METHODS FOR PRODUCING SYNGAS FROM BIOMASS-CO2 COUPLED CONVERTER SMELTING PROCESSES

Abstract

A method for producing syngas from a biomass-CO.sub.2 coupled converter smelting process is provided, including: initiating smelting in a converter by injecting a primary injection gas while simultaneously injecting biomass and a carrier gas; 5-90 seconds after the smelting begins, increasing an injection flow rate of the primary injection gas from 60% to 100% of a designed flow rate, and keeping injecting the carrier gas at the designed flow rate; when an oxygen concentration in the syngas drops to 1%, injecting the biomass at the designed flow rate; in a mid-decarburization period: reducing the injection flow rate of the primary injection gas, and increasing the injection flow rate of the biomass to a maximum value; after a peak decarburization phase: increasing the injection flow rate of the primary injection gas, and decreasing the injection flow rates of the biomass and the carrier gas.

Claims

1. A method for producing syngas from a biomass-CO.sub.2 coupled converter smelting process, comprising: initiating smelting in a converter by injecting a primary injection gas while simultaneously injecting a biomass and a carrier gas, wherein the primary injection gas is oxygen (O.sub.2) or a mixture of O.sub.2 and CO.sub.2, injected at 60% of a designed flow rate; and the carrier gas is injected at the designed flow rate and includes CO.sub.2; 5-90 seconds after the smelting begins, increasing an injection flow rate of the primary injection gas from 60% to 100% of the designed flow rate, and keeping injecting the carrier gas at the designed flow rate: when an oxygen concentration in the syngas drops to 1%, injecting the biomass at the designed flow rate, while maintaining a powder-to-gas ratio of 0.5-1.5 between an injection flow rate of the biomass and an injection flow rate of the carrier gas throughout the smelting; in a mid-decarburization period: reducing the injection flow rate of the primary injection gas: increasing the injection flow rate of the biomass to a maximum value; and modulating in real-time the injection flow rate of the carrier gas and the injection flow rate of the biomass; after a peak decarburization phase: increasing the injection flow rate of the primary injection gas: decreasing the injection flow rate of the biomass and the injection flow rate of the carrier gas; and in a final smelting stage: further increasing the injection flow rate of the primary injection gas: further decreasing the injection flow rate of the biomass and the injection flow rate of the carrier gas; and terminating biomass injection after exceeding 90% of a total smelting duration to obtain the syngas.

2. The method according to claim 1, wherein the biomass is a biomass feedstock or a carbonized biomass, and the biomass has a particle size of 50 mesh-800 mesh, a moisture content 30 wt %, and a calorific value of 500-6000 kcal/kg.

3. The method according to claim 1, wherein during the mid-decarburization period, the powder-to-gas ratio is controlled to be in a range of 1.2-1.7: after the peak decarburization phase, the powder-to-gas ratio is controlled to be in a range of 1.1-1.4; and in the final smelting stage, the powder-to-gas ratio is controlled to be in a range of 0.8-1.2.

4. The method according to claim 1, wherein the method adopts an apparatus including: a syngas injection lance extending into an interior of the converter, wherein the syngas injection lance includes a primary injection gas channel for injecting the primary injection gas and a biomass conveying duct for co-injecting the biomass and the carrier gas, with the biomass conveying duct being connected to a biomass injection nozzle and the primary injection gas channel being connected to a main injection nozzle.

5. The method according to claim 4, wherein a vertical distance between an outlet of the biomass injection nozzle and an outlet of the main injection nozzle is in a range of 0-3 m.

6. The method according to claim 4, wherein the apparatus further includes a biomass carrier gas system and a biomass injection system connected to the biomass carrier gas system via the biomass conveying duct, wherein the biomass injection system is connected to the syngas injection lance.

7. The method according to claim 6, wherein the apparatus further includes an injection smelting system configured to set injection parameters for both the biomass carrier gas system and the biomass injection system.

8. The method according to claim 4, wherein the syngas injection lance is connected to an oxygen system through an oxygen channel.

9. The method according to claim 4, wherein the apparatus further includes a syngas composition analyzer configured to control both a lance height setting and injection parameters of the syngas injection lance.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0017] The present disclosure will be further illustrated by way of exemplary embodiments, which will be described in detail through the accompanying drawings. These embodiments are not limiting, and in these embodiments the same numbering indicates the same structure, wherein:

[0018] FIG. 1 is a flowchart of an exemplary process for producing syngas from a biomass-CO.sub.2 coupled converter smelting process according to some embodiments of the present disclosure;

[0019] FIG. 2 is an exemplary structural diagram of an apparatus adopted in a method for producing syngas from a biomass-CO.sub.2 coupled converter smelting process according to Embodiment 1 of the present disclosure;

[0020] FIG. 3 is an exemplary structural diagram of a syngas injection lance according to Embodiment 1 of the present disclosure; and

[0021] FIG. 4 is a diagram of variation in injection flow rates of a carrier gas, a biomass, and a primary injection gas according to Embodiment 1 of the present disclosure.

[0022] In the figures, 1syngas injection lance, 2converter, 3oxygen system, 4oxygen channel, 5biomass carrier gas system, 6biomass injection system, 7biomass injection channel, 8injection smelting system, 9syngas composition analyzer, 1-1primary injection gas channel, 1-2biomass conveying duct, 1-3main injection nozzle, 1-4biomass injection nozzle.

DETAILED DESCRIPTION

[0023] Flowcharts are used in the present disclosure to illustrate operations performed by a system according to embodiments of the present disclosure. It should be understood that the operations mentioned earlier or later are not necessarily executed in a precise sequence. Instead, the operations may be processed in reverse order or simultaneously. Meanwhile, other operations may be added to these processes, or one or more operations may be removed.

