A method and system for producing calcined petroleum coke in a delayed coking process

Abstract

The present application belongs to the field of metallurgy, material and chemical industry, and relates to a method and system for preparing calcined petroleum coke by a coking process in a coking reactor. The method for preparing calcined petroleum coke by the coking process in the coking reactor comprises the following steps: rapidly heating residual oil to 600-800 DEG C, introducing a reducing gas for desulfurization reaction, continuously heating for high-temperature reaction after the desulfurization reaction is completed, and taking out calcined petroleum coke and an oil-gas mixture after cooling. The oil-gas mixture is subjected to fractionation to obtain gasoline, diesel and wax oil. The present application adopts a variable temperature system for desulfurization reaction and high-temperature reaction in the coking reactor, and has a simple process flow, and can easily obtain high-quality calcined petroleum coke with low sulfur content, high particle stability, small amount of powder coke, large true density and high graphitization degree.

Description

Technical Field

[0001] This invention belongs to the fields of metallurgy, materials and chemical engineering, and relates to a method and system for preparing calcined petroleum coke by batch coking process. Background Technology

[0002] Petroleum coke, characterized by its low volatile matter content and high fixed carbon content, is widely used in metallurgy, materials science, and chemical industries. However, the decline in crude oil quality leads to an increase in the sulfur content of petroleum coke, a major byproduct of crude oil refining, exacerbating the pressure on downstream enterprises using petroleum coke as a raw material to control sulfur emissions. Therefore, exploring efficient and economical technologies for removing sulfur from crude oil refining residues is of great significance in alleviating the pressure on downstream enterprises to reduce sulfur emissions.

[0003] Sulfur in petroleum coke is mainly composed of organic sulfur, among which thiophenes and their derivatives are the most difficult to remove. Current research on thiophene removal from petroleum coke includes alkali metal desulfurization, high-temperature calcination desulfurization, and hydrodesulfurization. However, high-temperature calcination and hydrocatalytic desulfurization methods require large amounts of energy and expensive equipment and materials, resulting in high desulfurization costs. Therefore, it is necessary to develop a highly efficient, economical technology for producing low-sulfur petroleum coke that is less likely to generate secondary pollution.

[0004] When raw petroleum coke is used in graphite electrodes for steelmaking or in anode paste (molten electrodes) for aluminum and magnesium production, it must be calcined to meet the requirements. Calcinated petroleum coke is the product of high-temperature calcination of petroleum coke. Calcination of petroleum coke is an important step in carbon production, involving high-temperature calcination under air-isolated conditions. Its purpose is to remove volatiles, moisture, and some sulfur from the petroleum coke, improving its true density, resistivity, strength, coefficient of thermal expansion, and chemical stability. During calcination, as volatiles escape from the petroleum coke, its macroscopic structure and microstructure undergo significant changes, resulting in improved physical and chemical properties.

[0005] Existing technologies all involve first preparing petroleum coke, and then calcining it to obtain the final product. For example, existing technology CN112408357A relates to a calcination process for petroleum coke, including the following steps: first, the petroleum coke is crushed and dried; then, the dried petroleum coke is irradiated with microwaves for a period of time; next, the petroleum coke is extracted using a composite extractant to obtain pre-treated petroleum coke; finally, the pre-treated petroleum coke is calcined to obtain desulfurized petroleum coke. This invention first crushes and grinds the petroleum coke to fully expose the sulfur-containing structures in the petroleum coke, ensuring the smooth progress of the desulfurization reaction. Microwave treatment of the petroleum coke allows it to dissolve better in the composite extractant. The composite solvent and petroleum coke are mixed to extract and desulfurize the petroleum coke, and the pre-treated petroleum coke is then calcined at high temperature to obtain low-sulfur petroleum coke. However, the petroleum coke prepared in this way has a large amount of coke powder and poor stability. Summary of the Invention

[0006] The purpose of this invention is to provide a method and system for preparing calcined petroleum coke using a batch coking process, so as to obtain high-quality calcined petroleum coke with excellent comprehensive performance.

