Molten metal reaction kettle

Abstract

The invention relates to a molten metal reaction kettle, belongs to the technical field of recycling of recyclable and renewable resources such as household garbage, industrial garbage and biomass, and solves the problems of incapability of realizing same-quality or high-quality utilization caused by incomplete decomposition of macromolecular organic matters in the prior art, secondary pollution to the environment and the like. The molten metal reaction kettle is characterized by comprising a primary molten metal reaction kettle and a secondary molten metal reaction kettle which are communicated with each other through a gas-liquid channel, a first metal pool is arranged in the first-stage molten metal reaction kettle, a second metal pool is arranged in the second-stage molten metal reaction kettle, the bottom of the second metal pool is higher than the bottom of the first metal pool, and the first-stage molten metal reaction kettle and the second-stage molten metal reaction kettle are horizontally arranged in a staggered mode. The same-quality and high-quality reutilization of recyclable and renewable resources such as household garbage, industrial garbage and biomass is realized.

Description

Technical Field

[0001] The invention relates to the technical field of recycling recyclable and renewable resources such as domestic waste, industrial waste and biomass, and in particular to a molten metal reactor. Background Art

[0002] In the context of global carbon reduction, there are three areas that are recognized as difficult to get rid of carbon dependence, namely the aviation and shipping industry, the ocean shipping industry and the plastics production industry. Through the recycling and reuse of recyclable resources, the reuse of renewable resources and the conversion and utilization of carbon dioxide, the dependence on disposable fossil energy can be reduced to a certain extent. However, due to the extremely high stability and high capture cost of carbon dioxide, its direct conversion and utilization faces huge challenges. Therefore, the recycling and reuse of recyclable resources and the reuse of renewable resources have become a more realistic and preferred choice.

[0003] At present, the resource and energy utilization technology of biomass (a renewable resource) and low-quality waste plastics (a recyclable resource) is mainly thermal treatment technology, which is divided into direct incineration and pyrolysis gasification. Since direct incineration is solid heterogeneous combustion, there are problems of incomplete combustion, low efficiency and secondary pollution caused by incomplete combustion, especially dioxin emissions, which restrict the widespread application of this technology. Pyrolysis gasification can convert urban domestic waste into three types of products with relatively stable components, namely gas, liquid and solid, for utilization, which can effectively improve its utilization efficiency, scope and economy. From the perspective of pollutant emissions, the pyrolysis gasification process is carried out in an oxygen-poor or anoxic atmosphere, which in principle reduces the generation of dioxins. At the same time, most of the heavy metals are dissolved into ash and slag during the pyrolysis gasification process, reducing emissions. Therefore, the development of pyrolysis gasification technology is an important way to achieve harmless, resource-based and energy-based utilization of domestic waste.

[0004] Pyrolysis gasification technology is to use heat energy to break chemical bonds, isomerize and polymerize small molecules in the absence of oxygen or anoxic conditions, and convert large molecular organic matter into small molecular fuel gas, tar and coke. Existing pyrolysis gasification technologies include the Landgard system using rotary kiln pyrolysis, the CAO system using grate incineration technology, and the Purox system using internal heating moving bed. These pyrolysis gasification technologies generally have problems such as complex target product composition, poor quality, high subsequent recycling costs, and inability to achieve high-quality utilization. During the gasification process, flue gas may contain harmful substances such as nitrogen oxides, dioxins, and heavy metals, causing secondary pollution to the environment. The process is complex and the construction and operation costs are high. Summary of the invention

[0005] In view of the above analysis, an embodiment of the present invention aims to provide a molten metal reactor to solve at least one of the problems that existing pyrolysis gasification equipment cannot achieve the same or even high-quality recycling, and the problem of complex structure.

[0006] On the one hand, an embodiment of the present invention provides a molten metal reactor, comprising a primary molten metal reactor and a secondary molten metal reactor interconnected by a gas-liquid channel;

[0007] A first metal pool is provided inside the first molten metal reactor, and a second metal pool is provided inside the second molten metal reactor, wherein the bottom of the second metal pool is higher than the bottom of the first metal pool, and the first molten metal reactor and the second molten metal reactor are arranged horizontally and 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 reaction kettle, and the channel outlet is connected to the secondary molten metal reaction kettle;

[0010] The channel inlet and the channel outlet are both semicircular in shape, the channel inlet diameter is larger than the channel outlet diameter, and the center lines of the two are collinearly aligned.

[0011] Exemplarily, there is a distance between the center line of the channel inlet and the bottom of the first-stage molten metal reaction kettle, and the bottom arc of the channel outlet fits with the bottom of the second-stage molten metal reaction kettle.

[0012] Furthermore, the channel body includes a first-level molten metal reactor side wall section and a second-level molten metal reactor side wall section, the channel inlet is formed on the inner side wall of the first-level molten metal reactor, and the channel outlet is formed on the inner side wall of the second-level molten metal reactor.

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

[0014] Furthermore, the bottom of the first-stage molten metal reaction kettle and the second-stage molten metal reaction kettle are both provided with a melting groove, and the melting groove is located below the first metal pool and the second metal pool.

[0015] Preferably, the inner side walls of the first-stage molten metal reaction kettle and the second-stage molten metal reaction kettle are both provided with electromagnetic induction external heating devices.

[0016] On the other hand, an embodiment of the present invention further provides a molten metal-based gasification method, in which a material containing a polymer compound undergoes a decomposition and gasification reaction 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 first-level molten metal reactor 1, and the gasifying agent is sprayed to the drop point at the upper end of the liquid surface of the first metal pool 101 through the gasifying agent spray gun above the first-level molten metal reactor 1. The material undergoes a first-level gasification reaction under the action of the molten metal and the gasifying agent, and a first mixed gas is obtained after the reaction;

[0019] S1-2, the first mixed gas is sprayed to the bottom of the molten metal in the secondary molten metal reactor 2 through the gas-liquid channel, and passes upward through the molten metal layer and the slag liquid layer to perform 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. The present invention designs a reactor based on molten metal, and adopts a two-stage molten metal reactor interconnected by a gas-liquid channel to perform a decomposition and gasification reaction on materials containing high molecular polymers. The crude gas (gasification gas containing organic components) generated by the gasification of the first molten metal reactor is sprayed into the bottom layer of the molten metal in the second molten metal reactor through the gas-liquid channel. The crude gas is further decomposed by the high-temperature molten metal layer and the high-temperature slag liquid layer of the second molten metal reactor and is completely gasified into an inorganic mixed gas, ensuring that no high molecular weight 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 shrinking conical path from the channel inlet to the channel outlet. The channel is always infiltrated with molten metal to ensure that the material will not block the channel.

[0023] 3. The metal pools of different heights are connected in the present invention, and the smallest cross-sectional area of ​​the channel is completely filled with molten metal. On the one hand, it effectively prevents the accumulation of block materials and the possible blockage problems; on the other hand, it ensures that gas exchange cannot be carried out between the two reactors 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 slag and crude gas generated after the material reacts in the primary molten metal reactor are sprayed into the secondary molten metal reactor together, and finally enter the slag liquid layer of the secondary molten metal reactor, and are regularly 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, ash, etc., to ensure the purity of the product gas.