[0024] Embodiments of the present disclosure will be described in detail below in connection with embodiments, but it will be appreciated by those skilled in the art that the following embodiments are for a sole purpose of illustrating the present disclosure and should not be considered as limiting the scope of the present disclosure. In embodiments in which specific conditions are not noted, conventional conditions or conditions recommended by manufacturers are followed. Reagents or instruments used for which manufacturers are not indicated are conventional products which may be obtained through commercially available purchase.

[0025] FIG. 1 is a flowchart of an exemplary process for producing syngas from a biomass-CO.sub.2 coupled converter smelting process according to some embodiments of the present disclosure. As shown in FIG. 1, process 100 includes operation 110-operation 150. In some embodiments, the process 100 is executed by a computer device.

[0026] In 110, smelting in a converter is initiated by injecting a primary injection gas while simultaneously injecting a biomass and a carrier gas, wherein the primary injection gas is injected at 60% of a designed flow rate, and the carrier gas is injected at the designed flow rate.

[0027] The primary injection gas refers to a gas used to provide oxygen needed for a smelting reaction.

[0028] In some embodiments, the primary injection gas may include one or more types of gas. For example, the primary injection gas may be oxygen (O.sub.2) or a mixture of O.sub.2 and CO.sub.2.

[0029] In some embodiments, proportions of O.sub.2 and CO.sub.2 in the primary injection gas are determined by the computer device in a process parameter determination phase.

[0030] In some embodiments, in the process parameter determination phase prior to initiating smelting in the converter, process parameters for various phases of smelting may be determined by the computer device. For example, the computer device may determine the designed flow rate, an injection flow rate of the biomass, an injection flow rate of the carrier gas, a powder-to-gas ratio of the injection flow rate of the biomass to the injection flow rate of the carrier gas, an injection flow rate of the primary injection gas in a mid-decarburization period, an injection flow rate of the primary injection gas after a peak decarburization phase, and an injection flow rate of the primary injection gas in a final smelting stage.

[0031] In some embodiments, the computer device may determine the proportions of O.sub.2 and CO.sub.2 in the primary injection gas by querying a preset table. The preset table may include relationships between process phases and the proportion of CO.sub.2. In some embodiments, the preset table may be preset by the computer device based on defaults. For example, 5-90 seconds after initiating smelting in the converter, a volume ratio of CO.sub.2 to the primary injection gas is 5%; in the mid-decarburization period, a volume ratio of CO.sub.2 to the primary injection gas is 11%; after the peak decarburization phase, a volume ratio of CO.sub.2 to the primary injection gas is 8%; and in the final smelting stage, a volume ratio of CO.sub.2 to the primary injection gas is 0%. The biomass refers to a material used to produce the syngas.

[0032] In some embodiments, the biomass may be a biomass feedstock or a carbonized biomass. The biomass feedstock refers to a natural plant material (e.g., corn straw, rice husk, wood chips, coconut shells, etc.) that has not been thermochemically treated. The carbonized biomass refers to a virgin biomass which has been carbonized (e.g., carbonized pine carbon powder and coconut shell carbon powder).

[0033] In some embodiments, the biomass may be a powdered material. The biomass has a particle size of 50 mesh-800 mesh, a moisture content 30 wt %, and a calorific value of 500-6000 kcal/kg.

[0034] In some embodiments, the particle size of the biomass may be in a range of 50 mesh-125 mesh, 125 mesh-200 mesh, 200 mesh-275 mesh, 275 mesh-350 mesh, 350 mesh-425 mesh, 425 mesh-500 mesh, 500 mesh-575 mesh, 575 mesh-650 mesh, 650 mesh-725 mesh, or 725 mesh-800 mesh. In some embodiments, the particle size of the biomass may be one or more of 50 mesh, 125 mesh, 200 mesh, 275 mesh, 350 mesh, 425 mesh, 500 mesh, 575 mesh, 650 mesh, 725 mesh, 800 mesh, or the like.

[0035] In some embodiments, the calorific value of the biomass may in a range of 500-1050 kcal/kg, 1050-1600 kcal/kg, 1600-2150 kcal/kg, 2150-2700 kcal/kg, 2700-3250 kcal/kg, 3250-3800 kcal/kg, 3800-4350 kcal/kg, 4350-4900 kcal/kg, 4900-5450 kcal/kg, or 5450-6000 kcal/kg. In some embodiments, the calorific value of the biomass may be one or more of 500 kcal/kg, 1050 kcal/kg, 1600 kcal/kg, 2150 kcal/kg, 2700 kcal/kg, 3250 kcal/kg, 3800 kcal/kg, 4350 kcal/kg, 4900 kcal/kg, 5450 kcal/kg, 6000 kcal/kg, or the like.

[0036] In some embodiments of the present disclosure, consideration of the biomass feedstock and the carbonized biomass helps enhance the material selection versatility of biomass, reduce costs, facilitate rapid release of reducing gases, and increase CO production.

[0037] The carrier gas refers to a gaseous medium used to inject the biomass into the converter.

[0038] In some embodiments, the carrier gas may include a mixture of one or more of N.sub.2, Ar, O.sub.2, and CO.sub.2.

[0039] In some embodiments, the carrier gas may be used as a delivery medium to ensure proper fluidization and injection of the biomass.

[0040] In some embodiments, the carrier gas may also be directly involved in a reaction with the biomass to increase a carbon conversion rate.

[0041] In some embodiments, the primary injection gas may be injected to the converter through a primary injection gas channel of a syngas injection lance, and the biomass and the carrier gas may be injected to the converter through a biomass conveying duct of the syngas injection lance. The primary injection gas is injected at 60% of the designed flow rate and the carrier gas is injected at the designed flow rate.

[0042] In some embodiments, the primary injection gas may also be injected at 50%, 70%, 80%, etc., of the designed flow rate when the smelting in the converter is initiated.

[0043] More descriptions regarding the syngas injection lance, the primary injection gas channel, the biomass conveying duct, and the converter may be found in FIG. 2 and related description thereof.

