Process for converting liquid plant biomass in delayed coking unit

Abstract

The invention relates to the co-processing of a liquid plant biomass of lignocellulosic origin and a residual fraction from petroleum distillation, in which the injection of a renewable feed is carried out through the top of a coker, the problems of accelerated coking in the furnace tube and clogging in the plant lines that inevitably occur when a renewable feed of this type is co-processed with a mixture of the main (fossil) feed are avoided. In the invention, renewable material is injected together with acceleration gas through the top of the reactor by means of a suitable injector in order to minimize the likelihood of system clogging during injection. Due to the physical and chemical properties of the lignocellulosic feed, the addition of this type of feed through the top of the reactor may also lead to difficulties associated with the likelihood of line clogging in the inlet of the reactor, since such reactor interior typically has a top temperature of about 440 DEG C. In order to overcome this technical problem, the invention proposes to inject the bio-oil and the gas stream using an auxiliary feed system comprising a tank, a pump and a feed injector. The injection system of the present invention facilitates increased speed of renewable feed in the reactor inlet, improved cooling and dispersion.

Description

Technical Field

[0001] This invention belongs to the fields of chemical and materials engineering and describes the co-processing of renewable materials derived from lignocellulose in a delayed coking unit (DCU) to produce fuels with a lower carbon footprint using existing refining equipment. Background Technology

[0002] Crude oil will maintain its dominant share in the world's energy matrix for decades to come. The share of oil in global primary energy demand is projected to steadily decline from 31% in 2018 to 29% by 2040. However, the transportation sector (road, air, and sea) accounts for 49% of total oil demand, and this figure is expected to rise to 60% by 2040. Crude oil's dominance in the transportation sector can be attributed to the vast infrastructure already established, large-scale production, and the availability of low-cost, high-energy-density fuels.

[0003] However, achieving net-zero CO2 emissions by 2050 or 2070 is crucial to limiting the rise in global average temperature to well below 2°C, whether or not it implicitly depends on negative global net CO2 emissions. Regions are responding to this goal with varying targets; for example, under the Paris Agreement, Europe and Colombia have committed to reductions of 40% and 20% respectively by 2030.

[0004] Regarding emissions from liquid fuels in the transportation sector, there are various options for achieving targets, ranging from fuel efficiency and low-carbon fuels to electric / hybrid vehicles. Regarding low-carbon intensity fuels, several technological options have been proposed to date to reduce CO2 emissions during oil production and refining. However, final use accounts for approximately 80% of total lifecycle emissions.

[0005] Therefore, liquid fuels still need to achieve lower net emissions in the fuel cycle. One possible solution to this problem lies in eventually using fuels produced from sustainable biomass. In this sense, biofuels derived from lignocellulosic biomass have been developed for decades and are attracting increasing attention due to greenhouse gas emissions from fossil fuel flows.

[0006] Lignocellulosic biomass is an abundant and low-cost renewable material because it is a forestry or agro-industrial residue. Regardless of the process used (fast, slow, catalytic, hydrothermal pyrolysis), the pyrolysis of this material produces pyrolysis oils, commonly known as bio-oils, which have the potential to be used as feedstock in refineries for the production of fuels and petrochemical products, utilizing existing process equipment, thus requiring low investment for processing. However, these oils typically contain high concentrations of water, oxygenated organic compounds, and contaminants in their composition, posing challenges to their processing in refineries.

