Bio-oil utilization system

Abstract

Provided is a system for utilizing bio-oil, which can easily and effectively utilize bio-oil regardless of the properties and supply / demand balance of bio-oil while utilizing existing refinery equipment. The system is provided with an atmospheric distillation device, a bio-oil supply means, and at least one device selected from the group consisting of a gas recovery device, a hydrofining device, a naphtha fractionation device, a fluid catalytic cracking device, and a reduced pressure distillation device. The bio-oil supply means supplies the bio-oil, which is derived from biomass and has been subjected to a hydrodeoxygenation treatment, to the atmospheric distillation device together with a raw material oil including crude oil.

Description

Technical Field

[0001] The technology of the present disclosure relates to a bio-oil utilization system. Background Art

[0002] In recent years, the use of renewable energy to replace fossil fuels has been advocated. In addition to the use of natural energy (sunlight, wind power, geothermal heat, etc.), the use of biological resources including animal and plant resources (so-called biomass) as renewable energy has also been studied, and the development of technologies for their practical application has been prevalent in recent years. The use of biomass can suppress the increase in the total amount of carbon dioxide caused by the use of fossil fuels, which is also beneficial from the perspective of carbon neutrality.

[0003] For example, the technology of hydrogenating and modifying animal and vegetable fats to obtain a light oil composition has attracted attention. As such a technology, the following is known: a raw material containing animal and vegetable fats and sulfur-containing hydrocarbon compounds is contacted with a sulfide catalyst to obtain a fraction, and the fraction is further hydrogenated using a metal catalyst supported on a carrier containing a crystalline molecular sieve, and the resulting substance is used as light oil (for example, Patent Document 1, etc.). In addition, for example, Patent Document 2 discloses a method of pre-treating biogrease by pyrolysis, vacuum distillation, catalytic cracking deoxygenation reaction, and hydrofining, and then subjecting it to atmospheric distillation to produce fuel oil (specifically, gasoline fraction and diesel (light oil) fraction).

[0004] Prior art literature

[0005] Patent Literature

[0006] Patent Document 1: Japanese Patent Application Publication No. 2009-161669

[0007] Patent Document 2: U.S. Patent Application Publication No. 2021 / 355393 Summary of the invention

[0008] Problems to be solved by the invention

[0009] The technologies described in Patent Documents 1 and 2 are technologies that intend to purify biomass such as animal and vegetable oils and bio-greases and utilize the refined bio-oil. Therefore, it is necessary to install independent refining equipment for the purification of these biomasses. That is, the technologies described in Patent Documents 1 and 2 lack the perspective of effectively utilizing various devices attached to the refinery facilities and existing refinery facilities.

[0010] In addition, bio-oil has a wide boiling point range, and when it is simply distilled, it has limitations in terms of quality for use as light oil, fuel oil, etc., and it cannot be said that the effective use of bio-oil is sufficient. On the other hand, if it is desired to use it as light oil, fuel oil, etc. without restriction, it is necessary to perform various refining, so not only the equipment cost but also the cost required for refining will increase. From this point of view, it is important to effectively utilize various devices of existing refinery facilities.

[0011] However, in the case of using bio-oil derived from biomass to replace the components derived from crude oil, such as the so-called biodiesel fuel oil of Patent Document 1, the required amount of bio-oil sometimes changes according to the increase or decrease in the demand for fuel oil in various uses and the balance between bio-oil and various fractions used in combination. On the other hand, regarding bio-oil, there are also cases where biological resources (biomass) including animal and plant resources that serve as its raw materials cannot be supplied in a certain amount, and there are cases accompanied by complicated operations such as achieving a balance between supply and demand. This is also the same as the case where bio-oil is used as a part of a fuel oil composition for uses other than biodiesel fuel oil, such as ships, aircraft, etc.

[0012] In the case of the technology of Patent Document 2, biogrease is subjected to a predetermined pretreatment and then subjected to atmospheric distillation to utilize the obtained fraction as fuel oil (gasoline fraction, diesel fraction). Therefore, similarly to Patent Document 1, it is necessary to strike a balance between supply and demand.

[0013] In this way, once the supply source and the application are determined, it is necessary to strictly balance the supply and demand, and the operation is very complicated. In addition, if the supply and demand cannot be balanced, for example, if the supply of biomass-derived bio-oil is too much, a storage tank for the bio-oil is required, and on the other hand, if the demand for the application is too much, it is necessary to adjust the amount of crude oil-derived fraction that should be replaced by bio-oil, etc., and the impact may spread to the entire refinery.

