JP2012162649A - System and method for producing diesel fuel - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a system for producing a diesel fuel by a catalytic cracking process, wherein: temperature of the production system can be controlled effectively; and a catalyst can be renewed as a whole.SOLUTION: The system includes: a reactor vessel that has the catalyst for changing a raw oil supplied from a raw material tank into a cracked oil comprising hydrocarbon; a first fractionator for separating a light oil from the cracked oil obtained from the reactor vessel; a second fractionator for collecting a light oil fraction from the light oil obtained by the first fractionator; a cooler for cooling the light oil fraction collected in the second fractionator to produce a product oil; and a raw oil-supplying line for making the raw oil supplied from the raw material tank to the reactor vessel possible to be supplied to the reactor after using the raw oil as heat medium sequentially for the cooler, the second fractionator and the first fractionator. The raw oil-supplying line includes: a raw oil-supplying pump for supplying the raw oil to a downstream side; a first preheater installed between the cooler and the second fractionator, and used for heating the raw oil; and a second preheater installed between the second fractionator and the first fractionator, and used for heating the raw oil.

Description

  The present invention relates to a diesel fuel manufacturing system and a diesel fuel manufacturing method manufactured using a catalyst. In particular, as a raw material for producing diesel fuel, it is possible to use waste edible oil, vegetable oil, animal oil, and various mineral oils alone or in combination, and a biodiesel fuel production system by a catalytic cracking method and biodiesel fuel It relates to a manufacturing method.

  A transesterification method (FAME) has been put into practical use and widely adopted as a light oil alternative fuel technology using fats and oils such as waste cooking oil (for example, Patent Document 1). However, the transesterification method has a slow reaction rate, requires petroleum-derived methanol, and has problems such as treatment of glycerin, which is a by-product, and wastewater treatment that occurs in the washing step.

  Moreover, there exists a hydrogenation method as another method (for example, patent document 2). Although this hydrogenation method has a high reaction rate and high quality as a light oil, it requires a hydrogen source and high-pressure gas equipment, generates water as a by-product, and is low in temperature because synthetic oil is paraffin. There are problems such as poor fluidity.

  As another method, there is a fluidized bed catalytic cracking (FCC) method (for example, Patent Document 3). The reforming of waste cooking oil by this method requires large-scale equipment such as a circulating fluidized bed, and when using a zeolite (USY type, etc.) that is an FCC catalyst, catalytic cracking (cracking) proceeds too much, and gas, However, there is a problem that light oil content is reduced.

  As another method, there is a catalytic decomposition method (for example, Patent Document 4). The catalytic cracking method is a method of decomposing into light gases such as light oily hydrocarbons, carbon dioxide, and propane by a decarboxylation decomposition reaction that cleaves the ester bond portion of fats and oils by the action of a solid catalyst.

JP 2008-1856 A JP 2007-153928 A JP 2007-177193 A JP 2006-28570 A

  In the catalytic cracking method of Patent Document 1, it is necessary to warm the solid catalyst to the reaction temperature, and in order to obtain diesel fuel as a final product from the gas components obtained in the reactor, a fractionator or a cooling device is used. It is necessary to provide a vessel. In order to ensure the performance such as final product quality and yield and stable operation, it is necessary to control the reactor, the fractionator, the cooler, and the like at a predetermined temperature. A heating medium and a cooling medium are required for temperature control of these apparatuses. Moreover, since the cooling heat quantity in a fractionator or a cooler is discarded as a heat loss, there is a problem in heat utilization. In addition, since the heating process and the cooling process are mixed, there is a problem that the amount of heat consumption increases.

  Further, when the reaction proceeds with the catalyst, coke or the like is deposited on the catalyst in the reactor, so it is necessary to regenerate the catalyst by supplying air (oxygen) to the reactor to burn off the coke. However, if air is supplied in a fixed bed reactor, the temperature may increase due to local coke combustion. In such a case, it is necessary to reduce the amount of air so that the temperature falls below the heat resistance temperature of the catalyst. Thus, if the amount of air is reduced, heat dispersion is suppressed, so that only more local catalyst regeneration is possible.

  Therefore, the present invention has been made in view of the problems and circumstances of the above-described technology, and its purpose is to perform contact temperature control that can effectively control the temperature of the manufacturing system and regenerate the catalyst as a whole. An object of the present invention is to provide a diesel fuel production system and a diesel fuel production method by a decomposition method.

