JP4796401B2 - Biomass treatment using fluid catalytic cracking - Google Patents

Description

  The present invention relates to a method for treating biomass using fluid catalytic cracking.

  Conventionally, biomass is considered promising as an automobile fuel or petrochemical raw material from the viewpoint of energy security and the reduction of carbon dioxide gas.

  Many attempts have been made to use biomass as fuel oil for automobiles. For example, Patent Documents 1 to 5 below disclose a method in which vegetable oil or animal oil, which is biomass, is mixed with mineral oil and used as a fuel for a diesel engine. However, if the biomass is simply mixed with mineral oil, the stability of the obtained fuel becomes insufficient and management becomes difficult because the biomass contains unsaturated bonds and oxygen. In addition, these components may adversely affect materials used in automobiles.

On the other hand, Patent Document 6 below discloses a method for producing gasoline by bringing a higher fatty acid glycerin ester into contact with a zeolite-containing catalyst.
JP-A-61-57686 Japanese Patent Publication No. 6-510804 Japanese Patent Application Laid-Open No. 07-82576 JP-A-8-41468 JP-A-10-152687 JP 59-62694 A

  However, even the above-described conventional method has room for improvement in terms of the following points that can be put to practical use.

  That is, according to the method described in Patent Document 6, gasoline can be produced at a laboratory level, but biomass can be produced using an industrial level fluid catalytic cracker (hereinafter referred to as “FCC” in some cases). In the case of treatment, the amount of coke produced is increased as compared with a vacuum gas oil generally used as a mineral oil-based FCC raw material (hereinafter sometimes referred to as “VGO”). In FCC, the heat generated by coke combustion in catalyst regeneration is used as the amount of heat necessary for the vaporization and decomposition reaction of the raw material oil, and the operation is performed by balancing these. When coke increases and the amount of heat becomes excessive, it is necessary to remove the excess amount of heat by cooling the catalyst or extracting carbon monoxide from the first stage regeneration in the second stage regeneration of the catalyst. Although there is a difference in the ability to remove the excess heat by each FCC, it is common to operate at the upper limit of the ability. Furthermore, in recent years, carbon dioxide emissions have been limited due to stricter environmental regulations, and the amount of coke has become a constraint in operation in virtually all FCCs. Because of this situation, if coke increases due to the introduction of biomass, the severity of operation will be lowered to lower the coke yield, and at the same time the gasoline yield will be sacrificed, or the appropriate oil amount itself will be lowered. It becomes economically disadvantageous.

  This invention is made | formed in view of the subject which the said prior art has, and aims at providing the processing method of biomass which can process biomass efficiently and stably in a fluid catalytic cracking apparatus. .

Therefore, the present invention is a method for treating biomass by catalytic cracking using a fluid catalytic cracking apparatus having a reaction zone, a separation zone, a stripping zone, and a regeneration zone, and in the reaction zone, feedstock oil containing biomass is treated. , Using a catalyst containing 10 to 50% by mass of ultrastable Y-type zeolite, outlet temperature of reaction zone 480 to 540 ° C., catalyst / oil ratio 4 to 12 wt / wt, reaction pressure 1 to 3 kg / cm ² G, raw material In the first step in which the contact time between the oil and the catalyst is 1 to 3 seconds, and in the regeneration zone, the catalyst used in the first step is subjected to a regeneration zone temperature of 640 to 720 ° C and a regeneration zone pressure of 1 And a second step of processing under conditions of 3 to 3 kg / cm ² G and an oxygen concentration of 0 to 3 mol% in the exhaust gas at the regeneration zone outlet.

  According to the biomass processing method of the present invention, when processing biomass using a fluid catalytic cracking apparatus, the raw material oil containing biomass is processed in the reaction zone using the specific catalyst under the specific conditions, In addition, by treating the catalyst subjected to the treatment in the regeneration zone under the specific condition, an increase in the amount of coke generated due to the treatment of biomass is sufficiently suppressed. Therefore, biomass can be processed efficiently and stably in a fluid catalytic cracking apparatus.

  The biomass used in the present invention preferably contains an oil and fat component having an oxygen content of 0.1 to 13% by mass and a boiling point of 230 ° C. or higher, derived from animal and vegetable oils.