[0014] In addition, since bio-oil uses biological resources (biomass) including animal and plant resources as raw materials, its properties are sometimes not fixed. Therefore, once the use of bio-oil is determined, in order to ensure the properties required for the use, for example, when using it in combination with fractions from other crude oil sources, it is sometimes necessary to adjust the amount of the fractions from other crude oil sources to ensure the required properties, thereby re-evaluating the overall balance. However, such re-evaluation is not easy.

[0015] The technology disclosed in the present invention has been completed in view of such actual conditions, and its purpose is to provide a bio-oil utilization system that can easily and effectively utilize the bio-oil by utilizing existing refinery facilities without considering the properties of the bio-oil and the supply-demand balance.

[0016] Solutions to Solve Problems

[0017] In order to solve the above-mentioned problems, the technology disclosed in the present invention provides the following bio-oil utilization system.

[0018] 1. A bio-oil utilization system comprising an atmospheric distillation unit and a bio-oil supply mechanism, and at least one device selected from a gas recovery unit, a hydrotreating unit, a naphtha fractionation unit, a fluid catalytic cracking unit, and a vacuum distillation unit,

[0019] The bio-oil supply mechanism supplies bio-oil derived from biomass and subjected to a hydrodeoxygenation treatment to the atmospheric distillation apparatus together with a feedstock oil including crude oil.

[0020] 2. According to the bio-oil utilization system described in 1 above, the raw oil further contains at least one selected from waste plastic pyrolysis oil and grease.

[0021] 3. The bio-oil utilization system according to 1 or 2 above, further comprising a dehydration treatment device for the bio-oil.

[0022] 4. The bio-oil utilization system according to any one of 1 to 3 above, wherein the hydrodeoxygenated bio-oil has an oxygen content of 10 mass % or less, a chlorine content of 10 mass ppm or less, and an acid value of 10 mgKOH / g or less.

[0023] 5. The bio-oil utilization system according to any one of 1 to 4 above, wherein the biomass is at least one selected from herbaceous biomass, woody biomass, biomass derived from microorganisms, algae biomass, and organic waste biomass.

[0024] 6. The bio-oil utilization system according to any one of 1 to 5 above, wherein the biomass is inedible biomass.

[0025] Effects of the Invention

[0026] According to the technology disclosed in the present invention, it is possible to provide a bio-oil utilization system that can easily and effectively utilize bio-oil regardless of the properties of the bio-oil or the supply-demand balance while utilizing existing refinery facilities.

[0027] BRIEF DESCRIPTION OF THE DRAWINGS

[0028] Figure 1 This is a flowchart showing a preferred embodiment of the bio-oil utilization system according to the present embodiment.

[0029] Figure 2 This is a flowchart showing a preferred embodiment of the bio-oil supply mechanism in the bio-oil utilization system according to the present embodiment.

[0030] Figure 3 This is a flow chart showing a preferred embodiment of a hydrodeoxygenation treatment facility for performing hydrodeoxygenation treatment of bio-oil used in the bio-oil utilization system of the present embodiment. DETAILED DESCRIPTION

[0031] The following is a description of an embodiment of the technology disclosed herein (hereinafter sometimes referred to as "the present embodiment"). It should be noted that in this specification, the upper and lower limits of the numerical ranges of "above", "below", and "to" are values ​​that can be combined arbitrarily, and the values ​​of the embodiments can also be used as the upper and lower limits.

[0032] 〔Bio-oil Utilization System〕

[0033] The bio-oil utilization system of this embodiment is briefly described as follows: Figures 1 to 3 Provide explanation. Figure 1 is a flow chart showing a preferred embodiment of the bio-oil utilization system of the present embodiment. Figure 2 is a flow chart showing a preferred embodiment of the bio-oil supply mechanism, Figure 3 This is a flow chart showing a preferred embodiment of a facility for performing hydrodeoxygenation treatment of bio-oil.

[0034] Figure 1 The bio-oil utilization system shown includes an atmospheric distillation apparatus 21 and a bio-oil supply mechanism 1 , and is a system for supplying bio-oil to the atmospheric distillation apparatus 21 together with feedstock oil.

[0035] The bio-oil supplied to the atmospheric distillation device 21 is a product that has been subjected to a hydrodeoxygenation treatment. The bio-oil may be subjected to a hydrodeoxygenation treatment before being supplied to the atmospheric distillation device 21, and thus the hydrodeoxygenation treatment may be performed before being supplied to the bio-oil supply mechanism 1, or may be performed between the bio-oil supply mechanism 1 and the atmospheric distillation device 21. Figure 1 and Figure 2 As shown, the bio-oil supply mechanism 1 is supplied with bio-oil (bio-oil that has not been subjected to a hydrodeoxygenation treatment) or bio-oil that has been subjected to a hydrodeoxygenation treatment.