The diesel fuel production system of the present invention comprises:
A raw material tank for storing raw material oil;
A reactor having a catalyst for converting the feedstock supplied from the feedstock tank into cracked oil comprising hydrocarbons;
A first fractionator for separating light oil from the cracked oil obtained in the reactor;
A second fractionator for recovering a light oil fraction from the light oil obtained in the first fractionator;
A cooler that cools the light oil fraction recovered in the second fractionator into product oil;
The raw material oil that can be supplied to the reactor after using the raw material oil supplied from the raw material tank to the reactor as a heating medium in the order of the cooler, the second fractionator, and the first fractionator. With oil supply line,
The feedstock supply line is
A feed oil supply pump for supplying the feed oil downstream;
A first preheater installed between the cooler and the second fractionator to heat the feedstock;
A second preheater installed between the second fractionator and the first fractionator for heating the feedstock.

  According to the above configuration, the first fractionator, the second fractionator, and the cooler are structured to exchange heat, the raw oil is used as the heat medium, and the cooler, the second fractionator, and the first fractionator. Since the heat is used in this order, the preheating amount of the raw material oil can be covered by the cooling heat amount of the fractionator and the cooler, and the heat consumption can be reduced. Further, by preheating the raw material oil, the temperature range in each fractionator is reduced, and stable temperature control is possible from the start of operation to steady operation.

  In the present invention, the raw material oil is, for example, waste edible oil, vegetable oil, animal oil, and various mineral oils alone or mixed. Examples of the waste cooking oil include tempura oil and fried oil. Examples of vegetable oils include rapeseed oil, soybean oil, sesame oil, safflower oil, cottonseed oil, rice oil, peanut oil, sunflower oil, corn oil, olive oil, palm oil, coconut oil, jatropha oil, peanut oil and the like. Examples of animal fats include beef tallow (hett), pork oil (lard) and the like. Examples of the mineral oil include various hydrocarbon-based mineral oils. In the catalytic cracking method using a solid catalyst, it is preferable to heat the raw material oil in advance. The preheating temperature is a temperature range in which the raw material oil is not vaporized, and a temperature range in which the catalytic reaction is efficiently performed is preferable, for example, a temperature range of 200 to 400 ° C., preferably a temperature range of 300 to 350 ° C. . Since the raw material oil is preheated and kept in the catalytic reaction temperature range while being liquid, it is preferable because there is no oxidative deterioration due to vaporization.

The catalyst used in the catalytic cracking method is a solid catalyst. Examples of the solid catalyst include zeolite, ion exchange resin, lime, clay, metal oxide, metal carbonate, composite oxide such as SiO ₂ —MgO and SiO ₂ —CaO, or supported metal oxide, and the like. A supported metal oxide of SiO ₂ —MgO is preferred. When this supported metal oxide of SiO ₂ —MgO is used, the yield of the obtained diesel fuel (light oil) is preferably 60% or more. In addition, the method for fixing the solid catalyst is not particularly limited, and the fixed catalyst reactor is configured by fixing the solid catalyst to the fixing member.

  The cracked oil obtained by the reaction of the raw material oil in the fixed catalyst reactor is subjected to two-stage fractionation using the first fractionator and the second fractionator. The fractionation temperature range of the first fractionator is high, and the fractionation temperature range of the second fractionator is a fractionation temperature range lower than that. The fractionation temperature range of the first fractionator is preferably a temperature range that is preferable for separating boiling components higher than light oil, for example, a temperature range of 250 ° C to 360 ° C is preferred, and 300 ° C is more preferred. Further, the fractionation temperature range of the second fractionator is preferably a preferred temperature range for separating the boiling components below light oil, for example, a temperature range of 120 ° C. to 200 ° C. is preferable, and a temperature of 140 ° C. to 170 ° C. A range is more preferred. Moreover, it is preferable to carry out fractional distillation as it is depending on the amount of heat of the cracked oil. For example, the temperature of the cracked oil gas supplied to the first fractionator is set to 350 ° C. or more in consideration of the temperature drop in the first fractionator, and the temperature of the light oil gas supplied to the second fractionator is the first. You may comprise so that it may become the temperature range which considered the temperature fall in a 2 fractionator. By this two-stage fractionation, hydrocarbon oils such as combustible gas components, naphtha / kerosene / light oil, and residues (coke) are continuously fractionated.

  And the light oil fraction (gaseous form) obtained with the 2nd fractionator is cooled, and liquid product oil (diesel fuel) is obtained. The diesel fuel produced according to the present invention is light oil that conforms to the JIS K2204 standard, and is distinguished from conventional biodiesel fuel (BDF) and light oil substitute fuel.

In one embodiment of the invention, a first temperature control unit that controls a heating temperature of the raw material oil to a predetermined range by the first preheater;
A second temperature control unit configured to control the heating temperature of the raw material oil to a predetermined range by the second preheater.