[0007] Delayed coking is a refining process based on the thermal conversion of residual oil fractions (typically vacuum residue (VR)) into lighter and higher-value liquid streams (naphtha and gas oil), which require hydrotreating before being incorporated into the refinery's fuel pool. The process also produces liquefied petroleum gas, fuel gas, and coke. Because it is a non-catalytic conversion process of residual oil fractions, delayed coking has the potential to process feedstocks from biomass pyrolysis, as it is unaffected by the potential loss of catalytic activity due to contaminants present in this type of feedstock. Existing technology

[0008] Some existing literature describes the processing of renewable materials derived from lignocellulose in delayed coking units for fuel production, for example:

[0009] Patent document US8603325B2 describes the co-processing of bio-oil with feedstock (typically VR) from a delayed coking unit, which is then injected into a transfer line between the furnace and the reactor. According to this document, the resulting coke exhibits properties beneficial for reactor decoking, potentially reducing cycle time and increasing unit capacity. Furthermore, patent document US9840671B2 relates to the co-processing of bio-oil with vacuum residue, aiming to reduce coke yield compared to that produced from vacuum residue with high carbon residue. According to this document, the bio-oil is mixed with fossil feedstock and fed into the furnace of the unit, where the mixture is heated to approximately 500°C, thereby allowing sufficient energy to be provided for the thermal cracking reactions occurring in the coker.

[0010] However, as disclosed in the prior art, it is widely known that bio-oils obtained through various biomass pyrolysis processes (fast pyrolysis, slow pyrolysis, catalytic pyrolysis, hydrothermal liquefaction) are unstable at high temperatures and cannot be heated above 80°C because their molecules are composed of different reactive oxygen-containing functional groups that may react and polymerize at high temperatures (e.g., those present in the coking furnaces of the processes described in the two patents), thereby increasing the viscosity of the medium (Diebold, J.; Scahill, J. Biomass to Gasoline. American Chemical Society Symposium on Production Analysis, and Upgrading of Pyrolysis Oils from Biomass, pp. 264-276, 1988). Furthermore, according to the prior art processes, there is a possibility of accelerated coking within a very short operating time and blockage of coking furnace tubes or transfer lines between the furnace and reactor, which may render the processing described in the aforementioned patents infeasible.

[0011] The difference between this invention and the two patents lies in the use of an auxiliary feeding system. Bio-oil and gas flow are injected through an inlet line at the top of the reactor, thus avoiding the renewable feed passing through the high-temperature furnace tubes or the bottom region of the reactor. The injection of pressurized acceleration gas, mixed online with the bio-oil, aims to increase the entry velocity of the material through the top of the reactor, thereby preventing the accumulation of bio-oil polymerization products in the line and subsequent blockage. In addition to the acceleration gas, this invention also envisions the addition of organic solvents, with or without additives, to improve reaction performance, said organic solvents being mixed with the bio-oil in a tank or online.

[0012] A scientific paper titled "SUPPLY CHAIN ​​DESIGN AND INTEGRATION FOR THE CO-PROCESSING OF BIO-OIL AND VACUUM GAS OIL IN A REFINERY" discloses that the co-processing of bio-oil and vacuum gas oil (VGO) helps add renewable carbon to the product and reduces the production cost of biofuels by utilizing existing refinery infrastructure. The paper reveals that biofuels derived from lignocellulosic biomass have been under development for decades and are attracting increasing attention due to fossil fuel scarcity and global warming. Furthermore, the paper examines the integration of biomass and crude oil supplies for the co-processing of bio-oil and VGO, taking CO2 emissions into account.

[0013] However, the aforementioned literature does not mention processing distillation residue feedstocks rich in asphaltenes, with high carbon and metal content, such as vacuum residue or atmospheric residue, nor does it mention co-processing these feedstocks with renewable source streams. Furthermore, the described processes involve fluidized bed catalytic cracking where the conversion reaction occurs through thermal and catalytic effects, which differs from delayed coking where bottom-of-barrel charge conversion occurs thermally.

[0014] A scientific paper titled "BIO-OIL CO-PROCESSING CAN SUBSTANTIALLY CONTRIBUTE TORENEWABLE FUEL PRODUCTION POTENTIAL AND MEET AIR QUALITY STANDARDS" discloses that co-processing crude bio-oil derived from lignocellulosic biomass in existing refineries represents a short-term greenhouse gas mitigation strategy, producing partially renewable hydrocarbon fuels that are compatible with infrastructure and require very little capital. This paper facilitates a quantitative assessment of atmospheric emission changes from various bio-oil co-processing fractions in refinery fluidized bed catalytic cracking units.