[0036] In addition, Figure 1 In the bio-oil utilization system shown, the feedstock oil and the bio-oil subjected to the hydrodeoxygenation treatment are supplied to the atmospheric distillation unit 21, and then fractionated into various fractions of naphtha, kerosene, and light oil, and these fractions are further processed in the refining equipment such as the gas recovery unit 22, the naphtha fractionation unit 23, and the hydrotreating unit 24. In addition, the heavy oil fraction distilled from the bottom of the tower is further distilled in the vacuum distillation unit 25, supplied to the hydrotreating unit 24, and further supplied to the fluid catalytic cracking unit 26, etc., and desulfurized by direct desulfurization or indirect desulfurization.

[0037] As the distillation atmospheric pressure device provided in the bio-oil utilization system of the present embodiment, the gas recovery device, the hydrotreating device, the naphtha fractionating device, the fluidized catalytic cracking device, and the vacuum distillation device for supplying various fractions distilled from the atmospheric pressure device can be used, each device provided in the existing refinery facilities. By effectively utilizing each device provided in the existing refinery facilities, not only the equipment cost but also the cost required for refining can be reduced.

[0038] In addition, by supplying the bio-oil subjected to the hydrodeoxygenation treatment to the atmospheric distillation apparatus, the bio-oil subjected to the hydrodeoxygenation treatment is fractionated into various fractions in the atmospheric distillation apparatus. That is, the various fractions distilled by atmospheric distillation of the bio-oil subjected to the hydrodeoxygenation treatment are allocated to the various fractions distilled by atmospheric distillation of the raw material oil corresponding to the various fractions, and the various fractions are used according to the purpose. Therefore, when receiving the bio-oil, the balance of supply and demand generated by determining the supply source and the purpose is not considered, and the bio-oil can be effectively used without more or less. In addition, the various fractions contained in the bio-oil subjected to the hydrodeoxygenation treatment are only allocated to the various fractions distilled by atmospheric distillation of the raw material oil corresponding to the various fractions, so there is no need to consider the properties of the bio-oil.

[0039] As described above, the bio-oil utilization system of the present embodiment is a system that can easily and effectively utilize bio-oil without considering the properties of bio-oil and the supply-demand balance while utilizing the existing refinery facilities.

[0040] (Bio-oil)

[0041] The bio-oil used in the bio-oil utilization system of the present embodiment is a substance that has been subjected to a hydrodeoxygenation treatment. Moreover, the bio-oil is a liquid component produced from non-fossil resources, mainly derived from biomass, and is preferably divided into the following two types.

[0042] (i) Oxygen-containing compounds that are liquid at room temperature or slightly heated, such as vegetable oils (palm oil, soybean oil, etc.), waste cooking oils, animal fats, oils extracted from algae, and cashew nut shell liquid (CNSL)

[0043] (ii) Through pyrolysis and solvent thermal liquefaction, solid biomass (herbs, wood, agricultural residues, fermentation residues, algae, etc.) is converted into liquid oxygen-containing compounds at room temperature.

[0044] Here, pyrolysis means heating (for example, 290 to 600° C.) and decomposing solid biomass to liquefy it. Solvothermal liquefaction means heating (for example, 250 to 450° C.) and decomposing solid biomass to liquefy it together with a solvent to liquefy it.

[0045] Solid biomass can be dried or crushed. A suitable heat medium can also be used for pyrolysis. Electromagnetic waves such as microwaves can also be used for pyrolysis. In pyrolysis, a catalyst can be added to promote cracking, and some hydrogen can also be added. The solvent for solvothermal liquefaction can be an organic solvent, water, or ionic liquids. Solvothermal liquefaction can be set to a subcritical state or can be carried out under a supercritical state. In solvothermal liquefaction, a catalyst can be added to promote cracking, and some hydrogen can also be added.

[0046] Biomass as a raw material of bio-oil refers to a resource of organic matter derived from animals and plants other than fossil fuels, and representative examples thereof include herbaceous biomass, woody biomass, biomass derived from microorganisms, algae biomass, and organic waste biomass. In the system of the present embodiment, bio-oil derived from a single biomass or a combination of multiple biomasses can be used among these biomasses.

[0047] Representative examples of herbaceous biomass include palm tree trunks and empty fruit bunches, palm fruit fibers and seeds, bagasse (sweet residues of sugarcane and high biomass sugarcane), sugarcane tops (tops and leaves of sugarcane), energy sugarcane, rice straw, wheat straw, corn stems and leaves and residues (corn stalks, corn cobs, corn husks), husks and shells of jatropha seeds, cashew nut shells, switchgrass, sugarcane grass, high biomass yield crops, energy crops, and energy sugarcane.