  According to this configuration, for example, at the start-up of the operation, the feed oil is heated to a predetermined temperature in each of the first and second preheaters and supplied in the order of the second fractionator, the first fractionator, and the reactor. Therefore, the heat medium in the temperature range required for each fractionator can be effectively supplied, and the temperature of the raw material supplied to the reactor can be made suitable for the catalytic reaction. For example, at the time of start-up, normal temperature raw material oil is heated to 150 to 240 ° C. with a second preheater and heated to 250 to 350 ° C. with a first preheater.

  The first and second temperature control units include, for example, various temperature sensors, thermostats, thyristors, temperature indicating controllers, information processing devices (including control programs), dedicated control circuits, firmware, etc. alone or in combination thereof. It is configured and outputs a control signal (information) on whether or not to heat, such as an ON / OFF signal and a PID signal, to the controller of the preheater. The temperature sensor can be installed, for example, in the first and second preheaters, the feed oil supply lines before and after the first and second preheaters, and the first and second fractionators.

In one embodiment of the invention, the first temperature control unit includes a first temperature detector that detects a temperature in the second fractionator, and according to the temperature of the first temperature detector, The heating temperature of the raw oil is controlled within a predetermined range by the first preheater,
The second temperature control unit includes a second temperature detector that detects a temperature in the first fractionator, and the second preheater controls the feed oil according to the temperature of the second temperature detector. The heating temperature is controlled within a predetermined range.

  According to this configuration, for example, temperature control can be suitably performed so that the temperature of the first fractionator and the second fractionator falls within a predetermined range during steady operation. When the temperature of each fractionator exceeds a predetermined range temperature, it can function as a cooling medium without heating the raw material oil (or lowering the heating temperature) in each preheater, or each fractionator The raw oil can be heated by each preheater so as to function as a heating medium so that the temperature of the vessel does not fall below a predetermined range temperature.

Moreover, in one embodiment of the above invention, a combustor for combusting the remaining fractional distillation residue obtained by recovering the light oil fraction from the light oil in the second fractionator;
A combustion exhaust gas supply line for supplying a part of the combustion exhaust gas discharged by burning the remainder of fractionation in the combustor to the reactor for regeneration of the catalyst;
A temperature detector for the reactor for detecting the temperature in the reactor;
A gas supply amount control unit configured to control a combustion exhaust gas supply amount by a feeding unit installed in the combustion exhaust gas supply line according to the temperature detected by the reactor temperature detector;

According to this configuration, combustion exhaust gas (oxygen concentration lower than that of air) obtained by burning the remaining fraction (eg, combustible gas, naphtha, kerosene, etc.) separated by the second fractionator with the combustor. Part of the gas) can be used as regeneration air for the catalyst. Since combustion exhaust gas components other than oxygen (O ₂ ) act as a cooling medium, the amount of regeneration air can be increased, and as a result, regeneration of the catalyst can be performed quickly. Increasing the amount of regenerated air increases the flow velocity, promotes gas diffusion into the catalyst layer, and makes it possible to regenerate the entire catalyst evenly. Further, since the temperature rise of the catalyst due to coke combustion is suppressed, temperature control is easy and stable temperature control is possible. Combustion exhaust gas is used, and it is not necessary to dilute the air and use it as regeneration air. In addition, while detecting the combustion temperature of the catalyst with the reactor temperature detector, the combustion exhaust gas can be supplied by the gas supply control unit so that the temperature becomes lower than the heat resistant temperature of the catalyst.

  An example of the feeding means is a fan. The gas supply amount control unit has, for example, a temperature sensor that detects the combustion temperature of the catalyst, and adjusts the rotation speed of the fan according to the detection result to control the supply amount of the combustion gas, or to adjust the flow rate adjustment valve. Control.

In one embodiment of the invention, the reactor includes a first reactor and a second reactor,
The reactor temperature detector includes a third temperature detector that detects the temperature in the first reactor, and a fourth temperature detector that detects the temperature in the second reactor,
In the raw material oil supply line, a raw material oil supply switching unit that switches the supply of the raw material oil to the first reactor or the second reactor;
A first cracked oil gas line from the first reactor to the first fractionator; a second cracked oil gas line from the second reactor to the first fractionator;
A combustion exhaust gas supply switching unit for switching the supply of the combustion exhaust gas to the first reactor or the second reactor in the combustion exhaust gas line;
In either one of the first reactor and the second reactor, the feed oil supply switching unit and the combustion exhaust gas are used so that the feed oil is decomposed by the catalyst and the catalyst is regenerated on the other side. A control unit for controlling the supply switching unit,
The gas supply amount control unit controls the combustion exhaust gas supply amount by the feeding means installed in the combustion exhaust gas supply line according to the temperature detected by the third temperature detector or the fourth temperature detector.

  According to this configuration, since the catalytic cracking of the raw material oil by the catalyst and the regeneration of the catalyst can be performed simultaneously, continuous production of diesel fuel becomes possible.

