Method for converting liquid plant biomass in a delayed coking unit

Abstract

The present invention relates to the coprocessing of liquid plant biomass of lignocellulosic origin and residual fractions from petroleum distillation, in which the injection of the renewable charge is carried out through the top of the coker, avoiding the problems of accelerated coking in the oven tubes and obstructions in the unit lines which inevitably occur when this type of renewable charge is coprocessed in a mixture with the main (fossil) charge. In the present invention, the renewable material is injected through the top of the reactor, in conjunction with an accelerating gas, by means of a suitable injector, so as to minimize the possibility of obstruction of the system during injection. Due to the physical and chemical characteristics of lignocellulosic charges, the addition of this type of charge through the top of the reactor could also lead to difficulties related to the possibility of obstruction of the line in the reactor inlet, since the usual top temperature inside such reactors is around 440°C. In order to overcome this technical problem, the present invention proposes using an auxiliary charging system for injecting bio-oil and a gas stream, comprising a tank, a pump and a charging injector. The injection system of the present invention promotes increased speed, cooling and improved dispersion of the renewable charge in the inlet of the reactor.

Description

[0001] FIELD OF THE INVENTION

[0001] The present invention is within the field of Chemical and Materials Engineering and describes the co-processing of renewable material of lignocellulosic origin in delayed coking units (RCUs) for the generation of fuels with a lower carbon footprint by using existing refining units. BACKGROUND OF THE INVENTION

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

[0003] However, a target of net-zero CO2 emissions by 2050 or 2070 is essential to limit the global average temperature increase to below 2°C, with or without an implicit reliance on net-negative global CO2 emissions. Various regions are responding to this goal with different targets; for example, Europe and Colombia have committed to reductions of 40% and 20% by 2030, respectively, under the Paris Agreement.

[0004] Regarding liquid fuel-based emissions for the transportation sector, there are a number of options to achieve the target, from fuel efficiency and low-carbon fuels to electric / hybrid vehicles. Regarding low-carbon fuels, several technological options have been proposed to date to reduce CO2 emissions during petroleum production and refining. However, end-use accounts for approximately 80% of total life-cycle emissions.

[0005] Liquid fuels, therefore, still need to achieve lower net fuel cycle emissions. A possible solution to this problem lies in the end use of fuels produced from sustainable biomass. In this regard, biofuels derived from lignocellulosic biomass have been developed for several decades and have attracted increasing attention due to the greenhouse gas emissions caused by fossil fuels.

[0006] Lignocellulosic biomass is an abundant and low-cost renewable material, as it is a residue from forestry or agribusiness. Pyrolysis of this material, regardless of the process employed (fast, slow, catalytic, or hydrothermal), produces pyrolysis oil, commonly called bio-oil, which has potential for use as a feedstock in refineries for the production of fuels and petrochemicals, leveraging existing processing units and thus requiring low investment for processing. However, these oils typically contain high concentrations of water, oxygenated organic compounds, and contaminants, posing challenges for their processing in oil refineries.

[0007] Delayed coking is a refining process based on the thermal conversion of residual petroleum fractions, typically Vacuum Residue (VRS), into lighter, higher-value liquid streams (naphthas and gas oils), which require hydrotreatment before being added to the refinery's fuel pool. This process also generates liquefied petroleum gas, fuel gas, and coke. Because it is a non-catalytic conversion process for residual petroleum fractions, delayed coking has the potential to process feedstocks from biomass pyrolysis, as it is not impacted by the loss of catalytic activity that contaminants present in this type of feedstock can cause. STATE OF THE ART

[0008] Some State of the Art documents describe the processing of renewable material of lignocellulosic origin in delayed coking units for fuel generation, such as:

[0009] Patent document US8603325B2 describes the co-processing of bio-oil mixed with the feedstock of the Delayed Coking Unit, typically a RV, injected into the transfer line between the furnace and the reactor. According to the document, the coke formed has characteristics that facilitate reactor decoking, potentially reducing cycle time and increasing unit capacity. Additionally, patent document US9840671B2 refers to the co-processing of bio-oil mixed with vacuum residue, with the aim of reducing the coke yield compared to that generated from vacuum residues with high carbon residue. According to the document, the bio-oil is mixed with the fossil feedstock and sent to the unit's furnaces to heat the mixture to temperatures of around 500°C, providing sufficient energy for thermal cracking reactions to occur in the coke reactors.

