Process condition simulation method and simulation device for regulating and controlling dry quenching burn-out rate

Abstract

The invention relates to a process condition simulation method and simulation device for regulating and controlling the burn-out rate of dry quenching. The method comprises the following steps: setting the temperature rise time in a simulation reaction to be equal to the cooling time of coke in a dry quenching furnace in industrial production; the initial temperature is equal to the coke discharge temperature of a dry quenching furnace in industrial production; the volume flow rate of the mixed gas is determined by the volume space velocity of cooled circulating gas reacted with coke in the fixed bed in industrial production and the accumulation volume of a coke material in the simulated reaction; the concentration of reaction gas is equal to that of circulating gas in industrial production; the method comprises the following steps: placing a coke material in a constant-temperature area of a reaction section, heating to an initial temperature, recording the mass, then introducing a mixed gas of a reaction gas and an inert gas, heating to a red coke temperature from the initial temperature within the heating time, and recording the mass; and calculating the dry quenching burn-out rate. Compared with the prior art, the method provided by the invention has the advantages that the integrating degree of conditions and actual working conditions is high, and the influence of the actual working condition change on the dry quenching burn-out rate can be accurately reflected.

Description

Technical Field

[0001] This invention belongs to the field of dry quenching technology in the coking industry, and relates to a method and device for simulating process conditions to control the burn-off rate of dry quenching coke. Background Technology

[0002] Dry quenching coke production uses nitrogen (N2) as the cooling medium. After absorbing the sensible heat of the red-hot coke, the heat is recovered by steam generated in a waste heat boiler and returned to the cooling section. This cycle continues until the coke is cooled to below 250°C. The release of residual volatiles from the coke gradually increases the amount of combustible components such as carbon monoxide (CO) and hydrogen (H2) in the circulating gas. To prevent the risk of explosion of the circulating gas, air is generally continuously introduced to control the content of combustible components within a safe range. In the section from the annular flue to the boiler inlet, oxygen (O2) from the introduced air reacts with carbon monoxide, hydrogen, and coke powder in the circulating gas to produce carbon dioxide (CO2) and water vapor (H2O) (2CO + O2 → 2CO2, 2H2 + O2 → 2H2O, C + O2 → CO2). The carbon dioxide in the circulating gas enters the dry quenching furnace and reacts with the high-temperature coke to produce carbon monoxide (CO2 + C → 2CO). Simultaneously, the water vapor in the circulating gas reacts with the coke to produce carbon monoxide, carbon dioxide, and hydrogen (C + H2O → CO + H2, C + 2H2O → CO2 + 2H2). This cyclical process causes coke burn-off. The theoretical design value for coke burn-off rate in dry quenching equipment is around 1%, but the actual value is often much higher, generally above 1.5%, and sometimes even higher.

[0003] Excessive coke loss not only reduces the economic benefits of dry quenching production but also increases carbon emissions. Therefore, controlling coke loss is crucial for optimizing the operation of dry quenching systems. Currently, methods to reduce coke loss include optimizing air introduction (CN104650930A, CN114281115A, CN118562518A, CN117073397A) and dehydrating (CN116162474A) and removing carbon dioxide (CN211199118U, CN110655932A) the circulating gas. The aim of these techniques is to reduce coke loss through optimizing the composition of the circulating gas. However, due to the lack of a direct correlation between circulating gas composition and dry quenching loss rate, it is difficult to quantitatively determine the scale of dehydration and carbon dioxide removal in actual production. Therefore, establishing a simple, efficient, and low-cost method and apparatus for simulating dry quenching coke burn-off, determining the relationship between the composition of the dry quenching coke circulating gas and the dry quenching coke burn-off rate under different operating conditions, and thus guiding the actual production to control the composition of the dry quenching coke circulating gas and effectively reduce the dry quenching coke burn-off rate, has important economic and environmental significance.

[0004] Patent CN116486929A discloses a simulation control method for reducing the burn-off rate of dry quenching coke ovens. The method involves placing a coke sample in a reactor and then placing it into a heating furnace; the mass of the coke sample is recorded as m1. After checking the airtightness, the power is turned on, and the heating furnace is heated to 920–950°C under a protective atmosphere. After maintaining a stable temperature for a period of time, the blower is turned on, and circulating gas for the dry quenching coke oven is introduced according to the set air-to-material ratio. A programmed cooling process is then performed to lower the heating furnace temperature to below 150°C, at which point the heating process is stopped. Heat the coke, cut off the circulating gas, cool it to room temperature, remove the reacted coke, weigh its mass and record it as m2; calculate the coke burn-off rate X; the obtained coke burn-off rate X characterizes the coke burn-off rate in the dry quenching oven, compare it with the design value of the burn-off rate, and under the premise of constant air-fuel ratio, set several optimization schemes for the dry quenching circulating gas composition by adjusting the opening of the air guide valve; select the optimization scheme with the lowest coke burn-off rate X, control and optimize the composition of the dry quenching circulating gas in production, and reduce the dry quenching burn-off rate. In actual production, the dry quenching loss rate is affected by the dry quenching production conditions, including the composition of the circulating gas, the air-to-material ratio (circulating gas volume / coke discharge volume), and the coke discharge temperature. However, in the simulation test, the coke is in a static state while the gas is in a flowing state, making it impossible to directly set the air-to-material ratio. This patent does not specify the method for setting the air-to-material ratio. Furthermore, the temperature range from the red-hot state of the coke to the coke discharge temperature represents the temperature range of the reaction between the coke and the circulating gas. The coke discharge temperature is a variable value affected by the circulating gas volume and the coke discharge volume. This patent sets a constant termination temperature for the reaction between the coke and the circulating gas, which cannot adapt to changes in actual working conditions.

[0005] Patent CN118778576A discloses a method and system for optimizing the dry quenching coke burn-off rate. The method includes: acquiring multiple sets of actual production data of the dry quenching furnace at a preset data acquisition cycle; wherein the actual production data includes the circulating air volume; measuring the cold coke screening composition and the corresponding circulating gas flow ratio in the dry quenching furnace under multiple preset circulating air volumes, and determining the coke porosity based on the cold coke screening composition; calculating the dry quenching coke burn-off rate corresponding to each preset circulating air volume based on the actual production data under preset stable operating conditions; inputting the circulating gas flow ratio, coke porosity, and dry quenching coke burn-off rate under each preset circulating air volume into the burn-off rate optimization model and calculating the adjustment coefficient; and determining whether the dry quenching coke burn-off rate needs to be optimized based on the magnitude of the adjustment coefficient. However, the dry quenching burn-off rate optimization model established by this patent only considers the relationship between two parameters, coke porosity and circulating gas flow rate ratio, and the dry quenching burn-off rate, and sets other operating parameters to a stable state. Therefore, it is not applicable to operating conditions where changes occur, such as circulating gas composition, coke discharge rate, and coke discharge temperature. Summary of the Invention

[0006] The purpose of this invention is to overcome at least one defect in the prior art by providing a method and apparatus for simulating process conditions for controlling the dry quenching coke burn-off rate. The method and conditions involved in this invention have a high degree of consistency with actual working conditions and can accurately reflect the impact of changes in actual working conditions on the dry quenching coke burn-off rate.