[0025] 5. The first-stage molten metal reaction kettle and the second-stage molten metal reaction kettle of the present invention are provided with a molten groove at the bottom, and the inner wall of the first-stage molten metal reaction kettle and the second-stage molten metal reaction kettle are provided with an electromagnetic induction external heating device, which can heat the molten metal by an electromagnetic vortex method to maintain the heat of the metal pool, and has a simple structure and is easy to operate.

[0026] 6. The present invention is aimed at various types of domestic waste and / or industrial waste containing high molecular weight polymers, especially high molecular weight polymers containing bromide, and designs a two-stage gasification reaction based on a molten metal reactor. The molten metal is used as the medium and the gasifying agent is used to decompose the high molecular weight compound, and the renewable and recyclable materials containing the high molecular weight compound are completely decomposed into an inorganic mixed gas, including CO, H 2 , CO 2 , and a small amount of escaped inorganic gases such as HCl and HBr. The inorganic mixed gas after purification is: the volume fraction of synthesis gas (CO+H 2 ), the remainder is CO 2 The purified mixed gas can enter the subsequent processing stage. For example, the Fischer-Tropsch synthesis reaction can be used to produce environmentally friendly products such as green methanol, sustainable aviation fuel (SAF), and high-quality green plastics, which will help gradually reduce dependence on disposable petrochemical resources.

[0027] The polymer material first undergoes a rapid primary gasification reaction under the action of molten metal and gasifier to generate a first mixed gas containing organic matter ranging from methane to C40. The first mixed gas passes through the molten metal again and undergoes a secondary gasification reaction with the action of the gasifier to completely decompose into an inorganic mixed gas. The inorganic mixed gas further passes through the slag liquid layer to capture ash, sulfur, chlorides, etc. into the slag liquid, making the obtained product synthesis gas purer and without causing problems such as coking at the back end.

[0028] In the present invention, the above-mentioned technical solutions can also be combined with each other to achieve more preferred combination solutions. Other features and advantages of the present invention will be described in the subsequent description, and some advantages can become obvious from the description, or can be understood by practicing the present invention. The purpose and other advantages of the present invention can be realized and obtained through the contents particularly pointed out in the description and the drawings. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] The drawings are only for the purpose of illustrating particular embodiments and are not to be considered limiting of the present invention. Like reference symbols denote like components throughout the drawings.

[0030] Figure 1 This is an appearance diagram of the molten metal reaction kettle of the present invention;

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

[0032] Figure 3 This is a working state diagram of the molten metal reaction kettle of the present invention after adding molten iron and slag liquid;

[0033] Figure 4 This is a diagram of the 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 A partial enlarged view of the middle part;

[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 material-shifting piece of the present invention;

[0038] Fig. 9 It is a top view of the inner material-shifting sheet unit and the rotating shaft of the present invention;

[0039] Fig.10 This is a front view of the first paddle of the present invention;

[0040] Fig.11 A top view of the upper material-picking sheet and the rotating shaft outside the upper area of ​​the rotating shaft of the present invention;

[0041] Fig.12 It is a top view of the lower part of the outer side of the lower area of ​​the rotating shaft and the rotating shaft of the present invention;

[0042] Fig.13 It is a top view of the upper section of the material-prying piece and the rotating shaft in the tapered material-prying opening area of ​​the present invention;

[0043] Fig.14 A top view of the shovel paddle and the rotating shaft of the present invention;

[0044] Fig.15 It is a top view of the blanking port flange of the present invention;

[0045] Fig.16 It is a three-dimensional structural diagram of the conical blanking port, blanking port flange and shoveling paddle of the present invention;

[0046] Fig.17 Schematic diagram of the angle relationship of the inner side stripping piece unit in the top view of the present invention Figure 1 ;

[0047] Fig.18 Schematic diagram of the angle relationship of the inner side stripping piece unit in the top view of the present invention Figure 2 ;

[0048] Fig.19 This is a schematic diagram of the angle relationship of the inner side material removal piece unit in the main viewing angle of embodiment 5 of the present invention;

[0049] Fig. 20 This is a schematic diagram of the angle relationship of the upper outer side of the material-diverting piece unit in the top view of Example 5 of the present invention;

[0050] Fig.21 This is a schematic diagram of the angle relationship of the lower outer side of the material-diverting piece unit in the top view of Example 5 of the present invention;

[0051] Fig. 22 This is a schematic diagram of the angle relationship of the outer side shifting piece unit in the main viewing angle of embodiment 5 of the present invention;

[0052] Fig.23 This is a diagram of a gasification system based on molten metal according to Example 1 of the present invention.

[0053] Reference numerals:

[0054] 1-primary molten metal reactor; 101-first metal pool; 102-feeding port; 2-secondary molten metal reactor; 201-second metal pool; 202-slag liquid pool; 3-gas-liquid channel; 4-liquid discharge port; 501-upper slag discharge port; 502-middle slag discharge port; 503-lower slag discharge port; 601-first gasifier spray gun installation port; 602-second gasifier spray gun installation port; 7-third gasifier spray gun installation port; 8-biomass spray gun installation port; 9-synthesis gas outlet; 10-second screw conveyor; 11-melting ditch; 12-third gasifier spray gun; 13-biomass spray gun; 14-first gasifier spray gun; 15-second gasifier spray gun; 16-feeding tank A; 17-feeding tank Material tank B; 18-first screw conveyor; 19-loading tank; 20-second screw conveyor; 21-material tank body; 22-feeding port flange; 23-heat exchange jacket; 24-medium inlet; 25-medium outlet; 26-fins; 27-conical feeding port; 28-shrink flange; 29-rotating shaft; 30-inner paddle unit; 31-outer upper paddle; 32-outer lower paddle; 33-lower end bearing; 34-upper end bearing; 35-second paddle; 36-first transmission shaft; 37-third paddle; 38-first paddle; 39-second transmission shaft; O1-center of the cross section of the rotating shaft; O2-center of the circle where the outer arc of the first paddle is located; a-center angle of the first paddle. DETAILED DESCRIPTION

[0055] The preferred embodiments of the present invention are described in detail below in conjunction with the accompanying drawings, wherein the accompanying drawings constitute a 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 used to limit the scope of the present invention.

[0056] On the 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 interconnected by a gas-liquid channel 3;

[0057] The first molten metal reactor 1 is provided with a first metal pool 101 inside, and the second 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 first molten metal reactor 1 and the second molten metal reactor 2 are arranged horizontally and staggered.

[0058] The height difference between the metal pools of the secondary molten metal reactor 2 and the primary molten metal reactor 1 can ensure that the primary molten metal reactor 1 has sufficient reaction pool volume to maintain the gasification reaction, and can also ensure that the gas generated by 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 sufficient reaction, thereby ensuring that the macromolecular gas that has not fully contacted with the molten iron in the primary molten metal reactor 1 is fully in contact with the molten iron in the secondary molten metal reactor 2, ensuring that it is completely vaporized into inorganic matter and no macromolecular gas exists.