[0044] It should be noted that at the beginning of the smelting in the converter, the temperature inside the converter cranium is low, and the Si and Mn contents in hot mental are high. Si and Mn react violently with O.sub.2. If the primary injection gas is injected at 100% of the designed flow rate at the beginning, localized over-oxidation may occur in the converter, along with significant molten pool splashing, which can easily lead to issues such as lance burning and lance clogging. The primary injection gas is injected at a lower percentage (e.g., 60%) of the designed flow rate at first. After the temperature inside the converter rises, and Si and Mn are consumed in large quantities, at which time it enters the mid-decarburization period, and the temperature is relatively high, the primary injection gas is then injected at 100% of the designed flow rate, which allows for a better carbon reaction, improves safety, and reduces spattering.

[0045] If the carrier gas solely excludes O.sub.2 and CO.sub.2 and is only responsible for transporting the biomass and does not take part in the reaction, the carrier gas may be injected at 100% of the designed flow rate at the beginning of the smelting in the converter. Because the temperature inside the converter is low and the concentration of O.sub.2 is high at the beginning of the smelting in the converter, injecting the biomass immediately at this time may cause the biomass to be completely burned, and the syngas unable to be generated. In order to avoid waste of the biomass, the biomass may not be injected immediately at the beginning of the smelting in the converter.

[0046] The designed flow rate refers to a preset volume of gas or a mass of material injected per unit time. For example, the designed flow rate may be a preset volume of injected primary injection gas or a preset mass of injected biomass in an hour.

[0047] The unit of the designed flow rate may be Nm.sup.3/h, kg/h, or kg/min.

[0048] In some embodiments, the designed flow rate may include a first designed flow rate, a second designed flow rate, and a third designed flow rate. The first designed flow rate refers to a designed flow rate of the primary injection gas, with a unit of Nm.sup.3/h, the second designed flow rate refers to a designed flow rate of the biomass, with a unit of kg/h or kg/min, and the third designed flow rate refers to a designed flow rate of the carrier gas, with a unit of Nm.sup.3/h.

[0049] In some embodiments, the computer device may preset the designed flow rate based on defaults in the process parameter determination phase. For example, in the process parameter determination phase, the computer device may determine the designed flow rate based on a nominal capacity of the converter, a recovery volume of the syngas, etc. The nominal capacity of the converter refers to a maximum weight of molten steel which the converter is capable of handling, with a unit of ton (t). The recovery volume of the syngas refers to a volume of syngas recovered from smelting each ton of steel, with a unit of Nm.sup.3/t.

[0050] In 120, 5-90 seconds after the smelting begins, the injection flow rate of the primary injection gas is increased from 60% to 100% of the designed flow rate, and the carrier gas is injected kept at the designed flow rate; when an oxygen concentration in the syngas drops to 1%, the biomass is injected at the designed flow rate, while a powder-to-gas ratio between the injection flow rate of the biomass and the injection flow rate of the carrier gas throughout the smelting is maintained in a range of 0.5-1.5.

[0051] In some embodiments, the oxygen concentration may be determined by a syngas composition analyzer.

[0052] More descriptions regarding the syngas composition analyzer may be found in FIG. 2 and related descriptions thereof.

[0053] The injection flow rate refers to a volume of gas or a mass of material injected per unit time. The unit of the injection flow rate may be Nm.sup.3/h, kg/h or kg/min.

[0054] In some embodiments, the injection flow rate may be determined by the syngas composition analyzer.

[0055] The powder-to-gas ratio refers to a ratio of the injection flow rate of the biomass to the injection flow rate of the carrier gas. The powder-to-gas ratio may be represented by a numerical value. The larger the numerical value, the larger the injection flow rate of the biomass over the injection flow rate of the carrier gas.

[0056] In some embodiments, a dimensionless ratio between the injection flow rate of the biomass and the injection flow rate of the carrier gas may be designated as the powder-to-gas ratio.

[0057] In some embodiments, the computer device controls the powder-to-gas ratio between the injection flow rate of the biomass and the injection flow rate of the carrier gas through controlling the injection flow rate of the carrier gas from a biomass carrier gas system and the injection flow rate of the biomass from a biomass injection system. In some embodiments, in the mid-decarburization period, the powder-to-gas ratio is controlled to be in a range of 1.2-1.7; after the peak decarburization phase, the powder-to-gas ratio is controlled to be in a range of 1.1-1.4; and in the final smelting stage, the powder-to-gas ratio is controlled to be in a range of 0.8-1.2. More descriptions regarding the biomass carrier gas system and the biomass injection system may be found in FIG. 2 and related descriptions thereof.

[0058] In some embodiments of the present disclosure, controlling the powder-to-gas ratio during different process phases is conducive to accurately matching reaction requirements, avoiding early over-oxygen burnout, ensuring full synergy between the biomass-CO.sub.2 in a mid-stage high-carbon zone, and preventing clogging in a final low-oxygen zone, thereby improving carbonization efficiency.

[0059] In 130, in the mid-decarburization period, the injection flow rate of the primary injection gas is reduced; the injection flow rate of the biomass is increased to a maximum value; and the injection flow rate of the carrier gas and the injection flow rate of the biomass are modulated in real-time.

[0060] The mid-decarburization period refers to a phase in which a large amount of carbon in hot mental in the converter is oxidized.

[0061] In some embodiments, the computer device may determine whether a process phase has reached the mid-decarburization period in a plurality of ways. For example, the computer device may determine the silicon content in the hot mental by sensors (e.g., X-ray fluorescence spectrometers, atomic absorption spectrometers, etc.), and when the silicon content in the hot mental is reduced below a first threshold (e.g., 0.03%), the process phase is determined to have entered the mid-decarburization period.

[0062] As another example, the computer device may determine the carbon content in the hot mental by sensors (e.g., X-ray fluorescence spectrometers, atomic absorption spectrometers, etc.), and when the carbon content in the hot mental is reduced below a second threshold (e.g., 1%), the process phase is determined to have entered the mid-decarburization period.