[0007] The objective of this invention can be achieved through the following technical solutions:

[0008] One of the technical solutions of the present invention is to provide a method for simulating process conditions to control the dry quenching coke burn-off rate, the method comprising the following steps:

[0009] S1. In the simulated reaction of coke and reactant gases, the heating time is equivalent to the cooling time t of the coke in the dry quenching furnace in industrial production. 冷却时间 ;

[0010] In the simulated reaction of coke and reactant gases, the initial temperature is set to be the same as the coke discharge temperature of the dry quenching furnace in industrial production.

[0011] S2, Sampling coke materials;

[0012] In the simulated reaction of coke and reactant gases, the volumetric flow rate Q of the mixed gas is set. 气体体积流量 In the industrial production of dry quenching coke, the volumetric space velocity (GHSV) of the circulating gas that reacts with and cools the coke in the fixed bed is... 体积空速 And in the simulated reaction of coke with reactant gases, the packing volume V of the coke material. 焦炭材料堆积体积 Sure;

[0013] In the simulated reaction of coke and reactant gases, the concentration of reactant gases is equivalent to the composition of circulating gases in the industrial production of dry quenching coke.

[0014] S3. Place the coke material in the constant temperature zone of the reaction section, heat it to the initial temperature, and record the mass m0 of the coke material at the initial temperature. Then, introduce a mixture of reaction gas and inert gas, and heat it from the initial temperature to the red coke temperature within the heating time. Record the mass m1 of the coke material at the red coke temperature.

[0015] Calculate the dry quenching coke loss rate η 干熄焦烧蚀率 It is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red coking temperature.

[0016] Furthermore, in step S2, the cooling section space of the dry quenching furnace is approximated as having a volume of V. 冷却段内容积 The outer tube has a diameter of R1 and a height of L. 冷却段高度 The cylindrical shape, with the coke in the cooling section having an approximate volume of V. 焦炭堆积体积 The inner tube has a diameter of R2 and a height of L. 冷却段高度The cylindrical shape allows circulating gas to flow between the concentric sleeve annular gaps, approximating the coke cooling section as a simplified fixed-bed model.

[0017] Furthermore, the cooling time t of the coke in the dry quenching furnace in step S1 冷却时间 The volume V of the cooling section of the dry quenching furnace 冷却段内容积 The bulk density ρ of coke 焦炭堆积密度 and the coke discharge G of the dry quenching furnace 排焦量 Confirmed, the calculation formula is as follows:

[0018]

[0019] Among them, the downward movement speed U of coke in the cooling section 焦炭下移速度 The amount of coke discharged from the dry quenching furnace, G 排焦量 The bulk density ρ of coke 焦炭堆积密度 The cross-sectional area of ​​the cooling section of the dry quenching furnace is A. 冷却段内截面积 Confirmed, the calculation formula is as follows:

[0020]

[0021] As a preferred technical solution, the linear velocity U of the circulating gas in the cooling section 气体线速度 The circulating gas quantity Q of the dry quenching furnace 循环气体量 The cross-sectional area of ​​the cooling section is A. 冷却段内截面积 The porosity ε of coke in the cooling section bed 空隙率 Confirmed, the calculation formula is as follows:

[0022]

[0023] Among them, the porosity ε of coke in the cooling section bed 空隙率 From the bulk density ρ of coke 焦炭堆积密度 and apparent density ρ 焦炭表观密度 Confirmed, the calculation formula is as follows:

[0024]

[0025] As can be seen from the dimensions of the dry quenching furnace and the production conditions, the downward movement velocity U of the coke in the cooling section is... 焦炭下移速度 Relative to the linear velocity U of the circulating gas in the cooling section 气体线速度 The amount of coke in the cooling section is negligible, so it can be approximated as a simplified fixed-bed model.

[0026] Furthermore, the cooling time t of the coke in the dry quenching furnace in step S1 冷却时间 It lasts for 2 to 4 hours.

[0027] Furthermore, the coke discharge temperature of the dry quenching furnace in step S1 is 150–250°C;

[0028] In step S3, the red-burning temperature is 1000℃.

[0029] Furthermore, the method for sampling coke material in step S2 includes the following steps:

[0030] Take the coke from the dry-quenched furnace, discard the foamy coke and the furnace head coke, break the coke into nearly spherical coke granules, remove the coke powder adhering to the coke granules, reduce the coke granules into several portions, dry them for later use, and obtain several portions of coke material.

[0031] As a preferred technical solution, the particle size of the coke particles is 15-25 mm.

[0032] Furthermore, the method for removing coke powder adhering to coke particles includes the following steps:

[0033] The coke particles were soaked in a dispersant and then ultrasonicated.

[0034] The dispersant is selected from one or more of methanol, ethanol, n-propanol, isopropanol, n-butanol, and isobutanol;

[0035] The ultrasound duration is 0.5–1 hour, and the frequency is 30–50 kHz.

[0036] Furthermore, in step S2, the volumetric flow rate Q of the mixed gas... 气体体积流量 The calculation formula is as follows:

[0037] Q 气体体积流量 =GHSV 体积空速 ×V 焦炭材料堆积体积

[0038] Among them, the volume hourly space velocity (GHSV) of the circulating gas cooled by the reaction with coke in the fixed bed 体积空速 The circulating gas quantity Q of the dry quenching furnace 循环气体量 and cooling section volume V 冷却段内容积 Confirmed, the calculation formula is as follows:

[0039]

[0040] As a preferred technical solution, the mass m of the coke material in step S3 焦炭材料质量 It ranges from 50 to 500g.

[0041] As a preferred technical solution, in step S3, the temperature is raised to the initial temperature under the protection of an inert gas.

[0042] Further, in step S3, the reactant gas is selected from one or more of oxygen (O2), carbon dioxide (CO2), and water vapor (H2O), and the inert gas is nitrogen (N2). The volume percentage concentration of oxygen is ≤3%, the volume percentage concentration of carbon dioxide is ≤20%, the volume percentage concentration of water vapor is ≤15%, and the dry quenching coke loss rate η干熄焦烧蚀率 The calculations are used to guide the optimization of the circulating gas composition in industrial dry quenching furnaces.

[0043] One of the technical solutions of the present invention is to provide a simulation device for regulating the dry quenching coke burn-off rate. This device uses the method described above to simulate the regulation of the dry quenching coke burn-off rate. The device includes a hanging basket, a balance, and a high-temperature furnace. The hanging basket is suspended below the balance and contains coke. The hanging basket is placed inside the high-temperature furnace. The flow rate is determined according to the mixed gas volume flow rate Q. 气体体积流量 The flow rate of each component is calculated based on the concentration of each component in the mixed gas. The flow rate of each component in the mixed gas is controlled. The mixed gas is introduced into a high-temperature furnace to react with coke. The temperature and time of the reaction in the high-temperature furnace are recorded. The mass of coke before and after the reaction is recorded using a balance.