[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 first-level molten metal reactor, and the channel outlet is connected to the second-level molten metal reactor; the channel inlet and the channel outlet are both semicircular in shape, the channel inlet diameter is larger than the channel outlet diameter, and the center lines of the two are collinearly aligned.

[0061] Specifically, there is a distance between the center line of the channel inlet and the bottom of the first-stage molten metal reaction kettle, and the bottom arc of the channel outlet fits with the bottom of the second-stage molten metal reaction kettle.

[0062] Preferably, the distance between the center line of the channel inlet and the bottom of the first 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 a possible design, the volume of the first metal pool 101 is 56 cubic meters, and the distance between the upper end surface of the channel inlet and the bottom of the first metal pool 101 in the first molten metal reactor 1 is 2 meters.

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

[0065] It should be noted that the axial cross-section of the channel body is semicircular, wherein the diameter of the semicircle gradually decreases from the channel entrance to the channel exit, the straight edge of the channel body is placed horizontally, and the arc edge smoothly transitions from the channel entrance to the channel exit, forming a gradually shrinking conical path.

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

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

[0068] Specifically, when the molten metal reactor system is in operation, the material freely falls into the first metal pool 101 through the feed port 102 at the top of the first molten metal reactor 1 (the material falling height is 3 to 3.5 meters), and at the same time, the gasifying agent is sprayed to the falling position through the first gasifying agent spray gun 14 and the second gasifying agent spray gun 15, so that the material and the molten metal are impact mixed to perform a primary gasification reaction, so that the material reacts fully and is rapidly gasified to generate a first mixed gas; the first mixed gas is rapidly generated in large quantities (the reaction time is within 0.1 seconds), so that the internal pressure of the first molten metal reactor 1 increases (the pressure inside the reactor is 1.5~1.8MPa), which increases the pressure difference between the first molten metal reactor 1 and the second molten metal reactor 2 (such as 0.2-0.6Mpa). Under the action of the pressure difference, the first mixed gas is sprayed to the bottom of the second metal pool 201 of the second molten metal reactor 2 through the gas-liquid channel 3, and at the same time, the gasifying agent is sprayed to the second metal pool 201 through the third gasifying agent spray gun 12 and / or the biomass powder is sprayed to the second metal pool 201 through the biomass spray gun 13. The first mixed gas passes through the molten metal layer and the slag liquid layer from the bottom to the top for a second thorough decomposition to obtain an inorganic mixed gas.

[0069] It should be noted that when the first mixed gas is sprayed from the first molten metal reactor 1 to the bottom of the second metal pool 201 of the second 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 semicircular arc of the channel outlet of the inner wall of the secondary molten metal reactor 2, but cannot be pressed further downward; the space of the channel inlet section is significantly larger than the channel space of the channel outlet section, and such a design is conducive to the accelerated flow of gas.

[0070] The metal pools of different heights are connected in the present invention, and the smallest cross-sectional area of ​​the channel is completely filled with molten iron, which effectively prevents the accumulation of block materials and possible blockage problems; on the other hand, ensures that gas exchange cannot be performed between the two reactors before the reaction.

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

[0072] In a possible design, the first gasifier spray gun mounting port 601 and the second gasifier spray gun mounting port 602 are arranged symmetrically at 180°, and the angles with the horizontal direction are both 45°, and the axes of the first gasifier spray gun mounting port 601 and the second gasifier spray gun mounting port 602 pass through the center point of the cross section of the first metal pool 101.

[0073] In a possible design, the third gasification agent spray gun installation port 7 and the biomass spray gun installation port 8 are arranged symmetrically at 180°, and the angle with the horizontal direction is 60°, and the axis of the third gasification agent spray gun installation port 7 and the biomass spray gun installation port 8 passes through the center point of the cross section of the second metal pool 201.

[0074] Preferably, the first-stage molten metal reaction kettle 1 further comprises a drain port 4 on the outer side wall of the kettle body, and 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 comprises 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 liquid level, the middle liquid level and the lower liquid level of the liquid in the slag liquid pool 202, respectively.

[0076] The upper slag discharge port 501 is used to regularly discharge the ash brought in by the material; the middle slag discharge port 502 is used to partially discharge the slag liquid in the slag liquid pool when replacing the gasification agent spray gun; the lower slag discharge port 503 is used to completely discharge the slag liquid in the slag liquid pool when the furnace is shut down.

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

[0078] Preferably, the bottom of the first-level molten metal reaction kettle 1 and the second-level molten metal reaction kettle 2 are both provided with a molten groove 11 , and the molten groove 11 is located below the first metal pool 101 and the second metal pool 201 .

[0079] Exemplarily, the inner walls of the primary molten metal reaction kettle 1 and the secondary molten metal reaction kettle 2 are both provided with electromagnetic induction external heating devices.

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

[0081] Furthermore, infrared thermometers are provided on the tops of the first-level molten metal reactor 1 and the second-level molten metal reactor 2; and molten metal observation communicating vessels are provided on the side walls of the first-level molten metal reactor 1 and the second-level molten metal reactor 2 to obtain liquid level information through electromagnetic correlation.

[0082] On the other hand, a specific embodiment of the present invention further discloses a molten metal-based gasification method, wherein a material containing a polymer compound undergoes a decomposition and gasification reaction in the molten metal reaction system to generate an inorganic mixed gas, and the decomposition and gasification reaction process is as follows:

[0083] S1-1, the material is dropped from the top of the first-level molten metal reactor 1, and the gasifying agent is sprayed to the drop point at the upper end of the liquid surface of the first metal pool 101 through the gasifying agent spray gun above the first-level molten metal reactor 1. The material undergoes a first-level gasification reaction under the action of the molten metal and the gasifying agent, and a first mixed gas is obtained after the reaction;

[0084] S1-2, the first mixed gas is sprayed to the bottom of the molten metal in the secondary molten metal reactor 2 through the gas-liquid channel, and passes upward through the molten metal layer and the slag liquid layer to perform 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 to 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 a 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, with molten metal as the medium and heat source, the material containing the polymer compound undergoes a decomposition and gasification reaction under the action of the gasifying agent to generate an inorganic mixed gas including CO and H 2 .

[0087] It should be noted that the molten metal can be molten iron with a temperature of 1400-1700°C. On the one hand, metallic iron serves as a reaction heat source, and its melting temperature range is 1400°C to 1700°C, which is suitable for the required temperature range of the decomposition gasification reaction. On the other hand, metallic iron serves as a catalyst. First, in the first step of the reaction, the molten iron reacts with the carbon, oxygen and water in the material to generate Fe 3 C and FeO, while producing H 2 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, accelerates the oxygen reduction process, and also reduces the activation energy of the water thermal decomposition reaction, thereby greatly improving the overall reaction efficiency; in the second step reaction, the liquid Fe 3 C and FeO further react to produce metallic iron and CO; through this two-step reaction mechanism, the iron liquid optimizes the reaction path, making the catalytic process produce more CO rather than CO 2 , thereby effectively reducing greenhouse gas emissions; the molten iron not only improves the overall efficiency of the reaction during the entire reaction process, but also reduces the reaction energy consumption through its catalytic effect, while achieving environmental friendliness.