[0015] Although it also involves fluidized catalytic cracking technology and co-processing of bio-oil and vacuum gas oil, the aforementioned articles do not use asphalt-rich and contaminated residual feedstocks in these devices as in this invention.

[0016] Patent application US2010024283A1 discloses a method for producing bio-oil by delayed coking with modified feedstock, wherein, in addition to the usual fresh hydrocarbon feed (vacuum residue, atmospheric residue, etc.), the feedstock of a conventional coking unit also includes biomass for co-processing. The aforementioned document provides the possibility of using biomass directly and alone or in any ratio during the delayed coking process. Furthermore, it discloses that this feedstock can be used in the fresh feedstock of the unit, in the coke tower during the reaction or quenching step (reducing the temperature of the hydrocarbon stream in the effluent), in the furnace inlet line, in the furnace outlet line, or in the coke tower outlet line.

[0017] However, the aforementioned literature involves introducing unprocessed solid plant biomass into the coking reactor in addition to first-generation vegetable oils, which differs from the present invention in overcoming the inherent difficulties related to thermal instability and chemical instability in the co-processing of liquid plant biomass obtained from the pyrolysis of lignocellulosic materials.

[0018] This invention offers advantages related to reduced coke yield and increased liquid yield, thereby improving the profitability of delayed coking units (DCUs). However, unlike existing technologies, this invention processes bio-oil in a manner that does not impair the operation of the DCU furnace, as the material is injected through the top of the reactor, resulting in less coke and less CO2.

[0019] The purpose of this invention is to help alleviate various problems related to environmental pollution. In view of the current need to reduce greenhouse gas emissions from the combustion of fossil fuels used in various modes of transportation, this invention proposes co-processing renewable materials derived from the pyrolysis of agricultural and forestry residues in a CRU to produce fuels with a lower carbon footprint using existing refining equipment.

[0020] In view of the above disclosure, the present invention relates to a method for converting liquid plant biomass in a delayed coking unit, which can be applied when it is desired to co-process liquid plant biomass with residual oil fractions to obtain a stream with higher added value and a smaller carbon footprint, thereby producing fuel in which diesel is the main product after hydrotreating. Summary of the Invention

[0021] This invention aims to address the co-processing of liquid plant biomass (preferably bio-oil) and vacuum residue (VR) by injecting liquid plant biomass via the top of the coker. This avoids the problem of accelerated coking in the furnace tubes when this type of unstable feed is injected at the furnace inlet as a mixture with fossil feed, and also avoids blockage of the transfer line between the furnace and reactor when bio-oil is injected at the reactor inlet. In this invention, the renewable feed is injected together with an accelerating gas through an injector of appropriate size to minimize the possibility of system blockage during injection, ensuring process operational stability and avoiding premature shutdowns, efficiency losses, and plant profitability. Organic solvents, with or without additives, can be mixed with the renewable feed to enhance the thermal cracking reaction inside the reactor. Attached Figure Description

[0022] In order to obtain a complete and detailed visualization of the purpose of this invention, Figure 1 Presented as follows:

[0023] Figure 1The interconnections of the elements of the present invention are shown, wherein: 1 represents the main feed (fossil); 2 represents the mixture corresponding to the main feed and natural reclaimed material; 3 represents the furnace; 4 represents the heated and partially vaporized mixture (corresponding to the main feed and natural reclaimed material); 5 represents the coking reactor; 6 represents the liquid plant biomass stream injected into the reactor; 7 represents the accelerating gas; 8 represents the organic vapor; 9 represents the fractionation tower; 10 represents the liquid fraction; 11 represents the process gas; and 12 represents the coke; 13 represents the liquid plant biomass pump; 14 represents the liquid plant biomass stream pumped by the pump; 15 represents the liquid plant biomass tank; and 16 represents the injector.