[0044] As a preferred technical solution, the bottom of the hanging basket is provided with a through hole, through which the mixed gas can pass through and react with the coke.

[0045] As a preferred technical solution, the device further includes a computer and a temperature controller. The high-temperature furnace is connected to the temperature controller, and the temperature controller is connected to the computer. The temperature controller controls and records the temperature and time of the reaction in the high-temperature furnace, and sends the temperature and time data to the computer for processing. The mass data of coke before and after the reaction recorded by the balance is also sent to the computer for processing.

[0046] As a preferred technical solution, the device further includes a thermal reaction tube, which is installed in a high-temperature furnace. The hanging basket is installed in the constant temperature zone of the reaction section of the thermal reaction tube. The hanging rope for suspending the basket passes through the top of the thermal reaction tube and is connected to the balance. The mixed gas enters the thermal reaction tube from below and exits from the top.

[0047] As a preferred technical solution, the device further includes a mass flow controller, a steam generator, and gas cylinders. Gas cylinders for oxygen, carbon dioxide, and nitrogen are all connected to the steam generator via pipelines. Mass flow controllers are installed on the pipelines corresponding to oxygen, carbon dioxide, and nitrogen to control the flow rates of oxygen, carbon dioxide, and nitrogen, and to set the flow rate of steam from the steam generator. The steam generator is connected to a thermal reaction tube. Nitrogen is mixed with at least one of oxygen, carbon dioxide, and steam, and then introduced into the thermal reaction tube. Nitrogen is mixed with oxygen and carbon dioxide via a confluence pipeline, and nitrogen is mixed with steam by being introduced into the steam generator.

[0048] As a preferred technical solution, the device further includes a buffer bottle, the steam generator is connected to the buffer bottle, the buffer bottle is connected to the hot reaction tube, and the buffer bottle allows the gas to be fully premixed.

[0049] As a preferred technical solution, based on the mass m of the coke material焦炭材料质量 Design and manufacture hanging baskets of suitable sizes;

[0050] The bulk volume V of coke material 焦炭材料堆积体积 The mass m of the coke material 焦炭材料质量 and bulk density ρ 焦炭材料堆积密度 Confirmed, the calculation formula is as follows:

[0051]

[0052] The stacking height h of coke material 焦炭材料堆积高度 The volume of coke material V 焦炭材料堆积体积 and the cross-sectional area A of the hanging basket 吊筐内截面积 Confirmed, the calculation formula is as follows:

[0053]

[0054] The volume of the hanging basket is greater than or equal to the stacked volume of the coke material, V. 焦炭材料堆积体积 Then the height of the processing basket is greater than or equal to the stacking height h of the coke material. 焦炭材料堆积高度 .

[0055] Compared with the prior art, the present invention has the following beneficial effects:

[0056] (1) Based on industrial production conditions, this invention sets out key production conditions that affect the dry quenching coke burn-off rate, including the composition of circulating gas, the volumetric space velocity of the circulating gas that reacts with and cools the coke in the fixed bed, the coke discharge temperature of the dry quenching furnace, and the cooling time of the coke in the dry quenching furnace. These represent the concentration of the reacting gas in the gas-solid reaction, the volumetric flow rate of the mixed gas and the mass (bulk volume) of the coke material, the initial temperature, and the heating time under simulated conditions, respectively. This invention can accurately reflect the impact of changes in actual working conditions on the dry quenching coke burn-off rate, thereby effectively controlling the dry quenching coke burn-off rate by optimizing the composition of circulating gas.

[0057] (2) The present invention uses online real-time recording of coke thermogravimetric data, while the general test method requires waiting for the coke to cool completely to room temperature before weighing. During the cooling process, the coke will undergo further pyrolysis and weight loss. The present invention avoids the error caused by this process and can accurately provide the coke burn-off rate results.

[0058] (3) This invention can quickly and accurately reflect the impact of changes in the composition of the dry quenching cycle on the coke burn-off rate, which is beneficial for industrial production to directly refer to optimize the composition of the circulating gas to reduce the coke burn-off rate, and can shorten the production control cycle and reduce related cost inputs.

[0059] (4) Based on actual industrial production conditions, this invention sets key conditions for the reaction of dry quenching coke with related components of circulating gas, which facilitates coking enterprises to conduct prediction and analysis of dry quenching coke burn-off rate according to their own production conditions, thereby guiding the optimization of circulating gas composition to effectively reduce dry quenching coke burn-off rate. The methods and conditions involved are highly consistent with actual working conditions, the equipment is simple, easy to operate, low in cost, and highly accurate in results, making it suitable for widespread use. Attached Figure Description

[0060] Figure 1 This is a schematic diagram of the simulation device for regulating the dry quenching burn-off rate in an embodiment of the present invention.

[0061] Explanation of markings in the diagram:

[0062] 1—Temperature controller, 2—Heat reaction tube, 3—Hanging basket, 4—Balance, 5—High temperature furnace, 6—Buffer bottle, 7—Mass flow controller, 8—Steam generator, 9—Gas cylinder. Detailed Implementation

[0063] The present invention will now be described in detail with reference to specific embodiments. These embodiments are based on the technical solution of the present invention and provide detailed implementation methods and specific operating procedures. However, the scope of protection of the present invention is not limited to the following embodiments.

[0064] In the description of this invention, it should be noted that the terms "center," "upper," "lower," "left," "right," "vertical," "horizontal," "inner," and "outer," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing this invention and for simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this invention. Furthermore, the terms "first," "second," "third," etc., used to describe a common object only indicate different instances of the same object, and do not imply that the objects described in this way must be in a given order, whether temporally, spatially, sequentially, or in any other way.

[0065] In the description of this invention, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "connection," and "linking" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this invention based on the specific circumstances.

[0066] Unless otherwise specified, the equipment used in the following embodiments is conventional equipment in the art; unless otherwise specified, the reagents used are commercially available products or prepared by conventional methods in the art. In the following embodiments, unless otherwise described in detail, conventional experimental methods in the art can be used.

[0067] Example 1:

[0068] A simulation device for regulating the burn-off rate of dry quenching coke, such as Figure 1 As shown, the system includes a hanging basket 3, a balance 4, and a high-temperature furnace 5. The hanging basket 3 is suspended below the balance 4 and contains coke. The hanging basket 3 is placed inside the high-temperature furnace 5. The flow rate of the mixed gas is Q. 气体体积流量 The flow rate of each component is calculated based on the concentration of each component in the mixed gas. The flow rate of each component in the mixed gas is controlled. The mixed gas is introduced into the high-temperature furnace 5 to react with the coke. The temperature and time of the reaction in the high-temperature furnace 5 are recorded. The mass of the coke before and after the reaction is recorded by the balance 4.