[0007] To solve the above-mentioned technical problems, the technical solution of the present invention is as follows:

[0008] A method for preparing calcined petroleum coke using a batch coking process includes the following steps:

[0009] The residual oil is rapidly heated to 600-800℃, and a reducing gas is introduced to carry out a desulfurization reaction. After the desulfurization reaction is completed, heating is continued to carry out a high-temperature reaction. After cooling, the oil is taken out to obtain calcined petroleum coke and an oil-gas mixture. The oil-gas mixture is fractionated to obtain gasoline, diesel and wax oil.

[0010] Conventional reductive desulfurization of residual oil occurs at temperatures below 300-500℃. However, at low temperatures, large amounts of catalysts are required to accelerate the desulfurization rate. Using catalysts results in low desulfurization efficiency and can easily cause secondary pollution. This invention performs desulfurization at 600-800℃ without adding a catalyst. At this temperature, sulfides in the residual oil, existing in the form of simple sulfides, thiols, and sulfones, are easily removed by reduction reactions with reducing gases, resulting in excellent desulfurization. It also prevents sulfur from accumulating in the calcined petroleum coke and transforming into more complex thiophene-like sulfur compounds that are intercalated with aromatic carbons and difficult to remove during subsequent high-temperature reactions. Furthermore, at this temperature, the intermediate products after desulfurization experience increased hardness, which contributes to improving the hardness of the calcined petroleum coke.

[0011] Preferably, the residue oil is one or more of heavy oil, vacuum residue, and cracked residue oil.

[0012] Preferably, the reaction apparatus is a coking reactor.

[0013] Preferably, the coking reactor is heated by direct heating, which has a strong heating capacity and can quickly heat the material to a high temperature of 1300°C.

[0014] Preferably, the reducing gas is H2 or ammonia, and more preferably hydrogen.

[0015] Preferably, the flow rate of the reducing gas is 5-12 L / h, and the introduction time is 10-30 min.

[0016] Using hydrogen as a reducing gas for desulfurization has advantages such as high desulfurization efficiency, wide applicability of raw materials, and mild reaction conditions. The amount of hydrogen introduced affects the reaction rate, desulfurization effect, and product quality. Too little hydrogen leads to incomplete desulfurization and a slow reaction rate, while too much hydrogen can increase the reaction rate within a certain range, but it will increase energy consumption and cost.

[0017] Preferably, the high-temperature reaction temperature inside the calcination equipment is 1150-1300℃.

[0018] Calcination of the raw materials removes volatiles, causing them to shrink in volume, increase in density, and improve strength, while also achieving better thermal stability. During calcination, the molecular structure of the petroleum coke also changes, and as it undergoes continuous pyrolysis and condensation reactions, impurities such as hydrogen, oxygen, and sulfur are successively discharged, reducing chemical activity and stabilizing physicochemical properties. This results in high-quality calcined petroleum coke with excellent comprehensive properties, including low ash content, low volatile matter, low sulfur content, high strength, and low coke powder content.

[0019] If the calcination temperature is too low during the high-temperature reaction, impurities in the petroleum coke cannot be completely volatilized, resulting in excessive impurities. Furthermore, the petroleum coke does not shrink sufficiently, leading to inadequate pyrolysis and condensation reactions. This can cause deformation of the product during roasting and graphitization, affecting product quality. Conversely, if the calcination temperature is too high, the shrinkage rate of the raw product during roasting and graphitization is small, with shrinkage relying solely on the binder. This results in a porous product with low bulk density and mechanical strength. In addition, high temperatures increase the size of crystals in the coke, leading to increased brittleness and a higher susceptibility to cracking and fracture.

[0020] Preferably, the high-temperature reaction time in the calcination equipment is 2-4 hours.