[0024] Figure 2 It shows the relationship with Figure 1 The same elements of the invention shown are interconnected, but an online injection of an organic solvent 17 with or without additives is shown, which can be mixed with renewable feed to enhance the thermal cracking reaction inside the reactor.

[0025] Figure 3 It shows the relationship with Figure 1 The same elements of the invention shown are interconnected, but it is shown that an organic solvent 17 with or without additives is mixed with a renewable feed in tank 15 to enhance the thermal cracking reaction inside the reactor. Detailed Implementation

[0026] This invention relates to a method for producing fuel by co-processing a renewable stream (liquid plant biomass) of lignocellulose origin in a delayed coking unit. In this method, the co-processing of liquid plant biomass and fossil residue feedstock (e.g., vacuum residue (VR)) occurs at the top of a coking reactor, the liquid plant biomass being produced by processing solid plant biomass from agro-industrial residues in a pyrolysis or liquefaction unit.

[0027] The method of the present invention can be described by the following steps:

[0028] a. Provide liquid plant biomass 6 of lignocellulose source with high lignin content and hydrocarbon stream 1 from oil refining (vacuum residue, atmospheric residue or other residual fractions from oil distillation);

[0029] b. The refinery hydrocarbon stream (main feed (fossil) 1) is introduced to the bottom of the fractionator column 9, where the stream receives natural reclaimed material to form a combined feed, which is heated in the furnace 3 of the delayed coking unit to reach the process temperature required for thermal cracking to occur inside the reactor 5.

[0030] c. Using pump 13, which constitutes the auxiliary feed system, the renewable feed (bio-oil) 6 from tank 15 of the auxiliary feed system is fed together with the gas flow (accelerator gas) 7 to the top of the delayed coking reactor 5, so that the mixture passes through injector 16 under suitable conditions to avoid blockage problems in the pipeline and at the reactor inlet.

[0031] d. Reaction conditions that subject the feed to thermal cracking;

[0032] e. The generated organic vapor 8 enters the fractionator column 9, producing liquid fraction 10 and process gas 11, which are separated into hydrocarbon streams with different boiling point ranges;

[0033] f. Subjecting a liquid hydrocarbon stream in the range of naphtha and light and medium gas oils to a hydrotreating step to obtain a hydrogenated liquid product with renewable contents; and

[0034] g. Remove coke 12 from the reactor to obtain raw petroleum coke with renewable contents.

[0035] according to Figure 1 In the aforementioned method, the main feed 1 is preheated at the bottom of the fractionator column 9. Subsequently, a mixture 2 corresponding to the main feed and natural recoveries is heated to a temperature of 490°C to 510°C in the furnace 3 of the unit. The natural recoveries consist of heavier hydrocarbons produced by the thermal cracking of the feed in the reactor. These hydrocarbons condense in the bottom region of the fractionator column and are incorporated into the unit's fresh feed (main feed), while the mixture is heated in the furnace. The heated and partially vaporized mixture 4 is fed to the bottom of a delayed coking reactor 5, typically at a temperature of 470°C to 490°C. Renewable feed 6 and acceleration gas 7 are injected through the top of reactor 5 at a temperature below 60°C. The thermal cracking and coking reactions of the fossil and renewable feeds occur at high temperatures (400°C to 500°C) inside the reactor, producing organic vapors 8 and coke 12. Coke 12 is retained in the reactor until the switching moment when the main feed is sent to another empty reactor, and vapor 8 enters the fractionator column 9 to produce liquid fraction 10 and process gas 11, which are sent for processing.

[0036] To demonstrate the potential of the aforementioned method, the invention will be described in more detail with respect to the steps performed and their respective parameters.