[0069] Balance 4 uses an electronic balance, which makes it convenient to send quality data;

[0070] The bottom of the hanging basket 3 has a through hole, through which the mixed gas can pass through and react with the coke;

[0071] The hanging basket 3 is made of quartz. The inertness of quartz prevents the hanging basket 3 from reacting with the mixed gas and coke and causing weight changes.

[0072] The device also includes a computer and a temperature controller 1. The high-temperature furnace 5 is connected to the temperature controller 1, and the temperature controller 1 is connected to the computer. The temperature and time of the reaction in the high-temperature furnace 5 are controlled and recorded by the temperature controller 1, and the temperature and time data are sent to the computer for processing. The mass data of coke before and after the reaction recorded by the balance 4 are sent to the computer for processing.

[0073] The device also includes a hot reaction tube 2, which is installed in a high-temperature furnace 5. A hanging basket 3 is installed in the constant temperature zone of the reaction section of the hot reaction tube 2. The hanging rope of the hanging basket 3 passes through the top of the hot reaction tube 2 and is connected to the balance 4. The mixed gas enters the hot reaction tube 2 from below and exits from the top.

[0074] The suspension rope is made of one or more precious metals, such as platinum and rhodium. In this embodiment, a platinum-rhodium alloy is preferred. Precious metals have good high-temperature stability, strong oxidation resistance, and excellent corrosion resistance, so that the suspension rope will not react with the mixed gas and cause weight changes.

[0075] The thermal reaction tube 2 is a vertical thermal reaction tube, that is, the thermal reaction tube 2 is vertically installed in the high temperature furnace 5;

[0076] The device also includes a mass flow controller 7, a steam generator 8, and gas cylinders 9. The mixed gas includes a reactive gas and an inert gas. The reactive gas is selected from one or more of oxygen (O2), carbon dioxide (CO2), and water vapor (H2O). The inert gas is nitrogen (N2). The gas cylinders 9 for oxygen, carbon dioxide, and nitrogen are all connected to the steam generator 8 through pipelines. Mass flow controllers 7 are installed on the pipelines for oxygen, carbon dioxide, and nitrogen to control the flow rates of oxygen, carbon dioxide, and nitrogen. The flow rate of water vapor in the steam generator 8 is set. The steam generator 8 is connected to the hot reaction tube 2. Nitrogen is mixed with at least one of oxygen, carbon dioxide, and water vapor and then introduced into the hot reaction tube 2. Nitrogen is mixed with oxygen and carbon dioxide through a confluence pipeline and mixed with water vapor by being introduced into the steam generator 8.

[0077] The device also includes a buffer bottle 6, a steam generator 8 connected to the buffer bottle 6, and the buffer bottle 6 connected to the hot reaction tube 2. The buffer bottle 6 allows the gas to be fully premixed.

[0078] A dry quenching system of a steel company has a cooling section volume V of the dry quenching furnace. 冷却段内容积 480m 3 The inner diameter R1 of the cooling section shell is 7.8m, and the circulating gas volume Q 循环气体量 100×10 3 m 3 / h, coke discharge capacity G 排焦量 70t / h (70×10 3 The coke discharge rate is 250℃, and the basic properties of the coke are shown in Table 1.

[0079] Table 1. Basic properties of coke in Example 1

[0080]

[0081] A method for simulating process conditions for controlling the burn-off rate of dry quenching coke, using the aforementioned device to simulate process conditions for controlling the burn-off rate of dry quenching coke, comprises the following specific steps:

[0082] S1. Consider the cooling section space of the dry quenching furnace as having a volume of V. 冷却段内容积 The outer tube has a diameter of R1 and a height of L. 冷却段高度 The cylinder, with the coke in the cooling section considered to have a volume of V 焦炭堆积体积 The inner tube has a diameter of R2 and a height of L. 冷却段高度 The cylindrical shape is assumed to have circulating gas flowing between the concentric annular gaps of the sleeves. The cross-sectional area of ​​the cooling section of the dry quenching furnace is A. 冷却段空隙截面积 ;

[0083] The linear velocity U of the circulating gas in the cooling section 气体线速度The circulating gas quantity Q of the dry quenching furnace 循环气体量 The cross-sectional area of ​​the cooling section is A. 冷却段内截面积 The porosity ε of coke in the cooling section bed 空隙率 Confirmed, the calculation formula is as follows:

[0084]

[0085] The porosity ε of coke in the cooling section bed 空隙率 From the bulk density ρ of coke 焦炭堆积密度 and apparent density ρ 焦炭表观密度 The calculation formula and specific values ​​are as follows:

[0086]

[0087] The linear velocity U of the circulating gas in the cooling section 气体线速度 The specific values ​​are as follows:

[0088]

[0089] The downward movement velocity U of coke in the cooling section 焦炭下移速度 The amount of coke discharged from the dry quenching furnace, G 排焦量 The bulk density ρ of coke 焦炭堆积密度 The cross-sectional area of ​​the cooling section of the dry quenching furnace is A. 冷却段内截面积 The calculation formula and specific values ​​are as follows:

[0090]

[0091] As can be seen from the dimensions of the dry quenching furnace and the production conditions, the downward movement velocity U of the coke in the cooling section is... 焦炭下移速度 The linear velocity U of the circulating gas in the cooling section 气体线速度 10 -4 The multiple, i.e., the downward movement speed U of the coke in the cooling section. 焦炭下移速度 Relative to the linear velocity U of the circulating gas in the cooling section 气体线速度 The amount of coke in the cooling section is negligible, so the coke in the cooling section can be regarded as a simplified fixed bed model.

[0092] The volumetric space velocity (GHSV) of the circulating gas cooled by the reaction with coke in the fixed bed 体积空速 The circulating gas quantity Q of the dry quenching furnace 循环气体量 and cooling section volume V 冷却段内容积 The calculation formula and specific values ​​are as follows:

[0093]

[0094] Cooling time t of coke in dry quenching furnace 冷却时间 The volume V of the cooling section of the dry quenching furnace 冷却段内容积 The bulk density ρ of coke 焦炭堆积密度and the coke discharge G of the dry quenching furnace 排焦量 The calculation formula and specific values ​​are as follows:

[0095]

[0096] In the simulated reaction of coke and reactant gases, the heating time is set to be equivalent to the cooling time t of the coke in the dry quenching furnace in industrial production. 冷却时间 ;

[0097] In the simulated reaction of coke and reactant gases, the initial temperature is set to be the same as the coke discharge temperature of the dry quenching furnace in industrial production.

