A molten metal reactor vessel

Abstract

The present application relates to a kind of molten metal reaction kettle, belong to the recycling technology field based on recyclable, renewable resources such as domestic waste, industrial waste and biomass, solve the problem that macromolecular organic matter in prior art is not completely decomposed, leading to cannot realize the same quality or high-quality utilization problem, and secondary pollution to environment and other problems.A kind of molten metal reaction kettle, characterized by, including by gas-liquid passage intercommunication first molten metal reaction kettle and secondary molten metal reaction kettle;The first molten metal reaction kettle inside is equipped with first metal pool, secondary molten reaction kettle inside is equipped with second metal pool, wherein the bottom of second metal pool is higher than the bottom of first metal pool, and first molten metal reaction kettle and secondary molten metal reaction kettle staggered arrangement horizontally.It is realized that domestic waste, industrial waste and biomass and other recyclable, renewable resources are the same quality and high-quality recycling.

Description

Technical Field

[0001] This invention relates to the field of recycling technology based on recyclable and renewable resources such as municipal solid waste, industrial waste and biomass, and particularly to a molten metal reactor. Background Technology

[0002] Against the backdrop of global carbon reduction, three sectors are widely recognized as struggling to break free from carbon dependence: aviation and shipping, ocean shipping, and plastics manufacturing. Recycling and reusing recyclable resources, reusing renewable resources, and converting carbon dioxide can reduce reliance on primary fossil fuels to some extent. However, the extremely high stability and cost of capturing carbon dioxide make its direct conversion and utilization a significant challenge. Therefore, recycling and reusing recyclable resources and reusing renewable resources have become more realistic and preferred options.

[0003] Currently, the main technologies for the resource and energy utilization of biomass (a renewable resource) and low-quality waste plastics (a recyclable resource) are thermal treatment technologies, divided into direct incineration and pyrolysis gasification. Direct incineration, being a solid-state heterogeneous combustion process, suffers from incomplete combustion, low efficiency, and secondary pollution, particularly dioxin emissions, which hinders its widespread application. Pyrolysis gasification, on the other hand, can convert municipal solid waste into three relatively stable products: gas, liquid, and solid, effectively improving its utilization efficiency, scope, and economic viability. From a pollutant emission perspective, the pyrolysis gasification process takes place in an oxygen-deficient or oxygen-deficient atmosphere, which in principle reduces dioxin formation. Simultaneously, most heavy metals dissolve into the ash during pyrolysis gasification, reducing emissions. Therefore, developing pyrolysis gasification technology is an important way to achieve the harmless, resource-based, and energy-based utilization of municipal solid waste.

[0004] Pyrolysis gasification technology utilizes thermal energy under anaerobic or hypoxic conditions to cause reactions such as bond breaking, isomerization, and small-molecule polymerization in the components of a gas, converting large-molecule organic matter into small-molecule fuel gas, tar, and coke. Existing pyrolysis gasification technologies, such as the Landgard system using rotary kiln pyrolysis, the CAO system using grate combustion technology, and the Purox system using an internally heated moving bed, generally suffer from problems such as complex target product composition, poor quality, high subsequent reuse costs, and inability to achieve high-quality utilization. Furthermore, the flue gas produced during gasification may contain harmful substances such as nitrogen oxides, dioxins, and heavy metals, causing secondary pollution to the environment. Additionally, the processes are complex, and construction and operating costs are high. Summary of the Invention

[0005] In view of the above analysis, the present invention aims to provide a molten metal reactor to solve at least one of the following problems: the inability of existing pyrolysis gasification equipment to achieve the same or even high quality of reuse, and the complexity of its structure.

[0006] On one hand, embodiments of the present invention provide a molten metal reactor, including a primary molten metal reactor and a secondary molten metal reactor that are interconnected by a gas-liquid channel;

[0007] The primary molten metal reactor has a first metal pool inside, and the secondary molten metal reactor has a second metal pool inside. The bottom of the second metal pool is higher than the bottom of the first metal pool, and the primary and secondary molten metal reactors are horizontally staggered.

[0008] Furthermore, the gas-liquid channel is a semi-conical channel, and the axial section of the semi-conical channel is higher than the curved surface of the semi-conical channel.

[0009] Specifically, the semi-conical channel includes a channel inlet, a channel body, and a channel outlet. The channel inlet is connected to the primary molten metal reactor, and the channel outlet is connected to the secondary molten metal reactor.

[0010] Both the channel entrance and the channel exit are semi-circular in shape, with the diameter of the channel entrance being larger than the diameter of the channel exit, and their center lines being collinear and aligned.

[0011] For example, there is a distance between the centerline of the channel inlet and the bottom of the primary molten metal reactor, and the bottom arc of the channel outlet is in contact with the bottom of the secondary molten metal reactor.

[0012] Furthermore, the main body of the channel includes a primary molten metal reactor sidewall section and a secondary molten metal reactor sidewall section, the channel inlet is formed in the inner sidewall of the primary molten metal reactor, and the channel outlet is formed in the inner sidewall of the secondary molten metal reactor.

[0013] Preferably, the top of the primary molten metal reactor is provided with a feed inlet and a gasifying agent spray gun installation port; the top of the secondary molten metal reactor is provided with a synthesis gas outlet; and a slag-liquid pool is provided above the second metal pool of the secondary molten metal reactor.

[0014] Furthermore, both the first-stage molten metal reactor and the second-stage molten metal reactor are provided with molten grooves at their bottoms, which are located below the first metal pool and the second metal pool.

[0015] Preferably, both the primary molten metal reactor and the secondary molten metal reactor are equipped with electromagnetic induction external heating devices on their inner sidewalls.

[0016] On the other hand, embodiments of the present invention also provide a gasification method based on molten metal, wherein materials containing polymer compounds undergo decomposition and gasification reactions in a molten metal reactor to generate an inorganic mixed gas.

[0017] Specifically, the decomposition and gasification reaction process is as follows:

[0018] S1-1. The material is dropped from the top of the primary molten metal reactor 1. At the same time as the material is dropped, the gasifying agent is sprayed onto the upper part of the liquid surface of the first metal pool 101 through the gasifying agent spray gun above the primary molten metal reactor 1. The material undergoes a primary gasification reaction under the action of molten metal and gasifying agent, and the first mixed gas is obtained after the reaction.

[0019] S1-2, the first mixed gas is injected into the bottom of the molten metal in the secondary molten metal reactor 2 through the gas-liquid channel, and then passes upward through the molten metal layer and slag liquid layer to carry out a secondary gasification reaction to obtain an inorganic mixed gas.

[0020] Compared with the prior art, the present invention can achieve at least one of the following beneficial effects:

[0021] 1. This invention designs a reaction vessel based on molten metal, employing a two-stage molten metal reaction vessel interconnected by a gas-liquid channel to decompose and gasify materials containing high molecular weight polymers. The crude gas (gasified gas containing organic components) generated by the gasification in the first-stage molten metal reaction vessel is injected into the bottom layer of the molten metal in the second-stage molten metal reaction vessel through the gas-liquid channel. The crude gas is further decomposed and completely gasified into an inorganic mixed gas after passing through the high-temperature molten metal layer and the high-temperature slag liquid layer in the second-stage molten metal reaction vessel, ensuring that no polymer escapes.

[0022] 2. The gas-liquid channel between the primary molten metal reactor and the secondary molten metal reactor of the present invention adopts a semi-conical structure channel design, forming a gradually narrowing conical path from the channel inlet to the channel outlet. The channel is always wetted with molten metal, ensuring that the material will not block the channel.

[0023] 3. The interconnected design of the metal pools with different heights in this invention ensures that the minimum cross-sectional area of ​​the channel is completely filled with molten metal. This effectively prevents the accumulation of lumpy materials and potential blockages. Furthermore, it ensures that no gas exchange can occur between the two reaction vessels before the reaction.

[0024] 4. The secondary molten metal reactor of the present invention includes a molten metal layer and a slag liquid layer. The molten slag and crude gas generated after the material reacts in the primary molten metal reactor are sprayed together into the secondary molten metal reactor and finally enter the slag liquid layer of the secondary molten metal reactor. The slag liquid is periodically discharged from the reaction system through the upper slag discharge port. The design of the slag liquid layer further avoids the escape of large molecular organic matter, and at the same time can capture harmful components such as sulfur, salt, and ash to ensure the purity of the product gas.

[0025] 5. The bottom of both the primary and secondary molten metal reactors of this invention is provided with a melting groove, and the inner sidewalls of both the primary and secondary molten metal reactors are provided with an electromagnetic induction external heating device, which can heat the molten metal by electromagnetic vortex method and maintain the heat of the metal pool. The structure is simple and the operation is convenient.

[0026] 6. This invention targets various types of municipal solid waste and / or industrial waste containing polymers, especially polymers containing bromides. It designs a two-stage gasification reaction based on a molten metal reactor. Using molten metal as the medium, a gasifying agent is used to decompose the polymer compounds, completely decomposing renewable and recyclable materials containing polymers into an inorganic mixture, including CO, H2, CO2, and small amounts of escaped inorganic gases such as HCl and HBr. The purified inorganic mixture is a synthesis gas (CO+H2) with a volume fraction greater than 90% and the remainder being CO2. The purified mixture can then be used in subsequent processing stages, such as producing green methanol, sustainable aviation fuel (SAF), and high-quality green plastics through Fischer-Tropsch synthesis, which helps to gradually reduce dependence on single-use petrochemical resources.