[0037] Liquid plant biomass (bio-oil) from rapid pyrolysis, slow pyrolysis, catalytic pyrolysis, and hydrothermal liquefaction processes is a thermally unstable product composed of molecules containing various oxygen-containing functional groups, which may undergo chemical interactions when heated above 80°C. Therefore, adding bio-oil through the top of the reactor initially presents difficulties related to the potential for blockage in the reactor inlet line, as the typical top temperature inside such a reactor is approximately 440°C.

[0038] In this sense, the present invention proposes the use of an auxiliary feeding system for injecting bio-oil and accelerating gas, the auxiliary feeding system consisting of a tank, a pump, and a feed injector. The flow rates of the bio-oil and gas must be controlled by a suitable flow controller to maintain process stability.

[0039] The injection of pressurized accelerating gases (e.g., nitrogen, carbon dioxide, process gases, and other gases) mixed online with the bio-oil aims to increase the inflow velocity of the material into the reactor to the range of 2 m / s to 8 m / s, thereby preventing the accumulation of bio-oil polymerization products in the pipeline and subsequent blockage. The injection of these gases also promotes the dispersion of the bio-oil within the reactor, facilitating the distribution of the material across the transverse flow reactor cross-section. Furthermore, it promotes cooling of the injector within the reactor, hindering the polymerization of bio-oil molecules at the injection point due to the high temperature of the system.

[0040] Therefore, to increase the velocity at the reactor inlet, the injection system of the present invention envisions a ratio of the injector diameter to the diameter of the bio-oil feed line reduced to 0.2 to 0.7. Accelerator gas is injected at a percentage ranging from 0.5 wt% to 10 wt% relative to the total feed flow rate of the device.

[0041] After injection at appropriate rates, the bio-oil stream undergoes the process reaction conditions in the top region of the reactor, namely a temperature of 400°C to 500°C and a flow rate of 0.2 kgf / cm³. 2 Up to 5 kgf / cm 2 The gauge pressure. In the delayed coking step, typical reaction conditions are: (i) furnace outlet temperature in the range of 490°C to 510°C, (ii) gauge pressure at the top of the reactor in the range of 10 kPa to 500 kPa, (iii) recycle ratio in the range of 0 volume / volume% to 50 volume / volume%, and (iv) recycle time in the range of 10 hours to 50 hours.

[0042] Then, the vapor generated by the cracking of bio-oil molecules is fractionated together with the vapor generated by the thermal cracking of fossil streams to obtain a liquid product with renewable contents. At the same time, the free radicals of heavy lignocellulose fragments undergo polymerization and coking to form a coke bed inside the reactor.

[0043] When bio-oil is added at the top of the reactor, the product yield distribution is more favorable than when it is processed as a mixture with VR, because even when the processed VR has a relatively low carbon residue, there is less coke formation and more liquid. Furthermore, bio-oil added at the top of the reactor can help control foam generated by the thermal cracking reaction due to its aromatic properties, acting as an antifoaming agent, either in place of or mixed with conventional antifoaming agents.

[0044] Compared to the usual method of injecting bio-oil at the bottom of the reactor and mixing it with VR, the aforementioned method also provides a lower CO2 generation when bio-oil is injected at the top of the reactor.

[0045] To demonstrate the potential of the invention, the embodiments listed above will be described in more detail through examples of the embodiments and the results obtained. It should be emphasized that the following description is intended only to clarify the understanding of the proposed invention and to disclose embodiments of the invention in even more detail, and is not intended to limit the invention. In this way, variations similar to the embodiments are also covered by the scope of the invention.

[0046] The implementation of the plan Shi example

[0047] The present invention can be applied in delayed coking units when it is desired to co-process liquid lignocellulosic biomass (bio-oil) with residual oil fraction (VR) to obtain a stream with higher added value and a lower carbon footprint, thereby producing fuel in which diesel is the main product after hydrotreating.