[0088] The material reacts rapidly under the action of molten iron and gasifying agent, and the theoretical reaction time is within 0.1 second. Based on the high reaction rate, the introduction of gasifying agent can be stopped within 2 to 3 minutes after the feeding is stopped. Since there are a large amount of carbon-containing substances in the molten iron, the gasifying agent needs to be continued to be gasified after the feeding is stopped.

[0089] It is worth noting that, in theory, there is no loss of molten iron during the reaction process. However, in actual operation, some molten iron will be lost along with the slag liquid. For example, in the process of gasifying each ton of biomass, the loss of molten iron does not exceed 1kg. To compensate for this loss, iron ore is added to the molten metal together with the material during the reaction process to supplement the molten iron.

[0090] Preferably, the molten metal may be copper liquid, and the temperature is 1000-1300° C. When the material containing the polymer compound is a circuit board, the copper liquid is used as a medium and a heat source to achieve complete decomposition and gasification of the material into synthesis gas, and the metallic copper in the circuit board directly enters the copper liquid, which is beneficial to the recovery of copper in the circuit board.

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

[0092] In terms of system thermal balance: when oxygen is used as the gasifier, the polymer chain cleavage reaction in the material is an endothermic reaction. The incomplete oxidation reaction involving oxygen will release a large amount of heat. Therefore, the temperature required for the reaction can be maintained by the heat generated by the gasification reaction itself. No external heating is required to maintain the system thermal balance. When water vapor is used as the gasifier, the polymer chain cleavage reaction in the material is an endothermic reaction. Water vapor decomposes into H at high temperature. 2 The reaction with CO is also an endothermic reaction, so external heating is needed to maintain the thermal balance of the system; when a mixed gas of oxygen and water vapor is used as the gasifying agent, the external heating is adjusted according to the ratio of the two.

[0093] Product synthesis gas composition: When the gasification agent is all oxygen, the oxidation degree is high, the proportion of CO generated is high, and some CO 2 When water vapor is used as the gasifying agent, the water gas reaction (C+H 2 O→CO+H 2 ), which can increase the total volume of product syngas and H 2 proportion.

[0094] In one possible design, the gasifying agent is oxygen, and the purified inorganic mixed gas includes CO, H 2 and CO 2 , of which CO accounts for 60% by volume, H 2 The volume accounts for 39%, CO 2 The volume accounts for 1%.

[0095] In one possible design, the gasifier is water vapor, and the purified inorganic mixed gas includes CO and H 2 Mixed gas, of which CO accounts for 40% by volume, H 2 The volume accounts for 60%.

[0096] Preferably, the purification of the inorganic mixed gas includes dust removal, washing (such as alkaline washing), etc., and the components and composition of the inorganic mixed gas are detected after purification. This is because after the decomposition and gasification reaction is completed, the temperature of the mixed gas is high and it is 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 an electromagnetic vortex method to maintain the thermal balance of the system with low energy consumption.

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

[0099] The gasifier is sprayed into the molten metal through the gasifier spray gun at a speed of more than 200m / s, which is conducive to the impact mixing of the material and the molten metal, so that the reaction can be more fully carried out. When the gasifier is oxygen, the oxygen sprayed into the molten metal can react with the molten metal for oxidation. Since there are a large number of carbon-containing substances in the molten iron, the introduction of the gasifier is stopped within 2 to 3 minutes after the feeding is stopped, so that it is completely gasified, ensuring that the oxygen injection amount is appropriate to avoid overflow or excessive gasifier.

[0100] It should be noted that the material containing the polymer compound includes one or more of domestic 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 a powder state and sprayed into the molten metal through a spray gun. The decomposition and gasification reaction is carried out under the action of the molten metal and the gasifying agent. The spraying speed of the biomass powder is 200-250m / s.

[0102] Specifically, the biomass is carbonized by waste heat, ground into biomass powder, and sprayed directly into the bottom of the molten metal iron liquid through a spray gun. After the biomass airflow and the gasification agent airflow collide, the iron liquid forms a boiling state, and the biomass and the gasification agent are gasified into an inorganic mixed gas under the high energy and high heat reaction environment provided by the high temperature iron liquid and the catalytic effect of the metal.

[0103] Since the biomass particles are relatively small and no large polymer substances exist after carbonization, they can be completely decomposed through a single decomposition and gasification reaction.

[0104] Furthermore, the material includes domestic waste and / or industrial waste, and the decomposition gasification reaction includes a primary gasification reaction and a secondary gasification reaction; after the material undergoes 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, and undergoes a secondary gasification reaction under the action of the molten metal and the gasifying agent to generate an inorganic mixed gas including CO and H 2 The inorganic mixed gas passes upward through the slag liquid layer for displacement and filtration, and the very small escaped part can be subsequently purified.

[0105] It is worth noting that since domestic waste and industrial waste contain various types of high-molecular polymers containing bromides that are much larger than biomass molecules, as well as metal and non-metal inorganic substances, they cannot be directly sprayed to the bottom of the molten metal through a spray gun after pretreatment, and their specific gravity is much smaller than that of metals, it is impossible to ensure sufficient contact and sufficient contact time between the material and the molten iron. Therefore, after the primary gasification reaction, the first mixed gas produced contains organic matter ranging from methane to C40, and the proportion is uncontrollable. It must undergo a secondary reaction to completely decompose the inorganic matter.

[0106] The first mixed gas passes upward through the molten metal layer and fully contacts with the molten iron to ensure that it is completely vaporized into inorganic substances without the presence of large molecular gases, thereby 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. At the same time, since the gas is pure and entirely inorganic, it will not cause coking and other problems at the back end.

[0107] Specifically, the slag liquid layer includes dolomite and limestone, and the ratio of the two can be 2:1.

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

[0109] In a possible design, the industrial waste includes circuit boards, the molten metal is copper liquid, and the decomposition 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 copper liquid and a gasifier, the generated first mixed gas is passed into the bottom of the copper liquid and passes upward through the copper liquid layer, and undergoes a secondary gasification reaction under the action of the copper liquid and the gasifier to obtain an inorganic mixed gas; while the primary gasification reaction is being carried out, the metallic copper in the circuit board enters the copper liquid.

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

[0111] Furthermore, the purified inorganic mixed gas enters the back-end reaction system for Fischer-Tropsch synthesis to produce green products such as green methanol, green SAF jet fuel, and green high-quality plastics.

[0112] On the other hand, a specific embodiment of the present invention further discloses a molten metal-based gasification system for realizing the gasification method, comprising a feeding and preheating material system, a gasifying agent supply system, a molten metal reaction system, a synthesis gas purification and heat exchange system, and a synthesis gas storage system connected in sequence through pipelines; the feeding and preheating material system is connected to the inlet of the molten metal reaction system through a sealed interface; the gasifying agent supply system comprises a superheated steam boiler and / or an oxygen tank, and the outlets of the two are respectively connected to the gasifying agent spray guns introduced into the molten metal reaction system.