[0098] S2. According to the sampling method specified in GB / T 1997-2008 "Sampling and Preparation of Coke Samples", take 5 kg of coke from a dry quenching furnace according to the specified proportion. The coke particle size should be ≥25 mm. Completely discard large-pore, honeycomb-shaped blister coke and furnace head coke with black tips that is not completely gray. Crush the coke into nearly spherical coke lumps with a particle size of 23±2 mm. Soak the coke lumps in anhydrous ethanol and sonicate them in an ultrasonic cleaner for 0.75 h at a frequency of 40 kHz to remove the coke powder adhering to the coke lumps. Reduce the coke lumps to several portions, each not less than 600 g, and dry them in a drying oven for later use. Measure the bulk density ρ of the coke material. 焦炭材料堆积密度 555 kg / m 3 (0.555g / cm 3 );

[0099] In the industrial production of dry quenching coke, the volume hourly space velocity (GHSV) of the circulating gas that reacts with and cools the coke in the fixed bed is... 体积空速 And the quality of coke materials m 焦炭材料质量 Design and fabricate heat reaction tubes 2 and hanging baskets 3 of appropriate dimensions;

[0100] If 500g of coke material is used in each simulated reaction, then the bulk volume V of the coke material is... 焦炭材料堆积体积 The mass m of the coke material 焦炭材料质量 and bulk density ρ 焦炭材料堆积密度 The calculation formula and specific values ​​are as follows:

[0101]

[0102] The inner diameter of the designed thermal reaction tube 2 is 10.5 cm, and the inner diameter of the hanging basket 3 is 10 cm. Therefore, the stacking height h of the coke material is... 焦炭材料堆积高度 The volume of coke material V 焦炭材料堆积体积 The cross-sectional area A of the hanging basket 3 吊筐内截面积 The calculation formula and specific values ​​are as follows:

[0103]

[0104] The volume of the hanging basket 3 is greater than or equal to the stacking volume of the coke material, V. 焦炭材料堆积体积 The height of the processing basket 3 is 12cm, the height of the heat reaction tube 2 is 32cm, and the distance between the top and bottom of the basket 3 and the heat reaction tube 2 is 10cm.

[0105] Mixed gas volume flow rate Q 气体体积流量 The calculation formula and specific values ​​are as follows:

[0106] Q 气体体积流量 =GHSV 体积空速 ×V 焦炭材料堆积体积 =208h -1 ×901cm 3 =187408cm 3 / h=3.12L / min

[0107] In the simulated reaction of coke and reactant gases, the volumetric flow rate Q of the mixed gas is set. 气体体积流量 In the industrial production of dry quenching coke, the volumetric space velocity (GHSV) of the circulating gas that reacts with and cools the coke in the fixed bed is... 体积空速 And in the simulated reaction of coke with reactant gases, the packing volume V of the coke material. 焦炭材料堆积体积 Sure;

[0108] In the simulated reaction of coke and reactant gases, the concentration of reactant gases is equivalent to the composition of circulating gases in the industrial production of dry quenching coke.

[0109] S3. Determine the burn-off rate of coke under different circulating gas compositions.

[0110] S3.1 Weigh 500g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 250℃. Record the reading m0 of balance 4 as 500.0382g. Then, a mixture of oxygen and nitrogen with 0.5% oxygen is introduced. The volumetric flow rate of the mixed gas is Q. 气体体积流量 The flow rate was 3.12 L / min. The temperature was increased from the initial temperature of 250℃ to the red char temperature of 1000℃ within a heating time of 3.3h. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 498.3381g.

[0111] Calculate the burn loss rate η of coke in 0.5% oxygen. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0112]

[0113] S3.2 Weigh 500g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 250℃. Record the reading m0 of balance 4 as 500.0124g. Then, a mixture of carbon dioxide and nitrogen (10% carbon dioxide) is introduced. The volumetric flow rate of the mixed gas is Q. 气体体积流量 The flow rate was 3.12 L / min. The temperature was increased from the initial temperature of 250℃ to the red char temperature of 1000℃ within a heating time of 3.3h. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 495.4623g.

[0114] Calculate the burn loss rate η of coke in 10% carbon dioxide. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0115]

[0116] S3.3 Weigh 500g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 250℃. Record the reading m0 of balance 4 as 500.0032g. Then, a mixture of water vapor and nitrogen gas with 15% water vapor is introduced. The volumetric flow rate of the mixed gas is Q. 气体体积流量 The flow rate was 3.12 L / min. The temperature was increased from the initial temperature of 250℃ to the red char temperature of 1000℃ within a heating time of 3.3h. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 487.9531g.

[0117] Calculate the burn loss rate η of coke in 15% steam. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0118]

[0119] S3.4 Weigh 500g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 250℃. Record the reading m0 of balance 4 as 500.0021g. Then, introduce a mixed gas of oxygen (1.5% oxygen) and nitrogen (5% carbon dioxide). The volumetric flow rate of the mixed gas is Q. 气体体积流量 The flow rate was 3.12 L / min. The temperature was increased from the initial temperature of 250℃ to the red char temperature of 1000℃ within a heating time of 3.3h. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 497.7021g.

[0120] Calculate the burn loss η of coke in 1.5% oxygen and 5% carbon dioxide. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0121]

[0122] S3.5 Weigh 500g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 250℃. Record the reading m0 of balance 4 as 500.0210g. Then, introduce a mixed gas of oxygen (3% oxygen) and nitrogen (5% water vapor). The volumetric flow rate of the mixed gas is Q. 气体体积流量 The flow rate was 3.12 L / min. The temperature was increased from the initial temperature of 250℃ to the red char temperature of 1000℃ within a heating time of 3.3h. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 490.4206g.

[0123] Calculate the burn loss η of coke in 3% oxygen and 5% water vapor. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0124]

[0125] S3.6 Weigh 500g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 250℃. Record the reading m0 of balance 4 as 500.0062g. Then, introduce a mixed gas of carbon dioxide (20% carbon dioxide) and nitrogen (5% water vapor). The volumetric flow rate of the mixed gas is Q. 气体体积流量 The flow rate was 3.12 L / min. The temperature was increased from the initial temperature of 250℃ to the red char temperature of 1000℃ within a heating time of 3.3h. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 488.3061g.

[0126] Calculate the burn loss η of coke in 20% carbon dioxide and 5% water vapor. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0127]

[0128] S3.7 Weigh 500g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 250℃. Record the reading m0 of balance 4 as 500.0014g. Then, introduce a mixed gas of oxygen, carbon dioxide, water vapor and nitrogen, which contains 3% oxygen, 5% carbon dioxide and 15% water vapor. The volumetric flow rate of the mixed gas is Q. 气体体积流量 The flow rate was 3.12 L / min. The temperature was increased from the initial temperature of 250℃ to the red char temperature of 1000℃ within a heating time of 3.3h. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 486.7514g.