[0027] The polymer material first undergoes a rapid primary gasification reaction under the action of molten metal and a gasifying agent, generating a first mixed gas containing organic compounds ranging from methane to C40. The first mixed gas then passes through the molten metal again and undergoes a secondary gasification reaction with the help of the gasifying agent, completely decomposing into an inorganic mixed gas. The inorganic mixed gas further passes through the slag liquid layer, capturing ash, sulfur, chlorides, etc. into the slag liquid, making the obtained product syngas purer and preventing problems such as coking at the downstream end.

[0028] In this invention, the above-described technical solutions can be combined with each other to achieve more preferred combinations. Other features and advantages of this invention will be set forth in the following description, and some advantages may become apparent from the description or be learned by practicing the invention. The objects and other advantages of this invention can be realized and obtained from what is particularly pointed out in the description and drawings. Attached Figure Description

[0029] The accompanying drawings are for illustrative purposes only and are not intended to limit the invention. Throughout the drawings, the same reference numerals denote the same parts.

[0030] Figure 1 This is an external view of the molten metal reactor of the present invention;

[0031] Figure 2 This is a cross-sectional view of the molten metal reaction vessel of the present invention;

[0032] Figure 3This is a diagram showing the working state of the molten metal reactor of the present invention after molten iron and slag are added;

[0033] Figure 4 This is a diagram of the material feeding and preheating system of the present invention;

[0034] Figure 5 This is a diagram of the external heat exchange system of the feeding tank of the present invention;

[0035] Figure 6 For the present invention Figure 5 Enlarged view of a portion of point A in the middle;

[0036] Figure 7 This is a longitudinal sectional view of the feeding tank of the present invention;

[0037] Figure 8 This is a front view of the rotating shaft and the feeding plate of the present invention;

[0038] Figure 9 This is a top view of the inner feed plate unit and the rotation axis of the present invention;

[0039] Figure 10 This is a front view of the first blade of the present invention;

[0040] Figure 11 This is a top view of the upper outer part of the upper region of the rotating shaft and the rotating shaft of the present invention;

[0041] Figure 12 This is a top view of the lower outer part of the lower region of the rotating shaft and the rotating shaft of the present invention;

[0042] Figure 13 This is a top view of the upper section of the tapered discharge port and the rotating axis of the present invention.

[0043] Figure 14 This is a top view of the material scraper and rotating shaft of the present invention;

[0044] Figure 15 This is a top view of the material discharge flange of the present invention;

[0045] Figure 16 This is a three-dimensional structural diagram of the conical discharge port, discharge port flange, and scraper blade of the present invention;

[0046] Figure 17 This is a schematic diagram of the angular relationship of the inner material feeding unit from a top-down view of the present invention. Figure 1 ;

[0047] Figure 18 This is a schematic diagram of the angular relationship of the inner material feeding unit from a top-down view of the present invention. Figure 2 ;

[0048] Figure 19 This is a schematic diagram of the angle relationship of the inner side material feeding piece unit from the main viewpoint in Embodiment 5 of the present invention;

[0049] Figure 20 This is a schematic diagram of the angle relationship of the outer upper material feeding plate unit from a top view in Embodiment 5 of the present invention;

[0050] Figure 21 This is a schematic diagram of the angle relationship of the lower outer part of the material feeding plate unit from a top view in Embodiment 5 of the present invention;

[0051] Figure 22 This is a schematic diagram of the angle relationship of the outer material feeding plate unit from the main viewpoint in Embodiment 5 of the present invention;

[0052] Figure 23 This is a diagram of the gasification system based on molten metal in Embodiment 1 of the present invention.

[0053] Figure label:

[0054] 1- Primary molten metal reactor; 101- First metal pool; 102- Feed inlet; 2- Secondary molten metal reactor; 201- Second metal pool; 202- Slag-liquid pool; 3- Gas-liquid channel; 4- Drain outlet; 501- Upper slag outlet; 502- Middle slag outlet; 503- Lower slag outlet; 601- First gasifying agent spray gun installation port; 602- Second gasifying agent spray gun installation port; 7- Third gasifying agent spray gun installation port; 8- Biomass spray gun installation port; 9- Syngas outlet; 10- Second screw conveyor; 11- Melting trench; 12- Third gasifying agent spray gun; 13- Biomass spray gun; 14- First gasifying agent spray gun; 15- Second gasifying agent spray gun; 16- Transfer tank A; 17- Transfer Material tank B; 18-First screw conveyor; 19-Feeding tank; 20-Second screw conveyor; 21-Material tank body; 22-Discharge port flange; 23-Heat exchange jacket; 24-Medium inlet; 25-Medium outlet; 26-Fin; 27-Conical discharge port; 28-Narrow flange; 29-Rotating shaft; 30-Inner side material feeding plate unit; 31-Outer upper material feeding plate; 32-Outer lower material feeding plate; 33-Lower end bearing; 34-Upper end bearing; 35-Second blade; 36-First drive shaft; 37-Third blade; 38-First blade; 39-Second drive shaft; O1-Center of the cross-section of the rotating shaft; O2-Center of the outer arc of the first blade; a-Central angle of the first blade. Detailed Implementation

[0055] Preferred embodiments of the present invention will now be described in detail with reference to the accompanying drawings, which form part of this application and are used together with the embodiments of the present invention to illustrate the principles of the present invention, but are not intended to limit the scope of the present invention.

[0056] On one hand, a specific embodiment of the present invention discloses a molten metal reactor 1, comprising a primary molten metal reactor 1 and a secondary molten metal reactor 2 that are interconnected by a gas-liquid channel 3;

[0057] The primary molten metal reactor 1 is provided with a first metal pool 101 inside, and the secondary molten metal reactor 2 is provided with a second metal pool 201 inside. The bottom of the second metal pool 201 is higher than the bottom of the first metal pool 101, and the primary molten metal reactor 1 and the secondary molten metal reactor 2 are horizontally staggered.

[0058] The height difference between the metal pools of the secondary molten metal reactor 2 and the primary molten metal reactor 1 ensures that the primary molten metal reactor 1 has sufficient molten pool volume to maintain the gasification reaction, and also ensures that the gas generated in the primary molten metal reactor 1 enters the bottom of the molten metal in the secondary molten metal reactor 2. The secondary molten metal reactor 2 has sufficient molten pool height to ensure a complete reaction. This ensures that the large molecular gases that did not have sufficient contact with the molten iron in the primary molten metal reactor 1 have sufficient contact with the molten iron in the secondary molten metal reactor 2, ensuring complete gasification into inorganic substances and the absence of large molecular gases.

[0059] Preferably, the gas-liquid channel 3 is a semi-conical channel, and the axial section of the semi-conical channel is higher than the curved surface of the semi-conical channel.

[0060] Furthermore, the semi-conical channel includes a channel inlet, a channel body, and a channel outlet. The channel inlet is connected to the primary molten metal reactor, and the channel outlet is connected to the secondary molten metal reactor. Both the channel inlet and the channel outlet are semi-circular in shape, with the diameter of the channel inlet being larger than the diameter of the channel outlet, and their center lines being collinear and aligned.

[0061] Specifically, there is a distance between the centerline of the channel inlet and the bottom of the primary molten metal reactor, and the bottom arc of the channel outlet is in contact with the bottom of the secondary molten metal reactor.

[0062] Preferably, the distance between the centerline of the channel inlet and the bottom of the primary molten metal reactor is determined according to the volume of the first metal pool and the liquid level of the molten metal in the first metal pool. When the first metal pool is filled with molten metal, the top of the channel inlet is flush with the liquid level of the molten metal.

[0063] In one possible design, the first metal pool 101 has a volume of 56 cubic meters, and the distance between the upper end of the channel inlet and the bottom of the first metal pool 101 inside the primary molten metal reactor 1 is 2 meters.

[0064] The main body of the channel includes a primary molten metal reactor sidewall section and a secondary molten metal reactor sidewall section. The channel inlet is formed on the inner sidewall of the primary molten metal reactor 1, and the channel outlet is formed on the inner sidewall of the secondary molten metal reactor 2.

[0065] It should be noted that the axial cross-section of the main body of the channel is semi-circular, with the diameter of the semi-circle gradually decreasing from the channel entrance to the channel exit. The straight edge of the main body of the channel is placed horizontally, and the arc edge smoothly transitions from the channel entrance to the channel exit, forming a gradually narrowing conical path.

[0066] In one possible design, the channel inlet is a semicircle with a cross-section of 1.8 to 2 meters in diameter; the channel outlet is a semicircle with a cross-section of 0.6 to 0.8 meters in diameter.

[0067] Furthermore, the top of the primary molten metal reactor 1 is provided with a feed inlet 102, a first gasifying agent spray gun mounting port 601, and a second gasifying agent spray gun mounting port 602; the top of the secondary molten metal reactor 2 is provided with a syngas outlet 9; the upper part of the outer wall of the secondary molten metal reactor 2 is also provided with a third gasifying agent spray gun mounting port 7 and a biomass spray gun mounting port 8; a slag-liquid pool 202 is provided above the second metal pool 201 of the secondary molten metal reactor 2.