[0113] Furthermore, the feeding and preheating system includes a loading tank 19, a pouring tank A16 and a pouring tank B17 connected in parallel, and a first screw conveyor 18 and a second screw conveyor 19. The discharge ports of the pouring tank A16 and the pouring tank 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 feed port of the loading tank 19 through a pipe, the discharge port of the loading tank 19 is connected to the inlet of the second screw conveyor 20 through a pipe, and the outlet of the second screw conveyor 20 is connected to an external device through a sealing interface.

[0114] Preferably, the dump tanks A16 and B17 are designed to serve as backup for each other, ensuring that continuous material transportation can be maintained when a single tank fails, and can be flexibly switched according to production needs, thereby reducing downtime and improving production efficiency.

[0115] Furthermore, the loading 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 penetrating the tank body 21, and a material shifting piece disposed along the axial direction of the rotating shaft 29;

[0116] The material-shifting pieces include outer material-shifting pieces and inner material-shifting pieces, wherein the outer material-shifting pieces and the inner material-shifting pieces are alternately arranged in sequence along the axial direction of the rotating shaft 29;

[0117] The projections of the outer material-shifting piece and the inner material-shifting piece on the radial plane of the rotation shaft 29 do not overlap.

[0118] It should be noted that, in the outer and inner shifting pieces, the outer side and the inner side are relative, and are used to qualitatively illustrate the distance of the overall shifting piece from the rotation axis.

[0119] Specifically, the outer stripping piece and the inner stripping piece are fixedly arranged on the rotating shaft 29. Figures 8 to 22 shown.

[0120] Furthermore, the inner paddle sheet includes a plurality of inner paddle sheet units 30, and the inner paddle sheet unit 30 includes three first paddles 38, and 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 at the same time, it is upwardly raised by 10° to 60° along the axis of the rotating shaft relative to the radial plane of the rotating shaft 29.

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

[0122] Preferably, the plane of the first paddle 38 forms an angle of 30°, 40°, 50°, 60°, 75°, 80°, 85° with the axis of the rotating shaft 29, and at the same time rises 10°, 20°, 30°, 40°, 45°, 50°, 60° upward along the axis of the rotating shaft 29 relative to the radial plane of the rotating shaft 29. The angle between the plane of the first paddle 38 and the axis of the rotating shaft 29 and the spiral slope angle formed upward by the edge of the first paddle 38 are selected and adjusted according to the density and particle size of the material.

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

[0124] The inner arc of the first paddle 38 is in contact with the rotating shaft 29, and the thickness of the first paddle 38 increases along the rotating direction of the rotating shaft 29. The thickness design of the first paddle 38 can reduce the resistance during rotation.

[0125] Furthermore, the outer paddle piece includes a plurality of outer paddle piece units, and the outer paddle piece unit includes two second paddle pieces 35 . The second paddle pieces 35 are fixedly connected to the rotating shaft 29 through first transmission shafts 36 .

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

[0127] Exemplarily, the outer paddle piece includes an outer lower paddle piece 32 distributed in the lower area of ​​the rotating shaft, the second paddle 35 of the outer lower paddle piece unit of the outer lower paddle piece 32 is a rectangular paddle, and the angle b2 between the plane of the second paddle piece 35 and the axis of the rotating shaft 29 is 10°~60°; at the same time, the angle c2 between the horizontal axis of the plane of the second paddle piece 35 and the extended line of the axis of its first transmission shaft 36 is 15°~75°; and c2>c1.

[0128] Preferably, b1 is 10°, 20°, 30°, 40°, 45°, 50°, 60°, c1 is 15°, 20°, 30°, 40°, 45°, 50°, 60°, 75°; b2 is 10°, 20°, 30°, 40°, 45°, 50°, 60°, c2 is 15°, 20°, 30°, 40°, 45°, 50°, 60°, 75°. The angle between the plane of the second paddle 35 and the axis of the rotating shaft 29, the angle between the horizontal axis of the plane of the second paddle 35 and the extended line of the axis of the first transmission 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 transmission shafts 36 in the outer paddle sheet 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, thereby ensuring the balance of the structure and uniform force on the blades; the first transmission shafts 36 of multiple outer paddle sheet units are arranged in an overlapping radial layout, that is, in the projection on the radial plane of the rotating shaft 29, the radial layout of the first transmission shafts 36 at different heights is the same; the two first paddle blades 35 in the outer paddle sheet unit are centrally symmetrical with respect to the center of the rotating shaft 29.

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

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

[0133] Furthermore, after the material is fed through the feed port, 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 is combined with different material-shifting pieces on the rotating shaft 29. The outer material-shifting pieces play the role of shifting the material inward and upward, and the inner material-shifting pieces play the role of shifting the material outward and upward. This allows the material in the tank to flow inward and outward to ensure uniform heating of the material. At the same time, the material is constantly flipped upward to avoid bridging blockage of elastic materials.

[0135] Preferably, the loading tank 19 also includes a conical blanking port 27, the upper end of the conical blanking port 27 is connected to the bottom of the tank body 21 through a blanking port flange 22, and the lower end of the conical blanking port 27 is connected to an external conveying device through a reduction flange 28; the rotating shaft 29 passes through the blanking port flange 22 and the conical blanking port 27 area, and is fixedly installed on the inner side of the reduction flange 28 of the conical blanking port 27 through the lower end bearing 33 and the 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°C. There is no need to cool the bearing to avoid taking away heat. At the same time, there is no need for dynamic sealing. It can be directly sealed in the feeding tank 19, avoiding the difficulty of high-temperature sealing.

[0137] Furthermore, the outer stripper also includes a stripper for a blanking port distributed in the area of ​​the tapered blanking port 27 of the rotating shaft, and the second blade 35 of the outer stripper unit of the blanking port stripper is an inverted trapezoidal blade, and 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°, 60°. The inverted trapezoidal blade includes two side edges, a long bottom edge and a short bottom edge parallel to the first transmission shaft, one of the side edges is connected to the first transmission shaft, and the long bottom edge is located above the short bottom edge.

[0138] The shape design of the second paddle 35 in the material drop opening area is mainly to adapt to the conical space in the material drop opening area and effectively turn over the materials in the area.

[0139] It is worth noting that a blanking opening is provided on the blanking opening flange 22, and the cross section of the blanking opening is trapezoidal, with a small top and a large bottom, so as to prevent material from being stuck.

[0140] Preferably, a material scraping paddle is provided above the blanking port flange 22 to further avoid material bridging and blockage.

[0141] Specifically, the shoveling paddle includes two third paddles 37, and the third paddles 37 are fixedly connected to the rotating shaft 29 through second transmission shafts 39 respectively; the third paddles 37 are rectangular paddles, and the angle b4 between the plane of the third paddle 39 and the axis of the rotating shaft 29 is 60°~85°, preferably b4 is 60°, 70°, 75°, 80°, 85°; the two second transmission shafts 39 are arranged in a colinear manner, and their connecting line passes through the center of the cross section of the rotating shaft 29 at the same height.

[0142] In a possible design, the conical discharge port 27 has a taper of 10°, which improves the flow characteristics of the material and prevents the material from arching or clogging at the discharge port.