In addition, another diesel fuel production method of the present invention includes:
A catalytic cracking step in which the feedstock oil is brought into contact with the catalyst and converted into a cracked oil composed of hydrocarbons;
A first fractionation step for separating light oil from the cracked oil obtained in the catalytic cracking step;
A second fractionation step of recovering a light oil fraction from the light oil obtained in the first fractionation step;
A cooling step of cooling the gas oil fraction recovered in the second fractionation step to produce product oil;
Supply of the raw material oil that can be supplied to the catalytic cracking step after using the raw material oil supplied to the catalytic cracking step as a heating medium in the order of the cooling step, the second fractional distillation step, and the first fractional distillation step. A process,
The raw oil supply step includes
A first preheating step of heating the feedstock supplied to the second fractionation step to a predetermined range temperature;
And a second preheating step of heating the feedstock supplied to the first fractionation step to a predetermined range temperature.

  According to this configuration, the raw material oil is used as the heat medium, and the heat is used in the order of the cooling step, the second fractionation step, and the first fractionation step, so that the raw material can be used depending on the amount of cooling heat in the fractionation step and the cooling step. The amount of preheated oil can be covered and the amount of heat consumed can be reduced. Further, by preheating the raw material oil, the temperature range in each fractionator is reduced, and stable temperature control is possible from the start of operation to steady operation.

Moreover, in one embodiment of the above invention, a combustion step of burning the remaining fractional distillation fraction obtained by collecting the diesel oil fraction from the light oil in the second fractionation step;
A catalyst regeneration step of supplying a part of the combustion exhaust gas discharged by burning the fractional distillation residue in the combustion step to regenerate the catalyst used in the catalytic cracking step,
The catalyst regeneration step includes
A gas supply amount control step for controlling a supply amount of the combustion exhaust gas;

According to this configuration, a part of the combustion exhaust gas (gas having a lower oxygen concentration than air) discharged by burning the remaining fraction can be used as regeneration air for the catalyst. Since combustion exhaust gas components other than oxygen (O ₂ ) act as a cooling medium, the amount of regeneration air can be increased, and as a result, regeneration of the catalyst can be performed quickly. Increasing the amount of regenerated air increases the flow velocity, promotes gas diffusion into the catalyst layer, and makes it possible to regenerate the entire catalyst evenly. Further, since the temperature rise of the catalyst due to coke combustion is suppressed, temperature control is easy and stable temperature control is possible. Further, it is preferable to detect the temperature of the catalyst and control the gas supply amount according to the detected temperature so that the catalyst does not exceed its heat resistance temperature.

Moreover, in one Embodiment of the said invention, the said catalytic cracking process has a 1st reaction process and a 2nd reaction process for carrying out catalytic cracking of the said raw material oil by the said catalyst alternately,
While either one of the first reaction step and the second reaction step is catalytically cracking the raw material oil with the catalyst, the catalyst regeneration step is performed on the catalyst used in the other step. .

  According to this configuration, since the contact reaction step of the raw material oil by the catalyst and the catalyst regeneration step of regenerating the catalyst can be performed simultaneously in parallel, it is possible to continuously manufacture diesel fuel.

It is a figure for demonstrating an example of the diesel fuel manufacturing system of Embodiment 1. FIG. It is a figure for demonstrating an example of the diesel fuel manufacturing system of Embodiment 2. FIG. It is a figure for demonstrating an example of the diesel fuel manufacturing system of Embodiment 3. FIG.

(Embodiment 1)
An example of a diesel fuel production system according to Embodiment 1 will be described with reference to FIG. The diesel fuel production system is obtained with a raw material tank 1 for storing raw material oil, a reactor 5 having a catalyst for converting raw material oil supplied from the raw material tank 1 into cracked oil made of hydrocarbons, and the reactor 5. A first fractionator 6 for separating light oil from the cracked oil obtained, a second fractionator 7 for recovering a light oil fraction from the light oil obtained by the first fractionator 6, and a second fractionator 7 includes a cooler 8 that cools the light oil fraction collected in 7 to produce product oil, and a product oil tank 9 that stores product oil (diesel fuel) that is cooled by the cooler 8 to become liquid. The raw material oil supplied from the raw material tank 1 to the reactor 5 can be supplied to the reactor 5 after being used as a heat medium in the order of the cooler 8, the second fractionator 7 and the first fractionator 6. The raw material oil supply line L is provided. In this raw material oil supply line L, the front stage supply line L1 passes through the raw material oil supply pump 2 and the cooler 8 for supplying the raw material oil downstream, and the middle stage supply line L2 includes the cooler 8 and the second supply line L2. Passing through the first preheater 3 and the second fractionator 7 installed between the fractionator 7 and heating the feedstock, the latter supply line L3 is connected to the second fractionator 7 and the first fractionator. It passes between the second preheater 4 and the first fractionator 6 that are installed between the vessel 6 and heats the feedstock.