[0068] Specifically, during the operation of the molten metal reactor system, the material falls freely from the feed inlet 102 at the top of the primary molten metal reactor 1 into the first metal pool 101 (falling height 3-3.5 meters). Simultaneously, gasifying agent is sprayed onto the falling material through the first gasifying agent spray gun 14 and the second gasifying agent spray gun 15, causing the material to impact and mix with the molten metal to carry out a primary gasification reaction, allowing the material to fully react and rapidly gasify to generate a first mixed gas. The rapid and large-scale generation of the first mixed gas (reaction time within 0.1 seconds) increases the internal pressure of the primary molten metal reactor 1 (internal pressure is...). The pressure difference between the primary molten metal reactor 1 and the secondary molten metal reactor 2 is increased to 1.5-1.8 MPa (e.g., 0.2-0.6 MPa). Under the action of the pressure difference, the first mixed gas is injected into the bottom of the second metal pool 201 of the secondary molten metal reactor 2 through the gas-liquid channel 3. At the same time, the gasifying agent is injected into the second metal pool 201 through the third gasifying agent spray gun 12 and / or the biomass powder is injected into the second metal pool 201 through the biomass spray gun 13. The first mixed gas undergoes secondary complete decomposition from the bottom up through the molten metal layer and the slag liquid layer to obtain inorganic mixed gas.

[0069] It should be noted that when the first mixed gas is injected from the first-stage molten metal reactor 1 to the bottom of the second metal pool 201 of the second-stage molten metal reactor 2 through the gas-liquid channel 3 under pressure, the molten iron in the first metal pool 101 is pressed to the bottom of the semi-circular arc of the channel outlet on the inner side wall of the second-stage molten metal reactor 2, but cannot be pressed down further; the space of the channel inlet section is significantly larger than the channel outlet section, and this design is conducive to the accelerated flow of gas.

[0070] The invention features a metal pool interconnection design with different heights, where the minimum cross-sectional area of ​​the channel is completely filled with molten iron. This effectively prevents the accumulation of lumpy materials and potential blockages, while also ensuring that gas exchange cannot occur between the two reaction vessels before the reaction begins.

[0071] In one possible design, the first metal pool 101 has a volume of 56 cubic meters, the second metal pool 201 has a volume of 25 cubic meters, the bottom of the second metal pool 201 is 2 meters higher than the top of the first metal pool 101, and the material processing capacity is 80-100 tons per hour.

[0072] In one possible design, the first gasifying agent spray gun mounting port 601 and the second gasifying agent spray gun mounting port 602 are arranged symmetrically at 180°, and the angle with the horizontal direction is 45°. The axes of the first gasifying agent spray gun mounting port 601 and the second gasifying agent spray gun mounting port 602 pass through the center point of the cross-section of the first metal pool 101.

[0073] In one possible design, the third gasifying agent spray gun mounting port 7 and the biomass spray gun mounting port 8 are arranged symmetrically at 180°, and the angle between them and the horizontal direction is 60°. The axes of the third gasifying agent spray gun mounting port 7 and the biomass spray gun mounting port 8 pass through the center point of the cross-section of the second metal pool 201.

[0074] Preferably, the primary molten metal reactor 1 further includes a drain port 4 on the outer wall of the reactor body. The drain port 4 is located at the bottom of the first metal pool 101 and is used to discharge the molten metal in the metal pool.

[0075] Specifically, the secondary molten metal reactor 2 further includes a lower slag discharge port 503, a middle slag discharge port 502, and an upper slag discharge port 501 on the outer wall of the reactor body. The lower slag discharge port 503, the middle slag discharge port 502, and the upper slag discharge port 501 correspond to the upper, middle, and lower liquid levels in the slag-liquid pool 202, respectively.

[0076] The upper slag discharge port 501 is used to periodically discharge the ash brought in by the material; the middle slag discharge port 502 is used to discharge part of the slag liquid in the slag liquid pool when changing the gasifying agent spray gun; and the lower slag discharge port 503 is used to discharge all the slag liquid in the slag liquid pool when the furnace is shut down.

[0077] In one possible design, the cross-sectional area of ​​the syngas outlet 9 is 0.8–1 m². 2 The outlet velocity of the inorganic mixed gas of the product is 30-35 m / s.

[0078] Preferably, both the bottom of the primary molten metal reactor 1 and the secondary molten metal reactor 2 are provided with a molten groove 11, which is located below the first metal pool 101 and the second metal pool 201.

[0079] For example, both the primary molten metal reactor 1 and the secondary molten metal reactor 2 are equipped with electromagnetic induction external heating devices on their inner sidewalls.

[0080] The molten metal reactor of the present invention uses molten metal as a heat source and can be heated by electromagnetic vortex method to maintain the heat of the metal pool.

[0081] Furthermore, both the primary molten metal reactor 1 and the secondary molten metal reactor 2 are equipped with infrared thermometers at their tops; both the primary molten metal reactor 1 and the secondary molten metal reactor 2 are equipped with molten iron observation and communication devices on their side walls, which obtain liquid level information through electromagnetic correlation.

[0082] On the other hand, a specific embodiment of the present invention also discloses a gasification method based on molten metal, wherein materials containing polymeric compounds undergo a decomposition and gasification reaction within the molten metal reaction system to generate an inorganic mixed gas. The decomposition and gasification reaction process is as follows:

[0083] S1-1. The material is dropped from the top of the primary molten metal reactor 1. At the same time as the material is dropped, the gasifying agent is sprayed onto the upper part of the liquid surface of the first metal pool 101 through the gasifying agent spray gun above the primary molten metal reactor 1. The material undergoes a primary gasification reaction under the action of molten metal and gasifying agent, and the first mixed gas is obtained after the reaction.

[0084] S1-2, the first mixed gas is injected into the bottom of the molten metal in the secondary molten metal reactor 2 through the gas-liquid channel, and then passes upward through the molten metal layer and slag liquid layer to carry out a secondary gasification reaction to obtain an inorganic mixed gas.

[0085] Preferably, when the material is only biomass powder, the decomposition and gasification reaction process is as follows: the biomass powder and the gasifying agent are respectively sprayed onto the bottom of the molten metal through the biomass spray gun 13 and the gasifying agent spray gun located above the secondary melting reactor 2, and the decomposition and gasification reaction is carried out under the action of the molten metal and the gasifying agent, and an inorganic mixed gas is obtained after the reaction.

[0086] Specifically, using molten metal as a medium and heat source, materials containing high molecular weight compounds undergo decomposition and gasification reactions under the action of a gasifying agent to generate an inorganic mixed gas, including CO and H2.

[0087] It should be noted that the molten metal can be liquid iron, with a temperature of 1400-1700℃. On the one hand, metallic iron serves as a heat source for the reaction, and its melting temperature range of 1400℃ to 1700℃ is suitable for the temperature range required for decomposition and gasification reactions. On the other hand, metallic iron acts as a catalyst. In the first step of the reaction, the liquid iron reacts with carbon, oxygen, and water in the material to generate Fe3C and FeO, while simultaneously producing H2 and CO. In this process, the liquid iron not only promotes the conversion of carbon but also significantly reduces the activation energy of the oxygen reduction reaction, accelerating the oxygen reduction process. It also reduces the activation energy of the hydropyrolysis reaction, thereby greatly improving the overall reaction efficiency. In the second step of the reaction, liquid Fe3C and FeO further react to generate metallic iron and CO. Through this two-step reaction mechanism, the liquid iron optimizes the reaction path, causing the catalytic process to generate more CO rather than CO2, thus effectively reducing greenhouse gas emissions. Throughout the entire reaction process, the liquid iron not only improves the overall efficiency of the reaction but also reduces reaction energy consumption through its catalytic effect, achieving environmental friendliness.

[0088] The material reacts rapidly under the action of molten iron and gasifying agent, with a theoretical reaction time of less than 0.1 seconds. Based on the high reaction rate, the gasifying agent can be stopped within 2 to 3 minutes after the feed is stopped. Since there is a large amount of carbon-containing material in the molten iron, the gasifying agent needs to be continued to be introduced to gasify it after the feed is stopped.

[0089] It is worth noting that, theoretically, there is no loss of molten iron during the reaction process. However, in actual operation, some molten iron is lost when discharged with the slag. For example, the loss of molten iron is no more than 1 kg per ton of biomass gasification. To compensate for this loss, iron ore is added to the molten metal along with the other materials during the reaction to replenish the molten iron.

[0090] Preferably, the molten metal can be liquid copper at a temperature of 1000-1300℃. When the material containing polymer compounds is a circuit board, using liquid copper as a medium and heat source allows for the complete decomposition and gasification of the material into syngas, while the metallic copper in the circuit board directly enters the liquid copper, which is beneficial for the recovery of copper from the circuit board.

[0091] It is worth noting that the vaporizing agent is one or a mixture of two of oxygen and superheated steam.