[0010] However, as revealed in the State of the Art, it is widely known that bio-oils obtained by different biomass pyrolysis processes (fast pyrolysis, slow pyrolysis, catalytic pyrolysis, hydrothermal liquefaction) are unstable at high temperatures and cannot be heated beyond 80°C, since their molecules are constituted by different reactive oxygenated functional groups that, at high temperatures (such as those existing in the coke ovens of the processes described in both patents) can react and polymerize, which increases 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, p. 264-276, 1988).Furthermore, according to the State of the Art processes, there is the possibility of accelerated coking and obstruction of the coke oven tubes or the transfer line between the oven and the reactor in a very short period of operation, which may make processing unfeasible as described in the patents above.

[0011] The present invention, in turn, differs from both patents by proposing the use of an auxiliary feed system for injecting bio-oil and a gas stream through an inlet line at the top of the reactor, avoiding the passage of the renewable feed through the furnace tubes or the bottom region of the reactor, which has higher temperatures. The injection of a pressurized accelerator gas, which is mixed in-line with the bio-oil, aims to increase the inlet velocity of this material at the top of the reactor, preventing the accumulation of bio-oil polymerization products in the line and their consequent clogging. In addition to the accelerator gas, the addition of an organic solvent, with or without additives that improve reaction performance, mixed with the bio-oil in the tank or in-line, is also contemplated by the present invention.

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

[0013] However, the aforementioned document does not address the processing of distillation residual feedstocks rich in asphaltene molecules, with high carbon residue and metal content, such as vacuum residue or atmospheric residue, nor the co-processing of these feedstocks with renewable sources. Furthermore, the process described refers to fluid catalytic cracking technology, in which conversion reactions occur through thermal and catalytic effects, unlike delayed coking technology, in which the conversion of bottom feedstocks occurs thermally.

[0014] The scientific article, titled "BIO-OIL CO-PROCESSING CAN SUBSTANTIALLY CONTRIBUTE TO RENEWABLE FUEL PRODUCTION POTENTIAL AND MEET AIR QUALITY STANDARDS," reveals that the co-processing of crude bio-oil derived from lignocellulosic biomass in existing oil refineries represents a near-term greenhouse gas mitigation strategy, producing partially renewable, infrastructure-compatible hydrocarbon fuel with minimal capital requirements. The paper provides a quantitative assessment of changes in atmospheric emissions across a range of bio-oil co-processing fractions in refinery fluid catalytic cracking units.

[0015] Although it also refers to fluid catalytic cracking technology and co-processing of bio-oil with vacuum diesel, the aforementioned article does not use residual loads rich in asphaltenes and contaminants in these units according to the present invention.

[0016] Patent application US2010024283A1 discloses a process for producing bio-oil by delayed coking with modified feedstock, in which the conventional coking unit feed includes, in addition to the usual fresh hydrocarbon feed (vacuum residue, atmospheric residue, etc.), a biomass feed for co-processing. The document offers the possibility of directly using biomasses separately or mixed in any proportion in the delayed coking process. Furthermore, it is revealed that this feed can be made in the unit's fresh feed, in the coke drum during the reaction or quench stage (a hydrocarbon stream that reduces the effluent temperature), in the furnace inlet line, in the furnace outlet line, or in the coke drum outlet line.

[0017] However, the aforementioned document deals with the introduction of raw solid vegetable biomass into the coking reactor, in addition to first-generation vegetable oils, differing from the present invention with regard to overcoming the difficulties inherent in the co-processing of liquid vegetable biomass obtained from the pyrolysis of lignocellulosic materials, related to thermal and chemical instability.

[0018] The present invention provides advantages related to reducing coke yield and increasing liquid yield, increasing the profitability of Delayed Coking Units (RCUs). However, unlike the prior art, the present invention presents bio-oil processing in a way that does not compromise the operation of RCU furnaces, due to the injection of the material through the top of the reactor, generating less coke and less CO2.