[0048] Typical examples of woody biomass include coniferous trees and broad-leaved trees such as cedar, cypress, hinoki, cherry, eucalyptus, beech, and bamboo.

[0049] Typical examples of the biomass derived from microorganisms include mixed sludge from sewage treatment plants, wastewater sludge from food processing plants, etc., and brewer's yeast residues and shochu residues from breweries.

[0050] Typical examples of algae-based biomass include microalgae such as algae classified into green algae, yellow dinoflagellates, diatoms, dinoflagellates, unicellular eukaryotic algae, freshwater unicellular green algae (Chlorella), and cyanobacteria.

[0051] In addition, representative and preferred examples of organic waste-based biomass include food-based biomass such as food waste (kitchen garbage), animal and plant residues (food processing residues), and paper-based biomass such as paper waste and waste paper.

[0052] As the oil and fat, for example, plant oil and fat such as esters of fatty acids and glycerol obtained by extracting and refining lipids contained in plants such as oil palm, soybean, rapeseed, corn, and rice, animal oil and fat such as lard, which are liquid at room temperature, solid fats that become liquid by heating to about 100° C. or less, etc. can be used. In addition, hydrogenated oil and fat that has been hydrogenated and has a reduced unsaturated fatty acid content can also be used as the oil and fat.

[0053] The biomass used as the raw material of bio-oil may be any of edible biomass and inedible biomass, but inedible biomass (e.g., trunks, seeds, stems and leaves, etc.) among herbaceous biomass and inedible biomass represented by woody biomass are preferably used because they cannot be used as food, and thus the biomass can be effectively utilized.

[0054] (Hydrodeoxygenation treatment)

[0055] The bio-oil used in the system of the present embodiment is a substance that has been subjected to a hydrodeoxygenation treatment. Since the bio-oil is derived from the above-mentioned biomass, as a general property, it has a property that the oxygen content is higher than that of raw oils such as crude oil. If it is used in a state where the oxygen content is high, that is, if it is not subjected to a hydrodeoxygenation treatment, for example, in the case of using an atmospheric distillation apparatus used for atmospheric distillation of an existing crude oil, it becomes a cause of corrosion and contamination of the atmospheric distillation apparatus and various downstream apparatuses. Therefore, in the system of the present embodiment, the bio-oil that has been subjected to a hydrodeoxygenation treatment is used.

[0056] The hydrodeoxygenation treatment can be adopted without particular limitation as long as it is a treatment capable of removing oxygen contained in the bio-oil. As an apparatus for performing the hydrodeoxygenation treatment, for example, a typical preferred example is Figure 3 The apparatus shown carries out the hydrodeoxygenation treatment of bio-oil.

[0057] Figure 3 The hydrodeoxygenation treatment equipment shown has a heating furnace for heating bio-oil and hydrogen used for hydrodeoxygenation, and a reaction tower for performing a hydrodeoxygenation reaction on a fluid containing the bio-oil and hydrogen heated by the heating furnace. The bio-oil after the hydrodeoxygenation reaction in the reaction tower contains water generated as a by-product by the reaction. The bio-oil subjected to the hydrodeoxygenation treatment containing water is used to heat the bio-oil supplied to the reaction tower in a feed / effluent heat exchanger, and then separated into hydrogen-rich gas, water, and bio-oil subjected to the hydrodeoxygenation treatment in a high-pressure separator. The separated bio-oil subjected to the hydrodeoxygenation treatment is supplied to the bio-oil supply mechanism after the contained gas is volatilized in a low-pressure separator.

[0058] In addition, the hydrogen-rich gas is used as recycled hydrogen for hydrodeoxygenation reaction after hydrogen sulfide is removed in the adsorption tower.

[0059] The reaction tower used in the hydrodeoxygenation reaction of bio-oil is filled with a catalyst in which at least one active metal species selected from active metal species such as nickel, cobalt, molybdenum, tungsten, sulfur, etc., such as NiMo, CoMo, NiCoMo, NiMoW, NiMoS, CoMoS, is supported on a carrier such as alumina and silica, and the hydrodeoxygenation reaction is carried out using these catalysts.

[0060] As various conditions for the reaction in the reaction tower, the reaction temperature is usually 300° C. or higher, preferably 320° C. or higher, more preferably 340° C. or higher, and the upper limit is usually 400° C. or lower, preferably 380° C. or lower, more preferably 360° C. or lower. That is, the fluid containing bio-oil and hydrogen is heated to the above temperature in the heating furnace.