[0092] Regarding system thermal balance: When oxygen is used exclusively as the gasifying agent, the polymer chain breaking reaction in the material is an endothermic reaction, and the incomplete oxidation reaction involving oxygen releases a large amount of heat. Therefore, the heat generated by the gasification reaction itself can maintain the temperature required for the reaction, and the system thermal balance can be maintained without external heating. When water vapor is used exclusively as the gasifying agent, the polymer chain breaking reaction in the material is an endothermic reaction, and the decomposition of water vapor into H2 and CO at high temperature is also an endothermic reaction. Therefore, external heating is required to maintain the system thermal balance. When a mixture of oxygen and water vapor is used as the gasifying agent, the external heating situation is adjusted according to the ratio of the two.

[0093] Regarding the composition of the product syngas: when all the gasifying agent is oxygen, the degree of oxidation is high, the proportion of CO generated is high, and some CO2 will be generated at the same time; when all the gasifying agent is water vapor, it will promote the water gas reaction (C+H2O→CO+H2), which can increase the total volume of the product syngas and the proportion of H2.

[0094] In one possible design, the vaporizing agent is oxygen, and the purified inorganic mixture includes CO, H2 and CO2, wherein CO accounts for 60% by volume, H2 accounts for 39% by volume and CO2 accounts for 1% by volume.

[0095] In one possible design, the vaporizing agent is water vapor, and the purified inorganic mixture includes a mixture of CO and H2, wherein CO accounts for 40% by volume and H2 accounts for 60% by volume.

[0096] Preferably, the purification of the inorganic mixture includes dust removal and washing (e.g., alkaline washing). The composition and structure of the inorganic mixture are detected after purification because the temperature of the mixture is high after the decomposition and gasification reaction is completed, making it difficult to detect directly.

[0097] Preferably, the decomposition and gasification reaction of the present invention uses molten metal as a heat source and can be heated by electromagnetic vortex method to maintain the system's heat balance, resulting in low energy consumption.

[0098] Furthermore, the gasifying agent is sprayed into the molten metal through a spray gun at a speed of 200–250 m / s.

[0099] The gasifying agent is injected into the molten metal at a speed of over 200 m / s through a gasifying agent spray gun, which facilitates impact mixing between the material and the molten metal, allowing the reaction to proceed more fully. When the gasifying agent is oxygen, the oxygen injected into the molten metal can undergo an oxidation reaction with the molten metal. Since the molten iron contains a large amount of carbonaceous material, the gasifying agent should be stopped for 2-3 minutes after the feed is stopped to allow it to completely vaporize, ensuring an appropriate oxygen injection rate and preventing gasifying agent overflow or excess.

[0100] It should be noted that the materials containing polymeric compounds include one or more of household waste, industrial waste, and biomass. The industrial waste includes circuit boards.

[0101] Preferably, the material is biomass. Before the decomposition and gasification reaction, the biomass is processed into powder and sprayed into molten metal through a spray gun. Under the action of the molten metal and the gasifying agent, the decomposition and gasification reaction takes place. The spraying speed of the biomass powder is 200-250 m / s.

[0102] Specifically, after the biomass is carbonized using waste heat, it is ground into biomass powder and sprayed directly into the bottom of the molten iron through a spray gun. After the biomass gas stream and the gasifying agent gas stream collide, the molten iron boils. Under the high-energy, high-heat reaction environment provided by the high-temperature molten iron and the catalytic effect of the metal, the biomass and gasifying agent are gasified into an inorganic mixture.

[0103] Because biomass particles are small and carbonization eliminates the presence of large polymers, it can be completely decomposed through a single decomposition and gasification reaction.

[0104] Furthermore, the materials include municipal solid waste and / or industrial waste, and the decomposition gasification reaction includes a primary gasification reaction and a secondary gasification reaction. After the materials undergo a primary gasification reaction under the action of molten metal and a gasifying agent, the generated first mixed gas is introduced into the bottom of the molten metal and passes upward through the molten metal layer. Under the action of the molten metal and the gasifying agent, a secondary gasification reaction is carried out to generate an inorganic mixed gas, including CO and H2. The inorganic mixed gas passes upward through the slag-liquid layer for displacement and filtration, and a very small portion that escapes can be purified through subsequent treatment.

[0105] It is worth noting that because municipal solid waste and industrial waste contain various bromide-containing polymers that are much larger than biomass molecules, as well as inorganic substances, both metallic and non-metallic, they cannot be directly sprayed onto the bottom of the molten metal after pretreatment. Furthermore, their specific gravity is much lower than that of metals, making it impossible to ensure sufficient contact and contact time between the material and the molten iron. Therefore, after the first-stage gasification reaction, the first mixed gas produced contains organic matter ranging from methane to C40, and the proportion is uncontrollable. A second-stage reaction is necessary to completely decompose the inorganic substances.

[0106] The first mixed gas rises through the molten metal layer, making full contact with the molten iron to ensure complete vaporization into inorganic substances, with no large molecular gases present, thus obtaining an inorganic mixed gas. The inorganic mixed gas continues to pass through the slag liquid layer, which not only prevents the escape of high molecules but also captures ash, sulfur, chlorides, etc. into the slag liquid, making the obtained gas purer and free of organic compounds. Furthermore, because the gas is pure and consists entirely of inorganic substances, it will not cause problems such as coking at the downstream end.

[0107] Specifically, the slag-liquid layer comprises dolomite and limestone, with a ratio of 2:1.

[0108] It should be noted that the inorganic mixture produced by the decomposition and gasification reaction of this invention contains only inorganic components and does not contain organic hydrocarbon compounds such as methane and acetylene.

[0109] In one possible design, the industrial waste includes circuit boards, the molten metal is liquid copper, and the decomposition and gasification reaction includes a primary gasification reaction and a secondary gasification reaction. After the circuit board undergoes a primary gasification reaction under the action of the liquid copper and the gasifying agent, the generated first mixed gas is introduced into the bottom of the liquid copper and passes upward through the liquid copper layer. Under the action of the liquid copper and the gasifying agent, a secondary gasification reaction is carried out to obtain an inorganic mixed gas. At the same time as the primary gasification reaction, the metallic copper in the circuit board enters the liquid copper.

[0110] Preferably, preheating the material to above 400°C before the primary gasification reaction is beneficial for maintaining the thermal balance of the decomposition gasification reaction system.

[0111] Furthermore, the purified inorganic mixture enters the downstream reaction system for Fischer-Tropsch synthesis to produce green methanol, green SAF jet fuel, and green high-quality plastics, among other green products.

[0112] On the other hand, a specific embodiment of the present invention also discloses a gasification system based on molten metal for implementing the gasification method, including a feeding and preheating system, a gasifying agent supply system, a molten metal reaction system, a syngas purification and heat exchange system, and a syngas storage system connected in sequence via pipelines; the feeding and preheating system is connected to the inlet of the molten metal reaction system through a sealed interface; the gasifying agent supply system includes a superheated steam boiler and / or an oxygen tank, the outlets of which are respectively connected to a gasifying agent spray gun that enters the molten metal reaction system.

[0113] Furthermore, the feeding and preheating material system includes a feeding tank 19, parallel feeding tanks A16 and B17, a first screw conveyor 18, and a second screw conveyor 19. The outlets of the feeding tanks A16 and B17 are respectively connected to the inlet of the first screw conveyor 18 through pipes. The outlet of the first screw conveyor 18 is connected to the inlet of the feeding tank 19 through a pipe. The discharge port of the feeding tank 19 is connected to the inlet of the second screw conveyor 20 through a pipe. The outlet of the second screw conveyor 20 is connected to external equipment through a sealed interface.

[0114] Preferably, the design of the material discharge tanks A16 and B17 as backups for each other ensures that the continuous material conveying can be maintained even if a single tank fails. It also allows for flexible switching according to production needs, reducing downtime and improving production efficiency.

[0115] Furthermore, the feeding tank 19 includes a tank body 21, a heat exchange jacket 23 disposed outside the tank body 21, a rotating shaft 29 disposed along the height direction of the tank body 21 and passing through the tank body 21, and a feeding plate disposed axially along the rotating shaft 29.

[0116] The material feeding plate includes an outer material feeding plate and an inner material feeding plate, wherein the outer material feeding plate and the inner material feeding plate are arranged alternately along the axial direction of the rotation axis 29.

[0117] The projections of the outer and inner feed plates on the radial plane of the rotation axis 29 do not overlap.

[0118] It should be noted that the terms "outer" and "inner" are relative and are used to qualitatively describe the distance of the outer and inner feed plates from the rotation axis.

[0119] Specifically, the outer and inner material-pulling plates are fixedly mounted on the rotating shaft 29. For example... Figures 8-22 As shown.

[0120] Furthermore, the inner material-pushing plate includes a plurality of inner material-pushing plate units 30, and each inner material-pushing plate unit 30 includes three first blades 38. The three first blades 38 are evenly arranged circumferentially around the rotation axis 29. The plane of the first blade 38 forms an angle of 30° to 85° with the axis of the rotation axis 29, and at the same time, it is tilted upwards by 10° to 60° relative to the radial plane of the rotation axis 29 along the axis of the rotation axis.