[0143] Preferably, the upper end bearing 34 of the rotating shaft is dynamically sealed at the connection with the top of the tank body 21. The sealing requirement is that under the condition of the sealing gas pressure of 1.0MPa to 1.5MPa, the leakage standard of the dynamic test is that the leakage is controlled within ≤0.10Nm when the speed is 0-60r / 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 in the tank body 21.

[0145] Preferably, fins 26 are installed on the outside of the heating coil to increase the heat exchange area and improve the heat exchange effect.

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

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

[0148] In a possible design, each material conveying channel and heat exchange medium pipeline is equipped with a control valve, and the external air temperature is 750-850°C.

[0149] The feeding and preheating system of the present invention avoids the problem of bridging and blocking of elastic materials on the one hand, and solves the problem of uneven preheating of the vertical tank on the other hand by adding a stirring system to the vertical tank. The design of the vertical tank is adopted, and multiple groups of paddle units are arranged along the longitudinal direction of the rotating shaft. Based on the angle setting of the paddles of the paddle units and combined with the rotation of the rotating shaft, when the paddles are moved, on the one hand, part of the material is moved to the center of the tank to loosen the material upward, and on the other hand, part of the material is moved to the outer wall of the tank, which promotes the flow of the material inside and outside, promotes heat exchange, and ensures that the material is heated evenly. At the same time, the material is constantly flipped upward, which can effectively avoid bridging and blocking of the elastic material.

[0150] In one possible design, when the feeding and preheating system of the present invention is applied to a decomposition and gasification reaction system of recyclable and renewable resources such as domestic waste, industrial waste and biomass, the air exchanges heat with the 1500°C high-temperature synthesis gas 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 waste heat recovery of the product synthesis gas and saving energy consumption.

[0151] In summary, the present invention designs a reactor based on molten metal, adopts a two-stage molten metal reactor interconnected by a gas-liquid channel, and performs a decomposition and gasification reaction on a material containing a high molecular polymer. The crude gas (gasified gas containing organic components) generated by the gasification of the first molten metal reactor is sprayed into the bottom layer of the iron liquid of the second molten metal reactor through the gas-liquid channel. The crude gas is further decomposed by the high-temperature iron liquid layer and the high-temperature slag liquid layer of the second molten metal reactor and completely decomposed into an inorganic mixed gas to ensure that no high molecular weight escapes. The inorganic mixed gas after purification is: a synthetic gas (CO+H 2 ), the remainder is CO 2 The purified mixed gas can enter the subsequent processing stage. For example, the Fischer-Tropsch synthesis reaction can be used to produce environmentally friendly products such as green methanol, sustainable aviation fuel (SAF), and high-quality green plastics, which will help gradually reduce dependence on disposable petrochemical resources.

[0152] The molten metal reactor and the molten metal gasification method of the present invention are described below in conjunction with 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 Fig.23 shown.

[0155] Molten metal reactor: Figure 1 , Figure 2As shown, it comprises a primary molten metal reactor 1 and a secondary molten metal reactor 2 which are interconnected through a gas-liquid channel 3; a first metal pool 101 is provided inside the primary molten metal reactor 1, and a second metal pool 201 is provided inside the secondary molten metal reactor 2, 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 and staggered;

[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; the channel inlet and the channel outlet are both semicircular in shape, the channel inlet diameter is larger than the channel outlet diameter, and the center lines of the two are collinearly aligned. There is a distance between the center line of the channel inlet and the bottom of the primary molten metal reactor 1, and the bottom arc of the channel outlet fits with the bottom of the secondary molten metal reactor 2;

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

[0158] Gasification system: Fig.23 As shown, it includes a feeding and preheating system, a gasifying agent supply system, a molten metal reaction system, a synthesis gas purification and heat exchange system, and a synthesis gas storage system which are sequentially connected through 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, and the outlets of the two are respectively connected to the gasifying agent spray guns that are introduced into the molten metal reaction system.

[0159] The synthesis gas purification and heat exchange system includes a cyclone dust collector, a heat exchanger, a bag dust collector, a washing tower and an air compressor. The inlet of the cyclone dust collector is connected to the synthesis gas 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 to the bag dust collector and the washing tower in sequence. The washing tower outlet is connected to the synthesis gas storage system; and air is transported 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 synthesis gas storage system comprises a compressor and a synthesis gas storage tank connected to the compressor outlet through a pipeline, and the compressor inlet is connected to the washing tower outlet through a pipeline.

[0161] When the gasification system is in use: the material is dropped into the molten metal surface of the first metal pool 101 in the first molten metal reactor 1 through the feeding and preheating system, and oxygen is sprayed to the drop point at the upper end of the liquid surface through the first gasifying agent spray gun 14 and the second gasifying agent spray gun 15 above the first molten metal reactor 1 while dropping the material, and the material undergoes a primary gasification reaction under the catalysis of the molten metal, and a first mixed gas is obtained after the reaction, and the generation of the first mixed gas in the first molten metal reactor 1 makes the pressure in the first molten metal reactor 1 higher than the pressure in the second molten metal reactor 2, so that the first mixed gas enters the bottom of the second metal pool 201 of the second molten 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, and the product inorganic mixed gas is discharged from the synthesis gas outlet 9 to the cyclone dust collector for dust removal, and then enters the synthesis gas purification agent heat exchange system, and further dust removal and purification are carried out after completing the heat exchange, and finally enters the synthesis gas 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 the air compressor sends air to the cold end inlet of the heat exchanger. After heat exchange, the synthesis gas temperature at the hot end outlet decreases, and the air temperature at the cold end outlet increases; the air is sent from the cold end outlet to the heat exchange jacket on the outer wall of the loading tank and the unloading tank to preheat the material.

[0163] The slag discharge process of the system is as follows: the 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 a specified height.

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

[0165] Materials: domestic waste, industrial waste and biomass, with a processing capacity of 100 tons / hour; the gasifying agent is oxygen, and the molten metal is liquid iron with 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 secondary 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 0.8m 2 The channel inlet is a semicircle with a cross section of 1.8 to 2 meters in diameter, and the distance from the upper end surface of the channel inlet to the bottom of the first metal pool is 2 meters; the channel outlet is a semicircle with a cross section of 0.6 to 0.8 meters in diameter.

[0167] When the system is used for the first time: iron powder with particle size less than 2 mm is added to the first metal pool 101 and the second metal pool 201 respectively, and after heating to a molten state, dolomite powder and limestone powder are added to the second metal pool 201 to form a slag liquid layer.

[0168] The main design parameters of the decomposition gasification reaction and subsequent treatment process are as follows: the material is dropped into the molten metal surface in the first metal pool 101 of the first molten metal reactor 1 through the feeding and preheating system. At the same time, oxygen is sprayed to the drop point at the upper end of the liquid surface through the first gasifier spray gun 14 and the second gasifier spray gun 15 above the first molten metal reactor 1 at a speed of 200m / s. The material undergoes a primary gasification reaction under the catalysis of the molten iron, and a first mixed gas is obtained after the reaction. The pressure in the first molten metal reactor 1 reaches 1.5MPa. 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 50-150m / s and passes through the molten metal and slag liquid layer. At the same time, the third gasifying agent spray gun 12 sprays oxygen to the second metal pool 201 at a speed of 200m / s, and the biomass spray gun 13 sprays biomass powder to the second metal pool 201 at a speed of 200m / s. The product inorganic mixed gas is discharged from the synthesis gas outlet 9 to the cyclone dust collector for dust removal at a speed of 30-35m / s, and then enters the synthesis gas purifier heat exchange system. After the heat exchange is completed, the temperature drops to below 300°C, and further dust removal and purification are carried out, and then enters the synthesis gas storage tank.

