil filter 13. The catalyst powder carried by the conveying oil can be retained in the filter assembly, so that the catalyst powder is prevented from entering the first reactor 10 and/or the second reactor 11 along with the conveying oil in the subsequent operation process, and further being combined with substances such as colloid, asphalt and the like contained in the raw oil to generate coking.

The waste oil tank 14 is located below the waste oil filter 13, the second end of the waste oil tank is communicated with the waste oil tank area through a pipeline, a switch valve and a waste oil pump 15 are arranged on the pipeline between the communicated waste oil tank 14 and the waste oil tank area, and the waste oil pump 15 can adopt a centrifugal pump and the like. The transportation oil from which the impurities have been removed can be transported to the waste oil tank zone by the pumping action of the waste oil pump 15 through a pipe between the waste oil tank 14 and the waste oil tank zone.

Example 2

The system of example 1 was used to load and unload catalyst on-line, the specific steps were as follows:

the on-off valve on the delivery oil inlet pipe between the delivery oil storage tank 6 and the second end of the loading and unloading tank 9, the delivery oil pump 7, and the delivery oil heater 8 are opened. The transportation oil from the transportation oil storage tank 6 enters the transportation oil heater 8 by the pumping action of the transportation oil pump 7, and the temperature of the transportation oil is increased to 350 ℃ after the transportation oil heater 8 is heated. The heated transfer oil enters the loading and unloading tank 9 from the second end under the pumping action of the transfer oil pump 7, so that the ambient temperature in the loading and unloading tank 9 is raised to be higher than the minimum boost temperature (namely the MPT temperature). The on-off valve on the delivery oil inlet pipe between the delivery oil heater 8 and the second end of the loading and unloading tank 9 is closed. The conveying oil is wax oil.

Opening a switch valve on a hydrogen inlet pipeline, introducing hydrogen into the loading and unloading tank 9, increasing the internal pressure of the loading and unloading tank 9 to 17MPa, and closing the switch valve on the hydrogen inlet pipeline, wherein the internal pressure of the loading and unloading tank 9 is lower than the internal pressure of the second reactor 11 by 0.5MPa because the internal pressure of the second reactor 11 is 17.5 MPa.

In the process of introducing hydrogen into the loading and unloading tank 9, opening switching valves on a pipeline between the delivery oil heater 8 and the position B, an unloading agent pipeline between the position B and the loading and unloading tank 9, a pipeline between a waste oil outlet of the loading and unloading tank 9 and the waste oil filter 13 and a pipeline between the waste oil filter 13 and the waste oil tank 14, flushing and preheating the unloading agent pipeline between the position B and the loading and unloading tank 9 by the heated delivery oil, then entering the loading and unloading tank 9, and entering the waste oil filter 13 through the waste oil outlet.

After washing for 10min, the on-off valve (not shown) on the discharge line between the bottom of the second reactor 11 and the position B and the on-off valve on the communication line between the waste oil filter 13 and the waste oil tank 14 were opened, and the on-off valve on the line between the second end of the waste oil tank 14 and the waste oil tank area and the waste oil pump 15 were opened to supply oil to the waste oil tank area. Due to the pressure difference between the charge-discharge tank 9 and the second reactor 11, the used catalyst in the second reactor 11 is sent to the charge-discharge tank 9 together with the transfer oil, and the excess transfer oil is sent to the waste oil filter 13 through the waste oil outlet. The transport oil is filtered by the filter assembly in the waste oil filter 13, and then impurities such as catalyst powder attached to the pipe wall carried in the transport oil are removed, and the filtered transport oil is pumped into the waste oil tank 14 and then is sent to the waste oil tank area under the pumping action of the waste oil pump 15 in the subsequent process.

The discharge amount of the catalyst is determined by the level detector, and after the discharging is completed, the on-off valve (not shown) on the pipeline between the bottom of the second reactor 11 and the position B is closed, and the discharging pipeline between the loading and unloading tank 9 and the position B is continuously flushed with the conveying oil for 10 min.

After the flushing is completed, the waste oil pump 15, the delivery oil pump 7, and all the on-off valves are closed. The temperature in the first reactor 10 (originally 431 ℃) is raised by 1 ℃ through a temperature regulating component, a switch valve on a hydrogen inlet pipeline of the charging and discharging tank 9 is opened, and hydrogen is introduced into the charging and discharging tank 9, so that the internal pressure of the charging and discharging tank 9 is higher than that of the first reactor 10 (the internal pressure of the second reactor 10 is 17.5MPa) by 0.5 MPa.