[0121] Along the rotation direction of the rotating shaft 29, the edge of the first paddle forms a spiral slope of 10° to 60° upwards. This design allows the inner paddle to effectively push the material radially outwards and axially upwards when the rotating shaft rotates, thereby achieving material mixing and facilitating uniform heat transfer.

[0122] Preferably, the plane of the first impeller 38 forms an angle of 30°, 40°, 50°, 60°, 75°, 80°, or 85° with the axis of the rotation shaft 29, and simultaneously rises upwards along the axis of the rotation shaft 29 at angles of 10°, 20°, 30°, 40°, 45°, 50°, or 60° relative to the radial plane of the rotation shaft 29. The angle between the plane of the first impeller 38 and the axis of the rotation shaft 29, as well as the spiral slope angle formed by the edge of the first impeller 38, are determined and adjusted according to the density and particle size of the material.

[0123] It should be noted that the blade surface shape of the first blade 38 is an eccentric fan ring. The eccentric fan ring is part of an eccentric ring formed by two eccentric circles of different diameters, including an inner arc, an outer arc, and the long and short sides connecting the inner and outer arcs. Its geometric characteristics are: the circle containing the inner arc of the eccentric fan ring coincides with the outer circumference of the rotation shaft 29; the diameter of the circle containing the outer arc of the eccentric fan ring is 1.5 to 2.5 times the diameter of the circle containing the inner arc; and the central angle of the eccentric fan ring with the inner arc as its center is 90° to 120° (excluding 120°). Figure 13 , Figure 14 As shown, the center of the cross-section of the rotating shaft is O1, the center of the circle containing the outer arc of the first impeller is O2, and the central angle of the first impeller is α. The eccentric impeller design can increase the fluid velocity and effectively suppress the stirring dead zone below the impeller, thereby improving the mixing efficiency.

[0124] The inner arc of the first blade 38 fits against the rotating shaft 29, and the thickness of the first blade 38 increases along the rotation direction of the rotating shaft 29. The thickness design of the first blade 38 can reduce the resistance during rotation.

[0125] Furthermore, the outer material-pushing plate includes multiple outer material-pushing plate units, and each outer material-pushing plate unit includes two second paddles 35, which are respectively fixedly connected to the rotating shaft 29 via the first transmission shaft 36.

[0126] Specifically, the outer paddle includes an outer upper paddle 31 distributed in the upper region of the rotating shaft 29. The second blade 35 of the outer paddle unit of the outer upper paddle 31 is a rectangular blade. The angle b1 between the plane of the second blade 35 and the axis of the rotating shaft 29 is 10° to 60°, and the angle c1 between the horizontal axis of the plane of the second blade 35 and the extension line of the axis of the first transmission shaft 36 is 15° to 75°.

[0127] For example, the outer paddle includes an outer lower paddle 32 distributed in the lower region of the rotating shaft. The second blade 35 of the outer paddle unit of the outer lower paddle 32 is a rectangular blade. The angle b2 between the plane of the second blade 35 and the axis of the rotating shaft 29 is 10° to 60°. At the same time, the angle c2 between the horizontal axis of the plane of the second blade 35 and the extension line of the axis of the first transmission shaft 36 is 15° to 75°. And c2 > c1.

[0128] Preferably, b1 is 10°, 20°, 30°, 40°, 45°, 50°, 60°, and c1 is 15°, 20°, 30°, 40°, 45°, 50°, 60°, 75°; b2 is 10°, 20°, 30°, 40°, 45°, 50°, 60°, and c2 is 15°, 20°, 30°, 40°, 45°, 50°, 60°, 75°. The angle between the plane of the second blade 35 and the axis of the rotating shaft 29, the angle between the horizontal axis of the plane of the second blade 35 and the extension line of the axis of the first drive shaft 36, and the difference between c1 and c2 are selected and adjusted according to the density and particle size of the material.

[0129] In one possible design, c1 is 45° and c2 is 60°.

[0130] It should be noted that, in the projection on the radial plane of the rotating shaft 29, the two first drive shafts 36 in the outer feed plate unit are arranged in parallel, do not pass through the center of the rotating shaft 29, and are centrally symmetrical with respect to the center of the rotating shaft 29, ensuring the balance of the structure and the uniform force on the blades; the first drive shafts 36 of multiple outer feed plate units are arranged in an overlapping radial layout, that is, in the projection on the radial plane of the rotating shaft 29, the first drive shafts 36 at different heights have the same radial layout; the two first blades 35 in the outer feed plate unit are centrally symmetrical with respect to the center of the rotating shaft 29.

[0131] Specifically, when the rotating shaft rotates, the outer lower material-pushing blade 32 has a larger angle with the extended axis of the corresponding first transmission shaft 36 than the outer upper material-pushing blade 31. That is, the outer edge of the blade is farther from the inner wall of the tank body, and the inclination of the blade plane is closer to the center of the tank body. Because the lower the material is, the greater the material pressure and the more compacted it is, the larger the angle between the blade and the tank needs to be to reduce the resistance of rotation, which also plays the role of pushing the material inward and upward.

[0132] It should be noted that the number of outer material guide plates and the division of the upper and lower areas are determined based on the diameter of the rotating shaft, the characteristics of the material, and the mixing or conveying requirements, to ensure uniform distribution and effective movement of the material around the rotating shaft. The design of the outer material guide plates is coordinated with that of the inner material guide plates to achieve continuous flow of material around the rotating shaft.

[0133] Furthermore, after the material is fed through the inlet, the rotating shaft 29 rotates continuously in the feeding tank 19 at a speed greater than 60 r / min.

[0134] The rotation of the rotating shaft 29, combined with different material-pushing blades on the rotating shaft 29, the outer material-pushing blades push the material inward and upward, and the inner material-pushing blades push the material outward and upward. This causes the material in the tank to flow inward and outward, ensuring that the material is heated evenly. At the same time, the material is constantly turned upward, which can prevent the bridging and blockage of elastic materials.

[0135] Preferably, the feeding tank 19 further includes a conical discharge port 27. The upper end of the conical discharge port 27 is connected to the lower part of the tank body 21 through a discharge port flange 22, and the lower end of the conical discharge port 27 is connected to an external conveying device through a constriction flange 28. The rotating shaft 29 passes through the discharge port flange 22 and the area of ​​the conical discharge port 27, and is fixedly installed inside the constriction flange 28 of the conical discharge port 27 through a lower bearing 33 and a lower bearing seat.

[0136] Preferably, the lower end bearing 33 of the rotating shaft 29 is made of graphite, which can withstand high temperatures of 400-500℃. There is no need to cool the bearing, thus avoiding heat loss. At the same time, there is no need for dynamic sealing, as it is directly sealed in the feeding tank 19, avoiding the difficulties of high-temperature sealing.

[0137] Furthermore, the outer material feeding plate also includes a material feeding port feeding plate distributed in the region of the conical material feeding port 27 of the rotating shaft. The second blade 35 of the outer material feeding plate unit of the material feeding port feeding plate is an inverted trapezoidal blade. The angle b3 formed by the plane of the second blade 35 and the axis of the rotating shaft 29 is 10° to 60°, preferably b3 is 10°, 20°, 30°, 40°, 45°, 50°, or 60°. The inverted trapezoidal blade includes two sides, a long base and a short base parallel to the first drive shaft, one side being connected to its first drive shaft, and the long base being located above the short base.

[0138] The second blade 35 in the discharge port area is designed to adapt to the conical space of the discharge port area while effectively turning over the material in that area.

[0139] It is worth noting that the discharge port flange 22 has a discharge port with a trapezoidal cross-section, which is smaller at the top and larger at the bottom, to prevent material from getting stuck.

[0140] Preferably, a material scraper is provided above the material discharge port flange 22 to further prevent material bridging and blockage.

[0141] Specifically, the shovel blade includes two third blades 37, which are fixedly connected to the rotating shaft 29 via second drive shafts 39. The third blades 37 are rectangular blades, and the angle b4 between the plane of the third blade 39 and the axis of the rotating shaft 29 is 60° to 85°, preferably b4 is 60°, 70°, 75°, 80°, or 85°. The two second drive shafts 39 are collinearly arranged, and the line connecting them passes through the center of the cross-section of the rotating shaft 29 at the same height.

[0142] In one possible design, the tapered discharge port 27 has a taper of 10° to improve the flow characteristics of the material and prevent the material from arching or clogging at the discharge port.

[0143] Preferably, a dynamic seal is applied at the connection between the upper bearing 34 of the rotating shaft and the top of the tank body 21. The sealing requirement is that, under a sealing gas pressure of 1.0 MPa to 1.5 MPa, the leakage rate during the dynamic test is controlled to be ≤0.10 Nm at a rotational speed of 0–60 r / min. 3 / h.

[0144] Furthermore, the heat exchange jacket 23 includes a shell and a heating coil; the heating coil surrounds the outer wall of the tank body 21, the medium inlet 24 is located at the lower end of the heating coil, and the medium outlet 25 is located at the upper end of the heating coil. It is used to preheat the material inside the tank body 21.

[0145] Preferably, fins 26 are installed on the outer side of the heating coil. This increases the heat exchange area and improves the heat exchange effect.