In the catalyst according to the present invention, the SiO ₂ / Al ₂ O ₃ of the ultrastable Y-type zeolite is preferably ₃ to 10.

In the said catalyst, it is preferable that alkaline-earth metal is introduced into the ion exchange sites of the ultrastable Y-type zeolite.

  The catalyst preferably further contains silica alumina as an active matrix.

  Moreover, in the 1st process which concerns on this invention, it is preferable to spray raw material oil in a reaction zone using the steam which is 2-6 mass% of raw material oil.

  Moreover, since the biomass processing method of the present invention uses biomass as a raw material, it is excellent in terms of energy security and carbon dioxide gas reduction. Therefore, according to the present invention, as will be described later, various fuels and petrochemical products using the product can be provided.

  That is, this invention provides the fuel for fuel cells characterized by containing the hydrogen obtained by the biomass processing method of the said invention.

  Moreover, this invention provides the gasoline characterized by including a part or all of the fraction of the boiling point 25-220 degreeC obtained by the processing method of the biomass of the said invention, or its hydride.

  Moreover, this invention provides the diesel fuel characterized by including the one part or all part of the fraction with a boiling point of 170-370 degreeC obtained by the processing method of the biomass of the said invention.

  Moreover, this invention provides the liquefied petroleum gas (LPG) characterized by containing the C3-C4 hydrocarbon obtained by the processing method of the biomass of the said invention.

  Moreover, this invention provides the synthetic resin characterized by containing the propylene obtained by the processing method of the biomass of the said invention as a structural monomer. Such a synthetic resin is preferably characterized in that the amount of carbon dioxide emission under environmental regulations can be counted as zero when discarded by combustion.

  Moreover, this invention provides the gasoline characterized by including the ether obtained by making the isobutylene obtained by the processing method of the biomass of the said invention react with methanol or ethanol.

  The present invention also provides a gasoline characterized by containing a reaction product obtained by reacting butylene obtained by the biomass processing method of the present invention with isobutane using an alkylation device.

  Moreover, this invention provides the gasoline characterized by containing the dimerization product of butylene obtained by the processing method of the biomass of the said invention.

  ADVANTAGE OF THE INVENTION According to this invention, the processing method of biomass which can process biomass efficiently and stably in a fluid catalytic cracking apparatus is provided. In addition, by using the biomass processing method of the present invention, a fuel and a petrochemical raw material that are useful in terms of energy security and carbon dioxide reduction are provided.

  Hereinafter, preferred embodiments of the present invention will be described in detail.

  In the present invention, a raw material oil containing biomass is used.

  As biomass, oil derived from plants or animals can be used. Such fats and oils contain esters of higher fatty acids and glycerin, and more specifically include vegetable oils such as palm oil, rapeseed oil, corn oil, soybean oil, and grape seed oil, and animal oils such as lard. These fats and oils may be used waste oil. It is preferable that the oxygen content of the biomass is 0.1 to 13% by mass. The biomass preferably contains a fraction having a boiling point of 230 ° C. or higher.

  In this invention, although the said biomass may be used independently, the mixed oil of biomass and mineral oil can also be used as raw material oil. Mineral oils include atmospheric residual oil obtained by distilling crude oil, vacuum gas oil obtained by further distillation of atmospheric residue under reduced pressure, vacuum residue, hydrotreated oil, or pyrolysis oil, and Of the mixture. Among these mineral oils, atmospheric residue, reduced residue and hydride thereof are referred to as “residue” in the present invention.

The catalyst used in the present invention contains 10 to 50% by mass, preferably 15 to 40% by mass, of ultrastable Y-type zeolite. Things as ultra stable Y-type zeolite _SiO 2 / _Al 2 _{O 3} is 3 to 10 is preferably used. SiO ₂ / _Al 2 _{O 3} is more preferably 7-9, further preferably 8-9. When SiO ₂ / Al ₂ O ₃ is less than 3, the catalytic activity becomes excessively large, and the amount of gas and LPG generated increases. _Also, the cost of the zeolite increases the SiO 2 / _Al 2 _{O 3} is more than 10 is not preferred in view of economy. As the ultrastable Y-type zeolite, those obtained by introducing an alkaline earth metal at the ion exchange site can be preferably used.