In the pressure adjusting process, a switch valve and a delivery oil pump 7 on a pipeline between a delivery oil storage tank 6 and a delivery oil heater 8 are opened, a switch valve on an additive pipeline between the delivery oil heater 8 and the top of a first reactor 10 is opened, delivery oil enters the additive pipeline between the delivery oil heater 8 and the top of the first reactor 10 under the pumping action of a centrifugal pump, and the additive pipeline is preheated and washed, so that catalyst powder remaining on the pipe wall enters the first reactor 10 along with the delivery oil.

After flushing for 10min, the on-off valve on the line between the charge-discharge tank 9 and the top of the first reactor 10 was opened. Due to the pressure difference between the loading and unloading tank 9 and the first reactor 10, the catalyst in the loading and unloading tank 9 is heated to 350 ℃ and is fed into the first reactor 10 together with the delivery oil, the flow rate of which is 10m³/h。

In the transportation process, open the ooff valve on the delivery oil inlet pipe between delivery oil heater 8 and the second end of loading and unloading jar 9, delivery oil after the heating is by the pump sending to loading and unloading jar 9 in to guarantee to add the delivery oil in the unloading jar 9 and maintain certain level, avoid adding the agent later stage and add and be "dry pan" state in the unloading jar 9, and then influence going on smoothly of agent process.

When the level detector DI indicates that there is no catalyst in the loading and unloading tank 9 (i.e. the additive is completed), the on-off valve on the pipeline between the loading and unloading tank 9 and the top of the first reactor 10 is closed, the on-off valve on the pipeline between the conveying oil heater 8 and the top of the first reactor 10 is opened, and the conveying oil continues to flush the additive pipeline communicated with the top of the first reactor 10 for 10 min. And after the flushing is finished, closing the switch valve.

When the catalyst in the first reactor 10 is partially deactivated, the on-off valve on the exhaust pipe of the loading and unloading tank 9 is opened, and the internal pressure of the loading and unloading tank 9 is made to be 0.5MPa lower than that of the first reactor 10 through pressure regulation.

In the pressure regulation process of the loading and unloading tank 9, switching valves of a pipeline between the conveying oil storage tank 6 and the conveying oil heater 8, a pipeline between the conveying oil heater 8 and the position A and a pipeline between the loading and unloading tank 9 and the position A are opened, and conveying oil heated to 350 ℃ flushes and preheats the unloading agent pipeline between the position A and the loading and unloading tank 9 for 10 min.

After the completion of the flushing, the on-off valve on the discharging line between the bottom of the first reactor 10 and the position a and the on-off valve on the line between the waste oil outlet of the loading and unloading tank 9 and the waste oil filter 13 are opened. Because of the pressure difference between the charge-discharge tank 9 and the first reactor 10, the spent catalyst in the first reactor 10 is sent to the charge-discharge tank 9 together with the transfer oil, and the excess transfer oil is sent to the spent oil filtering mechanism 13 through the spent oil outlet.

The discharge amount of the catalyst is determined according to the level detector DI, and after the discharging is completed, the on-off valve on the discharging pipeline between the bottom of the first reactor 10 and the position A is closed, and the discharging pipeline between the loading and unloading tank 9 and the position A is continuously flushed with the conveying oil for 10 min.

And (4) closing all the switch valves after the flushing is finished. The pressure in the loading and unloading tank 9 is discharged by the pressure relief valve, then the on-off valve on the oil inlet pipe of the conveying oil between the conveying oil heater 8 and the first end of the loading and unloading tank 9 and the conveying oil pump 7 are opened, and the on-off valve on the pipeline between the waste oil outlet of the loading and unloading tank 9 and the waste oil filter 13 is opened. The transportation oil enters the loading and unloading tank 9 from the first end, and washes the waste catalyst in the loading and unloading tank 9 from top to bottom under the action of gravity, so that the waste catalyst is cooled.

After the catalyst in the loading and unloading tank 9 has been cooled to a certain temperature, the on-off valve in the oil feed pipe for feeding oil between the oil-feeding heater 8 and the first end of the loading and unloading tank 9 and the oil-feeding pump 7 are closed, the on-off valve in the pipe between the waste oil outlet and the waste oil filter 13 are closed, and the pressures of the loading and unloading tank 9 and the waste catalyst tank 12 are adjusted by the pressure adjusting means (here, the internal pressures of the loading and unloading tank 9 and the waste catalyst tank 12 can be adjusted by using a flare system, or the internal pressures of the loading and unloading tank 9 and the waste catalyst tank 12 can be adjusted by the on-off valves in the exhaust pipe and the protective gas intake pipe), so that the internal pressure of the loading and unloading tank 9 is higher than the internal pressure of the waste catalyst tank 12 by 1 MPa.