[0061] The hydrogen supply amount, as the ratio of hydrogen to bio-oil (Nm3 / kL), is preferably 100 or more, more preferably 500 or more, further preferably 800 or more, and further preferably 1250 or more. The upper limit is preferably 2000 or less, and more preferably 1750 or less.

[0062] The hydrogen partial pressure is usually 4.0 MPa or more, preferably 5.0 MPa or more, more preferably 6.0 MPa or more, and further preferably 7.5 MPa or more, and the upper limit is usually 9.0 MPa or less, and preferably 8.5 MPa or less.

[0063] The location of the hydrodeoxygenation treatment equipment for hydrodeoxygenation treatment is not particularly limited as long as the hydrodeoxygenation treatment is carried out before the bio-oil is supplied to the atmospheric distillation device, for example Figure 3 As shown, it may be provided upstream of the bio-oil supply mechanism 1 described later, that is, before being supplied to the bio-oil supply mechanism 1 , or it may be provided in the bio-oil supply mechanism 1 as described later.

[0064] (Dehydration treatment device)

[0065] In addition, as a general property, bio-oil has a higher water content than crude oil and other raw material oils. In addition, depending on the type of biomass used as the raw material of bio-oil, the chlorine concentration may be high. Therefore, as with crude oil described later, it may become a major cause of clogging due to corrosion and contamination of atmospheric distillation devices and various devices downstream thereof. In order to reduce clogging due to corrosion and contamination, the bio-oil used in the system of the present embodiment is preferably dehydrated bio-oil. That is, the system of the present embodiment preferably includes a dehydration treatment device for bio-oil.

[0066] As a method for dehydrating bio-oil, any method that can remove water can be adopted without particular limitation. In addition, bio-oil contains salt like crude oil. If the removal of the salt is also considered, it is preferred to adopt the desalting treatment commonly performed on crude oil. Even when the salt concentration of bio-oil is low, water can be removed by desalting treatment, so it is preferred to perform desalting treatment regardless of the salt concentration. The method for desalting treatment will be described later in the desalting treatment of crude oil. In addition, bio-oil usually contains inorganic salts and organic chlorine compounds, but through dehydration treatment (desalting treatment), inorganic chlorine compounds are mainly removed together with water. Dehydration treatment is preferably performed on bio-oil before hydrodeoxygenation treatment.

[0067] The amount of bio-oil used is not particularly limited as long as the amount of bio-oil received is directly used as the amount of bio-oil used. However, considering the effective use of bio-oil, the stable operation of the system of this embodiment, etc., it is preferably 0.1 parts by mass or more relative to 100 parts by mass of the supply of raw oil, and the upper limit is preferably 30 parts by mass or less, and more preferably 25 parts by mass or less.

[0068] (Properties of bio-oil)

[0069] Representative properties of the bio-oil subjected to the hydrodeoxygenation treatment used in the system of the present embodiment will be described.

[0070] The oxygen content of the bio-oil subjected to the hydrodeoxygenation treatment used in the system of the present embodiment is preferably equal to that of crude oil, and is generally 10% by mass or less, preferably 5% by mass or less, and more preferably 1% by mass or less. As the lower limit, the lower the better, and 0% by mass, i.e., no oxygen is contained, is particularly preferred.

[0071] The chlorine content is usually 10 mass ppm or less, preferably 8 mass ppm or less, and more preferably 5 mass ppm or less. As the lower limit, the smaller the better, and particularly preferably 0 mass %, that is, no chlorine content.

[0072] The acid value is usually 10 mgKOH / g or less, preferably 8 mgKOH / g or less, and more preferably 5 mgKOH / g or less. The lower limit is preferably as small as possible, and is usually about 0.1 mgKOH / g.

[0073] (Crude Oil)

[0074] In the bio-oil utilization system of the present embodiment, the raw material oil used together with the bio-oil includes crude oil.

[0075] The crude oil is not particularly limited as long as it is crude oil that can be accepted in the refinery equipment. For example, it can include unprocessed oil from oil wells (Arabian heavy crude oil, Arabian medium crude oil, Arabian light crude oil, Arabian extra light crude oil, Kuwait, Oman, Qatar land, Qatar marine and other petroleum crude oils). In addition, for example, it can include coal liquefied oil, asphalt sand oil, oil sand oil, oil shale oil, Orinoco bitumen, synthetic crude oil obtained from them, and mixed oil obtained by mixing multiple types thereof.