[0021] If the calcination time is too short, the petroleum coke may not be fully calcined, and its physicochemical properties will not be significantly improved, resulting in lower density and strength. If the calcination time is too long, its crystal structure will change, causing cracks or fractures, reducing the mechanical strength and properties of the petroleum coke. Furthermore, excessively long calcination times also lead to energy waste and reduced production efficiency.

[0022] Preferably, the calcined petroleum coke has a sulfur content of <1%, a coke powder content of <30%, and a particle stability of >80%.

[0023] A system for preparing calcined petroleum coke using a batch coking process includes:

[0024] Coking feedstock storage device: It is used to store coking feedstock;

[0025] Reaction apparatus: It is used for desulfurization and coking reactions of coking raw materials;

[0026] Reducing gas storage device: It is used to store reducing gases;

[0027] Fractionation unit: It is used to receive oil and gas after high-temperature reaction and separate reducing gases;

[0028] The coking raw material storage device is connected in sequence to the reaction device and the fractionation device; the reducing gas storage device is connected to the reaction device; and the outlet of the fractionation device is connected to the reaction device.

[0029] Coking feedstock is transported from the coking feedstock storage unit to the reaction unit for desulfurization and high-temperature reactions. The resulting solid, after cooling, is calcined petroleum coke. The tail gas is transported to a fractionation unit for separation, separating reducing gases and other gases. The reducing gases are returned to the reaction unit, while other gases, such as low-molecular-weight hydrocarbons and low-molecular-weight fuel oils, are fractionated to obtain gasoline, diesel, and wax oil, which can be recovered as fuels. A reducing gas storage unit stores the reducing gases and transports them to the reaction unit via pipelines.

[0030] Preferably, the reaction apparatus is a coking reactor.

[0031] Preferably, the fractionation device is a fractionation tower.

[0032] Preferably, the cooling temperature of the solid after the high-temperature reaction is <50℃.

[0033] The present invention will be further explained below:

[0034] This invention prepares calcined petroleum coke using a batch coking process. By setting different temperature regimes, the coking raw materials undergo desulfurization and high-temperature reactions sequentially in the coking reactor. During the desulfurization stage, a reducing gas (H2) is introduced for desulfurization, utilizing the strong affinity between H and S atoms. At high temperatures, the introduction of hydrogen gas effectively removes sulfides (sulfides, thiols, sulfones, and thiophenes), resulting in excellent desulfurization. During high-temperature calcination, the petroleum coke forms a two-dimensional ordered carbon atom planar network, which gradually transforms into a three-dimensional ordered network, becoming increasingly ordered and dense. Simultaneously, volatile matter is removed and sulfur is discharged, resulting in high-quality calcined petroleum coke with low sulfur content, high particle stability, low coke powder content, high true density, and high graphitization degree.

[0035] The beneficial effects of this invention are as follows:

[0036] 1. The method for preparing high-quality calcined petroleum coke by the batch coking process of the present invention adopts a variable temperature regime for desulfurization reaction and high-temperature reaction in the coking reactor. The process is simple and can easily obtain high-quality calcined petroleum coke with low sulfur content, high particle stability, low amount of coke powder, high true density and high degree of graphitization.

[0037] 2. The method for preparing high-quality calcined petroleum coke using the batch coking process of the present invention involves rapidly carrying out a high-temperature reaction after the desulfurization reaction is completed, and the residual heat from the desulfurization reaction is directly used for the high-temperature reaction, thereby reducing heat loss and energy consumption.

[0038] 3. This invention uses H2 as a reducing gas to convert most of the sulfur in the residual oil into H2S gas. The excess H2 and H2S are treated to obtain H2, which is then sent to the coking reactor for desulfurization reaction, thus realizing the recycling of H2 and improving resource utilization.

[0039] 4. The process of this invention can produce calcined petroleum coke with excellent comprehensive performance in one step, which can be directly used as a raw material for carbon products.

[0040] 5. The method for preparing calcined petroleum coke of the present invention has a desulfurization rate of up to 99% and a calcined petroleum coke powder content of less than 30%, which has good application prospects. Attached Figure Description

[0041] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the accompanying drawings used in the description of the embodiments or the prior art will be briefly introduced below.