[0048] Example 1

[0049] The slow-pyrolysis bio-oil, with characteristics shown in Table 1, was injected at a ratio of 10 wt% relative to the feed for a continuous pilot plant with an average flow rate of 2.3 kg / h. Bio-oil injection was carried out through the top of the reactor, using N2 as the accelerating gas at a flow rate of 60 NL / h. The average furnace outlet temperature was maintained at 500°C, the average reactor top temperature at 440°C, and the average operating pressure at 1.8 kgf / cm³. 2 Feed characteristics are shown in Table 2, and gas, liquid, and coke yields are shown in Table 3.

[0050] Table 1: Characteristics of Bio-oil

[0051]

[0052] Table 2: Characteristics of vacuum residue

[0053]

[0054] To eliminate the influence of the accelerating gas injected through the top of the reactor on the product yield, pure VR was processed in the presence of N2, injected under the same conditions as that used for co-processing with bio-oil. A decrease in coke yield and an increase in the yield of the produced liquid were observed.

[0055] Table 3: Yields (mass / mass%) obtained in the pilot plant

[0056]

[0057] In this way, bio-oil can be processed continuously without heating it as a mixture with the main fossil feed, thus avoiding problems such as accelerated coking in the furnace and equipment blockage caused by the thermal instability of bio-oil.

[0058] Example 2

[0059] Laboratory tests were conducted to evaluate different methods of adding bio-oil to vacuum residue: top-feed addition and addition as a mixture with VR. For both addition methods, bio-oil ratios of 5% by mass and 10% by mass relative to the feed mass (corresponding to approximately 380 g VR pre-loaded into the reactor) were evaluated. The reactor was heated from ambient temperature to 500°C. For top-feed addition, all bio-oil material at ambient temperature was added when the internal temperature of the reactor reached approximately 440°C, and heating was maintained until 500°C. In the case of mixed addition, bio-oil material was added to VR contained in the reactor (both at ambient temperature), and heating was carried out until 500°C. For both addition methods, the tests were completed 60 minutes after the system reached the set temperature (500°C). The average operating pressure of the system was maintained at 1.8 kgf / cm³. 2 .

[0060] Compared to mixing with VR, injecting bio-oil through the top of the reactor resulted in lower coke yield, higher liquid yield, and lower CO2 production, as shown in Tables 4 and 5.

[0061] Table 4: Yields (mass / mass%) obtained by different bio-oil injection modes in a batch laboratory device

[0062]

[0063] Table 5: Gas composition (mass / mass%) obtained from different bio-oil injection modes in an intermittent laboratory setting

[0064]

[0065] Intermittent testing confirmed several advantages of injecting bio-oil through the top of the reactor compared to processing with a mixture of feedstock from a delayed coking unit.

[0066] Those skilled in the art will understand the knowledge presented herein and can reproduce the invention in the presented embodiments and other variations covered by the appended claims.

Claims

1. A method for co-processing a renewable stream of lignocellulose origin in a delayed coking unit to produce fuel, characterized in that... The method includes the following steps: a. Provide liquid plant biomass (6) of lignocellulose source with high lignin content and hydrocarbon streams (1) from oil refining (vacuum residue, atmospheric residue or other residual fractions from oil distillation); b. The refined hydrocarbon stream (main feed (fossil) (1)) is introduced into the bottom of the fractionator column (9), where the refined hydrocarbon stream (main feed (fossil) (1)) receives natural recyclables to form a combined feed, which is heated in the furnace (3) of the delayed coking unit to reach the process temperature required for thermal cracking reaction to occur inside the reactor (5); c. Using a pump (13) constituting the auxiliary feed system, the renewable feed (bio-oil) (6) from the tank (15) of the auxiliary feed system is fed together with the gas flow (accelerator gas) (7) to the top of the delayed coking reactor (5), so that the mixture passes through the injector (16) under suitable conditions to avoid blockage problems in the pipeline and at the reactor inlet; d. Reaction conditions that subject the feed to thermal cracking; e. The generated organic vapor (8) enters the fractionator column (9) to produce liquid fraction (10) and process gas (11), which are separated into hydrocarbon streams with different boiling point ranges; f. Subjecting a liquid hydrocarbon stream in the range of naphtha and light and medium gas oils to a hydrotreating step to obtain a hydrogenated liquid product with renewable contents; and g. Remove the coke (12) from the reactor to obtain raw petroleum coke with renewable contents.