[0076] As the crude oil supplied to the atmospheric distillation unit, it is preferable to use the crude oil obtained by pre-treating the above-mentioned crude oil as necessary.

[0077] Crude oil generally contains muddy water, seawater, etc., and therefore contains sodium, magnesium chlorides, carbonates, sulfates, etc. as impurities, which are the main causes of blockages caused by corrosion and contamination of atmospheric distillation equipment and various downstream equipment. Therefore, as a pretreatment, it is preferable to perform a desalting treatment to remove the water, salt and mud contained in the crude oil.

[0078] The desalting method may be carried out by a conventionally known method, such as an electric desalting method in which water is added to crude oil and stirred to dissolve the salt contained in the crude oil in the water, and a voltage is applied to a desalting tank to break the emulsion of water containing the salt to separate it, or a chemical desalting method in which an emulsion breaker is used to break the emulsion to separate it.

[0079] The crude oil pretreatment may be performed on the crude oil temporarily received in the crude oil tank. Furthermore, the pretreated crude oil is preferably supplied to the bio-oil supply mechanism in the system of the present embodiment.

[0080] As the raw material oil, in addition to the above-mentioned crude oil, other oils may be contained. As other oils, for example, waste plastic pyrolysis oil and the like are preferably cited.

[0081] Waste plastic pyrolysis oil is a substance formed by condensing oil gas obtained by pyrolysis of waste plastic. As waste plastic, for example, various materials constituting food bottles, shopping bags, food trays, packaging films, interior and exterior decorations of residential building materials, interior decorations of automobiles, etc., and exterior decoration components of electrical products can be representatively cited.

[0082] These waste plastic pyrolysis oils can be used alone or in combination of multiple types.

[0083] The content of crude oil contained in the feedstock oil is preferably 50 mass % or more, more preferably 80 mass % or more, further preferably 90 mass % or more, further preferably 95 mass % or more, and particularly preferably 100 mass %, i.e., the feedstock oil is only crude oil, based on the total amount of the feedstock oil.

[0084] (Atmospheric pressure distillation unit)

[0085] The atmospheric distillation apparatus of the bio-oil utilization system of the present embodiment may be a dedicated apparatus of the system of the present embodiment, or an atmospheric distillation apparatus of a refinery facility may be used. For the atmospheric distillation apparatus of the system of the present embodiment, if it is considered that the feedstock oil includes crude oil, various fractions distilled by atmospheric distillation of the bio-oil subjected to hydrodeoxygenation treatment are allocated to various fractions distilled by atmospheric distillation of the feedstock oil corresponding to the various fractions, and the various fractions are used according to the purpose, it is preferable to use an atmospheric distillation apparatus used for atmospheric distillation of crude oil of a refinery facility. It is possible to seek effective utilization of the existing refinery facility.

[0086] Therefore, the bio-oil utilization system of the present embodiment may exist independently, but is preferably incorporated into a refinery facility using crude oil. In addition, there is no need to newly install an atmospheric distillation apparatus for the bio-oil utilization system of the present embodiment.

[0087] An atmospheric distillation unit is a unit that distills feedstock oil including crude oil and bio-oil subjected to hydrodeoxygenation treatment from the top of a tower into various fractions such as a gas fraction, a naphtha fraction, a kerosene fraction, a light oil fraction, and a heavy oil fraction. The following describes the general uses of these various fractions.

[0088] The gas fraction is generally divided into light gas and LPG. The light gas is used as fuel gas after acid gas (sulfur-containing gas) is removed by amine refining treatment or the like as needed, and LPG is used as LP gas after impurities are removed as needed.

[0089] The naphtha fraction is distilled as a light naphtha fraction and a heavy naphtha fraction, or is distilled as a naphtha fraction. The light naphtha fraction is used as gasoline and as a raw material for an ethylene plant, and is converted into acetylene, propylene, butane, butene, etc. in addition to ethylene. The heavy naphtha fraction is subjected to desulfurization and denitrogenation treatments by hydrotreating treatments, and is used as a high-octane gasoline and a raw material for an aromatic hydrocarbon production plant by catalytic reforming treatment, and is converted into aromatic hydrocarbons such as benzene, xylene, and toluene.

[0090] When the naphtha fraction is fractionated as a naphtha fraction, the naphtha fraction is subjected to desulfurization and denitrogenation treatment by hydrotreating treatment and the like to be fractionated into a light naphtha fraction and a heavy naphtha fraction, and these fractions are used for various purposes after being subjected to the above-mentioned various treatments.

[0091] The kerosene fraction is subjected to desulfurization and denitrogenation treatments by hydrotreating treatments and is used as base oils such as kerosene and jet fuel.