[0042] Figure 1 This is a diagram of the equipment used in the batch coking process of the present invention to prepare calcined petroleum coke.

[0043] Among them, 1-residue oil storage tank, 2-coking reactor, 3-hydrogen storage cylinder, 4-fractionation tower;

[0044] Figure 2 This is a process flow diagram of the present invention. Detailed Implementation

[0045] The following specific implementation examples further illustrate this point, but the present invention is not limited thereto. Any modifications, equivalent substitutions, or improvements made within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

[0046] like Figure 1 As shown, a system for preparing calcined petroleum coke using a batch coking process includes:

[0047] Coking feedstock storage device: It is used to store coking feedstock;

[0048] Calcination unit: It is used to receive coking raw materials and subject them to desulfurization and high-temperature reactions;

[0049] Reducing gas storage device: used for transferring reducing gases;

[0050] Fractionation unit: It is used to receive the tail gas after high-temperature reaction and separate reducing gases;

[0051] The coking raw material storage device is connected in sequence to the calcination device and the fractionation device; the reducing gas storage device is connected to the calcination device, and the gas outlet of the fractionation device is connected to the calcination device.

[0052] Coking feedstock is transported from the coking feedstock storage unit to the calcination unit for desulfurization and high-temperature reaction, resulting in calcined petroleum coke after cooling. The tail gas is transported to the fractionation unit for separation, separating reducing gases and other gases. The reducing gases are transported to the calcination unit via pipeline, while the other gases are treated before being discharged. A reducing gas storage unit delivers the reducing gases to the calcination unit.

[0053] The calcination device is a coking reactor, the fractionation device is a fractionation tower, and the reducing gas storage device is a hydrogen storage cylinder, with hydrogen as the reducing gas.

[0054] Example 1

[0055] Such as process flow Figure 2 As shown, atmospheric residue oil is pumped into a coking reactor for desulfurization and high-temperature reactions. First, the temperature is rapidly increased to the desulfurization temperature (700℃), and hydrogen is introduced at a flow rate of 5 L / h for 10 minutes. Immediately after 10 minutes, the temperature is rapidly increased again for the high-temperature reaction stage: calcination at 1150℃ for 2 hours. After the coking reaction, the residue in the coking reactor is cooled to <50℃ before being removed to obtain calcined petroleum coke. Testing revealed an ash content of 0.45%, a sulfur content of 0.74%, a volatile matter content of 1.18%, a coke powder content (0-8 mm) of 27.87%, and a particle stability of 81.56%.

[0056] Example 2

[0057] Such as process flow Figure 2As shown, atmospheric residue oil is pumped into a coking reactor for desulfurization and high-temperature reactions. During the desulfurization stage, the desulfurization temperature is 800℃, hydrogen is introduced at a flow rate of 5 L / h for 10 min. During the high-temperature reaction stage, the calcination temperature is 1150℃ for 2 h. After the coking reaction, the residue in the coking reactor is cooled to <50℃ before being removed to obtain calcined petroleum coke. Testing revealed an ash content of 0.42%, a sulfur content of 0.55%, a volatile matter content of 1.09%, a coke powder content (0-8 mm) of 26.98%, and a particle stability of 82.13%.

[0058] Example 3

[0059] Such as process flow Figure 2 As shown, atmospheric residue oil is pumped into a coking reactor for desulfurization and high-temperature reactions. During the desulfurization stage, the desulfurization temperature is 400℃, hydrogen is introduced at a flow rate of 5 L / h for 10 min. During the high-temperature reaction stage, the calcination temperature is 1150℃ for 2 h. After the coking reaction, the residue in the coking reactor is cooled to <50℃ before being removed to obtain calcined petroleum coke. Testing revealed an ash content of 0.87%, a sulfur content of 2.21%, a volatile matter content of 1.87%, a coke powder content (0-8 mm) of 31.78%, and a particle stability of 77.85%.