2. The method according to claim 1, characterized in that... The liquid plant biomass is a lignocellulose source with a high lignin content of at least 10% by mass.

3. The method according to claim 1, characterized in that... The mixture (2) corresponding to the main feed and the natural recyclables is heated to a temperature of 490°C to 510°C in the furnace (3) of the apparatus.

4. The method according to claim 1 or 2, characterized in that... The liquid plant biomass is produced by processing solid plant biomass derived from agricultural and industrial residues in a pyrolysis or liquefaction device.

5. The method according to claim 1 or 2, characterized in that... The liquid plant biomass is preferably bio-oil.

6. The method according to claim 1 or 2, characterized in that... The liquid plant biomass corresponds to a ratio of 0.10 mass / mass% to 50 mass / mass% relative to the total feed to the delayed coking reactor.

7. The method according to claim 1, characterized in that... The selected hydrocarbon stream is preferably a residue from oil distillation with an initial boiling point above 400°C, whether it is atmospheric or vacuum distillation.

8. The method according to claim 1, characterized in that... Step (c) may involve using the bio-oil feed with an organic solvent, with or without additives dispersed in the organic phase, to improve the system’s reactivity.

9. The method according to claim 8, characterized in that... The organic solvent may be composed of methanol, ethanol, acetone, other polar solvents or solvent mixtures, and the additive dispersed in the organic solvent may be composed of metal oxides such as iron oxide, zinc oxide, titanium oxide, tungsten oxide, other oxides or oxide mixtures.

10. The method according to claim 1, characterized in that... Step (c) uses an auxiliary feeding system consisting of a tank, a pump and a feed injector to inject the liquid plant biomass feed and gas flow.

11. The method according to claim 1, characterized in that... A pressurized gas selected from nitrogen, carbon dioxide, process gases, and other gases is injected and mixed online with the bio-oil.

12. The method according to claim 11, characterized in that... The injection of the accelerating gas disperses the bio-oil inside the reactor, causing the material to enter the reactor at an inlet velocity of 2 m / s to 8 m / s.

13. The method according to claim 10, characterized in that... The diameter of the injector is reduced to a ratio of 0.2 to 0.7 relative to the diameter of the bio-oil feed line.

14. The method according to claim 1, characterized in that... In step (c), the renewable feed (6) and the accelerating gas (7) are passed through a temperature of 400°C to 500°C and 0.2 kgf / cm at a temperature below 60°C. 2 Up to 5 kgf / cm 2 The pressure is injected at the top of the coking unit to produce coke (12) with recyclable contents and organic vapor (8).

15. The method according to claim 1, characterized in that... The fuel obtained from the liquid fraction (10) of the fractionation of the organic vapor (8) is preferably diesel.

16. The method according to claim 1, characterized in that... The conditions for the delayed coking step are: furnace outlet temperature in the range of 490°C to 510°C, gauge pressure at the top of the reactor in the range of 10 kPa to 500 kPa, circulation ratio in the range of 0 volume / volume% to 50 volume / volume%, and circulation time in the range of 10 hours to 50 hours.

17. The method according to claim 1 or 11, characterized in that... The accelerating gas is injected at a percentage ranging from 0.5% to 10% of mass relative to the total feed flow rate of the device.

18. The method according to claim 1, characterized in that Compared to mixing with vacuum residue, injecting the bio-oil through the top of the reactor results in lower coke yield, higher liquid yield, and lower CO2 generation.

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