As a preferred embodiment of the catalyst used in the present invention, ultra-stable Y-type zeolite is formed into particles with a binder together with a filler which is a secondary active ingredient and can decompose large molecules of heavy oil, and a filler such as kaolin. The thing which was done is mentioned. Silica alumina is preferably used as the matrix component used in the catalyst of the present invention. The catalyst has an average particle size of 50 to 90 μm, a bulk density of 0.6 to 0.9 g / cm ³ , a surface area of 50 to 350 m ² / g, and a pore volume of 0.05 to 0.5 ml / g. Are preferred respectively.

  In addition to the ultrastable Y-type zeolite, the catalyst may further contain a crystalline aluminum silicate zeolite having a smaller pore size than that of the Y-type zeolite, silicoaluminophosphate (SAPO), and the like. Examples of such zeolite or SAPO include ZSM-5, β, ω, SAPO-5, SAPO-11, and SAPO-34. These zeolite or SAPO may be contained in the same catalyst particles as the catalyst particles containing the ultrastable Y-type zeolite, or may be contained as separate catalyst particles.

  Further, the fluid catalytic cracking device (FCC) used in the present invention is not particularly limited as long as it is a device having a reaction zone, a separation zone, a stripping zone and a regeneration zone. The FCC may be an existing device conventionally used for the treatment of mineral oil, or may be a device newly constructed for biomass processing.

  Moreover, the residual oil ratio in the present invention is not particularly limited, but the biomass treatment method of the present invention is preferably applied to a fluid catalytic cracking apparatus operated at a residual oil ratio of 10% by mass or more. A more preferable residual oil ratio is 30% by mass or more. In addition, the “residual oil ratio” in the present invention means a value (unit: mass%) in which the ratio of the residual oil in the feedstock oil of the fluid catalytic cracking apparatus is expressed by mass ratio.

In the FCC reaction zone, the reaction zone outlet temperature is 480 to 540 ° C., the catalyst / oil ratio is 4 to 12 wt / wt, the reaction pressure is 1 to 3 kg / cm ² G, and the contact time between the feedstock and the catalyst is 1 to 3 seconds. Fluid catalytic cracking is carried out as described below. Here, “fluid catalytic cracking” as used in the present invention means that the above-mentioned heavy feedstock such as biomass and mineral oil and the catalyst maintained in a fluidized state are continuously contacted under the operating conditions described later. This means that heavy feedstock oil is decomposed into light hydrocarbons mainly composed of gasoline and light olefins. In this fluid catalytic cracking, so-called riser cracking, in which both catalyst particles and raw material oil rise in the pipe, is often used.

  The “reaction zone outlet temperature” in the present invention is the outlet temperature of the fluidized bed reactor, and is the temperature before the decomposition product is quenched or decomposed with the catalyst. As described above, the outlet temperature of the reaction zone in the present invention is 480 to 540 ° C, preferably 490 to 520 ° C, more preferably 500 to 510 ° C. If the outlet temperature of the reaction zone is less than 480 ° C., the target products such as gasoline and light olefins cannot be obtained in high yield, and if it exceeds 540 ° C., thermal decomposition becomes remarkable and the amount of dry gas generated It will increase.

  Further, the “catalyst / oil ratio” referred to in the present invention is a ratio between the catalyst circulation rate (ton / h) and the feed oil supply speed (ton / h). As described above, the catalyst / oil ratio in the present invention is 4 to 12 wt / wt, preferably 5 to 10 wt / wt, and more preferably 6 to 8 wt / wt. When the catalyst / oil ratio is less than 4 wt / wt, a sufficient decomposition rate cannot be obtained. Further, when the catalyst / oil ratio exceeds 12, the amount of catalyst circulation becomes large, and the catalyst residence time necessary for catalyst regeneration cannot be ensured in the regeneration zone, or the regeneration temperature is lowered, so that the regeneration of the catalyst becomes insufficient. .