[0146] In one possible design, the heating coil has a cross-sectional dimension of 500*300mm and a total length of 400m.

[0147] It is worth noting that in the feeding and preheating material system of the present invention, the pouring tanks A16 and B17 have the same structure as the feeding tank 19; the medium inlet of the heat exchange jacket of the feeding tank is connected to the external air pipe for introducing hot air; the medium outlet of the heat exchange jacket of the feeding tank is connected to the medium inlet of pouring tank A and the medium inlet of pouring tank B through pipes respectively, and the medium outlet of pouring tank A and the medium outlet of pouring tank B are connected to the external air main pipe through pipes to send the heat-exchanged air back to the external air compressor.

[0148] In one possible design, control valves are provided on each material conveying channel and heat exchange medium pipeline, and the external air temperature is 750-850℃.

[0149] This invention's feeding and preheating system incorporates a stirring system into a vertical material tank. This avoids bridging and clogging issues caused by elastic materials and solves the problem of uneven preheating in vertical material tanks. The vertical material tank design incorporates multiple sets of material-pushing blade units arranged longitudinally along the rotation axis. Based on the angle of the blades in these units and in conjunction with the rotation of the shaft, the material-pushing blades simultaneously push some material towards the center of the tank, loosening it upwards, and push some material towards the outer wall of the tank. This promotes flow between the inside and outside of the material, enhances heat exchange, and ensures uniform heating. Simultaneously, the continuous upward movement of the material effectively prevents bridging and clogging caused by elastic materials.

[0150] In one possible design, when the feeding and preheating system of the present invention is applied to the decomposition and gasification reaction system of recyclable and renewable resources such as municipal solid waste, industrial waste and biomass, the air exchanges heat with the 1500°C high-temperature syngas generated by the decomposition and gasification reaction system in an external heat exchanger. After the heat exchange, the air is heated to 750-850°C and enters the feeding and preheating system to preheat the material, thereby realizing the recovery of waste heat from the product syngas and saving energy.

[0151] In summary, this invention designs a molten metal-based reactor, employing a two-stage molten metal reactor interconnected by gas-liquid channels. This reactor decomposes and gasifies materials containing high-molecular-weight polymers. The crude gas (containing organic components) generated by gasification in the first-stage molten metal reactor is injected into the bottom layer of the molten iron in the second-stage molten metal reactor through the gas-liquid channels. The crude gas undergoes further decomposition in the high-temperature molten iron and slag layers of the second-stage reactor, resulting in a completely decomposed inorganic mixture, ensuring no polymer escape. The purified inorganic mixture is composed of syngas (CO + H2) with a volume fraction greater than 90%, and the remainder is CO2. This purified mixture can then be used in subsequent processing stages, such as producing green methanol, sustainable aviation fuel (SAF), and high-quality green plastics through Fischer-Tropsch synthesis, thus contributing to a gradual reduction in dependence on primary petrochemical resources.

[0152] The molten metal reactor and the gasification method based on molten metal of the present invention will be described below with reference to specific embodiments.

[0153] Example 1

[0154] This embodiment provides a molten metal reactor and a gasification system based on the molten metal reactor, such as... Figures 1-2 and Figure 23 As shown.

[0155] Molten metal reaction vessel: such as Figure 1 , Figure 2As shown, it includes a primary molten metal reactor 1 and a secondary molten metal reactor 2 that are interconnected by a gas-liquid channel 3; the primary molten metal reactor 1 is provided with a first metal pool 101 inside, and the secondary molten metal reactor 2 is provided with a second metal pool 201 inside, wherein the bottom of the second metal pool 201 is higher than the bottom of the first metal pool 101, and the primary molten metal reactor 1 and the secondary molten metal reactor 2 are arranged horizontally in a staggered manner;

[0156] The gas-liquid channel 3 is a semi-conical channel, and the axial section of the semi-conical channel is higher than the curved surface of the semi-conical channel. The semi-conical channel includes a channel inlet, a channel body, and a channel outlet. The channel inlet is connected to the primary molten metal reactor 1, and the channel outlet is connected to the secondary molten metal reactor 2. Both the channel inlet and the channel outlet are semi-circular, with the inlet diameter being larger than the outlet diameter, and their centerlines are collinear and aligned. There is a distance between the centerline of the channel inlet and the bottom of the primary molten metal reactor 1, and the bottom arc of the channel outlet is in contact with the bottom of the secondary molten metal reactor 2.

[0157] The top of the primary molten metal reactor 1 is provided with a feed inlet 102, a first gasifying agent spray gun mounting port 601, and a second gasifying agent spray gun mounting port 602; the top of the secondary molten metal reactor 2 is provided with a syngas outlet 9; the upper part of the outer wall of the secondary molten metal reactor 2 is also provided with a third gasifying agent spray gun mounting port 7 and a biomass spray gun mounting port 8; a slag-liquid pool 202 is provided above the second metal pool 201 of the secondary molten metal reactor 2.

[0158] Gasification system: such as Figure 23 As shown, it includes a feeding and preheating system, a gasifying agent supply system, a molten metal reaction system, a syngas purification and heat exchange system, and a syngas storage system connected in sequence via pipelines; the feeding and preheating system is connected to the inlet of the molten metal reaction system through a sealed interface; the gasifying agent supply system includes a superheated steam boiler and / or an oxygen tank, the outlets of which are respectively connected to the gasifying agent spray guns that are introduced into the molten metal reaction system.

[0159] The syngas purification and heat exchange system includes a cyclone dust collector, a heat exchanger, a bag filter dust collector, a scrubbing tower, and an air compressor. The inlet of the cyclone dust collector is connected to the syngas outlet of the secondary molten metal reactor, and its outlet is connected to the hot fluid inlet of the heat exchanger. The hot fluid outlet of the heat exchanger is connected in sequence to the bag filter dust collector and the scrubbing tower. The outlet of the scrubbing tower is connected to the syngas storage system. Air is supplied to the cold fluid inlet of the heat exchanger through the air compressor. After heat exchange in the heat exchanger, the air is sent to the heat exchange jacket of the feeding tank through a pipeline.

[0160] The syngas storage system includes a compressor and a syngas storage tank connected to the compressor outlet via a pipeline. The compressor inlet is connected to the scrubbing tower outlet via a pipeline.

[0161] When the gasification system is in use: the material is fed into the surface of the molten metal in the first metal pool 101 of the first-stage molten metal reactor 1 through the feeding and preheating material system. At the same time as the material is fed, oxygen is sprayed onto the upper part of the liquid surface at the material feeding point through the first gasifying agent spray gun 14 and the second gasifying agent spray gun 15 above the first-stage molten metal reactor 1. The material undergoes a first-stage gasification reaction under the catalysis of the molten metal. After the reaction, a first mixed gas is obtained. The generation of the first mixed gas in the first-stage molten metal reactor 1 makes the pressure in the first-stage molten metal reactor 1 higher than the pressure in the second-stage molten metal reactor 2. As a result, the first mixed gas enters the bottom of the second metal pool 201 of the second-stage molten metal reactor 2 through the gas-liquid channel 3 and passes through the molten metal and slag liquid layer. Oxygen is sprayed into the second metal pool 201 through the third gasifying agent spray gun 12 and / or biomass powder is sprayed into the second metal pool 201 through the biomass spray gun 13. The product inorganic mixed gas is discharged from the syngas outlet 9 to the cyclone dust collector for dust removal and then enters the syngas purifier heat exchange system. After heat exchange, it undergoes further dust removal and purification and finally enters the syngas storage tank.

[0162] The waste heat recovery process of this system is as follows: the high-temperature product synthesis gas enters the hot end inlet of the heat exchanger through the pipeline, and at the same time the air compressor sends air into the cold end inlet of the heat exchanger. After heat exchange, the temperature of the synthesis gas at the hot end outlet decreases and the temperature of the air at the cold end outlet increases. The air is sent from the cold end outlet into the heat exchange jacket on the outer wall of the feeding tank and the unloading tank to preheat the materials.

[0163] The slag discharge process of this system is as follows: slag is discharged once a day through the upper slag discharge port 501 of the secondary molten metal reactor 2, and the upper slag discharge port 501 is closed after the slag is discharged to the specified height.

[0164] Application of the gasification system in this embodiment:

[0165] Materials: municipal solid waste, industrial waste and biomass; processing capacity: 100 tons / hour; gasification agent: oxygen; molten metal: molten iron at a temperature of 1400-1700℃.

[0166] The main design parameters of the molten metal reactor are as follows: the volume of the first metal pool 101 is 56 cubic meters, the volume of the second metal pool 201 is 25 cubic meters, and the height difference between the bottom of the second metal pool 201 and the top of the first metal pool 101 is 2 meters; the height of the molten iron in the second molten reactor 2 is 2 meters, and the height of the slag layer is 3 meters; the inlet of the gas-liquid channel 3 is a semicircle with a cross-section of 2 meters in diameter, and the outlet of the channel is a semicircle with a cross-section of 0.8 meters in diameter; the cross-sectional area of ​​the synthesis gas outlet 9 is 0.8 m². 2 The channel entrance is a semicircle with a cross-section of 1.8 to 2 meters in diameter, and the distance from the upper end of the channel entrance to the bottom of the first metal pool is 2 meters; the channel exit is a semicircle with a cross-section of 0.6 to 0.8 meters in diameter.