  At the time of start-up, since the temperature of the piping of the raw material oil supply line L and each device is normal temperature, the first and second preheaters 3 and 4 heat the raw material oil so as to be in a predetermined temperature range. During steady operation, the first and second preheaters 3 and 4 are operated so that the temperatures in the first and second fractionators 6 and 7 and the feed temperature of the raw material reactor 5 are maintained at a predetermined temperature. Stop and control the temperature of the feedstock.

  For example, the raw material oil in the raw material tank 1 is at room temperature (ambient environmental temperature), and is sent as the heat medium of the cooler 8 at room temperature, where the light oil fraction obtained in the second fractionator 7 (for example, 150 The heat is exchanged with (~ 200 ° C.) and sent to the first preheater 3. The temperature of the raw material oil which passes the cooler 8 and is sent to the 1st preheater 3 is 50-80 degreeC, for example. Next, the raw material oil is heated (or not heated) by the first preheater 3 and sent as a heat medium for the second fractionator 7, where the gas components (light light) in the second fractionator 7 are sent. Oil gas) is exchanged with heat and sent to the second preheater 4. The temperature of the raw material oil which passes the 2nd fractionator 7 and is sent to the 2nd preheater 4 is 150-240 degreeC, for example. Next, the feed oil is heated (or not heated) by the second preheater 4 and sent as a heat medium of the first fractionator 6, where the gas components (decomposition) in the first fractionator 6 are sent. Oil gas) is exchanged with heat and sent to the reactor 5. The temperature of the feedstock that passes through the first fractionator 6 and is sent to the reactor 5 is, for example, 300 to 350 ° C. Next, the temperature in the reactor 5 is set to, for example, 400 to 450 ° C., the raw material oil is brought into contact with the solid catalyst 51 to perform a catalytic reaction, and the cracked oil gas thus obtained passes through the cracked oil gas line 10 for the first fractional distillation. Sent to the vessel 6. The temperature of the cracked oil gas sent to the first fractionator 6 is, for example, 380 to 420 ° C. Next, the cracked oil gas is fractionated in the first fractionator 6 to obtain a light oil gas, and this light oil gas is sent to the second fractionator 7 through the light oil gas line 11. The temperature of the light oil gas sent to the 2nd fractionator 7 is 250-300 degreeC, for example. Next, the light oil gas is fractionated in the second fractionator 7 to obtain a light oil distillate gas, which is sent to the cooler 8 through the light oil distillate gas line 12. The temperature of the gas oil distillate gas sent to the cooler 8 is, for example, 150 to 200 ° C. Next, the gas oil distillate gas is cooled in the cooler 8 to obtain liquid product oil (diesel fuel), which is sent to the product oil tank 9 through the product oil line 121 and collected.

  The heating source of the first and second preheaters 3 and 4 is not particularly limited, and can be realized by, for example, an electric heater, a burner, or a heat exchanger using hot air, steam, waste gas waste heat, or the like.

  The cooler 8 is not particularly limited, and is a device for cooling a gas into a liquid.

  The reactor 5 is filled with a solid catalyst 51. In FIG. 1, the solid catalyst 51 is fixed to the lower part of the reactor 5, and the raw material oil is supplied from the upper part of the solid catalyst 51. The feedstock oil undergoes catalytic cracking reaction with the solid catalyst 51 to obtain a hydrocarbon mixture (cracked oil) mainly composed of olefin / paraffin having 9 to 20 carbon atoms. Moreover, it is preferable that the reactor 5 is provided with a heating means for setting the internal temperature and the temperature of the solid catalyst 51 to a catalytic reaction temperature range (for example, 400 to 450 ° C.). The heating means is not particularly limited, and examples thereof include an electric heater, a burner, or a heat exchanger using hot air, steam, waste gas waste heat, and the like. Moreover, it is preferable to use inert gas, such as nitrogen gas, water vapor | steam, offgas, etc. as carrier gas for conveying the cracked oil generate | occur | produced in the reactor 5 to a back | latter stage. This carrier gas may be supplied continuously during operation, or may be supplied according to the operation status.

  A temperature sensor (for example, a thermocouple, a resistance temperature detector, etc.) is attached to the first fractionator 6, and a signal detected by this temperature sensor is sent to a TIC (temperature indicating controller) 30, and from the TIC 30 An ON / OFF signal is output to the heating source control unit of the second preheater 4 to heat or cool the temperature of the raw material oil to an appropriate temperature range so that the heat exchange in the first fractionator 6 is appropriately performed. .