The “reaction pressure” in the present invention means the total pressure of the fluidized bed reactor. The reaction pressure in the present invention are as described above 1 to 3 kg / cm ² G, preferably 1.2~2kg / cm ² G. When the reaction pressure is less than 1 kg / cm ² G, the difference from the atmospheric pressure becomes excessively small, and it becomes difficult to adjust the pressure with the control valve. In addition, when the reaction pressure is less than 1 kg / cm ² G, the pressure in the regeneration zone decreases accordingly, and the container must be enlarged to ensure the residence time of the gas necessary for regeneration. It is not preferable. On the other hand, when the reaction pressure exceeds 3 kg / cm ² G, the ratio of a bimolecular reaction such as a hydrogen transfer reaction to a decomposition reaction that is a unimolecular reaction increases. The “hydrogen transfer reaction” referred to here is a reaction in which olefins receive hydrogen from naphthene or the like and are converted to paraffin, which causes a decrease in the target light olefin, a decrease in gasoline octane number, and the like. It is a reaction.

  Further, the “contact time between the feedstock and the catalyst” as used in the present invention means that the reaction product and the catalyst are separated at the outlet of the reactor after the feedstock and the catalyst are brought into contact at the inlet of the fluidized bed reactor. It means time to complete. As described above, the contact time between the raw material oil and the catalyst in the present invention is 1 to 3 seconds, preferably 1 to 2 seconds.

  In the present invention, when introducing the raw material oil into the reaction zone, it is preferably sprayed with steam, and the amount of steam at this time is preferably 2 to 6% by mass with respect to the raw material oil. When the amount of steam is less than 2% by mass of the raw material oil, the particle size of the droplets at the time of spraying is not sufficiently small, the droplets and the catalyst are not sufficiently contacted, and the reaction efficiency tends to decrease. On the other hand, if the amount of steam exceeds 6% by mass of the raw material oil, the amount of water recovered in the product recovery zone, which will be described later, increases, which is economically undesirable.

  The mixture of the product, unreacted product and catalyst that have undergone catalytic cracking in the reaction zone is sent to the separation zone, where the catalyst is separated from the mixture. As the separation zone, a solid-liquid separation device using a centrifugal force such as a cyclone is preferably used.

  The catalyst separated in the separation zone is sent to the stripping zone, and most of hydrocarbons such as products and unreacted substances are removed from the catalyst particles in the stripping zone. On the other hand, part of the raw material becomes heavier carbonaceous matter (coke) during the reaction and can be deposited on the catalyst, but the catalyst with coke and partly heavy hydrocarbons adhered is regenerated from the stripping zone. Sent to the band (regeneration tower).

In the regeneration zone, the catalyst is treated under the conditions of a regeneration zone temperature of 640 to 720 ° C., a regeneration zone pressure of 1 to 3 kg / cm ² G, and an oxygen concentration of 0 to 3 mol% in the exhaust gas at the regeneration zone outlet. Oxidation of the catalyst to which etc. adhered is performed.

  As described above, the regeneration zone temperature in the present invention is 640 to 720 ° C, preferably 650 to 700 ° C, more preferably 670 to 690 ° C. When the regeneration zone temperature is less than 640 ° C., the combustion of coke becomes insufficient. On the other hand, when the regeneration zone temperature exceeds 720 ° C., deterioration of the catalyst is promoted, and it is necessary to use a more expensive member for withstanding the regeneration zone temperature as a material for the regeneration zone, which is not economically preferable.

The regeneration zone pressure in the present invention is 1 to 3 kg / cm ² G as described above. When the regeneration zone pressure is less than 1 kg / cm ² G, the residence time of the gas necessary for regeneration is ensured, so that the container in the regeneration zone becomes large, which is not economically preferable. When the regeneration zone pressure exceeds 3 kg / cm ² G, the pressure in the reaction zone increases accordingly, and an economically undesirable reaction such as a hydrogen transfer reaction occurs in the reaction zone, which is disadvantageous.

  In the present invention, the oxygen concentration in the exhaust gas at the outlet of the regeneration zone is 0 to 3 mol%. If the oxygen concentration exceeds 3 mol%, excess air is sent to the regeneration zone using excess power, which is not economically preferable.

  The catalyst subjected to the above oxidation treatment is a regenerated catalyst, and coke and heavy hydrocarbons deposited on the catalyst are reduced by combustion. This regenerated catalyst is continuously circulated through the reaction zone. In some cases, the decomposition products are quenched immediately before or after the separation zone in order to suppress unnecessary thermal decomposition or excessive decomposition. The catalyst is heated by the amount of heat generated by the combustion of the carbonaceous material in the regeneration zone, and the heat is brought into the reaction zone together with the catalyst. The heating and vaporization of the raw material oil is performed by this heat quantity. In addition, since the decomposition reaction is an endothermic reaction, the above-described amount of heat is also used as the heat of decomposition reaction. Thus, balancing the heat generation in the regeneration zone and the heat absorption in the reaction zone is an essential condition for FCC operation.