[0129] Calculate the burn loss η of coke in 3% oxygen, 5% carbon dioxide and 15% water vapor. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0130]

[0131] Example 2:

[0132] A dry quenching system of a steel company has a cooling section volume V of the dry quenching furnace. 冷却段内容积 315m 3 The inner diameter R1 of the cooling section shell is 8.2m, and the circulating gas volume Q 循环气体量 120×10 3 m 3 / h, coke discharge capacity G 排焦量 75t / h (75×10 3 The coke discharge rate is 200℃, and the basic properties of the coke are shown in Table 2.

[0133] Table 2 Basic properties of coke in Example 2

[0134]

[0135] A method for simulating process conditions for controlling the burn-off rate of dry quenching coke is provided, using the apparatus described in Example 1 to simulate the process conditions for controlling the burn-off rate of dry quenching coke, with the following differences:

[0136] S1, porosity ε of coke in the cooling section bed 空隙率 The specific values ​​are as follows:

[0137]

[0138] The linear velocity U of the circulating gas in the cooling section 气体线速度 The specific values ​​are as follows:

[0139]

[0140] The downward movement velocity U of coke in the cooling section 焦炭下移速度 The specific values ​​are as follows:

[0141]

[0142] As can be seen from the dimensions of the dry quenching furnace and the production conditions, the downward movement velocity U of the coke in the cooling section is... 焦炭下移速度 The linear velocity U of the circulating gas in the cooling section 气体线速度 10 -4 The multiple, i.e., the downward movement speed U of the coke in the cooling section. 焦炭下移速度 Relative to the linear velocity U of the circulating gas in the cooling section 气体线速度 The amount of coke in the cooling section is negligible, so the coke in the cooling section can be regarded as a simplified fixed bed model.

[0143] The volumetric space velocity (GHSV) of the circulating gas cooled by the reaction with coke in the fixed bed 体积空速 The specific values ​​are as follows:

[0144]

[0145] Cooling time t of coke in dry quenching furnace 冷却时间 The specific values ​​are as follows:

[0146]

[0147] S2. If 250g of coke material is used in each simulated reaction, then the bulk volume V of the coke material is... 焦炭材料堆积体积 The specific values ​​are as follows:

[0148]

[0149] The inner diameter of the designed thermal reaction tube 2 is 10.5 cm, and the inner diameter of the hanging basket 3 is 10 cm. Therefore, the stacking height h of the coke material is... 焦炭材料堆积高度 The specific values ​​are as follows:

[0150]

[0151] The volume of the hanging basket 3 is greater than or equal to the stacking volume of the coke material, V. 焦炭材料堆积体积 The height of the processing basket 3 is 6cm, the height of the heat reaction tube 2 is 26cm, and the distance between the top and bottom of the basket 3 and the heat reaction tube 2 is 10cm.

[0152] Mixed gas volume flow rate Q 气体体积流量 The calculation formula and specific values ​​are as follows:

[0153] Q 气体体积流量 =GHSV 体积空速 ×V 焦炭材料堆积体积 =381h-1 ×450cm 3 =171450cm 3 / h=2.86L / min

[0154] S3. Determine the burn-off rate of coke under different circulating gas compositions.

[0155] S3.1 Weigh 250g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 200℃. Record the reading m0 of balance 4 as 250.0182g. Then, a mixture of oxygen and nitrogen with 1.5% oxygen is introduced. The volumetric flow rate of the mixed gas is Q. 气体体积流量 The flow rate was 2.86 L / min. The temperature was increased from the initial temperature of 200℃ to the red char temperature of 1000℃ within a 2-hour heating time. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 248.7181 g.

[0156] Calculate the burn loss η of coke in 1.5% oxygen. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0157]

[0158] S3.2 Weigh 250g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 200℃. Record the reading m0 of balance 4 as 250.0102g. Then, a mixture of carbon dioxide and nitrogen (20% carbon dioxide) is introduced. The volumetric flow rate of the mixed gas is Q. 气体体积流量 The flow rate was 2.86 L / min. The temperature was increased from the initial temperature of 200℃ to the red char temperature of 1000℃ within a 2-hour heating time. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 247.5601g.

[0159] Calculate the burn loss rate η of coke in 20% carbon dioxide. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0160]

[0161] S3.3 Weigh 250g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 200℃. Record the reading m0 of balance 4 as 250.0205g. Then, a mixture of water vapor and nitrogen gas with 1% water vapor is introduced. The volumetric flow rate of the mixed gas is Q. 气体体积流量The flow rate was 2.86 L / min. The temperature was increased from the initial temperature of 200℃ to the red char temperature of 1000℃ within a 2-hour heating time. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 246.6702 g.

[0162] Calculate the burn-off rate η of coke in 1% steam. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0163]

[0164] S3.4 Weigh 250g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 200℃. Record the reading m0 of balance 4 as 250.0124g. Then, introduce a mixed gas of oxygen (3% oxygen and 20% carbon dioxide), carbon dioxide, and nitrogen. The volumetric flow rate of the mixed gas is Q. 气体体积流量 The flow rate was 2.86 L / min. The temperature was increased from the initial temperature of 200℃ to the red char temperature of 1000℃ within a 2-hour heating time. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 246.9372 g.

[0165] Calculate the burn loss η of coke in 3% oxygen and 20% carbon dioxide. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0166]

[0167] S3.5 Weigh 250g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 200℃. Record the reading m0 of balance 4 as 250.0241g. Then, introduce a mixed gas of oxygen, water vapor and nitrogen, which contains 1.5% oxygen and 15% water vapor. The volumetric flow rate of the mixed gas is Q. 气体体积流量 The flow rate was 2.86 L / min. The temperature was increased from the initial temperature of 200℃ to the red char temperature of 1000℃ within a 2-hour heating time. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 245.9737 g.

[0168] Calculate the burn loss η of coke in 1.5% oxygen and 15% water vapor. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0169]

[0170] S3.6 Weigh 250g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 200℃. Record the reading m0 of balance 4 as 250.0154g. Then, introduce a mixed gas of carbon dioxide (5% carbon dioxide) and nitrogen (15% water vapor). The volumetric flow rate of the mixed gas is Q. 气体体积流量 The flow rate was 2.86 L / min. The temperature was increased from the initial temperature of 200℃ to the red char temperature of 1000℃ within a 2-hour heating time. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 244.6151 g.

[0171] Calculate the burn loss η of coke in 5% carbon dioxide and 15% water vapor. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0172]

[0173] S3.7 Weigh 250g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 200℃. Record the reading m0 of balance 4 as 250.0004g. Then, introduce a mixed gas of oxygen, carbon dioxide, water vapor and nitrogen, which contains 1.5% oxygen, 20% carbon dioxide and 1% water vapor. The volumetric flow rate of the mixed gas is Q. 气体体积流量 The flow rate was 2.86 L / min. The temperature was increased from the initial temperature of 200℃ to the red char temperature of 1000℃ within a 2-hour heating time. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 245.0254 g.