  The second fractionator 7 is also provided with a temperature sensor (for example, a thermocouple, a resistance temperature detector, etc.), and a signal detected by this temperature sensor is sent to a TIC (temperature indicating controller) 20, An ON / OFF signal is output from the TIC 20 to the heating source control unit of the first preheater 3, and heat exchange in the second fractionator 7 is appropriately performed by heating or cooling to bring the temperature of the raw material oil within an appropriate temperature range. Let it be done.

  In the first fractionator 6, the cracked oil gas is separated into light oil gas and residual liquid, and this residual liquid can be returned to the reactor 5 through the residual liquid line 101 and used again as a reaction raw material. In the second fractionator 7, the light oil gas is separated into a light oil fraction and a fractional distillation residue (for example, combustible gas, naphtha, kerosene, etc.). 13 is discharged from the second fractionator 7 and burned by a combustor such as a burner, for example.

  Moreover, you may have further the removal means which removes the foreign material in raw material oil. It is preferable to remove the foreign matters in the raw material oil, since the efficiency of the catalytic cracking reaction due to the foreign matters adhering to the solid catalyst 51 can be prevented. As the removing means, a filter is preferable. As filtration performance, it can comprise with a filter of about 0.5 micrometer-5 micrometers, and about 1 micrometer is preferred. Examples of the foreign material include heaven waste in tempura oil. The raw material oil may be filtered through a filter in advance and then stored in the raw material oil tank 1, or the raw material oil supply line L may be provided with a filter.

(Embodiment 2)
The manufacturing system of Embodiment 2 is demonstrated with reference to FIG. The same reference numerals as those in FIG. 1 of the first embodiment have the same functional configuration, and thus the description thereof will be omitted, and features different from the first embodiment will be described in detail. In the second embodiment, the catalytic cracking reaction of the raw material oil is stopped, and the fixed catalyst 51 is regenerated. By using a part of the combustion exhaust gas for regeneration of the solid catalyst, local excessive combustion exceeding the heat resistance temperature of the solid catalyst can be suppressed, and the solid catalyst 51 can be effectively regenerated as a whole.

  The combustor 14 burns the remaining fraction fraction (naphtha, combustible gas, etc.) obtained by collecting the light oil fraction from the light oil in the second fractionator 7. This fraction residue is discharged from the second fractionator 7 through the fraction residue line 13 and sent to the combustor 14 where it is burned. The combustor 14 is a burner, for example.

  The combustor 14 burns the remainder of the fractionation and exhausts the combustion exhaust gas through the combustion exhaust gas line 15. A part of the combustion exhaust gas is sent to the reactor 5 through the combustion exhaust gas supply line 151 branched from the combustion exhaust gas line 15 and used for regeneration of the fixed catalyst 51.

  At the time of regeneration, the heating source (heater or the like) of the reactor 5 is turned off, combustion exhaust gas is sent, and combustion is performed to regenerate the solid catalyst. A fan 16 is installed in the combustion exhaust gas supply line 151, and a part of the combustion exhaust gas is sent to the reactor 5 by operating the fan 16. A temperature sensor (corresponding to a temperature detector for the reactor) is attached to the reactor 5, a signal detected by this temperature sensor is sent to the TIC 40, and a signal is output from the TIC 40 to the control unit of the fan 16. , And the amount of combustion exhaust gas fed by the fan 16 (combustion exhaust gas supply amount) is controlled (corresponding to a gas supply amount control unit). Further, the gas supply amount control unit may be configured to control the flow control valve together with or separately from the control of the fan 16. During the regeneration process, the temperature sensor controls the temperature of the solid catalyst 51 so that the temperature of the solid catalyst 51 is equal to or lower than the heat-resistant temperature (for example, 700 ° C. or lower).

  By burning the solid catalyst 51 of the reactor 5, exhaust gas (regenerated exhaust gas) is generated. The exhaust gas is preferably sent to the combustor 14 through the exhaust gas line 18 where it is burned.

  In addition, it is desirable that combustion exhaust gas is combustion-controlled in the combustor 14 so that the oxygen concentration is in the range of 1 to 10%, preferably 5 to 10%. In such a case, for example, an oxygen concentration sensor (not shown) is attached to the combustion exhaust gas line 15, and the control unit of the combustor 14 controls the combustion state in accordance with a signal from the oxygen concentration sensor.

  The temperature of the combustion exhaust gas is supplied to the reactor 5 in the range of 200 to 500 ° C., preferably 200 to 300 ° C. so that the combustion of coke adhering to the catalyst can be maintained and the catalyst is not overheated. It is desirable to do.

(Embodiment 3)
The manufacturing system of Embodiment 3 is demonstrated with reference to FIG. The same reference numerals as those in FIG. 2 according to the second embodiment have the same functional configuration, and thus description thereof will be omitted, and features different from the second embodiment will be described in detail.