[0019] The objective of the present invention is to contribute to mitigating various problems related to environmental pollution. Given the current demand for reducing greenhouse gas emissions generated by the burning of fossil fuels used in various modes of transportation, the present invention proposes the co-processing of renewable lignocellulosic material in UCRs, obtained from the pyrolysis of agroforestry residues, to generate fuels with a lower carbon footprint by utilizing existing refining units.

[0020] In view of the above, the present invention relates to the process of converting liquid plant biomass in a Delayed Coking Unit. Said process can be applied when it is desired to co-process liquid plant biomass with residual petroleum fractions to obtain streams with higher added value and a lower carbon footprint to, after hydrotreatment, produce fuels, with diesel being the main product. SUMMARY OF THE INVENTION

[0021] The present invention aims to co-process liquid plant biomass, preferably bio-oil, and vacuum residue (RV) by injecting liquid plant biomass through the top of the coke reactor. This avoids the problem of accelerated coking in the unit's furnace tubes when this type of unstable feedstock is injected mixed with the fossil feedstock at the furnace inlet. It also prevents clogging of the transfer line between the furnace and reactors when bio-oil is injected at the reactor inlet. In the present invention, the renewable feedstock is injected together with an accelerating gas through an appropriately sized injector to minimize the possibility of system clogging during injection, ensuring operational stability, preventing premature shutdowns, loss of efficiency, and unit profitability.An organic solvent, with or without additives, can be mixed with the renewable feedstock to enhance the thermal cracking reactions inside the reactor. BRIEF DESCRIPTION OF THE FIGURES.

[0022] To obtain a complete and total view of the objective of this invention, Figure 1 is presented as follows:

[0023] Figure 1 illustrates the interconnection of the elements of the present invention, in which: (1) represents the main load (fossil); (2) represents the mixture corresponding to the main load and the natural recycle; (3) represents the furnace; (4) represents the mixture (corresponding to the main load and the natural recycle) heated and partially vaporized; (5) represents the coking reactor; (6) represents the liquid vegetable biomass stream injected into the reactor; (7) represents the accelerating gas; (8) represents the organic vapors; (9) represents the fractionating tower, (10) represents the liquid fractions, (11) represents the process gas and (12) represents the coke, (13) represents the liquid vegetable biomass pump, (14) represents the liquid vegetable biomass stream sucked by the pump, (15) represents the liquid vegetable biomass tank, (16) represents the injector.

[0024] Figure 2 illustrates the same interconnection of the elements of the present invention shown in Figure 1, but with the representation of the in-line injection of an organic solvent (17), containing or not additives, which can be mixed with the renewable load to enhance the thermal cracking reactions inside the reactor.

[0025] Figure 3 illustrates the same interconnection of the elements of the present invention shown in Figure 1, but with the representation of the tank mixture (15) of an organic solvent (17), containing or not additives, to the renewable load, to enhance the thermal cracking reactions inside the reactor. DETAILED DESCRIPTION OF THE INVENTION

[0026] The present invention relates to a process for producing fuels from the co-processing of a renewable stream of lignocellulosic origin (liquid plant biomass) in delayed coking units. This process involves the co-processing of a liquid plant biomass produced by processing solid plant biomass from agro-industrial waste in pyrolysis or liquefaction units, and a fossil residual feedstock, such as vacuum residue (VRS), from the top of the coke reactor.

[0027] The process of the present invention can be described through the following steps: a. providing a liquid plant biomass (6) of lignocellulosic origin with a high lignin content and a stream of hydrocarbons from petroleum refining (1) (vacuum residue, atmospheric residue or other residual fraction from petroleum distillation); b. introducing the stream of hydrocarbons from petroleum refining (main (fossil) charge (1)) into the bottom of the fractionating tower (9), where this stream receives natural recycling, forming the combined charge that goes on to be heated in the ovens of the delayed coking unit (3), so that it reaches the process temperature necessary for thermal cracking reactions to occur inside the reactor (5); c.use the pump (13) that makes up the auxiliary loading system to send the renewable load (bio-oil) (6) from the tank (15) of the auxiliary loading system to the top of the delayed coking reactor (5) together with a gaseous stream (accelerator gas) (7), passing the mixture through the injector (16) under suitable conditions to avoid obstruction problems in the line and at the reactor inlet; d. subject the loads to thermal cracking reaction conditions; e. the generated organic vapors (8) proceed to the fractionating tower (9), generating liquid fractions (10) and process gas (11), which proceed to separation into hydrocarbon streams with different boiling point ranges; f. subject the liquid hydrocarbon streams in the naphtha and light and medium gas oil ranges to the hydrotreatment stage, obtaining hydrogenated liquid products with renewable content; and g. remove the coke (12) from the reactor to obtain green petroleum coke with renewable content.