[0092] The light oil fraction is subjected to desulfurization and denitrogenation treatments by hydrotreating treatments and is used as diesel light oil. In addition, the heavy light oil fraction (heavy light oil fraction) in the light oil fraction is lightened by catalytic cracking reaction in a catalytic cracking unit (FCC unit) to form fuel gas, pyrolysis gasoline, and pyrolysis light oil fraction. Pyrolysis gasoline is blended with naphtha fractions and used as gasoline, and pyrolysis light oil fractions are blended with heavy oil fractions and used as various heavy oils such as A heavy oil.

[0093] Furthermore, in addition to the heavy gas oil fraction, a desulfurized gas oil fraction obtained by subjecting the heavy fraction to a hydrotreating treatment (hydrodesulfurization and denitrification treatment) may be supplied to the catalytic cracking unit (FCC unit).

[0094] The heavy oil fraction is vacuum distilled in a vacuum distillation unit to become a vacuum light oil fraction, which is subjected to desulfurization and denitrogenation treatments through hydrofining treatments, and the resulting desulfurized light oil fraction is used directly as various raw materials for A heavy oil, etc., or is supplied to a catalytic cracking unit (FCC unit) for lightening and use. In addition, the vacuum residue fraction obtained from the bottom of the vacuum distillation unit is subjected to desulfurization and denitrogenation treatments through hydrofining treatments to become a desulfurized heavy oil fraction, which is used as various raw materials for A heavy oil, etc., and also as asphalt.

[0095] (Other devices)

[0096] The bio-oil utilization system of the present embodiment includes an atmospheric distillation apparatus and a bio-oil supply mechanism, and as other devices other than these apparatuses and mechanisms, includes at least one device selected from a gas recovery device, a hydrotreating device, a naphtha fractionation device, a fluid catalytic cracking device, and a vacuum distillation device. These devices are devices for treating various fractions obtained by fractionation in the atmospheric distillation apparatus, and are specifically devices for treating such as refining.

[0097] As an apparatus that can be used to treat various fractions obtained by the above-mentioned atmospheric distillation apparatus, there can be mentioned Figure 1 The devices shown are a gas recovery device 22, a naphtha fractionation device 23, a hydrotreating device 24, a vacuum distillation device 25, and a fluidized catalytic cracking device 26. The gas recovery device 22 is a device for recovering gas fractions, the naphtha fractionation device 23 is a device for fractionating the naphtha fraction into light naphtha and heavy naphtha, the hydrotreating device 24 is a device for desulfurization and denitrification by hydrotreating the naphtha fraction, kerosene fraction, light oil fraction, and heavy oil fraction, the vacuum distillation device 25 is a device for fractionating the vacuum light oil fraction by vacuum distillation of the heavy fraction, and the fluidized catalytic cracking device (FCC device) 26 is a device for performing catalytic cracking reaction of the desulfurized heavy oil fraction after the heavy light oil fraction and the vacuum light oil fraction have been subjected to the hydrotreating treatment.

[0098] The bio-oil utilization system of the present embodiment only needs to include one device selected from these other devices, and may also include two or more devices. In addition, from the perspective of effectively utilizing the existing refinery facilities, these other devices are preferably devices that the existing refinery facilities have. Therefore, when using the devices that the existing refinery facilities have, it can also be said that the above-mentioned other devices that the bio-oil utilization system of the present embodiment has can be changed according to what kind of devices the existing refinery facilities have.

[0099] (Bio-oil supply mechanism)

[0100] The bio-oil utilization system of the present embodiment includes a bio-oil supply mechanism for receiving bio-oil or bio-oil subjected to hydrodeoxygenation and feedstock oil and supplying them to the atmospheric distillation apparatus.

[0101] For the bio-oil supply mechanism, use Figure 2 Provide explanation. Figure 2 This is a flowchart showing a preferred embodiment of the bio-oil supply mechanism 1 in the bio-oil utilization system of the present embodiment. As the embodiment of the bio-oil supply mechanism 1, the following embodiments (i) to (iv) are representatively and preferably cited. Figure 2 (i) to (iii) in the above correspond to the following methods (i) to (iii).

[0102] (i) The bio-oil is received in a crude oil tank, the feedstock oil and the bio-oil are mixed in the crude oil tank, and the feedstock oil and the bio-oil are supplied to the atmospheric distillation device 21 .

[0103] (ii) The bio-oil is received in the bio-oil tank, the pipe for the bio-oil is connected to the pipe for the raw oil received in the crude oil tank, and the raw oil and the bio-oil are supplied to the atmospheric distillation device 21 .