  In FIG. 3, two reactors 5a and 5b are arranged in parallel. A catalytic cracking reaction by the solid catalyst 51a is performed in the reactor 5a to generate cracked oil, and the combustible deposit (coke) adhering to the solid catalyst 51b is burned in the other reactor 5b to regenerate the solid catalyst 51b. I am doing.

  Now, when the catalytic reaction efficiency of cracked oil decreases in the reactor 5a or when it operates for a certain period of time, it is desired to regenerate the fixed catalyst 51a of the reactor 5a and perform catalytic cracking of the raw material oil in the other reactor 5b. . In such a case, the raw material oil supply switching unit 50 attached to the raw material oil supply line L switches the supply of the raw material oil from the reactor 5a to the reactor 5b. The raw material oil supply switching unit 50 includes, for example, a flow path switching valve. The cracked oil gas is switched from the first cracked oil gas line 10a leading from the reactor 5a to the first fractionator 6, and is sent from the reactor 5b to the first fractionator 6 through the second cracked oil gas line 10b. . Further, the combustion exhaust gas supply switching unit 50 attached to the combustion exhaust gas line 151 switches the supply of combustion exhaust gas from the reactor 5b to the reactor 5a. The raw material oil supply switching unit 50 and the combustion exhaust gas supply switching unit 60 are controlled by a command from a control unit (not shown). For example, the control unit may be configured to instruct each switching unit 50, 60 by receiving an input instruction from an operator, or may be configured to automatically command each switching unit by a timer.

  Moreover, a temperature sensor is attached to each reactor 5a, 5b, and a signal detected by this temperature sensor is sent to each TIC 40, 41. A signal is output from the TIC 40 or TIC 41 connected to the reactor during catalyst regeneration to the control unit of the fan 16, the rotational speed (flow velocity) of the fan 16 is adjusted, and the amount of combustion exhaust gas fed by the fan 16 (combustion exhaust gas supply amount) ) Is controlled.

  The control unit also compares and judges the input amount of raw material oil and the recovered amount of product oil obtained, and when the decrease in yield falls below the threshold value, the solid catalyst in the reactor is burned and regenerated. It is preferable to control so as to. This control unit can be configured by an information processing device, firmware, a dedicated circuit or the like. In the case of the information processing device, a program describing a control procedure, a memory for storing the program, a CPU as a calculation unit, a main memory, etc. This is realized by the cooperation with hardware resources. The threshold value is set in advance, and for example, a 10% reduction value in yield can be used.

(Production method)
The manufacturing method of the diesel fuel of this invention is demonstrated below. This manufacturing method is suitably executed by the manufacturing system of the first to third embodiments. The present production method comprises a catalytic cracking step of bringing a feedstock oil into contact with a catalyst to convert it into a cracked oil comprising a hydrocarbon, a first fractionation step of separating light oil from the cracked oil obtained in the catalytic cracking step, A second fractionation step for recovering the light oil fraction from the light oil obtained in the first fractionation step, and a cooling step for cooling the light oil fraction collected in the second fractionation step to produce product oil (diesel fuel) And a raw material oil supply step for supplying the raw material oil supplied to the catalytic cracking step as a heating medium in the order of the cooling step, the second fractionation step, and the first fractionation step, and then supplying the raw material oil to the catalytic cracking step. Prepare. The raw material oil supply step heats the raw material oil supplied to the second fractionation step to a predetermined range temperature, and heats the raw material oil supplied to the first fractionation step to a predetermined range temperature. A second preheating step.

  In addition, a combustion process for burning the remaining fraction fraction collected from the light oil fraction in the second fractionation process and a part of the combustion exhaust gas discharged by burning the remainder fraction fraction in the combustion process And a catalyst regeneration step for supplying the catalyst used in the catalytic cracking step. The catalyst regeneration step includes a gas supply amount control step for controlling the supply amount of the combustion exhaust gas.

  Further, the catalytic cracking step has a first reaction step and a second reaction step for alternately catalytically cracking the raw material oil with a catalyst, and either one of the first reaction step and the second reaction step is performed. While the feedstock oil is catalytically cracked with the catalyst, the catalyst regeneration step is performed on the catalyst used in the other process.