[0063] In some embodiments, the injection flow rate of the primary injection gas, which is decreased, may be preset by a technician based on experience.

[0064] For example, in response to the process phase reaching the mid-decarburization period, the technician may reduce the injection flow rate of the primary injection gas by 1.5%, 3%, 7%, etc., of the designed flow rate.

[0065] More descriptions regarding the injection flow rate of the primary injection gas, which is decreased, may be found in Embodiment 1, Embodiment 2, and Embodiment 3.

[0066] The maximum value of the injection flow rate refers to a maximum value of the injection flow rate of the biomass allowed for the mid-decarburization period.

[0067] In some embodiments, in the process parameter determination phase, the maximum value of the injection flow rate may be determined based on the designed flow rate and a process coefficient. The process coefficient refers to a maximum ratio of the injection flow rate allowed in the process phase. For example, the process coefficient of the mid-decarburization period may be 1.28 or 1.42, the process coefficient after the peak decarburization phase of smelting in the converter may be 0.94, 1.11, or 1.21, and the process coefficient of the final smelting stage may be 0.78 or 0.83.

[0068] For example, if the designed flow rate of the biomass is 230 kg/min and the process coefficient in the mid-decarburization period is 1.28, the maximum value of the injection flow rate of the biomass may be determined to be 295 kg/min.

[0069] In some embodiments, the computer device may modulate in real-time the injection flow rate of the carrier gas and the injection flow rate of the biomass based on the proportions of CO and CO.sub.2 in the syngas.

[0070] For example, if the syngas composition analyzer detects that the proportion of CO in the syngas is increased, and the proportion of CO.sub.2 is decreased, the computer device may generate an increment control instruction and control the biomass carrier gas system and the biomass injection system to increase the injection flow rate of the carrier gas and the injection flow rate of the biomass based on the increment control instruction, and if the syngas composition analyzer detects that the proportion of CO in the syngas is decreased and the proportion of CO.sub.2 is increased, the computer device may generate a decrement control instruction and control the biomass carrier gas system and the biomass injection system to reduce the injection flow rate of the carrier gas and the injection flow rate of the biomass based on the decrement control instruction.

[0071] In 140, after the peak decarburization phase, the injection flow rate of the primary injection gas is increased; the injection flow rate of the biomass and the injection flow rate of the carrier gas are decreased.

[0072] The peak decarburization phase refers to a stage in which a decarburization rate reaches a maximum value.

[0073] In some embodiments, the computer device may determine whether a process phase reaches an end of the peak decarburization phase based on a plurality of ways. For example, the computer device may determine the carbon content in the hot mental by sensors (e.g., X-ray fluorescence spectrometers, atomic absorption spectrometers, etc.), and when the carbon content in the hot mental is increased to a first preset range (e.g., 0.44%-0.66%), the process phase is determined to have reached the end of the peak decarburization phase.

[0074] In some embodiments, the injection flow rate of the primary injection gas, which is increased, may be preset by the technician based on experience.

[0075] For example, in response to the process phase reaching the end of the peak decarburization phase, the technician may increase the injection flow rate of the primary injection gas by 1.6% or 3% of the designed flow rate.

[0076] In 150, in the final smelting stage, the injection flow rate of the primary injection gas is further increased; the injection flow rate of the biomass and the injection flow rate of the carrier gas are further decreased; and the biomass injection is terminated after exceeding 90% of a total smelting duration to obtain the syngas.

[0077] The final smelting stage refers to a stage immediately prior to cessation of converter smelting.

[0078] In some embodiments, the computer device may determine whether the process phase has reached the final smelting stage in a plurality of ways. For example, the computer device may determine the carbon content in the molten steel by sensors (e.g., X-ray fluorescence spectrometers, atomic absorption spectrometers, etc.), and when the carbon content in the molten steel is reduced to a second preset range (e.g., 0.25%-0.35%), the process phase is determined to have reached the final smelting stage.

[0079] The total smelting duration refers to a length of time between the beginning the cessation of converter smelting.

[0080] In some embodiments, the total smelting duration may be preset by a technician based on experience.

[0081] The syngas refers to a mixed gas produced by the converter during the smelting process.

[0082] In some embodiments, the syngas may be a mixture of CO, CO.sub.2, and N.sub.2.

[0083] It should be noted that because an increase in the amount of the syngas is realized after the reaction is completed, the final amount of the syngas obtained may be determined by using a following formula (1):

[00001]$\begin{array}{cc}{M}_g=\frac{{{\mathrm{CO}}_2}_{}{}_{{\mathrm{CO}}_2}{}_{{\mathrm{CO}}_2}}{12}+M_z& \left(1\right)\end{array}$ [0084] where M.sub.g is a mass flow rate of the syngas, with a unit of kg/h, is the powder-to-gas ratio, .sub.CO.sub.2 is a total amount of CO.sub.2, with a unit of Nm.sup.3/h, .sub.CO.sub.2, is a density of CO.sub.2, with a unit of kg/m.sup.3, .sub.CO.sub.2 is a CO.sub.2 reaction rate, with a unit of %, and M.sub.z is a mass flow rate of different types of biomass resolving gas, with a unit of kg/h, wherein, the different types of biomass resolving gas may include CO, H.sub.2, CH.sub.4, etc.

[0085] More descriptions regarding producing the syngas from coupling biomass with CO.sub.2 shown in FIG. 1 may be found in detailed descriptions of Embodiments 1-3 in the present disclosure.