[0060] Example 4

[0061] Such as process flow Figure 2 As shown, atmospheric residue oil is pumped into a coking reactor for desulfurization and high-temperature reactions. During the desulfurization stage, the desulfurization temperature is 1150℃, and hydrogen gas is introduced at a flow rate of 5 L / h for 10 minutes. After 10 minutes, the hydrogen introduction is stopped, and the high-temperature reaction stage begins: calcination temperature is 1150℃ for 2 hours. After the coking reaction is completed, the residue in the coking reactor is cooled to <50℃ before being removed to obtain calcined petroleum coke. Testing revealed an ash content of 0.61%, a sulfur content of 0.82%, a volatile matter content of 0.87%, a coke powder content (0-8 mm) of 29.98%, and a particle stability of 79.32%.

[0062] Example 5

[0063] Such as process flow Figure 2As shown, atmospheric residue oil is pumped into a coking reactor for desulfurization and high-temperature reactions. During the desulfurization stage, the desulfurization temperature is 800℃, hydrogen is introduced at a flow rate of 1L / h for 10 minutes. During the high-temperature reaction stage, the calcination temperature is 1150℃ for 2 hours. After the coking reaction, the residue in the coking reactor is cooled to <50℃ before being removed to obtain calcined petroleum coke. Testing revealed an ash content of 0.73%, a sulfur content of 1.56%, a volatile matter content of 1.12%, a coke powder content (0-8mm) of 31.11%, and a particle stability of 79.75%.

[0064] Example 6

[0065] Such as process flow Figure 2 As shown, atmospheric residue oil is pumped into a coking reactor for desulfurization and high-temperature reactions. During the desulfurization stage, the desulfurization temperature is 800℃, hydrogen is introduced at a flow rate of 25 L / h for 10 min. During the high-temperature reaction stage, the calcination temperature is 1150℃ for 2 h. After the coking reaction, the residue in the coking reactor is cooled to <50℃ before being removed to obtain calcined petroleum coke. Testing revealed an ash content of 0.40%, a sulfur content of 0.39%, a volatile matter content of 0.97%, a coke powder content (0-8 mm) of 25.11%, and a particle stability of 83.01%.

[0066] Example 7

[0067] Such as process flow Figure 2 As shown, atmospheric residue oil is pumped into a coking reactor for desulfurization and high-temperature reaction. During the desulfurization stage, the desulfurization temperature is 800℃, hydrogen is introduced at a flow rate of 10L / h for 10min. During the high-temperature reaction stage, the calcination temperature is 1150℃ for 2h. After the coking reaction, the residue in the coking reactor is cooled to <50℃ before being removed to obtain calcined petroleum coke. Testing shows that the ash content is 0.41%, the sulfur content is 0.43%, the volatile matter content is 1.01%, the 0-8mm coke powder content is 25.89%, and the particle stability is 82.99%.

[0068] Example 8

[0069] Such as process flow Figure 2As shown, atmospheric residue oil is pumped into a coking reactor for desulfurization and high-temperature reactions. During the desulfurization stage, the desulfurization temperature is 800℃, hydrogen is introduced at a flow rate of 5 L / h for 2 minutes. During the high-temperature reaction stage, the calcination temperature is 1150℃ for 2 hours. After the coking reaction, the residue in the coking reactor is cooled to <50℃ before being removed to obtain calcined petroleum coke. Testing revealed an ash content of 0.64%, a sulfur content of 2.34%, a volatile matter content of 1.37%, a coke powder content (0-8 mm) of 34.31%, and a particle stability of 77.31%.