[0167] When using this system for the first time: add iron powder with particles <2mm to the first metal pool 101 and the second metal pool 201 respectively, heat to the molten state, and then add dolomite powder and limestone powder to the second metal pool 201 to form a slag-liquid layer.

[0168] The main design parameters for the decomposition gasification reaction and subsequent processing are as follows: The material is fed into the first metal pool 101 of the first-stage molten metal reactor 1 through the feeding and preheating system. At the same time as the material is fed, oxygen is sprayed at a speed of 200 m / s onto the upper part of the liquid surface through the first gasifying agent spray gun 14 and the second gasifying agent spray gun 15 above the first-stage molten metal reactor 1. The material undergoes a first-stage gasification reaction under the catalysis of the molten iron. After the reaction, the first mixed gas is obtained and the pressure inside the first-stage molten metal reactor 1 reaches 1.5 MPa. The first mixed gas enters the bottom of the second metal pool 201 of the secondary melting reactor 2 through the gas-liquid channel 3 at a speed of 50-150 m / s and passes through the molten metal and slag liquid layer. At the same time, the third gasifying agent spray gun 12 sprays oxygen into the second metal pool 201 at a speed of 200 m / s, and the biomass spray gun 13 sprays biomass powder into the second metal pool 201 at a speed of 200 m / s. The product inorganic mixed gas is discharged from the syngas outlet 9 at a speed of 30-35 m / s to the cyclone dust collector for dust removal and then enters the syngas purifier heat exchange system. After heat exchange, the temperature drops to below 300℃ for further dust removal and purification, and then enters the syngas storage tank.

[0169] The main design parameters for the waste heat recovery process are as follows: the inorganic mixture of the product at a temperature of 1500℃ enters the hot end inlet of the heat exchanger through a pipeline, while the air compressor sends air into the cold end inlet of the heat exchanger. After heat exchange, the temperature of the inorganic mixture at the hot end outlet is 300℃, and the temperature of the air at the cold end outlet is 850℃. The air is sent from the cold end outlet into the heat exchange jacket 23 on the outer wall of the feeding tank 19 and the unloading tank to preheat the material to 400℃.

[0170] Example 2

[0171] This embodiment provides a gasification method based on molten metal. For example... Figure 3 As shown.

[0172] Materials: Domestic waste and industrial waste, with a processing capacity of 100 tons / hour.

[0173] The gasifying agent is oxygen, and the molten metal is molten iron at a temperature of 1400–1700°C. The process is carried out in a primary molten metal reactor and a secondary molten metal reactor.

[0174] The gasification process is as follows:

[0175] Step 1: Pre-process the material by pressing it into briquettes to a thickness of less than 80mm.

[0176] Step 2: The pretreated material is fed to the surface of the molten iron in the primary molten metal reactor. At the same time, oxygen is sprayed onto the surface of the molten iron at a speed of 200 m / s through the gasifying agent spray gun. The gasifying agent spraying is stopped within 2 to 3 minutes after the feeding is stopped. The material undergoes a primary gasification reaction under the catalysis of the molten iron, and the first mixed gas is obtained after the reaction.

[0177] Step 3: The first mixed gas enters the bottom of the molten iron in the secondary molten metal reactor through the gas-liquid channel, and passes through the molten iron layer and the slag layer above the molten iron layer in sequence. At the same time, oxygen is injected into the molten iron in the secondary molten metal reactor through the gasifying agent spray gun at a speed of 200 m / s. The injection of the gasifying agent is stopped within 2 to 3 minutes after the feeding is stopped. During this process, the first mixed gas undergoes a secondary gasification reaction and inorganic mixed gas is obtained from above the slag layer.

[0178] Step 4: The inorganic mixed gas is subjected to dust removal and alkaline washing purification.

[0179] The volume fractions of the components in the final product syngas were as follows: CO: 60%; H2: 39%; CO2: 1%.

[0180] Example 3

[0181] This embodiment provides a gasification method based on molten metal.

[0182] The material is biomass; the gasifying agent is oxygen; the molten metal is molten iron at a temperature of 1400–1700℃; the process is carried out in a secondary molten metal reactor.

[0183] The gasification process is as follows:

[0184] Step 1: Grind the biomass into biomass powder by carbonizing it with waste heat.

[0185] Step 2: Inject biomass powder into the molten iron in the secondary molten metal reactor at a speed of 200 m / s through a biomass spray gun. At the same time, inject oxygen into the molten iron at a speed of 200 m / s through a gasifying agent spray gun. Stop the injection of gasifying agent within 2 to 3 minutes after stopping the injection of biomass powder. During this process, the biomass undergoes a primary gasification reaction, and inorganic mixed gas is obtained from above the slag liquid layer.

[0186] Step 3: The inorganic mixed gas is subjected to dust removal and alkaline washing purification.

[0187] The volume fractions of the components in the final product syngas were as follows: CO: 60%; H2: 39%; CO2: 1%.

[0188] Example 4

[0189] This embodiment provides a gasification method based on molten metal.

[0190] The material is a circuit board; the gasifying agent is oxygen; and the molten metal is liquid copper. The process takes place in a primary molten metal reactor and a secondary molten metal reactor.

[0191] The gasification process is as follows:

[0192] Step 1: The crushed material is fed to the surface of the copper liquid in the primary molten metal reactor. At the same time, oxygen is sprayed onto the surface of the copper liquid at a speed of 250 m / s through the gasifying agent spray gun. The gasifying agent spraying is stopped within 2 to 3 minutes after the feeding stops. The material undergoes a primary gasification reaction under the action of the copper liquid and the gasifying agent. After the reaction, the first mixed gas is obtained. The metallic copper in the circuit board enters the copper liquid for recycling.

[0193] Step 2: The first mixed gas enters the bottom of the copper liquid in the secondary molten metal reactor through the gas-liquid channel, and passes through the copper liquid layer and the slag liquid layer above the copper liquid layer in sequence. At the same time, oxygen is injected into the copper liquid in the secondary molten metal reactor at a speed of 250 m / s through the gasifying agent spray gun. The injection of the gasifying agent is stopped within 2 to 3 minutes after the feeding is stopped. During this process, the first mixed gas undergoes a secondary gasification reaction and inorganic mixed gas is obtained from above the slag liquid layer.

[0194] Step 3: The inorganic mixed gas is subjected to dust removal and alkaline washing purification.

[0195] The volume fractions of the components in the final product syngas were as follows: CO: 60%; H2: 39%; CO2: 1%.

[0196] Example 5

[0197] This embodiment provides a preheating material and feeding system. For example... Figures 4-16 As shown.

[0198] It is used as a feedstock for decomposition and gasification reaction systems of recyclable and renewable resources such as municipal solid waste, industrial waste, and biomass.

[0199] The feeding and preheating system includes parallel-connected discharge tanks A16 and B17, a feeding tank 19, a first screw conveyor 18, and a second screw conveyor 20. The discharge ports of discharge tanks A16 and B17 are respectively connected to the inlet of the first screw conveyor 18 through pipes. The outlet of the first screw conveyor 18 is connected to the inlet of the feeding tank 19 through a pipe. The discharge port of the feeding tank 19 is connected to the inlet of the second screw conveyor 20 through a pipe. The outlet of the second screw conveyor 20 is connected to external equipment through a sealed interface.

[0200] The feeding tank 19 includes a tank body 21, a heat exchange jacket 23 disposed outside the tank body 21, a rotating shaft 29 disposed along the height direction of the tank body 21 and passing through the tank body, and a feeding plate disposed axially along the rotating shaft 29; the projections of the outer feeding plate and the inner feeding plate on the radial plane of the rotating shaft do not overlap.

[0201] The outer and inner paddles are fixedly mounted on the rotating shaft. The inner paddle includes an inner paddle unit 30, which includes three first paddles 38. The three first paddles 38 are evenly arranged circumferentially around the rotating shaft 29. The plane of the first paddle 38 forms an angle of 30° to 85° with the axis of the rotating shaft 29, and is also tilted upwards by 10° to 60° relative to the radial plane of the rotating shaft 29 along the axis of the rotating shaft 29.

[0202] The outer material-pushing plate includes multiple outer material-pushing plate units, and each outer material-pushing plate unit includes two second paddles 35. The second paddles 35 are respectively fixedly connected to the rotating shaft 29 via the first transmission shaft 36.

[0203] The outer paddle includes an upper outer paddle 31 distributed in the upper region of the rotating shaft. The second blade 35 of the outer paddle unit of the upper outer paddle 31 is a rectangular blade. The angle b1 between the plane of the second blade 35 and the axis of the rotating shaft 29 is 10° to 60°, and the angle c1 between the horizontal axis of the plane of the second blade 35 and the extension line of the axis of the first transmission shaft 36 is 15° to 75°.

[0204] For example, the outer paddle includes an outer lower paddle 32 distributed in the lower region of the rotating shaft. The second blade 35 of the outer paddle unit of the outer lower paddle 32 is a rectangular blade. The angle b2 between the plane of the second blade 35 and the axis of the rotating shaft 29 is 10° to 60°. At the same time, the angle c2 between the horizontal axis of the plane of the second blade 35 and the extension line of the axis of the first transmission shaft 36 is 15° to 75°. And c2 > c1.