  As a countermeasure when the heat becomes excessive, there is a method of cooling the catalyst. This method is a method in which a part of the catalyst in the regeneration zone is extracted and heat is used for generating steam to take away the heat of the catalyst.

As another countermeasure against excess heat, there is a method in which the regeneration zone is made up of two stages and the first regeneration zone is operated in an oxygen-deficient atmosphere. In this case, the combustion of coke becomes incomplete combustion, and carbon monoxide is discharged as exhaust gas. The difference between the heat of reaction when carbon is oxidized to carbon monoxide and the heat of reaction when carbon is oxidized to carbon dioxide can be discharged out of the system as surplus heat. The reaction heat (combustion heat) related to the combustion of coke is as follows.
H ₂ + 1 / 2O ₂ → H ₂ O 12.1 × 10 ⁴ kJ / kg (28900 kcal / kg)
C + 1 / 2O ₂ → CO 0.9 × 10 ⁴ kJ / kg (2200 kcal / kg)
C + O ₂ → CO ₂ 3.3 × 10 ⁴ kJ / kg (7820 kcal / kg)

  In addition, the carbon monoxide discharged | emitted out of the system can be further oxidized to a carbon dioxide, and the energy can also be collect | recovered as electric power or steam.

  Usually, the upper limit of the amount of coke produced by catalytic cracking is almost determined for each FCC. For example, the permissible value of the coke amount is determined by the amount of heat that can be discharged out of the system by the above-described countermeasure for excess heat. In addition, an upper limit value of the amount of carbon dioxide generated depending on the location of the FCC may be determined, and the allowable value of the coke amount is limited by the numerical value. Normally, the FCC is operated with as much oil flow as possible and as high a decomposition rate as possible, and as a result, operation is performed with the upper limit of the coke amount.

  However, when the conventional biomass-derived oxygen-containing raw material is treated with FCC, the amount of coke produced is lower than that of vacuum gas oil (hereinafter sometimes referred to as “VGO”), which is generally used as a mineral oil-based FCC raw material. Will increase. On the other hand, in the present invention, the raw material oil containing biomass and mineral oil is treated in the reaction zone using the specific catalyst under the specific conditions, and the catalyst used for the treatment is specified in the regeneration zone. By processing under the conditions, an increase in the amount of coke produced can be sufficiently suppressed, so that operation at the upper limit value of coke can be maintained.

  In the present invention, the amount of coke produced per feed oil (mass%) is referred to as “coke yield”. The coke yield in the present invention is preferably 2 to 12 mass%, more preferably 5 to 10 mass%. More preferably, it is 6-8 mass%. When the coke yield is less than 2% by mass, the heat necessary for the reaction tends to be insufficient. On the other hand, if the coke yield exceeds 12% by mass, the amount of heat generated in the regeneration zone becomes excessively large, which is not preferable because it is subject to operational restrictions such as a decrease in decomposition rate and a decrease in oil flow rate.

  In addition, the FCC in the present invention preferably further includes a product recovery zone. An example of such a product recovery zone is a product recovery facility that separates and recovers the product by its boiling point. The product recovery equipment includes a plurality of distillation towers, absorption towers, compressors, strippers, heat exchangers, and the like. The product obtained in the reaction zone is sent to the first distillation column through the separation zone. Here, the heat of the product is removed by a heat exchanger, and light oil and a fraction heavier than light oil are extracted from the tower bottom, and gasoline and a lighter fraction than gasoline are extracted from the tower top. It is also possible to extract light oil from the middle stage of the distillation tower and extract only heavy oil from the bottom of the tower.