[0086] In some embodiments of the present disclosure, synergistic conversion of the biomass and CO.sub.2 is efficiently realized by using high-temperature and low-oxygen environment in the converter during the converter smelting process to generate syngas with a high calorific value and chemical raw materials. Compared with traditional coal syngas, the present disclosure reduces a large amount of energy consumed by external heat sources, does not need to add new large-scale equipment, and skillfully combines carbon-neutral feedstock biomass with industrial waste gas CO.sub.2 in the converter smelting process, thereby realizing high-value utilization of CO.sub.2 and the biomass, which can provide assistance for development of low-carbon technology in the iron and steel industry, provide a new process for preparation of cheap raw material gas in the chemical industry simultaneously, and promote the synergistic carbon reduction in cogeneration of steel-chemical industry.

[0087] FIG. 2 is an exemplary structural diagram of an apparatus adopted in a method for producing syngas from a biomass-CO.sub.2 coupled converter smelting process according to Embodiment 1 of the present disclosure.

[0088] In some embodiments, the apparatus adopted by the method for producing syngas from a biomass-CO.sub.2 coupled converter smelting process may include a syngas injection lance 1.

[0089] The syngas injection lance 1 refers to a component for transmitting the primary injection gas, the carrier gas, and/or the biomass.

[0090] In some embodiments, the syngas injection lance 1 may extend into an interior of a converter 2.

[0091] The converter 2 refers to a device configured to smelt steel.

[0092] In some embodiments, the syngas injection lance 1 may be disposed on a top portion of the converter 2.

[0093] FIG. 3 is an exemplary structural diagram of a syngas injection lance according to Embodiment 1 of the present disclosure.

[0094] In some embodiments, as shown in FIG. 3, the syngas injection lance 1 includes a primary injection gas channel 1-1 for injecting the primary injection gas and a biomass conveying duct 1-2 for co-injecting the biomass and the carrier gas. The primary injection gas channel 1-1 is connected to a main injection nozzle 1-3, and the biomass conveying duct 1-2 is connected to a biomass injection nozzle 1-4.

[0095] The primary injection gas channel 1-1 refers to a channel for delivering the primary injection gas to the converter 2.

[0096] In some embodiments, the primary injection gas channel 1-1 is disposed inside the syngas injection lance 1. An outlet end of the primary injection gas channel 1-1 is connected to an outlet of the main injection nozzle 1-3 of the syngas injection lance 1. The outlet of the main injection nozzle 1-3 is an outlet for injecting the primary injection gas from the syngas injection lance 1.

[0097] The biomass conveying duct 1-2 refers to a channel for delivering the biomass and the carrier gas to the converter 2.

[0098] In some embodiments, the biomass conveying duct 1-2 is disposed coaxially or side-by-side with the primary injection gas channel 1-1 within the syngas injection lance 1, and an outlet end of the biomass conveying duct 1-2 is connected to an outlet of the biomass injection nozzle 1-4 of the syngas injection lance 1. The outlet of the biomass injection nozzle 1-4 is an outlet for injecting the biomass and the carrier gas from the syngas injection lance 1.

[0099] In some embodiments, a vertical distance between the outlet of the biomass injection nozzle 1-4 and the outlet of the main injection nozzle 1-3 is in a range of 0-3 m.

[0100] In some embodiments, the vertical distance between the outlet of the biomass injection nozzle 1-4 and the outlet of the main injection nozzle 1-3 may also be 0.5 m, 1 m, 2 m, 2.5 m, etc.

[0101] It should be noted that during the converter smelting process, the location of the main injection nozzle 1-3 is generally unchanged, and the locations of the biomass injection nozzle 1-4 may be adjusted. When the location of the biomass injection nozzle 1-4 is adjusted, controlling the biomass injection nozzle 1-4 within a certain range is necessary. If the location of the biomass injection nozzle 1-4 is close to a liquid level of the molten steel, the biomass may be injected into the molten steel without fulfilling an intended function, so the nozzle cannot be too close to the liquid level of the molten steel. If the location of the biomass injection nozzle 1-4 is too high from the liquid level of the molten steel, furnace lining inside the converter is affected, and the concentration of flue gas is too large to be easily controlled, so the distance between the two nozzles needs to be controlled.

[0102] In some embodiments, the apparatus adopted by the method for producing syngas from a biomass-CO.sub.2 coupled converter smelting process may include a biomass carrier gas system 5 and a biomass injection system 6 connected to the biomass carrier gas system 5 via the biomass conveying duct 1-2.

[0103] In some embodiments, the biomass carrier gas system 5 and the biomass injection system 6 may also be connected via a biomass injection channel 7.

[0104] In some embodiments, the biomass injection channel 7 may be a part of the biomass conveying duct 1-2.

[0105] The biomass carrier gas system 5 may be configured to generate and transmit the carrier gas.

[0106] In some embodiments, the biomass carrier gas system 5 may include an air separation device, an gas storage tank, a pressure reducing valve, a piping system, a flow control valve, and an injection system, and the biomass carrier gas system 5 may separate air through the air separation device to generate the carrier gas, store the carrier gas in the gas storage tank, deliver the carrier gas in the gas storage tank to the syngas injection lance, and mix the carrier gas with the biomass to obtain a mixed gas and then inject the mixed gas into the converter 2. Compositions of the carrier gas may be selected from one or more of N.sub.2, CO.sub.2, or O.sub.2 according to a process requirement.

[0107] In some embodiments, the biomass carrier gas system 5 may be disposed on an outer side of the converter 2 and connected to the biomass injection system 6 via the biomass injection channel 7.

[0108] The biomass injection system 6 may be configured to store and deliver the biomass.

[0109] In some embodiments, the biomass injection system 6 may include a storage tank, a pressure reducing valve, a piping system, a flow control valve, and an injection system, and the biomass injection system 6 may store the biomass through the storage tank, deliver the biomass in the storage tank to the syngas injection lance, and mix the carrier gas with the biomass to obtain a mixed gas and then inject the mixed gas into the converter 2.

[0110] In some embodiments, the biomass injection system 6 may be disposed on an outer side of the converter 2 and connected to the syngas injection lance 1 via the biomass conveying duct 1-2.