In the pressure adjusting process, the switching valve and the centrifugal pump on the pipe between the delivery oil heater 8 and the spent catalyst tank 12 are opened, and the delivery oil flushes and preheats the pipe between the delivery oil heater 8 and the spent catalyst tank 12.

After flushing for 10min, the on-off valve on the line between the charge-discharge tank 9 and the spent catalyst tank 12 was opened. Because of the pressure difference between the loading and unloading tank 9 and the waste catalyst tank 12, the waste catalyst in the loading and unloading tank 9 enters the waste catalyst tank 12 along with the conveying oil under the action of the pressure difference. In the transportation process, open the ooff valve on the pipeline between the first end of carrying oil heater 8 and loading and unloading jar 9, carry oil by the pump sending to loading and unloading jar 9 in to guarantee to carry oil in the loading and unloading jar 9 and maintain certain level, avoid the useless catalyst to shift the smooth going on that influences useless catalyst and shift of the interior insufficient delivery oil of later stage loading and unloading jar 9.

When the material level detector DI shows that no catalyst exists in the loading and unloading tank 9, the on-off valve between the loading and unloading tank 9 and the waste catalyst tank 12 is closed, the oil conveying heater 8 is closed, the on-off valve on the pipeline between the oil conveying heater 8 and the waste catalyst tank 12 is opened, and the conveying oil which is not required to be heated by the oil conveying heater 8 continuously washes the pipeline between the oil conveying heater 8 and the waste catalyst tank 12 for 10 min.

After the washing is completed, the on-off valve on the pipe between the delivery oil heater 8 and the spent catalyst tank 12 is closed, and the spent catalyst tank 12 is left standing for a while. When the weight component W4 shows that the mass of the waste catalyst tank 12 is unchanged within 2 hours continuously, the pressure in the waste catalyst tank 12 is relieved by a pressure relief valve, and protective gas is introduced into the waste catalyst tank 12, wherein the protective gas is nitrogen. The waste catalyst in the waste catalyst tank 12 is unloaded into a loading system and transported to a regeneration factory for regeneration, and the obtained regenerated catalyst is placed into a regenerated catalyst storage tank 4.

The pressure in the loading and unloading tank 9 is relieved by a relief valve, the pressure in the loading and unloading tank 9 is adjusted to 0.05MPa by a torch system, a switch valve on a torch pipeline is closed, a switch valve and a delivery oil pump 7 on a pipeline between a delivery oil storage tank 6 and a delivery oil heater 8 are opened, a switch valve and a delivery oil pump 7 on a delivery oil inlet pipe between the delivery oil heater 8 and the first end of the loading and unloading tank 9 are opened, and the heated delivery oil is pumped to the loading and unloading tank 9 until the volume of the delivery oil in the loading and unloading tank 9 reaches 50% of the volume of the loading and unloading tank.

And closing the switch valve on the oil inlet pipe of the conveying oil between the conveying oil heater 8 and the first end of the loading and unloading tank 9 and the conveying oil pump 7. Opening the on-off valves on the pipeline between the new catalyst storage tank 3 and the catalyst metering tank 5 and the pipeline between the regenerated catalyst storage tank 4 and the catalyst metering tank 5, allowing the new catalyst in the new catalyst storage tank 3 and the regenerated catalyst in the regenerated catalyst storage tank 4 to enter the catalyst metering tank 5 under the action of gravity, and weighing the new catalyst and the regenerated catalyst by the weighing component W3 in the catalyst metering tank 5. Wherein, the mass ratio of the new catalyst in the new catalyst storage tank 3 to the regenerated catalyst in the regenerated catalyst storage tank 4 is 8:2 (in the actual production process, the ratio of the new catalyst to the regenerated catalyst can be adjusted according to the activity of the whole catalyst in the second reactor 11).

Closing the on-off valves on the pipeline between the new catalyst storage tank 3 and the catalyst metering tank 5 and the pipeline between the regenerated catalyst storage tank 4 and the catalyst metering tank 5, opening the on-off valves on the exhaust pipeline and the protective gas inlet pipeline, introducing protective gas into the catalyst metering tank 5, introducing the protective gas into the catalyst metering tank 5, wherein the protective gas adopts nitrogen, and the air in the catalyst metering tank 5 is gradually replaced by the protective gas.