[0104] (iii) The pipe for the bio-oil and the pipe for the stock oil received in the crude oil tank are connected, and the stock oil and the bio-oil are supplied to the atmospheric distillation device 21 .

[0105] (iv) The bio-oil is received in a waste oil tank (reprocessed oil tank) in the refinery facility, a supply pipe from the waste oil tank is connected to a pipe for the raw oil, and the raw oil, the bio-oil, and optionally other reprocessed oil are supplied to the atmospheric distillation unit 21.

[0106] In the system of this embodiment, the bio-oil only needs to be hydrodeoxygenated when supplied to the atmospheric distillation device, and the bio-oil received by the bio-oil supply mechanism may or may not be hydrodeoxygenated bio-oil.

[0107] When receiving bio-oil that has not been subjected to hydrodeoxygenation treatment, in the case of the above-mentioned embodiment (i), a facility for conducting hydrodeoxygenation treatment before supplying to the crude oil tank may be provided.

[0108] In the case of (ii) above, it is sufficient to have a device for performing a hydrodeoxygenation treatment before supplying to the bio-oil tank or before connecting the pipe from the bio-oil tank to the stock oil. In the case of (iii) above, it is sufficient to have a device for performing a hydrodeoxygenation treatment before connecting the pipe to the stock oil.

[0109] The bio-oil supply mechanism only needs to have at least one of the above-mentioned modes (i) to (iv). Figure 2 From the perspective of reducing the initial equipment cost, any one of the above methods (i) to (iv) can be adopted. From the perspective of corresponding to the diversity of system operation, any two or more of the above methods (i) to (iv) can be adopted at the same time.

[0110] When any two or more methods are used simultaneously, taking into account both the initial equipment cost and the diversity of operation, a combination of the above methods (i) and (ii), the above methods (i) and (iii), and the above methods (ii) and (iii) is preferred.

[0111] As described above, considering the characteristic that the bio-oil subjected to the hydrodeoxygenation treatment is supplied to the atmospheric distillation apparatus together with the feedstock oil containing crude oil, the bio-oil utilization system of the present embodiment preferably utilizes the atmospheric distillation apparatus already existing in the refinery equipment, that is, the system of the present embodiment is preferably assembled in the refinery equipment using crude oil. It is possible to seek effective utilization of the existing refinery equipment. In addition, the above-mentioned gas recovery device, hydrotreating device, naphtha fractionation device, fluid catalytic cracking device and vacuum distillation device are also the same.

[0112] For the same reason, if the crude oil tank and the piping from the crude oil tank to the atmospheric distillation unit in the bio-oil supply mechanism of the system of this embodiment already exist in the refinery facilities, it is preferable to use the existing tanks and piping.

[0113] Regarding bio-oil, if there is already a bio-oil tank in the refinery facility, the existing tank can be used, and if not, a new tank can be installed. The same applies to the piping of bio-oil.

[0114] Furthermore, if pressure delivery of crude oil and bio-oil is required, a pump may be provided as required, and in the case of flow management, instruments such as a flow meter and a flow control valve may be provided.

[0115] Industrial Applicability

[0116] The bio-oil utilization system of this embodiment can be easily and effectively utilized regardless of the properties of the bio-oil and the supply-demand balance, and is therefore suitable for utilization in the form of an additional installation in an existing refinery facility.

Claims

1. A bio-oil utilization system comprising an atmospheric distillation unit and a bio-oil supply mechanism, and at least one device selected from a gas recovery unit, a hydrotreating unit, a naphtha fractionation unit, a fluid catalytic cracking unit, and a vacuum distillation unit, The bio-oil supply mechanism supplies bio-oil derived from biomass and subjected to a hydrodeoxygenation treatment to the atmospheric distillation apparatus together with a feedstock oil including crude oil.

2. The bio-oil utilization system according to claim 1, wherein: The raw material oil further comprises at least one selected from waste plastic pyrolysis oil and grease.

3. The bio-oil utilization system according to claim 1 or 2, wherein: The invention further comprises a dehydration treatment device for the bio-oil.

4. The bio-oil utilization system according to any one of claims 1 to 3, wherein: The hydrodeoxygenated bio-oil has an oxygen content of 10 mass % or less, a chlorine content of 10 mass ppm or less, and an acid value of 10 mgKOH / g or less.

5. The bio-oil utilization system according to any one of claims 1 to 4, wherein: The biomass is at least one selected from herbaceous biomass, woody biomass, biomass derived from microorganisms, algae biomass, and organic waste biomass.

6. The bio-oil utilization system according to any one of claims 1 to 5, wherein: The biomass is inedible biomass.

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