[0111] In some embodiments, the apparatus adopted by the method for producing syngas from a biomass-CO.sub.2 coupled converter smelting process may further include an injection smelting system 8 configured to set injection parameters for both the biomass carrier gas system 5 and the biomass injection system 6.

[0112] The injection parameters refer to parameters for setting the biomass carrier gas system 5 and the biomass injection system 6.

[0113] In some embodiments, the injection parameters may include biomass carrier gas system parameters and biomass injection system parameters.

[0114] In some embodiments, the injection parameters may be set by the injection smelting system 8 based on defaults.

[0115] The injection smelting system 8 may be configured to generate the injection parameters.

[0116] In some embodiments, the injection smelting system 8 may be integrated into the computer device or a processor. The processor may include a central processing unit (CPU), an application specific integrated circuit (ASIC), a microcontroller, etc., or any combination thereof.

[0117] In some embodiments, the syngas injection lance 1 is connected to an oxygen system 3 through an oxygen channel 4.

[0118] The oxygen channel 4 may be configured to transmit oxygen.

[0119] In some embodiments, the oxygen channel 4 may connect the primary injection gas channel 1-1 and the oxygen system 3.

[0120] The oxygen system 3 may be configured to store and deliver oxygen to provide an oxygen source for the primary injection gas.

[0121] In some embodiments, the oxygen system 3 may include a reactor, a gas storage tank, a pressure reducing valve, a piping system, a flow control valve, and an injection system, and the oxygen system 3 may generate oxygen through the reactor, store the generated oxygen in the gas storage tank, deliver the oxygen in the gas storage tank to the syngas injection lance, and inject the oxygen into the converter 2.

[0122] In some embodiments, the oxygen system 3 may be disposed on an outer side of the converter 2.

[0123] In some embodiments, the apparatus adopted by the method for producing syngas from a biomass-CO.sub.2 coupled converter smelting process may further include a syngas composition analyzer 9.

[0124] The syngas composition analyzer 9 refers to a device configured to monitor components of the syngas at a mouth of the converter 2 and a percentage of each component.

[0125] In some embodiments, the syngas composition analyzer 9 may include a plurality of types. For example, the syngas composition analyzer 9 may include a laser detection type, an infrared detection type, etc.

[0126] In some embodiments, the syngas composition analyzer 9 may be disposed at the mouth or in a flue of the converter 2.

[0127] In some embodiments, the syngas composition analyzer 9 is configured to control both a lance height setting and injection parameters of the syngas injection lance 1.

[0128] For example, during the converter smelting process, the syngas composition analyzer 9 detects an increase of the oxygen concentration in the syngas, which indicates an increase of oxidizability in the converter, and at this time, the computer device automatically lowers the distance from a nozzle of the syngas injection lance 1 to a liquid level of a molten pool (the lance height setting) to make the syngas injection lance 1 closer to the molten pool, thereby improving an injection effect, promoting an oxidation-reduction reaction, and reducing the oxygen concentration.

[0129] As another example, when the syngas composition analyzer 9 detects that the CO concentration is too low, the computer device may automatically increase the injection flow rate of the biomass while appropriately adjusting the injection flow rate of the carrier gas to increase the oxidation reaction rate of carbon in the converter, thereby increasing the amount of CO generated and optimizing components of the syngas.

[0130] The lance height setting refers to a vertical distance between an end of the syngas injection lance 1 and the liquid level of the molten steel in the converter 2.

[0131] In some embodiments, the syngas composition analyzer 9 may monitor the percentage of each component of the syngas in real time and send the percentage to the computer device to generate a control instruction to control the lance height setting of the syngas injection lance 1.

Embodiment 1

[0132] As shown in FIG. 2, in this embodiment, the process is applied to 300-ton converter steelmaking, with gas recovery adopting LT dry de-dusting, a recovery volume of the syngas (converter gas) is 128 Nm.sup.3/t steel, and a calorific value of the syngas is 1260 kcal/Nm.sup.3. The primary injection gas of the syngas injection lance 1 is O.sub.2, which is delivered by the oxygen system 3 through the oxygen channel 4, with a designed flow rate of 62000 Nm.sup.3/h. The carrier gas of the biomass conveying duct 1-2 is CO.sub.2 with a concentration of 99.5% and a designed flow rate of 8000 Nm.sup.3/h. The vertical distance between an outlet of the main injection nozzle 1-3 of the primary injection gas channel 1-1 and an outlet of the biomass injection nozzle 1-4 of the biomass conveying duct 1-2 is 1.4 m. A specific structure of the syngas injection lance 1 is shown in FIG. 3. A biomass storage capacity of the biomass injection system 6 is 4 t, and the syngas composition analyzer 9 adopts a laser detection type. Based on data of the syngas composition analyzer 9, the computer device controls the injection parameters and the lance height setting of the syngas injection lance 1 and modulates in real-time the powder-to-gas ratio and other parameters of biomass injection. The biomass is carbonized pine biomass carbon powder with a calorific value of 3750 kcal/kg, a particle size of 50 mesh-800 mesh, and a moisture content 30 wt %.

[0133] Within 90 seconds of initiating the converter smelting, the injection flow rate of the primary injection gas of the syngas injection lance 1 is increased from 60% to 100% of the designed flow rate, and the carrier gas of the biomass conveying duct 1-2 is kept unchanged of 7000 Nm.sup.3/h. Based on the syngas composition analyzer 9 displaying the O.sub.2 concentration in the syngas 1%, the biomass injection system 6 is started, a control valve of the biomass injection system 6 is opened, and the injection parameters of the biomass carrier gas system 5 and the biomass injection system 6 are set by the injection smelting system 8. Injection media are CO.sub.2 and the biomass, with the biomass delivered by the biomass carrier gas system 5 through the biomass injection channel 7. The injection flow rate of the biomass injection is set to 230 kg/min and an initial lance height setting of the syngas injection lance 1 is set to 2.5 m, while maintaining the powder-to-gas ratio of 1 between the injection flow rate of the biomass and the injection flow rate of the carrier gas.