  Light components obtained from the first distillation column are sent to a compressor and compressed, and then separated and recovered into gasoline, C4 fraction, C3 fraction, and dry gas via a plurality of absorption towers and distillation towers. The C4 fraction here refers to butane and butylene, which are hydrocarbons having 4 carbon atoms. The C3 fraction refers to propane and propylene which are hydrocarbons having 3 carbon atoms. The dry gas refers to a gas such as methane, ethylene which is a hydrocarbon having 2 or less carbon atoms, and hydrogen having a molecular weight smaller than that. Depending on the capability of the distillation tower, a portion of the C4 fraction may be mixed with gasoline, or a portion of the C4 fraction may be mixed with the C3 fraction.

  Since the temperature is below the dew point of water at and near the top of the first distillation tower, water derived from esters (oils and fats) contained in biomass is aggregated and contained in water in the conventional biomass processing method. Corrosion of the equipment due to the acid is a problem. On the other hand, according to the biomass processing method of the present invention, the generation of biomass-derived water and acid is sufficiently suppressed.

  As described above, according to the biomass processing method of the present invention, biomass can be efficiently and stably processed in a fluid catalytic cracking apparatus.

  In addition, since the biomass processing method of the present invention uses biomass as a raw material, it is excellent in terms of energy security and carbon dioxide gas reduction. Therefore, when manufacturing base materials for various fuels and raw materials for petrochemical products, Very useful to.

  For example, hydrogen obtained by the biomass processing method of the present invention can be used as a fuel for a fuel cell.

Moreover, the fraction of boiling point 25-220 degreeC obtained by the processing method of the biomass of the said invention can be used as a gasoline base material. Here, a part of the fraction having a boiling point of 25 to 220 ° C. may be used as a gasoline base material, or may be used as a gasoline base material. Alternatively, a fraction having a boiling point of 25 to 220 ° C. can be hydrotreated, and the resulting hydride can be used as a gasoline base material.

  The fraction having a boiling point of 170 to 370 ° C. obtained by the biomass processing method of the present invention can be used as a diesel fuel base material. Here, part of the fraction having a boiling point of 170 to 370 ° C. may be used as a diesel fuel base material, or all may be used as diesel fuel equipment.

  Further, the hydrocarbon having 3 or 4 carbon atoms obtained by the biomass processing method of the present invention can be used as a liquefied petroleum gas base material.

  Moreover, the propylene obtained by the biomass processing method of the present invention can be used as a constituent monomer of a synthetic resin. Since such a synthetic resin is made from biomass, it has the advantage that the amount of carbon dioxide emissions in environmental regulations can be counted as zero when burned and discarded.

  Moreover, the ether obtained by making the isobutylene obtained by the processing method of the biomass of the said invention react with methanol or ethanol can be used as a gasoline base material.

  In addition, a reaction product obtained by reacting butylene obtained by the biomass processing method of the present invention with isobutane using an alkylation apparatus can be used as a gasoline base material.

  The dimerized butylene obtained by the biomass processing method of the present invention can be used as a gasoline base material.

  EXAMPLES Hereinafter, although this invention is demonstrated more concretely based on an Example and a comparative example, this invention is not limited to a following example at all.

[Example 1]
In Example 1, soybean oil was used as biomass. The fatty acid composition of the soybean oil was 10-12 mass% palmitic acid, 2-5 mass% stearic acid, 20-25 mass% oleic acid, 50-57 mass% linoleic acid, and 5-9 mass% linolenic acid. . The soybean oil had an average molecular weight of 880 and an oxygen content of 11% by mass.

  Next, a catalyst was prepared as follows.

First, a diluted solution of JIS No. 3 water glass (SiO ₂ concentration 11.6% by mass) 21550 was dropped into 3370 g of 40% by mass sulfuric acid to obtain a silica sol having a pH of 3.0. 3500 g of ultrastable Y-type zeolite and 4000 g of kaolin were added to the total amount of the silica sol, kneaded, and spray dried with hot air at 250 ° C. The obtained spray-dried product was washed with 50 liters and 50 liters of 0.2 mass% ammonium sulfate, dried in an oven at 110 ° C., and calcined at 600 ° C. to obtain catalyst A. Table 2 shows the physical properties of the obtained catalyst A and the zeolite contained therein.