[0174] Calculate the burn loss η of coke in 1.5% oxygen, 20% carbon dioxide and 1% water vapor. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0175]

[0176] Example 3:

[0177] A dry quenching system of a steel company has a cooling section volume V of the dry quenching furnace. 冷却段内容积 480m 3 The inner diameter R1 of the cooling section shell is 8.6m, and the circulating gas volume Q 循环气体量 105×10 3 m 3 / h, coke discharge capacity G排焦量 For 60t / h (60×10 3 The coke discharge rate is 150℃, and the basic properties of the coke are shown in Table 3.

[0178] Table 3. Basic properties of coke in Example 3

[0179]

[0180] A method for simulating process conditions for controlling the burn-off rate of dry quenching coke is provided, using the apparatus described in Example 1 to simulate the process conditions for controlling the burn-off rate of dry quenching coke, with the following differences:

[0181] S1, porosity ε of coke in the cooling section bed 空隙率 The specific values ​​are as follows:

[0182]

[0183] The linear velocity U of the circulating gas in the cooling section 气体线速度 The specific values ​​are as follows:

[0184]

[0185] The downward movement velocity U of coke in the cooling section 焦炭下移速度 The specific values ​​are as follows:

[0186]

[0187] As can be seen from the dimensions of the dry quenching furnace and the production conditions, the downward movement velocity U of the coke in the cooling section is... 焦炭下移速度 The linear velocity U of the circulating gas in the cooling section 气体线速度 10 -4 The multiple, i.e., the downward movement speed U of the coke in the cooling section. 焦炭下移速度 Relative to the linear velocity U of the circulating gas in the cooling section 气体线速度 The amount of coke in the cooling section is negligible, so the coke in the cooling section can be regarded as a simplified fixed bed model.

[0188] The volumetric space velocity (GHSV) of the circulating gas cooled by the reaction with coke in the fixed bed 体积空速 The specific values ​​are as follows:

[0189]

[0190] Cooling time t of coke in dry quenching furnace 冷却时间 The specific values ​​are as follows:

[0191]

[0192] S2. If 50g of coke material is used in each simulated reaction, then the bulk volume V of the coke material is... 焦炭材料堆积体积The specific values ​​are as follows:

[0193]

[0194] The inner diameter of the designed thermal reaction tube 2 is 6.5 cm, and the inner diameter of the hanging basket 3 is 6 cm. Therefore, the stacking height h of the coke material is... 焦炭材料堆积高度 The specific values ​​are as follows:

[0195]

[0196] The volume of the hanging basket 3 is greater than or equal to the stacking volume of the coke material, V. 焦炭材料堆积体积 The height of the processing basket 3 is 4cm, the height of the heat reaction tube 2 is 24cm, and the distance between the top and bottom of the basket 3 and the heat reaction tube 2 is 10cm.

[0197] Mixed gas volume flow rate Q 气体体积流量 The calculation formula and specific values ​​are as follows:

[0198] Q 气体体积流量 =GHSV 体积空速 ×V 焦炭材料堆积体积 =219h -1 ×90cm 3 =19710cm 3 / h=0.33L / min

[0199] S3. Determine the burn-off rate of coke under different circulating gas compositions.

[0200] S3.1 Weigh 50g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 150℃. Record the reading m0 of balance 4 as 50.0082g. Then, a mixture of oxygen and nitrogen with 3% oxygen is introduced. The volumetric flow rate of the mixed gas is Q. 气体体积流量 The flow rate was 0.33 L / min. The temperature was increased from the initial temperature of 150℃ to the red char temperature of 1000℃ within a heating time of 4 hours. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 49.2281 g.

[0201] Calculate the burn loss rate η of coke in 3% oxygen. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0202]

[0203] S3.2 Weigh 50g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 150℃. Record the reading m0 of balance 4 as 50.0025g. Then, a mixture of carbon dioxide and nitrogen (5% carbon dioxide) is introduced. The volumetric flow rate of the mixed gas is Q. 气体体积流量 The flow rate was 0.33 L / min. The temperature was increased from the initial temperature of 150℃ to the red char temperature of 1000℃ within a heating time of 4 hours. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 49.6325g.

[0204] Calculate the burn loss rate η of coke in 5% carbon dioxide. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0205]

[0206] S3.3 Weigh 50g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 150℃. Record the reading m0 of balance 4 as 50.0282g. Then, a mixture of water vapor and nitrogen with 5% water vapor is introduced. The volumetric flow rate of the mixed gas is Q. 气体体积流量 The flow rate was 0.33 L / min. The temperature was increased from the initial temperature of 150℃ to the red char temperature of 1000℃ within a heating time of 4 hours. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 49.0927 g.

[0207] Calculate the burn-off rate η of coke in 5% steam. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0208]

[0209] S3.4 Weigh 50g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 150℃. Record the reading m0 of balance 4 as 50.0152g. Then, introduce a mixed gas of oxygen (0.5% oxygen) and carbon dioxide (10% carbon dioxide), and the volumetric flow rate Q of the mixed gas is recorded. 气体体积流量 The flow rate was 0.33 L / min. The temperature was increased from the initial temperature of 150℃ to the red char temperature of 1000℃ within a heating time of 4 hours. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 49.6901g.

[0210] Calculate the burn loss η of coke in 0.5% oxygen and 10% carbon dioxide. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0211]

[0212] S3.5 Weigh 50g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 150℃. Record the reading m0 of balance 4 as 50.0046g. Then, introduce a mixed gas of oxygen (0.5% oxygen) and water vapor (1% water vapor). The volumetric flow rate of the mixed gas is Q. 气体体积流量 The flow rate was 0.33 L / min. The temperature was increased from the initial temperature of 150℃ to the red char temperature of 1000℃ within a heating time of 4 hours. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 48.9845g.

[0213] Calculate the burn loss η of coke in 0.5% oxygen and 1% water vapor. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0214]

[0215] S3.6 Weigh 50g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 150℃. Record the reading m0 of balance 4 as 50.0016g. Then, introduce a mixed gas of carbon dioxide, water vapor and nitrogen (10% carbon dioxide and 1% water vapor). The volumetric flow rate of the mixed gas is Q. 气体体积流量 The flow rate was 0.33 L / min. The temperature was increased from the initial temperature of 150℃ to the red char temperature of 1000℃ within a heating time of 4 hours. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 49.0716g.

[0216] Calculate the burn loss η of coke in 10% carbon dioxide and 1% water vapor. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0217]

[0218] S3.7 Weigh 50g of coke material and place it in the constant temperature zone of the reaction section. Under the protection of inert nitrogen gas, heat it to the initial temperature of 150℃. Record the reading m0 of balance 4 as 50.0013g. Then, introduce a mixed gas of oxygen, carbon dioxide, water vapor and nitrogen, which contains 0.5% oxygen, 10% carbon dioxide and 5% water vapor. The volumetric flow rate of the mixed gas is Q. 气体体积流量 The flow rate was 0.33 L / min. The temperature was increased from the initial temperature of 150℃ to the red char temperature of 1000℃ within a heating time of 4 hours. The reading of balance 4 was collected in real time using online data acquisition software. The reading m1 of balance 4 at the red char temperature of 1000℃ was recorded as 48.8663 g.