[0070] Example 9

[0071] Such as process flow Figure 2 As shown, atmospheric residue oil is pumped into a coking reactor for desulfurization and high-temperature reactions. During the desulfurization stage, the desulfurization temperature is 800℃, hydrogen is introduced at a flow rate of 5 L / h for 40 min. During the high-temperature reaction stage, the calcination temperature is 1150℃ for 2 h. After the coking reaction, the residue in the coking reactor is cooled to <50℃ before being removed to obtain calcined petroleum coke. Testing revealed an ash content of 0.56%, a sulfur content of 0.51%, a volatile matter content of 0.95%, a coke powder content (0-8 mm) of 25.31%, and a particle stability of 83.43%.

[0072] Example 10

[0073] Such as process flow Figure 2 As shown, atmospheric residue oil is pumped into a coking reactor for desulfurization and high-temperature reactions. During the desulfurization stage, the desulfurization temperature is 800℃, hydrogen is introduced at a flow rate of 10 L / h for 30 min. During the high-temperature reaction stage, the calcination temperature is 1300℃ for 2 h. After the coking reaction, the residue in the coking reactor is cooled to <50℃ before being removed to obtain calcined petroleum coke. Testing revealed an ash content of 0.29%, a sulfur content of 0.30%, a volatile matter content of 0.78%, a coke powder content (0-8 mm) of 21.34%, and a particle stability of 87.41%.

[0074] Example 11

[0075] Such as process flow Figure 2As shown, atmospheric residue oil is pumped into a coking reactor for desulfurization and high-temperature reactions. During the desulfurization stage, the desulfurization temperature is 800℃, hydrogen is introduced at a flow rate of 10 L / h for 30 min. During the high-temperature reaction stage, the calcination temperature is 800℃ for 30 min. After the coking reaction, the residue in the coking reactor is cooled to <50℃ before being removed to obtain calcined petroleum coke. Testing revealed an ash content of 0.74%, a sulfur content of 0.45%, a volatile matter content of 0.98%, a coke powder content (0-8 mm) of 35.89%, and a particle stability of 69.76%.

[0076] Example 12

[0077] Such as process flow Figure 2 As shown, atmospheric residue oil is pumped into a coking reactor for desulfurization and high-temperature reactions. During the desulfurization stage, the desulfurization temperature is 800℃, hydrogen is introduced at a flow rate of 10 L / h for 30 min. During the high-temperature reaction stage, the calcination temperature is 1300℃ for 4 h. After the coking reaction, the residue in the coking reactor is cooled to <50℃ before being removed to obtain calcined petroleum coke. Testing revealed an ash content of 0.22%, a sulfur content of 0.28%, a volatile matter content of 0.46%, a coke powder content (0-8 mm) of 19.76%, and a particle stability of 90.32%.

[0078] Example 13

[0079] Such as process flow Figure 2 As shown, atmospheric residue oil is pumped into a coking reactor for desulfurization and high-temperature reactions. During the desulfurization stage, the desulfurization temperature is 800℃, hydrogen is introduced at a flow rate of 10 L / h for 30 min. During the high-temperature reaction stage, the calcination temperature is 1400℃ for 9 h. After the coking reaction, the residue in the coking reactor is cooled to <50℃ before being removed to obtain calcined petroleum coke. Testing revealed an ash content of 0.26%, a sulfur content of 0.27%, a volatile matter content of 0.51%, a coke powder content (0-8 mm) of 29.32%, and a particle stability of 74.56%.

[0080] Comparative Example 1

[0081] The residual oil is pumped into a heating furnace, where it flows at high speed and is heated to 480-510℃. It is then rapidly fed into a coking tower for coking, which takes 30 hours. After coking, the oil is cooled and discharged to obtain petroleum coke. The resulting petroleum coke is then sent to a carbon company for calcination in a tank-type calciner at 1250℃ for 10 hours. After cooling, the calcined petroleum coke is obtained. Testing revealed an ash content of 0.67%, a sulfur content of 1.23%, a volatile matter content of 1.65%, a coke powder content (0-8mm) of 30.01%, and a particle stability of 79.34%.