[0169] The main design parameters of the waste heat recovery process are as follows: the product inorganic mixed gas with a temperature of 1500°C enters the hot end inlet of the heat exchanger through a pipeline, and at the same time, the air compressor sends air to the cold end inlet of the heat exchanger. After heat exchange, the temperature of the inorganic mixed gas at the hot end outlet is 300°C, and the air temperature at the cold end outlet is 850°C; the air is sent from the cold end outlet to the heat exchange jacket 23 on the outer wall of the loading tank 19 and the unloading tank to preheat the material to 400°C.

[0170] Example 2

[0171] This embodiment provides a gasification method based on molten metal. Figure 3 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 liquid 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:

[0175] Step 1: Pre-process the material into briquette to less than 80 mm.

[0176] Step 2: The pretreated material is delivered to the surface of the molten iron in the primary molten metal reactor, and oxygen is sprayed onto the surface of the molten iron at a speed of 200 m / s through a gasifier spray gun. The spraying of the gasifier 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 a 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, passes through the molten iron layer in the secondary molten metal reactor and the slag liquid layer above the molten iron layer in turn, and at the same time, oxygen is sprayed into the molten iron in the secondary molten metal reactor at a speed of 200m / s through the gasifier spray gun, and the spraying of the gasifier is stopped within 2 to 3 minutes after the feeding is stopped. The first mixed gas undergoes a secondary gasification reaction in this process, and an inorganic mixed gas is obtained from above the slag liquid layer.

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

[0179] After testing, the volume fractions of the components in the final product synthesis gas are: CO: 60%; H 2 :39%;CO 2 : 1%.

[0180] Example 3

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

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

[0183] The gasification process is:

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

[0185] Step 2, spraying biomass powder into the secondary molten metal reactor iron liquid through a biomass spray gun at a speed of 200m / s, and at the same time spraying oxygen into the iron liquid through a gasifier spray gun at a speed of 200m / s, and stopping the spraying of the gasifier within 2 to 3 minutes after stopping the spraying of the biomass powder. In this process, the biomass undergoes a primary gasification reaction, and an 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] After testing, the volume fractions of the components in the final product synthesis gas are: CO: 60%; H 2 :39%;CO 2 : 1%.

[0188] Example 4

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

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

[0191] The gasification process is:

[0192] Step 1: The crushed material is sent to the copper liquid surface of the primary molten metal reactor, and oxygen is sprayed to the copper liquid surface at a speed of 250m / s through a gasifier spray gun. The spraying of the gasifier is stopped within 2 to 3 minutes after the feeding is stopped. The material undergoes a primary gasification reaction under the action of the copper liquid and the gasifier, and a first mixed gas is obtained after the reaction. The metallic copper in the circuit board enters the copper liquid to be recovered.

[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, passes through the copper liquid layer in the secondary molten metal reactor and the slag liquid layer above the copper liquid layer in sequence, and at the same time, oxygen is sprayed into the copper liquid in the secondary molten metal reactor at a speed of 250m / s through the gasifier spray gun, and the spraying of the gasifier is stopped within 2 to 3 minutes after the feeding is stopped. The first mixed gas undergoes a secondary gasification reaction in this process, and an 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] After testing, the volume fractions of the components in the final product synthesis gas are: CO: 60%; H 2 :39%;CO 2 : 1%.

[0196] Example 5

[0197] This embodiment provides a preheating material and feeding system. Figures 4 to 16 shown.

[0198] Used as feed for decomposition and gasification reaction systems of recyclable and renewable resources such as domestic waste, industrial waste and biomass.

[0199] The feeding and preheating system includes a pouring tank A16 and a pouring tank B17, a loading tank 19, a first screw conveyor 18, and a second screw conveyor 20 connected in parallel. The discharge ports of the pouring tank A16 and the pouring tank B17 are respectively connected to the inlet of the first screw conveyor 18 through pipelines, the outlet of the first screw conveyor 18 is connected to the feed port of the loading tank 19 through a pipeline, the discharge port of the loading tank 19 is connected to the inlet of the second screw conveyor 20 through a pipeline, and the outlet of the second screw conveyor 20 is connected to external equipment through a sealing interface;

[0200] The loading tank 19 includes a tank body 21, a heat exchange jacket 23 arranged outside the tank body 21, a rotating shaft 29 arranged along the height direction of the tank body 21 and penetrating the tank body, and a material shifting piece arranged axially along the rotating shaft 29; the projections of the outer material shifting piece and the inner material shifting piece on the radial plane of the rotating shaft do not overlap.

[0201] The outer paddle and the inner paddle are fixedly arranged on the rotating shaft. The inner paddle includes an inner paddle unit 30, and the inner paddle unit 30 includes three first paddles 38, which are evenly arranged 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 at the same time, it rises 10° to 60° along the axis of the rotating shaft 29 relative to the radial plane of the rotating shaft 29.

[0202] The outer paddle piece includes a plurality of outer paddle piece units, and the outer paddle piece unit includes two second paddle pieces 35 . The second paddle pieces 35 are fixedly connected to the rotating shaft 29 through first transmission shafts 36 .

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

[0204] Exemplarily, the outer paddle piece includes an outer lower paddle piece 32 distributed in the lower area of ​​the rotating shaft, the second paddle 35 of the outer lower paddle piece unit of the outer lower paddle piece 32 is a rectangular paddle, and the angle b2 between the plane of the second paddle piece 35 and the axis of the rotating shaft 29 is 10°~60°, and the angle c2 between the horizontal axis of the plane of the second paddle piece 35 and the extended line of the axis of its first transmission shaft 36 is 15°~75°; and c2>c1.

[0205] The loading tank 19 also includes a conical blanking port 27, the upper end of the conical blanking port 27 is connected to the bottom of the tank body 21 through a blanking port flange 22, and the lower end of the conical blanking port 27 is connected to the external conveying equipment through a reduction flange 28; the rotating shaft 29 passes through the blanking port flange 22 and the conical blanking port 27 area, and is fixedly installed on the inner side of the reduction flange 28 of the conical blanking port 27 through the lower end bearing 33 and the lower bearing seat.

[0206] The outer stripper also includes a stripper of a blanking opening distributed in the area of ​​the tapered blanking opening 27 of the rotating shaft. The second blade 35 of the outer stripper unit of the blanking opening stripper is an inverted trapezoidal blade, and 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 side edges, a long bottom edge and a short bottom edge parallel to the first transmission shaft, one of the side edges is connected to the first transmission shaft, and the long bottom edge is located above the short bottom edge.