[0028] According to Figure 1, in this process, the main charge (1) is preheated at the bottom of the fractionating tower (9). The mixture corresponding to the main charge and the natural recycle (2) is subsequently heated to temperatures between 490°C and 510°C in the unit's furnace (3). The natural recycle consists of the heavier hydrocarbons produced by the thermal cracking of the charge in the reactor. These hydrocarbons are condensed at the bottom of the fractionating tower, being incorporated into the unit's fresh charge (main charge), and the mixture is heated in the furnaces. The heated and partially vaporized mixture (4) is sent to the bottom of the delayed coking reactor (5), which is generally at temperatures between 470 and 490°C. The renewable charge (6) and the accelerator gas (7) are injected through the top of the reactor (5) at temperatures below 60°C.The thermal cracking and coking reactions of fossil and renewable feedstocks occur at high temperatures inside the reactor (400 to 500ºC), generating organic vapors (8) and coke (12). The coke (12) remains in the reactor until the main feedstock is switched to another empty reactor, and the vapors (8) go to the fractionating tower (9), generating liquid fractions (10) and process gas (11), which are then sent for treatment.

[0029] To demonstrate the potential of the aforementioned process, the present invention will be described in more detail in terms of the steps performed and their respective parameters.

[0030] Liquid plant biomass (bio-oil) from fast pyrolysis, slow pyrolysis, catalytic pyrolysis, and hydrothermal liquefaction processes is a thermally unstable product composed of molecules containing different oxygenated functional groups that can interact chemically when heated above 80°C. Therefore, adding bio-oil at the top of the reactor would initially lead to difficulties related to the possibility of clogging the line at the reactor inlet, since the usual top temperature inside such reactors is around 440°C.

[0031] In this sense, the present invention proposes the use of an auxiliary loading system for the injection of bio-oil and an accelerating gas, consisting of a tank, a pump, and a loading injector. The bio-oil and gas flow rates must be controlled by appropriate flow controllers to maintain process stability.

[0032] The injection of a pressurized accelerating gas—e.g., nitrogen, carbon dioxide, process gas, etc.—mixed inline with the bio-oil aims to increase the inflow velocity of this material into the reactor to a range between 2 and 8 m / s, preventing the accumulation of bio-oil polymerization products in the line and consequent clogging. The injection of this gas also promotes the dispersion of the bio-oil within the reactor, facilitating the distribution of the material in the reactor sections transverse to the flow, in addition to promoting the cooling of the injector within the reactor, hindering the polymerization of the bio-oil molecules at the injection point due to the high system temperatures.

[0033] Therefore, the injection system of the present invention contemplates the reduction of the injector diameter in the proportion of 0.2 to 0.7 in relation to the diameter of the bio-oil feed line in order to increase the velocity at the reactor inlet. The accelerator gas is injected at a percentage in the range of 0.5% m / m to 10% m / m in relation to the total load flow rate of the unit.

[0034] After being injected under appropriate velocity conditions, the bio-oil stream is subjected to the reaction conditions of the process in the top region of the reactor, i.e., temperatures between 400°C and 500°C and gauge pressure between 0.2 and 5 kgf / cm2. In the delayed coking stage, the 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 reactors in the range of 10 kPa to 500 kPa, (iii) recycle ratio in the range of zero and 50% v / v and (iv) cycle time in the range of 10 to 50 hours.

[0035] The vapors resulting from the cracking of bio-oil molecules, together with the vapors from the thermal cracking of the fossil fuel stream, are fractionated and produce liquid products with renewable content, while radicals from heavy lignocellulosic fragments undergo polymerization and coking, forming the coke bed inside the reactor.

[0036] The product yield profile is more favorable when bio-oil is added to the top of the reactor than when it is processed in a mixture with RV, since there is less coke formation and more liquid, even when the processed RV has a relatively low carbon residue. Furthermore, bio-oil, when added to the top of the reactor, can help control the foam generated by thermal cracking reactions due to its aromatic character, acting as an antifoaming agent, replacing or blending with conventional antifoams.