And when the pressure in the catalyst metering tank 5 reaches 0.1MPa, closing the switch valves on the exhaust pipeline and the protective gas inlet pipeline, and opening the switch valve on the pipeline between the catalyst metering tank 5 and the charging and discharging tank 9. Due to the difference in height between the catalyst metering tank 5 and the charge/discharge tank 9, the catalyst filled in the catalyst metering tank 5 is sent to the charge/discharge tank 9 by gravity. In this process, the on-off valve on the feed pipe of the transfer oil between the transfer oil heater 8 and the second end of the loading and unloading tank 9 and the transfer oil pump 7 are opened, and the on-off valves on the pipe between the waste oil outlet of the loading and unloading tank 9 and the waste oil filter 13 and the pipe between the overflow port of the loading and unloading tank 9 and the waste oil filter 13 are opened. The transfer oil entering the charge-discharge tank 9 from the second end exchanges heat with the catalyst in the charge-discharge tank 9, thereby preheating the catalyst and sending the catalyst to the waste oil filter 13 through the overflow port.

When the weighing component W3 of the catalyst metering tank 5 shows that no catalyst exists in the weighing component, the switch valve on the pipeline between the catalyst metering tank 5 and the loading and unloading tank 9 is closed, the heated conveying oil enters the loading and unloading tank 9 from the second end of the loading and unloading tank 9, and the catalyst filled in the loading and unloading tank 9 is continuously washed and preheated for 10 min.

After the flushing and preheating are finished, the oil conveying pump 7 and all the switch valves are closed. And opening a switch valve on a hydrogen inlet pipeline, and introducing hydrogen into the loading and unloading tank 9 to ensure that the internal pressure of the loading and unloading tank 9 is increased to 17MPa and is 0.5MPa higher than the internal pressure of the second reactor 11.

During the pressure regulation, a pipe between the delivery oil storage tank 6 and the delivery oil heater 8 is openedAn on-line switch valve and a delivery oil pump 7, an oil delivery heater 8 is opened, and an on-line switch valve on a dosing pipeline between the oil delivery heater 8 and the top of a second reactor 11 is opened; the heated transport oil flushes and preheats the additive pipeline. After flushing for 10min, the on-off valve on the line between the charge-discharge tank 9 and the top of the second reactor 11 was opened. Due to the pressure difference between the loading and unloading tank 9 and the second reactor 11, the catalyst in the loading and unloading tank 9 is pumped into the second reactor 11 together with the transportation oil heated to 350 ℃, and the flow rate of the transportation oil is 10m ³/h。

In the process of adding the agent, the switching valve on the oil inlet pipe of the oil delivery heater 8 and the first end of the loading and unloading tank 9 and the oil delivery pump 7 are opened to ensure that the oil delivery in the loading and unloading tank 9 is maintained at a certain level, and the smooth proceeding of the agent adding process due to the insufficient oil delivery in the loading and unloading tank 9 in the later period of adding the agent is avoided.

When the level detector DI shows that no catalyst is present in the loading and unloading tank 9, the on-off valve on the pipeline between the loading and unloading tank 9 and the top of the second reactor 11 is closed, the on-off valve on the pipeline between the conveying oil heater 8 and the top of the second reactor 11 is opened, and the additive pipeline is continuously flushed with the heated conveying oil for 10 min.

And (5) after the flushing is finished, closing the oil conveying heater 8, the oil conveying pump 7 and all switch valves, and finishing the on-line loading and unloading process of the catalyst.

Example 3

The catalyst was charged in-line in the same manner as in example 2, except that the following conditions were applied:

the flow rate of the conveying oil is 15m³The temperature of the oil feed was 360 ℃.

Result detection

The catalysts were charged and discharged on-line in the same manner as in examples 2 to 4 and comparative example 1, respectively, and after three months of operation, density values at 50% tangential height (first position) and 60% tangential height (second position) from a lower tangent of the first reactor, where tangential height is a distance L0 between a top tangent and a bottom tangent of the first reactor and lower tangent 50% tangential height is a distance L1 between the material and the bottom tangent is 50% of a distance L0 between the top tangent and the bottom tangent, were shown by densitometers, and the results are shown in table 1.

TABLE 1 test results

As can be seen from table 1, the density values of the first reactor bottoms were significantly reduced compared to the prior art for three months of operation in the manner of examples 2-3. Therefore, the invention effectively solves the problems of loss caused by immediate discharge of the new agent in the second reactor after addition and bottom coking caused by excessive increase of the activity of the catalyst in the first reactor in the prior art, and ensures long-period stable operation of the device.

The foregoing embodiments are merely illustrative of the principles and utilities of the present invention and are not intended to limit the invention. Those skilled in the art can modify or change the above-described embodiments without departing from the spirit and scope of the present invention. Accordingly, it is intended that all equivalent modifications or changes which may be made by those skilled in the art without departing from the spirit and scope of the present invention as defined in the appended claims.