[0219] Calculate the burn loss η of coke in 0.5% oxygen, 10% carbon dioxide and 5% water vapor. 干熄焦烧蚀率 The value is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red-hot coking temperature. The calculation formula and specific values ​​are as follows.

[0220]

[0221] The above description of the embodiments is provided to enable those skilled in the art to understand and use the invention. It will be apparent to those skilled in the art that various modifications can be made to these embodiments, and the general principles described herein can be applied to other embodiments without inventive effort. Therefore, the present invention is not limited to the above embodiments, and any improvements and modifications made by those skilled in the art based on the disclosure of the present invention without departing from the scope of the invention should be within the protection scope of the present invention.

Claims

1. A method for simulating process conditions to control the dry quenching coke burn-off rate, characterized in that, The method includes the following steps: S1. In the simulated reaction of coke and reactant gases, the heating time is equivalent to the cooling time t of the coke in the dry quenching furnace in industrial production. 冷却时间 ; In the simulated reaction of coke and reactant gases, the initial temperature is set to be the same as the coke discharge temperature of the dry quenching furnace in industrial production. S2, Sampling coke materials; In the simulated reaction of coke and reactant gases, the volumetric flow rate Q of the mixed gas is set. 气体体积流量 In the industrial production of dry quenching coke, the volumetric space velocity (GHSV) of the circulating gas that reacts with and cools the coke in the fixed bed is... 体积空速 And in the simulated reaction of coke with reactant gases, the packing volume V of the coke material. 焦炭材料堆积体积 Sure; In the simulated reaction of coke and reactant gases, the concentration of reactant gases is equivalent to the composition of circulating gases in the industrial production of dry quenching coke. S3. Place the coke material in the constant temperature zone of the reaction section, heat it to the initial temperature, and record the mass m0 of the coke material at the initial temperature. Then, introduce a mixture of reaction gas and inert gas, and heat it from the initial temperature to the red coke temperature within the heating time. Record the mass m1 of the coke material at the red coke temperature. Calculate the dry quenching coke loss rate η 干熄焦烧蚀率 It is determined by the mass m0 of the coke material at the initial temperature and the mass m1 at the red coking temperature.

2. The method for simulating process conditions to regulate the dry quenching coke burn-off rate according to claim 1, characterized in that, In step S2, the cooling section space of the dry quenching furnace is approximated as having a volume of V. 冷却段内容积 The outer tube has a diameter of R1 and a height of L. 冷却段高度 The cylindrical shape, with the coke in the cooling section having an approximate volume of V. 焦炭堆积体积 The inner tube has a diameter of R2 and a height of L. 冷却段高度 The cylindrical shape allows circulating gas to flow between the concentric sleeve annular gaps, approximating the coke cooling section as a simplified fixed-bed model.

3. The method for simulating process conditions to regulate the dry quenching coke burn-off rate according to claim 1, characterized in that, The cooling time t of the coke in the dry quenching furnace in step S1 冷却时间 The volume V of the cooling section of the dry quenching furnace 冷却段内容积 The bulk density ρ of coke 焦炭堆积密度 and the coke discharge G of the dry quenching furnace 排焦量 Confirmed, the calculation formula is as follows: Among them, the downward movement speed U of coke in the cooling section 焦炭下移速度 The amount of coke discharged from the dry quenching furnace, G 排焦量 The bulk density ρ of coke 焦炭堆积密度 The cross-sectional area of ​​the cooling section of the dry quenching furnace is A. 冷却段内截面积 Confirmed, the calculation formula is as follows:

4. The method for simulating process conditions to regulate the dry quenching coke burn-off rate according to claim 3, characterized in that, The cooling time t of the coke in the dry quenching furnace in step S1 冷却时间 It lasts for 2 to 4 hours.

5. The method for simulating process conditions to regulate the dry quenching coke burn-off rate according to claim 1, characterized in that, The coke discharge temperature of the dry quenching furnace in step S1 is 150-250℃; In step S3, the red-burning temperature is 1000℃.

6. The method for simulating process conditions to regulate the dry quenching coke burn-off rate according to claim 1, characterized in that, The method for sampling coke material in step S2 includes the following steps: Take the coke from the dry-quenched furnace, discard the foamy coke and the furnace head coke, crush the coke into nearly spherical coke granules, remove the coke powder adhering to the coke granules, reduce the coke granules, dry them, and obtain several portions of coke material.

7. The method for simulating process conditions to regulate the dry quenching coke burn-off rate according to claim 6, characterized in that, The method for removing coke powder adhering to coke particles includes the following steps: The coke particles were soaked in a dispersant and then ultrasonicated. The dispersant is selected from one or more of methanol, ethanol, n-propanol, isopropanol, n-butanol, and isobutanol; The ultrasound duration is 0.5–1 hour, and the frequency is 30–50 kHz.

8. The method for simulating process conditions to regulate the dry quenching coke burn-off rate according to claim 1, characterized in that, The volumetric flow rate Q of the mixed gas in step S2 气体体积流量 The calculation formula is as follows: Q 气体体积流量 =GHSV 体积空速 ×V 焦炭材料堆积体积 Among them, the volume hourly space velocity (GHSV) of the circulating gas cooled by the reaction with coke in the fixed bed 体积空速 The circulating gas quantity Q of the dry quenching furnace 循环气体量 and cooling section volume V 冷却段内容积 Confirmed, the calculation formula is as follows:

9. The method for simulating process conditions to regulate the dry quenching coke burn-off rate according to claim 1, characterized in that, In step S3, the reactant gas is selected from one or more of oxygen, carbon dioxide, and water vapor, and nitrogen is used as the inert gas. The volume percentage concentration of oxygen is ≤3%, the volume percentage concentration of carbon dioxide is ≤20%, and the volume percentage concentration of water vapor is ≤15%. The dry quenching coke loss rate η 干熄焦烧蚀率 The calculations are used to guide the optimization of the circulating gas composition in industrial dry quenching furnaces.

10. A simulation device for regulating the dry quenching coke burn-off rate, characterized in that, The device simulates the control of dry quenching coke burn-off rate using the method described in any one of claims 1 to 9. The device includes a hanging basket (3), a balance (4), and a high-temperature furnace (5). The hanging basket (3) is suspended below the balance (4), and coke is placed inside the hanging basket (3). The hanging basket (3) is set inside the high-temperature furnace (5). The control is based on the mixed gas volume flow rate Q. 气体体积流量 The flow rate of each component is calculated by converting the concentration of each component in the mixed gas, and the flow rate of each component in the mixed gas is controlled. The mixed gas is introduced into the high-temperature furnace (5) to react with the coke. The temperature and time of the reaction in the high-temperature furnace (5) are recorded, and the mass of the coke before and after the reaction is recorded by the balance (4).

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