[0082] Table 1. Parameters of calcined petroleum coke in Examples 1-13

[0083]

[0084] As shown in Table 1, Examples 3-4 demonstrate that both excessively high and low desulfurization temperatures have a significant impact on desulfurization. Examples 5-6 illustrate instances of excessively low and high hydrogen flow rates, respectively. Example 5 shows that insufficient hydrogen flow affects the desulfurization effect, failing to provide the required amount of hydrogen for the reaction, resulting in low sulfur content in the calcined petroleum coke. Conversely, excessive hydrogen flow does not achieve a significant further desulfurization effect and results in excessive energy consumption and cost increases. Examples 8-9 illustrate the impact of hydrogen flow time. Short flow time leads to insufficient desulfurization, resulting in high sulfur content in the calcined petroleum coke. Long flow time results in excessive hydrogen flow, failing to significantly reduce sulfur content and causing energy waste and excessive cost increases. Example 11 shows that both excessively low calcination temperature and excessively short calcination time affect the mechanical strength and coke powder content of the calcined petroleum coke. Excessively low temperature and insufficient calcination time lead to incomplete pyrolysis and condensation reactions within the petroleum coke, resulting in a large amount of coke powder and low strength. Example 13 shows that excessively high calcination temperature and excessively long calcination time did not improve the overall performance of the calcined petroleum coke. Excessively high temperature led to high energy consumption and shortened equipment lifespan. Comparative Example 1 shows calcined petroleum coke produced by the current segmented coking and calcination process, which has high sulfur content, high volatile matter, and low strength.

[0085] Example 12 showed the best results, with the calcined petroleum coke having a low sulfur content of 0.28%, a coke powder content of 19.76% (0-8mm), and a particle stability as high as 90.32%. This indicates that hydrodesulfurization at 800℃ has a significant desulfurization effect. During high-temperature calcination, the carbon atoms reconnect and the aromatic rings rearrange, which greatly improves the particle stability and graphitization degree of the calcined petroleum coke. The high particle stability indicates that the calcined petroleum coke has high strength and good mechanical properties.

[0086] In summary, the method of this invention can yield calcined petroleum coke products with excellent overall performance, providing a new path for the production of high-quality calcined petroleum coke.

Claims

1. A method for preparing calcined petroleum coke using a batch coking process, characterized in that, Includes the following steps: The residual oil is rapidly heated to 600-800℃, and a reducing gas is introduced to carry out a desulfurization reaction. After the desulfurization reaction is completed, heating is continued for a high-temperature reaction. After cooling, the residue is removed to obtain calcined petroleum coke and an oil-gas mixture. The oil-gas mixture is fractionated to obtain gasoline, diesel, and wax oil. No catalyst is added during the desulfurization reaction. The reducing gas is H2 or ammonia; The high-temperature reaction time is 2-4 hours; The temperature of the high-temperature reaction is 1150-1300℃; The flow rate of the reducing gas is 5-15 L / h, and the introduction time is 10-30 min.

2. The method according to claim 1, characterized in that, The residue oil is one or more of heavy oil, vacuum residue oil, and cracked residue oil, and the reaction device is a coking reactor.

3. The method according to claim 1, characterized in that, The reducing gas is hydrogen.

4. The method according to any one of claims 1-3, characterized in that, The calcined petroleum coke has a sulfur content of <1%, a coke powder content of <30%, and a particle stability of >80%.

5. A system for implementing the batch coking process for preparing calcined petroleum coke according to any one of claims 1-4, characterized in that, include: Coking feedstock storage device: It is used to store coking feedstock; Reaction apparatus: It is used for desulfurization and coking reactions of coking raw materials; Reducing gas storage device: It is used to store reducing gases; Fractionation unit: It is used to receive oil and gas after high-temperature reaction and separate reducing gases; The coking raw material storage device is connected in sequence to the reaction device and the fractionation device; the reducing gas storage device is connected to the reaction device; and the outlet of the fractionation device is connected to the reaction device.

6. The system according to claim 5, characterized in that, The reaction apparatus is a coking reactor; the fractionation apparatus is a fractionation tower.

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