Claims

1. An on-line loading and unloading method of a catalyst for a boiling bed residual oil hydrogenation process is carried out in an on-line loading and unloading system of the catalyst for the boiling bed residual oil hydrogenation process, the system comprises a first reactor and a second reactor, and the first reactor and the second reactor are both boiling bed hydrogenation reactors, and the method is characterized by comprising the following steps of: adding the used catalyst in the second reactor into the first reactor, allowing the catalyst entering the first reactor to participate in residual oil hydrogenation, discharging the catalyst after the catalyst loses activity, and adding new catalyst into the second reactor.

2. The method for on-line loading and unloading of catalyst as claimed in claim 1, wherein the system further comprises a loading and unloading tank, and the step of loading the used catalyst in the second reactor into the first reactor comprises the steps of: the method comprises the steps of taking conveying oil as a carrier, enabling the used catalyst in the second reactor to enter the loading and unloading tank along with the conveying oil by adjusting the pressure difference between the second reactor and the loading and unloading tank, and enabling the catalyst in the loading and unloading tank to enter the first reactor along with the conveying oil by adjusting the pressure difference between the loading and unloading tank and the first reactor.

3. The on-line catalyst loading and unloading method according to claim 2, wherein the internal pressure of the second reactor is at least 0.2MPa higher than the internal pressure of the loading and unloading tank;

and/or the internal pressure of the loading and unloading tank is at least 0.2MPa higher than the internal pressure of the first reactor;

and/or the flow rate of the conveying oil is 5-15m during the process that the catalyst enters the first reactor³/h；

And/or the temperature of the conveying oil is 350-440 ℃ during the process that the catalyst enters the first reactor.

4. The method for loading and unloading catalyst on-line as recited in claim 1, wherein the system further comprises a loading and unloading tank, and the step of unloading the catalyst in the first reactor comprises the following steps: the catalyst in the first reactor enters the loading and unloading tank along with the conveying oil by adjusting the pressure difference between the first reactor and the loading and unloading tank by using the conveying oil as a carrier.

5. The on-line catalyst loading and unloading method according to claim 4, wherein the internal pressure of the first reactor during the unloading of the catalyst from the first reactor is at least 0.2MPa higher than the internal pressure of the loading and unloading tank;

and/or, the addition of fresh catalyst to the second reactor comprises the steps of: adding new catalyst and conveying oil into the loading and unloading tank, and adjusting the pressure difference between the loading and unloading tank and the second reactor to ensure that the new catalyst in the loading and unloading tank enters the second reactor along with the conveying oil;

and/or, further comprising the steps of: and (3) regenerating the catalyst discharged from the first reactor to obtain a regenerated catalyst, and adding the regenerated catalyst into the second reactor.

6. An on-line loading and unloading system of a catalyst for a boiling bed residual oil hydrogenation process is characterized by comprising the following components:

7. The catalyst on-line loading and unloading system of claim 6, wherein the transportation oil heater is communicated with a pipeline between the bottom of the first reactor and the loading and unloading tank;

and/or the conveying oil heater is communicated with a pipeline between the bottom of the second reactor and the loading and unloading tank;

and/or the delivery oil heater is communicated with a pipeline between the top of the first reactor and the loading and unloading tank;

and/or the delivery oil heater is communicated with a pipeline between the top of the second reactor and the loading and unloading tank;

and/or the oil conveying inlet pipe is communicated with the upper part or the middle part of the loading and unloading tank.

8. The on-line catalyst loading and unloading system of claim 6, wherein a level detector is arranged at the bottom of the loading and unloading tank;

and/or a densimeter is arranged at the bottom of the charging and discharging tank;

and/or a densimeter is arranged at the bottom of the first reactor;

and/or a density meter is arranged at the bottom of the second reactor.

9. The on-line catalyst loading and unloading system of claim 6, further comprising a waste oil filter, wherein the waste oil filter is communicated with the waste oil outlet of the loading and unloading tank and the delivery oil storage tank through a pipeline, and a waste oil tank is arranged on the pipeline communicated with the waste oil filter and the delivery oil storage tank;

And/or, still include new catalyst storage jar, new catalyst storage jar passes through the pipeline intercommunication add the jar of unloading, be provided with the catalyst metering tank on the new catalyst storage jar of intercommunication and the pipeline of adding the jar of unloading.

10. The on-line catalyst loading and unloading system as recited in claim 6, further comprising a regenerated catalyst storage tank, wherein the regenerated catalyst storage tank is communicated with the loading and unloading tank through a pipeline;

and/or, the reactor also comprises a waste catalyst tank which is communicated with a pipeline between the loading and unloading tank and the top of the first reactor and/or the top of the second reactor.