DESCRIPTION OF SYMBOLS 1 Raw material oil tank 2 Raw material oil pump 3 1st preheater 4 2nd preheater 5 Reactor 6 1st fractionator 7 2nd fractionator 8 Cooler 9 Product oil tank 14 Combustor 16 Fan 51 Solid catalyst L Raw material Oil supply line

Claims (8)

A raw material tank for storing raw material oil;
A reactor having a catalyst for converting the feedstock supplied from the feedstock tank into cracked oil comprising hydrocarbons;
A first fractionator for separating light oil from the cracked oil obtained in the reactor;
A second fractionator for recovering a light oil fraction from the light oil obtained in the first fractionator;
A cooler that cools the light oil fraction recovered in the second fractionator into product oil;
The raw material oil that can be supplied to the reactor after using the raw material oil supplied from the raw material tank to the reactor as a heating medium in the order of the cooler, the second fractionator, and the first fractionator. With oil supply line,
The feedstock supply line is
A feed oil supply pump for supplying the feed oil downstream;
A first preheater installed between the cooler and the second fractionator to heat the feedstock;
A diesel fuel production system comprising: a second preheater that is installed between the second fractionator and the first fractionator and heats the feedstock. A first temperature control unit for controlling the heating temperature of the raw material oil to a predetermined range by the first preheater;
The diesel fuel manufacturing system according to claim 1, further comprising: a second temperature control unit configured to control a heating temperature of the raw material oil within a predetermined range by the second preheater. The first temperature control unit includes a first temperature detector that detects a temperature in the second fractionator, and the first preheater controls the feed oil according to the temperature of the first temperature detector. Control the heating temperature to a predetermined range,
The second temperature control unit includes a second temperature detector that detects a temperature in the first fractionator, and the second preheater controls the feed oil according to the temperature of the second temperature detector. The diesel fuel production system according to claim 2, wherein the heating temperature is controlled within a predetermined range. A combustor for combusting the remaining fractional distillation residue obtained by collecting the gas oil fraction from the light oil in the second fractionator;
A combustion exhaust gas supply line for supplying a part of the combustion exhaust gas discharged by burning the remainder of fractionation in the combustor to the reactor for regeneration of the catalyst;
A temperature detector for the reactor for detecting the temperature in the reactor;
The gas supply amount control part which controls the combustion exhaust gas supply amount by the feeding means installed in the said combustion exhaust gas supply line according to the temperature detected by the said temperature detector for reactors is further provided. The diesel fuel manufacturing system of any one of Claims. The reactor has a first reactor and a second reactor,
The reactor temperature detector includes a third temperature detector that detects the temperature in the first reactor, and a fourth temperature detector that detects the temperature in the second reactor,
In the raw material oil supply line, a raw material oil supply switching unit that switches the supply of the raw material oil to the first reactor or the second reactor;
A first cracked oil gas line from the first reactor to the first fractionator; a second cracked oil gas line from the second reactor to the first fractionator;
A combustion exhaust gas supply switching unit for switching the supply of the combustion exhaust gas to the first reactor or the second reactor in the combustion exhaust gas line;
In either one of the first reactor and the second reactor, the feed oil supply switching unit and the combustion exhaust gas are used so that the feed oil is decomposed by the catalyst and the catalyst is regenerated on the other side. A control unit for controlling the supply switching unit,
The said gas supply amount control part controls the combustion exhaust gas supply amount by the sending means installed in the said combustion exhaust gas supply line according to the temperature detected by the said 3rd temperature detector or the 4th temperature detector. 4. The diesel fuel production system according to 4. A catalytic cracking step in which the feedstock oil is brought into contact with the catalyst and converted into a cracked oil composed of hydrocarbons;
A first fractionation step for separating light oil from the cracked oil obtained in the catalytic cracking step;
A second fractionation step of recovering a light oil fraction from the light oil obtained in the first fractionation step;
A cooling step of cooling the gas oil fraction recovered in the second fractionation step to produce product oil;
Supply of the raw material oil that can be supplied to the catalytic cracking step after using the raw material oil supplied to the catalytic cracking step as a heating medium in the order of the cooling step, the second fractional distillation step, and the first fractional distillation step. A process,
The raw oil supply step includes
A first preheating step of heating the feedstock supplied to the second fractionation step to a predetermined range temperature;
And a second preheating step of heating the feedstock supplied to the first fractionation step to a predetermined range temperature. A combustion step of burning the remaining fractional distillation fraction obtained by collecting the diesel oil fraction from the light oil in the second fractionation step;
A catalyst regeneration step of supplying a part of the combustion exhaust gas discharged by burning the fractional distillation residue in the combustion step to regenerate the catalyst used in the catalytic cracking step,
The catalyst regeneration step includes
The diesel fuel manufacturing method according to claim 6, further comprising a gas supply amount control step for controlling a supply amount of the combustion exhaust gas. The catalytic cracking step includes a first reaction step and a second reaction step for alternately catalytically cracking the raw material oil with the catalyst,
While either one of the first reaction step and the second reaction step is catalytically cracking the raw material oil with the catalyst, the catalyst regeneration step is performed on the catalyst used in the other step. The method for producing diesel fuel according to claim 7.

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