[0207] A scraping paddle is provided above the blanking port flange 22, and the scraping paddle includes two third paddles 37, and the third paddles 37 are fixedly connected to the rotating shaft 29 through second transmission shafts 39 respectively; the third paddle 37 is a rectangular paddle, and the angle b4 between the plane of the third paddle 37 and the axis of the rotating shaft 29 is 60°~85°; the two second transmission shafts 39 are arranged in the same line, and their connecting line passes through the center of the cross section of the rotating shaft 29 at the same height.

[0208] The pouring tank A16 and the pouring tank B17 have the same structure as the loading tank 19, wherein the pouring tank A16 and the pouring tank B17 are backup for each other.

[0209] The heat exchange jacket 23 includes an outer 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 respectively connected to the medium inlet 24 and the medium outlet 25 through the outer shell, wherein 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 the feeding and preheating system of the present invention is used:

[0211] The material is transported from the external silo to the pouring tank A16 (the pouring tank B17 is used as a backup), and the feeding is completed through the feeding port of the pouring tank A16; at the same time, the rotating shaft of the pouring tank A16 continuously rotates in the loading tank, and the material falls into the first screw conveyor 18 through the tapered dropping port of the pouring tank A16, and then enters the feeding port of the loading tank 19 from the outlet of the first screw conveyor 18; the rotating shaft of the loading tank 19 also rotates continuously, and the material enters the second screw conveyor 20 through the tapered dropping port of the loading 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 a water cooling system is provided outside the high-pressure resistant sealing interface.

[0212] When the material enters the dump tank A16, the external air enters the heat exchange jacket 23 of the system through the medium inlet 24 of the heat exchange jacket 23 of the feed tank, and after the heat exchange is completed, it returns to the air compressor through the medium outlet of the dump tank A16, so as to realize the recycling of the heat exchanged air. Before entering the system, the air exchanges heat with the 1500℃ high-temperature synthesis gas 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, the material is preheated to 400℃ through the above heat exchange process.

[0213] Application of this feeding and preheating system:

[0214] Used for feeding the decomposition gasification reaction system of recyclable and renewable resources such as domestic waste, industrial waste and biomass; conveying capacity 200m 3 / h.

[0215] Main equipment parameters of the system: the diameter of the tank body 21 is 4 meters, the lower diameter of the conical drop-out port 27 is 1 meter and the taper is 10°; the cross-sectional size of the heating coil is 500*300mm, and the total length is 400m; the number of inner paddle units is 8; the plane of the first paddle 38 forms an angle of 60° with the axis of the rotating shaft 29, and at the same time rises 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: The rotating shafts of the pouring tank and the loading tank rotate at a speed of 65r / min.

[0217] Main preheating parameters: Before entering this system, the air exchanges heat with the 1500℃ high-temperature gas 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, the material is preheated to 400℃ through the above heat exchange process.

[0218] During the operation of the entire system, the material is transported smoothly without blockage or bridging, and the material temperature is evenly distributed.

[0219] In summary, the present invention designs a reactor based on molten metal, adopts a two-stage molten metal reactor interconnected by a gas-liquid channel, and performs a decomposition and gasification reaction on a material containing a high molecular polymer. The crude gas (gasified gas containing organic components) generated by the gasification of the first molten metal reactor is sprayed into the bottom layer of the iron liquid of the second molten metal reactor through the gas-liquid channel. The crude gas is further decomposed by the high-temperature iron liquid layer and the high-temperature slag liquid layer of the second molten metal reactor and completely decomposed into an inorganic mixed gas to ensure that no high molecular weight escapes. The inorganic mixed gas after purification is: a synthetic gas (CO+H2 ), the remainder is CO 2 The purified mixed gas can enter the subsequent processing stage. For example, the Fischer-Tropsch synthesis reaction can be used to produce environmentally friendly products such as green methanol, sustainable aviation fuel (SAF), and high-quality green plastics, which will help gradually reduce dependence on disposable petrochemical resources.

[0220] The above description is only a preferred specific implementation manner of the present invention, but the protection scope of the present invention is not limited thereto. Any changes or substitutions that can be easily conceived by any technician familiar with the technical field within the technical scope disclosed by the present invention should be covered within the protection scope of the present invention.

Claims

1. A molten metal reactor, characterized in that: It includes a primary molten metal reaction kettle and a secondary molten metal reaction kettle which are interconnected through a gas-liquid channel; A first metal pool is provided inside the first molten metal reactor, and a second metal pool is provided inside the second molten metal reactor, wherein the bottom of the second metal pool is higher than the bottom of the first metal pool, and the first molten metal reactor and the second molten metal reactor are arranged horizontally and staggered.

2. The reactor according to claim 1, characterized in that: 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.

3. The reaction kettle according to claim 2, characterized in that: The semi-conical channel comprises a channel inlet, a channel body and a channel outlet, the channel inlet is connected to the first-level molten metal reaction kettle, and the channel outlet is connected to the second-level molten metal reaction kettle; The channel inlet and the channel outlet are both semicircular in shape, the channel inlet diameter is larger than the channel outlet diameter, and the center lines of the two are collinearly aligned.

4. The reactor according to claim 3, characterized in that: There is a distance between the center line of the channel inlet and the bottom of the first-stage molten metal reaction kettle, and the bottom arc of the channel outlet fits with the bottom of the second-stage molten metal reaction kettle.

5. The reactor according to claim 3, characterized in that: The channel body includes a first molten metal reactor side wall section and a second molten metal reactor side wall section, the channel inlet is formed on the inner side wall of the first molten metal reactor, and the channel outlet is formed on the inner side wall of the second molten metal reactor.

6. The reactor according to claim 1, characterized in that: The top of the first-level molten metal reactor is provided with a feed inlet and a gasification agent spray gun installation port; the top of the second-level molten metal reactor is provided with a synthesis gas outlet; and a slag liquid pool is provided above the second metal pool of the second-level molten metal reactor.

7. The reactor according to claim 1, characterized in that: The first-stage molten metal reaction kettle and the second-stage molten metal reaction kettle are both provided with a melting groove at the bottom, and the melting groove is located below the first metal pool and the second metal pool.

8. The reactor according to claim 1, characterized in that: The inner side walls of the first-stage molten metal reaction kettle and the second-stage molten metal reaction kettle are both provided with electromagnetic induction external heating devices.

9. A method for gasification based on molten metal, characterized in that: The material containing the polymer compound undergoes a decomposition and gasification reaction in the molten metal reactor described in any one of claims 1 to 8 to generate an inorganic mixed gas.

10. The gasification method according to claim 9, characterized in that: The decomposition and gasification reaction process is as follows: S1-1, the material is dropped from the top of the first-level molten metal reactor 1, and the gasifying agent is sprayed to the drop point at the upper end of the liquid surface of the first metal pool 101 through the gasifying agent spray gun above the first-level molten metal reactor 1. The material undergoes a first-level gasification reaction under the action of the molten metal and the gasifying agent, and a first mixed gas is obtained after the reaction; S1-2, the first mixed gas is sprayed to the bottom of the molten metal in the secondary molten metal reactor 2 through the gas-liquid channel, and passes upward through the molten metal layer and the slag liquid layer to perform a secondary gasification reaction to obtain an inorganic mixed gas.

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