[0205] The feeding tank 19 also includes a conical discharge port 27. The upper end of the conical discharge port 27 is connected to the lower part of the tank body 21 through a discharge port flange 22, and the lower end of the conical discharge port 27 is connected to an external conveying device through a constriction flange 28. The rotating shaft 29 passes through the area of ​​the discharge port flange 22 and the conical discharge port 27, and is fixedly installed inside the constriction flange 28 of the conical discharge port 27 through a lower bearing 33 and a lower bearing seat.

[0206] The outer material guide plate also includes a material guide plate distributed in the region of the conical material guide plate 27 of the rotating shaft. The second blade 35 of the outer material guide plate unit of the material guide plate is an inverted trapezoidal blade. The angle b3 formed by the plane of the second blade 35 and the axis of the rotating shaft 29 is 10° to 60°. The inverted trapezoidal blade includes two sides, a long base and a short base parallel to the first drive shaft, one side being connected to its first drive shaft, and the long base being located above the short base.

[0207] Above the discharge port flange 22 is a scraper, which includes two third blades 37. The third blades 37 are fixedly connected to the rotating shaft 29 via second drive shafts 39. The third blades 37 are rectangular blades, and the angle b4 between the plane of the third blade 37 and the axis of the rotating shaft 29 is 60° to 85°. The two second drive shafts 39 are collinearly arranged, and the line connecting them passes through the center of the cross-section of the rotating shaft 29 at the same height.

[0208] The discharge tanks A16 and B17 have the same structure as the loading tank 19, with the discharge tanks A16 and B17 serving as backups for each other.

[0209] The heat exchange jacket 23 includes a shell, a heating coil, a medium inlet 24, and a medium outlet 25. The heating coil is wrapped around the outer wall of the tank body 21, and its two ends are connected to the medium inlet 24 and the medium outlet 25 through the shell, respectively. The medium inlet 24 is located at the lower end of the heating coil, and the medium outlet 25 is located at the upper end of the heating coil. Fins 26 are installed on the outside of the heating coil.

[0210] When using the feeding and preheating material system of this invention:

[0211] Material is transported from an external silo to a discharge tank A16 (with discharge tank B17 as a backup), and fed through the inlet of discharge tank A16. Simultaneously, the rotating shaft of discharge tank A16 rotates continuously in the feeding tank, and material falls through the conical discharge port of discharge tank A16 into the first screw conveyor 18, and then enters the inlet of feeding tank 19 from the outlet of the first screw conveyor 18. The rotating shaft of feeding tank 19 also rotates continuously, and material enters the second screw conveyor 20 through the conical discharge port of feeding tank 19, and is finally transported to the decomposition and gasification reaction system. The outlet of the second screw conveyor 20 is connected to the decomposition and gasification reaction system through a high-pressure resistant sealing interface, and this high-pressure resistant sealing interface is equipped with an external water cooling system.

[0212] As the material enters the discharge tank A16, external air enters the heat exchange jacket 23 of this system through the medium inlet 24 of the feeding tank heat exchange jacket 23. After completing heat exchange, the air returns to the air compressor through the medium outlet of the discharge tank A16, realizing the recycling of the heat exchange air. Before entering this system, the air exchanges heat with the 1500℃ high-temperature syngas generated by the decomposition and gasification reaction system in the external heat exchanger. After the heat exchange, the air is heated to 850℃. Before the material enters the decomposition and gasification reaction system, it is preheated to 400℃ through the above heat exchange process.

[0213] Application of this feeding and preheating system:

[0214] Used for feeding decomposition and gasification reaction systems of municipal solid waste, industrial waste, and biomass and other recyclable and renewable resources; conveying capacity 200m³. 3 / h.

[0215] The main equipment parameters of the system are as follows: the diameter of the material tank body 21 is 4 meters, the diameter of the conical discharge port 27 is 1 meter and the taper is 10°; the cross-sectional dimensions of the heating coil are 500*300mm and the total length is 400m; the number of inner material feeding blade units is 8; the plane of the first blade 38 forms a 60° angle with the axis of the rotating shaft 29, and at the same time, it is raised 30° upward along the axis of the rotating shaft relative to the radial plane of the rotating shaft 29; b1=b2=b3=30°; b4=60°; c1=45°; c2=60°.

[0216] The main operating parameters of the system are: the rotating shafts of the pouring tank and the feeding tank rotate at a speed of 65 r / min.

[0217] Key preheating parameters: Before entering this system, the air exchanges heat with the 1500°C high-temperature gas generated by the decomposition and gasification reaction system in an external heat exchanger. After the heat exchange, the air is heated to 850°C. Before the material enters the decomposition and gasification reaction system, it is preheated to 400°C through the above heat exchange process.

[0218] During operation, the entire system ensures smooth material transport without blockages or bridging, and the material temperature is evenly distributed.

[0219] In summary, this invention designs a molten metal-based reactor, employing a two-stage molten metal reactor interconnected by gas-liquid channels. This reactor decomposes and gasifies materials containing high-molecular-weight polymers. The crude gas (containing organic components) generated by gasification in the first-stage molten metal reactor is injected into the bottom layer of the molten iron in the second-stage molten metal reactor through the gas-liquid channels. The crude gas undergoes further decomposition in the high-temperature molten iron and slag layers of the second-stage reactor, resulting in a completely decomposed inorganic mixture, ensuring no polymer escape. The purified inorganic mixture is composed of syngas (CO + H2) with a volume fraction greater than 90%, and the remainder is CO2. This purified mixture can then be used in subsequent processing stages, such as producing green methanol, sustainable aviation fuel (SAF), and high-quality green plastics through Fischer-Tropsch synthesis, thus contributing to a gradual reduction in dependence on primary petrochemical resources.

[0220] The above description is only a preferred embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Any changes or substitutions that can be easily conceived by those skilled in the art within the scope of the technology disclosed in the present invention should be included within the scope of protection of the present invention.

Claims

1. A molten metal reaction vessel, characterized in that, This includes a primary molten metal reactor and a secondary molten metal reactor that are interconnected via gas-liquid channels; The gas-liquid channel is a semi-conical channel, and the axial section of the semi-conical channel is higher than the curved surface of the semi-conical channel; The primary molten metal reactor is equipped with a first metal pool, and the secondary molten metal reactor is equipped with a second metal pool. The bottom of the second metal pool is higher than the bottom of the first metal pool, and the primary and secondary molten metal reactors are horizontally staggered.

2. The reaction vessel according to claim 1, characterized in that, The semi-conical channel includes a channel inlet, a channel body, and a channel outlet. The channel inlet is connected to the primary molten metal reactor, and the channel outlet is connected to the secondary molten metal reactor. Both the channel entrance and the channel exit are semi-circular in shape, with the diameter of the channel entrance being larger than the diameter of the channel exit, and their center lines being collinear and aligned.

3. The reaction vessel according to claim 2, characterized in that, There is a distance between the centerline of the channel inlet and the bottom of the primary molten metal reactor, and the bottom arc of the channel outlet is in contact with the bottom of the secondary molten metal reactor.

4. The reaction vessel according to claim 2, characterized in that, The main body of the channel includes a primary molten metal reactor sidewall section and a secondary molten metal reactor sidewall section. The channel inlet is formed on the inner sidewall of the primary molten metal reactor, and the channel outlet is formed on the inner sidewall of the secondary molten metal reactor.

5. The reaction vessel according to claim 1, characterized in that, The primary molten metal reactor is equipped with a feed inlet and a gasifying agent spray gun mounting port at its top; the secondary molten metal reactor is equipped with a synthesis gas outlet at its top; and a slag-liquid pool is located above the second metal pool of the secondary molten metal reactor.

6. The reaction vessel according to claim 1, characterized in that, Both the first-stage molten metal reactor and the second-stage molten metal reactor have molten grooves at their bottoms, which are located below the first metal pool and the second metal pool.

7. The reaction vessel according to claim 1, characterized in that, Both the primary molten metal reactor and the secondary molten metal reactor are equipped with electromagnetic induction external heating devices on their inner sidewalls.

8. A gasification method based on molten metal, characterized in that, Materials containing polymeric compounds undergo decomposition and gasification reactions in the molten metal reactor described in any one of claims 1 to 7 to generate an inorganic mixed gas.

9. The gasification method according to claim 8, characterized in that, The decomposition and gasification reaction process is as follows: S1-1. The material is dropped from the top of the primary molten metal reactor 1. At the same time as the material is dropped, the gasifying agent is sprayed onto the upper part of the liquid surface of the first metal pool 101 through the gasifying agent spray gun above the primary molten metal reactor 1. The material undergoes a primary gasification reaction under the action of molten metal and gasifying agent, and the first mixed gas is obtained after the reaction. S1-2, the first mixed gas is injected into the bottom of the molten metal in the secondary molten metal reactor 2 through the gas-liquid channel, and then passes upward through the molten metal layer and slag liquid layer to carry out a secondary gasification reaction to obtain an inorganic mixed gas.

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