  Next, catalyst A was pseudo-equilibrated by steaming. “Pseudo-equilibrium” means a method of bringing steam and the catalyst into contact with each other at a high temperature for a predetermined time to reproduce the deterioration state of the equilibrium catalyst in the fluid catalytic cracking apparatus. The catalyst was steamed with 100% steam. The “equilibrium catalyst” is a catalyst that is stored in a fluid catalytic cracking apparatus and has repeatedly reacted and regenerated for a certain period of time, and means one having a lower activity than an unused fresh catalyst. In the fluid catalytic cracking device, a part of the catalyst stored inside is taken out of the system, and a fresh catalyst is put in the device instead of the extracted catalyst, so that the equilibrium catalyst in the device is kept constant. Kept.

Next, the biomass as the raw material oil was treated with catalyst A which was pseudo-equilibrium using an adiabatic riser type FCC pilot device. The scale of the FCC pilot device was an inventory of 2 kg and a feed amount of 1 kg / h. The treatment conditions in the reaction zone were as follows: the outlet temperature of the reaction zone was 500 ° C., the catalyst / oil ratio was 6 wt / wt, the reaction pressure was 1 kg / cm ² G, and the contact time between the raw material oil and the catalyst was 2 seconds. The regeneration conditions of the catalyst in the regeneration zone were a regeneration zone temperature (regeneration tower temperature) of 720 ° C., a regeneration zone pressure of 1 kg / cm ² G, and an oxygen concentration in the exhaust gas at the regeneration zone outlet of 2 mol%. The yield of the obtained product is shown in Table 3. The yields in the table are all expressed by the weight ratio of the product to the total amount of the raw material oil.

[Comparative Example 1]
In Comparative Example 1, first, the same soybean oil and catalyst as in Example 1 were prepared.

Next, in the same apparatus as in Example 1, the feed rate was changed to 0.6 kg / h, and the treatment conditions in the reaction zone were as follows: the outlet temperature of the reaction zone was 500 ° C., the catalyst / oil ratio was 6 wt / wt, and the reaction pressure was 1 kg. / Cm ² G, the contact time of the feedstock and the catalyst is 3.3 seconds, and the regeneration conditions of the catalyst in the regeneration zone are the regeneration zone temperature (regeneration tower temperature) 720 ° C., the regeneration zone pressure 1 kg / cm ² G, the regeneration zone The treatment was performed with an oxygen concentration of 2 mol% in the exhaust gas at the outlet. The reaction results are shown in Table 3. In the case of Comparative Example 1, the amount of coke produced increased compared to Example 1. Further, it can be seen that the proportion of light components having 4 or less carbon atoms such as gas increases, while gasoline decreases, which is economically undesirable.

Claims (5)

By catalytic cracking using a fluid catalytic cracking device having a reaction zone, a separation zone, a stripping zone and a regeneration zone , the oxygen content is 0.1 to 13% by mass and the boiling point is 230 ° C. or higher, derived from animal and vegetable oils. A method for treating biomass containing a certain fat component ,
In the reaction zone, the raw material oil containing the biomass is converted to a catalyst containing 10 to 50% by mass of ultrastable Y-type zeolite, the reaction zone outlet temperature is 480 to 540 ° C., and the catalyst / oil ratio is 4 to 12 wt. / Wt, a reaction pressure of 1 to 3 kg / cm ² G, a first step of treating under conditions of a contact time of 1 to 3 seconds between the raw material oil and the catalyst;
In the regeneration zone, the catalyst subjected to the first step is subjected to a regeneration zone temperature of 640 to 720 ° C., a regeneration zone pressure of 1 to 3 kg / cm ² G, and an oxygen concentration of 0 to 3 mol% in exhaust gas at the regeneration zone outlet. A second step of processing under the conditions of:
A method for treating biomass characterized by comprising: In the catalyst, the ultrastable Y-type zeolite of _SiO 2 / _Al 2 _{O 3} (weight ratio) and wherein the 3 to 10, the processing method of the biomass according to claim 1. In the catalyst, the wherein the alkaline earth metal ion exchange sites of the ultrastable Y-type zeolite is introduced, the processing method of the biomass according to claim 1 or 2. Said catalyst and having containing a silica-alumina as an active matrix, biomass processing method according to any one of claims 1-3. The said 1st process WHEREIN: The said raw material oil is sprayed in the said reaction zone using the steam which is 2-6 mass% of the said raw material oil, The any one of Claims 1-4 characterized by the above-mentioned. The processing method of biomass as described in claim | item.