[0037] This process also provides lower CO2 generation when bio-oil is injected into the top of the reactor, compared to the usual injection mixed with RV at the bottom of the reactor.

[0038] To demonstrate the potential of the present invention, the embodiments listed above will be described in more detail through examples of embodiment, as well as the results obtained. It should be noted that the following description is intended solely to elucidate the understanding of the proposed invention and to disclose, in even greater detail, the embodiment of the invention without limiting it. Therefore, variables similar to the examples are also encompassed within the scope of the invention. EXAMPLES OF EMBODIMENT

[0039] The invention can be applied in delayed coking units when it is desired to co-process liquid lignocellulosic biomass (bio-oil) with residual petroleum fractions (RV) to obtain streams with higher added value and lower carbon footprint to, after hydrotreatment, produce fuels, with diesel being the main product. EXAMPLE 1

[0040] Slow pyrolysis bio-oil, whose characterization is presented in Table 1, was injected at a rate of 10% w / w relative to the load of a continuous pilot unit with an average flow rate of 2.3 kg / h. Bio-oil injection was performed 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 was maintained at 440°C, and the average operating pressure was 1.8 kgf / cm 2. The feed characterization is presented in Table 2 and the gas, liquid and coke yields are presented in Table 3. Table 1: Bio-oil characterization Table 2: Characterization of vacuum residue

[0041] To reduce the effect of the accelerating gas injected at the top of the reactor on product yield, pure RV was processed in the presence of N2, injected under the same conditions used for coprocessing with bio-oil. A reduction in coke yield and an increase in the produced liquid yield were observed. Table 3: Yields (% w / w) obtained in a pilot plant

[0042] This made it possible to process bio-oil continuously without the need to heat it in a mixture with the main fossil fuel, avoiding problems of accelerated coking in the furnace and equipment clogging due to the thermal instability of the bio-oil. EXAMPLE 2

[0043] Runs were conducted in the laboratory to evaluate different methods of adding bio-oil to a vacuum residue: top-loading and blending with RV. Proportions of 5 and 10% w / w of bio-oil relative to the charge mass (corresponding to approximately 380 g of RV, previously loaded into the reactor) were evaluated for both addition methods. The reactor was heated from room temperature to 500°C. For top-loading, the entire mass of bio-oil at room temperature was added when the temperature inside the reactor reached approximately 440°C, maintaining heating until 500°C. For blended addition, the bio-oil mass was added to the RV contained in the reactor, both at room temperature, and heated to 500°C. In both addition methods, the run was completed 60 minutes after the system reached the established temperature (500°C). The average operating pressure of the system was maintained at 1.8 kgf / cm2 .

[0044] The results showed lower coke yield, higher liquid yield, and lower CO2 generation when bio-oil is injected through the top of the reactor, compared to the mixture with RV, as shown in Tables 4 and 5. Table 4: Yields (% w / w) obtained from different bio-oil injection modes in a batch laboratory unit

[0002] Table 5: Gas composition (% w / w) obtained from different bio-oil injection modes in a batch laboratory unit

[0045] Batch tests confirmed the various advantages of injecting bio-oil through the top of the reactor, compared to processing in a mixture with the delayed coking unit load.

[0046] Those skilled in the art will appreciate the knowledge presented herein and will be able to reproduce the invention in the presented embodiments and in other variants, covered by the scope of the attached claims.

Claims

CLAIMS 1. Process for producing fuels from the co-processing of a renewable stream of lignocellulosic origin in delayed coking units, characterized by comprising the following steps: a. providing a liquid plant biomass (6) of lignocellulosic origin with a high lignin content and a stream of hydrocarbons from petroleum refining (1) (vacuum residue, atmospheric residue or other residual fraction from petroleum distillation); b. introducing the stream of hydrocarbons from petroleum refining (main (fossil) charge (1)) into the bottom of the fractionating tower (9), where it receives the natural recycle, forming the combined charge that goes on to be heated in the furnaces of the delayed coking unit (3), to reach the process temperature necessary for thermal cracking reactions to occur inside the reactor (5); c.use the pump (13) that makes up the auxiliary loading system to send the renewable load (bio-oil) (6) from the tank (15) of the auxiliary loading system to the top of the delayed coking reactor (5), together with a gaseous stream (accelerator gas) (7), passing the mixture through the injector (16) under suitable conditions to avoid obstruction problems in the line and at the reactor inlet; d. subject the loads to thermal cracking reaction conditions; e. the generated organic vapors (8) go to the fractionating tower (9), generating liquid fractions (10) and process gas (11), which go on to be separated into hydrocarbon streams with different boiling point ranges;. f. subjecting liquid hydrocarbon streams in the naphtha and light and medium gas oil ranges to the hydrotreatment step, obtaining hydrogenated liquid products with renewable content; and g. removing the coke (12) from the reactor to obtain green petroleum coke with renewable content.