[0134] When the converter smelting reaches the mid-decarburization period for 5-10 minutes, the injection flow rate of the primary injection gas O.sub.2 is adjusted to 60000 Nm.sup.3/h, the injection flow rate of the carrier gas of the biomass conveying duct 1-2 is adjusted to 6000 Nm.sup.3/h, the injection flow rate of the biomass is adjusted to 295 kg/min, and the injection flow rate of biomass-CO.sub.2 conversion to syngas reaches a maximum value. According to actual converter smelting, the injection flow rate of CO.sub.2 carrier gas and the injection flow rate of the biomass are modulated in real-time with an adjustment amplitude of 5%, and the powder-to-gas ratio is maintained at an average of 1.51 to realize rapid conversion of the biomass-CO.sub.2 in the mid-decarburization period.

[0135] After the peak decarburization phase of the converter smelting, the injection flow rate of the primary injection gas O.sub.2 is adjusted to 63000 Nm.sup.3/h, the injection flow rate of the carrier gas of the biomass conveying duct 1-2 is 6500 Nm.sup.3/h, and the injection flow rate of the biomass is 255 kg/min, the powder-to-gas ratio between the injection flow rate of the biomass and the injection flow rate of the carrier gas is maintained at 1.2, and the lance height setting of the syngas injection lance 1 is raised by 0.5 m, thereby maintaining output of the syngas and biomass conversion efficiency after the peak decarburization phase.

[0136] In the final smelting stage, the injection flow rate of the primary injection gas O.sub.2 is modulated in real-time to 65000 Nm.sup.3/h, the injection flow rate of the carrier gas of the biomass conveying duct 1-2 is adjusted to 5000 Nm.sup.3/h, and the injection flow rate of the biomass is adjusted to 180 kg/min, while maintaining the powder-to-gas ratio of 1.1 between the injection flow rate of the biomass and the injection flow rate of the carrier gas. While reaching a phase of 90% of the total smelting duration, based on the data of the syngas composition analyzer 9, the computer device firstly shuts off the biomass injection system 6, then adjusts the injection flow rate of the carrier gas of the biomass conveying duct 1-2 to 3000 Nm.sup.3/h, and lowers the distance of the nozzle of the syngas injection lance 1 from the liquid level of the molten pool (the lance height setting) to 1.8 m, thereby realizing stabilized control of steel composition and temperature at the end of the converter smelting.

[0137] After reaching an index of the converter smelting, the syngas injection lance 1 is raised and the steel is discharged. At the same time, a pressure relief device of the biomass injection system is opened and charging of the biomass is started to prepare for next converter smelting.

[0138] The total amount of the biomass injected during the converter smelting process is 3200 kg, and the injection amount per ton of steel is 10.81 kg, thereby realizing conversion of industrial exhaust CO.sub.2 by 5376 Nm.sup.3, an increase in syngas production by 10750 Nm.sup.3, and an increase of CO concentration in the gas by 11.8%. Variation in injection flow rates of the carrier gas, the primary injection gas, and the biomass of the specific process is shown in FIG. 4.

Embodiment 2

[0139] In this embodiment, the process is applied to 120-ton converter steelmaking, and the steel grade is HRB400. The gas recovery adopts OG wet de-dusting, the CO content in the syngas is 42.8%, and the recovery volume of the syngas (the converter gas) is 144 Nm.sup.3/t steel. The biomass is carbonized coconut husk biomass carbon powder with a calorific value of 3920 kcal/kg, a particle size of 50 mesh-800 mesh, and a moisture content 30 wt %. The vertical distance between the outlet of the main injection nozzle 1-3 of the syngas injection lance 1 and the outlet of the biomass injection nozzle 1-4 is 0.6 m. The primary injection gas is a mixture of O.sub.2 and CO.sub.2, with a total designed flow rate of 28000 Nm.sup.3/h. The carrier gas of the biomass conveying duct 1-2 is a mixture of N.sub.2 and CO.sub.2, with a designed flow rate of 4000 Nm.sup.3/h. The biomass storage capacity of the biomass injection system 6 is 3 t, and the syngas composition analyzer 9 adopts an infrared detection type. The data of the syngas composition analyzer 9 is acquired online during the smelting process, the lance height setting and the injection parameters of the syngas injection lance are controlled, and the powder-to-gas ratio and other parameters of the biomass injection are modulated in real-time.

[0140] Within 5 seconds of initiating the converter smelting, the injection flow rate of the primary injection gas (the mixture of O.sub.2 and CO.sub.2, with CO.sub.2 accounting for 5%) of the syngas injection lance 1 reaches 100%, and the biomass injection system 6 is started. The control valve of the biomass injection system 6 is opened, the injection flow rate of the biomass is set to 120 kg/min, and an initial lance position of the syngas injection lance 1 is set to 1.7 m. Based on a flame state at the mouth of the converter, the injection flow rate of the biomass is modulated in real-time, the powder-to-gas ratio is maintained at 0.8, and the injection flow rate of the carrier gas of the biomass conveying duct 1-2 is regulated by the powder-to-gas ratio.

[0141] When the converter smelting reaches the mid-decarburization period, the injection flow rate of the primary injection gas (the mixture of O.sub.2 and CO.sub.2, with CO.sub.2 accounting for 11%) is adjusted to 26000 Nm.sup.3/h, the injection flow rate of the biomass is adjusted to 170 kg/min, and the lance position of the syngas injection lance 1 is dropped to 1.9 m. Based on the overflow state of the converter smelting slag and flue gases, the injection flow rate of the biomass is adjusted with an adjustment range of 5% and the powder-to-gas ratio is maintained at 1.2 to maximize the conversion efficiency of CO.sub.2.