2. Process according to claim 1, characterized by the fact that the liquid vegetable biomass is of lignocellulosic origin with a high lignin content, with at least 10% by mass.

3. Process according to claim 1, characterized by the fact that the mixture corresponding to the main charge and the natural recycle (2) is heated to temperatures between 490-510°C in the furnace of the unit (3).

4. Process according to claim 1 or 2, characterized by the fact that the liquid vegetable biomass is produced from the processing of solid vegetable biomass originating from agro-industrial waste in pyrolysis or liquefaction units. 5.Process according to claim 1 or 2, characterized in that the liquid plant biomass is preferably bio-oil.

6. Process according to claim 1 or 2, characterized in that the liquid plant biomass corresponds to the proportion between 0.10% m / m and 50% m / m in relation to the total load of the delayed coking reactor.

7. Process according to claim 1, characterized in that the selected hydrocarbon streams are preferably residues from petroleum distillation, either atmospheric or distillation. vacuum, with an initial boiling point above 400°C.

8. Process, according to claim 1, characterized by the fact that step (c) can use a bio-oil charge in conjunction with an organic solvent containing or not additives dispersed in the organic phase to improve the reaction performance of the system.

9. Process, according to claim 8, characterized by the fact that the organic solvent can be constituted by methanol, ethanol, acetone, among other polar solvents or mixture of solvents, and the additives dispersed in the organic solvent can be constituted by metal oxides, such as iron oxide, zinc oxide, titanium oxide, tungsten oxide, among other oxides or mixtures of oxides.

10. Process, according to claim 1, characterized by the fact that step (c) uses an auxiliary charging system for injecting the liquid plant biomass charge and a gaseous stream, composed of a tank, pump and charging injector. 11.Process, according to claim 1, characterized by the fact that the injection of a pressurized accelerating gas selected from nitrogen, carbon dioxide, process gas, among others, is mixed in line with the bio-oil.

12. Process, according to claim 11, characterized by the fact that the injection of the accelerating gas disperses the bio-oil inside the reactor, promoting an entry velocity of this material into the reactor between 2 and 8 m / s.

13. Process, according to claim 10, characterized by the fact that the injector diameter is reduced in the proportion between 0.2 and 0.7 in relation to the diameter of the bio-oil feed line.

14. Process, according to claim 1, characterized by the fact that in step (c) the renewable charge (6) and the acceleration gas (7) are injected at temperatures below 60°C through the top of the coke reactor that is at temperatures between 400 and 500°C and a gauge pressure between 0.2 and 5 kgf / cm2, generating organic vapors (8) and coke (12) with renewable content.

15. Process, according to claim 1, characterized by the fact that the fuel obtained from the liquid fraction (10) of the fractionation of the organic vapors (8) is preferably diesel.

16. Process, according to claim 1, characterized by the fact that the conditions in the step related to delayed coking are: furnace outlet temperature in the range of 490°C to 510°C, top gauge pressure of the reactors in the range of 10 kPa to 500 kPa, recycle ratio in the range of zero and 50% v / v, cycle time in the range of 10 to 50 hours.

17. Process, according to claim 1 or 11, characterized by the fact that the acceleration gas is injected at a percentage in the range of 0.5% m / m to 10% m / m in relation to the total load flow rate of the unit. 18.Process, according to claim 1, characterized by the fact that a lower coke yield, higher liquid yield, and lower CO2 generation are obtained when the bio-oil is injected through the top of the reactor, in. relation to the mixture with vacuum residue. 5

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