[0142] After the peak decarburization phase of the converter smelting, the injection flow rate of the primary injection gas (the mixture of O.sub.2 and CO.sub.2, with CO.sub.2 accounting for 8%) is adjusted to 27000 Nm.sup.3/h, the powder-to-gas ratio is maintained at 1.1, and the injection flow rate of the biomass is adjusted to 145 kg/min to realize an increase of the total amount of the syngas.

[0143] In the final smelting stage, the injection flow rate of the primary injection gas O.sub.2 is modulated in real-time to 30000 Nm.sup.3/h, the injection flow rate of the biomass is adjusted to 100 kg/min, and the powder-to-gas ratio between the injection flow rate of the biomass and the injection flow rate of the carrier gas is maintained at 0.9. While reaching a phase of 95% of the total smelting duration, the biomass injection system 6 is firstly shut off, and then the carrier gas of the biomass conveying duct 1-2 is adjusted to N.sub.2, the injection flow rate of the carrier gas is adjusted to 1000 Nm.sup.3/h, and the distance of the nozzle of the syngas injection lance 1 from the liquid level of the molten pool (the lance height setting) is lowered to 1.5 m, thereby realizing the stabilized control of the steel composition and temperature at the end of the converter smelting.

[0144] After reaching the index of the converter smelting, the syngas injection lance 1 is raised and the steel is discharged. At the same time, the pressure relief device of the biomass injection system is opened and charging of the biomass is started to prepare for the next converter smelting.

[0145] The total amount of the biomass injected during the converter smelting process is 1550 kg, and the injection amount per ton of steel is 12.4 kg, thereby realizing the conversion of industrial exhaust CO.sub.2 by 2459 Nm.sup.3, the increase in syngas production by 4920 Nm.sup.3, and the increase in syngas recovery by 21.6%.

Embodiment 3

[0146] In this embodiment, the process is applied to 100-ton converter steelmaking, the gas recovery adopts the OG wet de-dusting, the CO content in the syngas is 43%, and the recovery volume of the syngas (the converter gas) is 135 Nm.sup.3/t. The biomass is corn straw biomass feedstock, and in order to ensure powder fluidity, 30% carbonized coconut husk biomass carbon powder is mixed in the biomass. the calorific value of the biomass is 2040 kcal/kg, the vertical distance between the outlet of the main injection nozzle 1-3 of the syngas injection lance 1 and the outlet of the biomass injection nozzle 1-4 is 0.5 m, the primary injection gas is O.sub.2 with a total designed flow rate of 23000 Nm.sup.3/h, the carrier gas of the biomass conveying duct 1-2 is CO.sub.2 with a designed flow rate of 4000 Nm.sup.3/h, the biomass storage capacity of the biomass injection system 6 is 3 t, and the syngas composition analyzer 9 adopts the infrared detection type. The data of the syngas composition analyzer 9 is acquired online during the smelting process, the lance height setting and injection parameters of syngas injection lance 1 are controlled, and the powder-to-gas ratio and other parameters of the biomass injection are modulated in real-time. The biomass has the particle size of 50 mesh-800 mesh and the moisture content 30 wt %.

[0147] Within 10 seconds of initiating the converter smelting, the injection flow rate of the primary injection gas of the syngas injection lance 1 reaches 23000 Nm.sup.3/h, the distance of the nozzle of the syngas injection lance 1 from the liquid level of the molten pool (the lance height setting) is lowered to 1.5 m, the biomass injection system 6 is started, and the injection flow rate of the biomass is set to 180 kg/min. Based on the flame state at the mouth of the converter, the injection flow rate of the biomass is modulated in real-time, the powder-to-gas ratio is maintained at 1.5, and the injection flow rate of the carrier gas of the biomass conveying duct 1-2 is regulated by the powder-to-gas ratio.

[0148] When the converter smelting reaches the mid-decarburization period, the injection flow rate of the primary injection gas O.sub.2 is adjusted to 20000 Nm.sup.3/h, the injection flow rate of the biomass is adjusted to 230 kg/min, and the lance height setting of the syngas injection lance 1 is increased to 1.8 m. Based on the overflow state of the converter smelting slag and flue gases, the injection flow rate of the biomass is adjusted with an adjustment range of 5% and the powder-to-gas ratio of 1.7 is maintained at 1.7.

[0149] After the peak decarburization phase of the converter smelting, the injection flow rate of the primary injection gas O.sub.2 is adjusted to 22000 Nm.sup.3/h, the injection flow rate of the biomass is adjusted to 170 kg/min, and the powder-to-gas ratio is maintained at 1.4.

[0150] In the final smelting stage, the injection flow rate of the primary injection gas O.sub.2 is modulated in real-time to 25000 Nm.sup.3/h, the injection flow rate of the biomass is adjusted to 140 kg/min, and the powder-to-gas ratio is maintained at 1.0. While reaching a phase of 95% of the total smelting duration, the biomass injection system 6 is firstly shut off, and then the injection flow rate of the carrier gas of the biomass conveying duct 1-2 is adjusted to 1000 Nm.sup.3/h, and the lance height setting of the syngas injection lance 1 is lowered to 1.2 m, thereby realizing the stabilized control of the steel composition and temperature at the end of the converter smelting.

[0151] After reaching the index of the converter smelting, the syngas injection lance 1 is raised and the steel is discharged. At the same time, the pressure relief device of the biomass injection system is opened, and charging of the biomass is started to prepare for the next converter smelting.

[0152] The total amount of the biomass injected during the converter smelting process is 2130 kg, and the injection amount per ton of steel is 20.3 kg, thereby realizing the conversion of industrial exhaust CO.sub.2 by 2386 Nm.sup.3 and the increase in syngas production by 4458 Nm.sup.3.

[0153] While the present disclosure has been illustrated and described in terms of specific embodiments, however, it should be realized that many other changes and modifications may be made without departing from the spirit and scope of the present disclosure. Thus, it is intended that all such changes and modifications falling within the scope of the present disclosure are included in the appended claims.