Device and method for producing synthesis gas from organic solid waste molten iron bath with pre-pyrolysis process

Abstract

This invention relates to a device and method for producing syngas from organic solid waste using a molten iron bath with a pre-pyrolysis process. The device includes a molten pool gasifier with a first feed pipe, a second feed pipe, and a syngas outlet pipe, and contains molten iron inside; a cooler connected to the syngas outlet pipe; a rake pyrolysis machine connected to the cooler; a condenser connected to the pyrolysis gas outlet of the rake pyrolysis machine; an oil-water separator connected to the condenser, which, after being pressurized by a high-pressure oil pump and vaporized by a vaporizer, is fed into an ejector as a primary high-pressure fluid; a heat exchanger connected to the pyrolysis non-condensable gas outlet and the heat exchange steam outlet of the condenser; and an ejector connected to the second feed pipe, the vaporizer, and the heat exchanger. This invention eliminates the need to crush organic solid waste to within 3mm, significantly reducing pre-treatment costs. Organic solid waste containing water-containing impurities and water-containing oil sludge do not require drying and can be directly put into production. There is no drying exhaust gas, and the entire process is exhaust-free, facilitating automated production.

Description

Technical Field

[0001] This invention relates to the energy field, specifically to an apparatus and method for producing syngas from organic solid waste using a molten iron bath with a pre-pyrolysis process. Background Technology

[0002] Currently, in the process of producing syngas from organic solid waste using an iron bath, light, thin, and soft organic solid waste undergoes multiple crushing processes to a thickness of less than 3mm, which results in high energy consumption, time-consuming, and labor-intensive crushing. Furthermore, organic solid waste containing water-containing impurities and water-containing oily sludge must be dried to remove moisture before being fed into the system. This leads to excessively high overall processing costs and hinders the improvement of processing efficiency.

[0003] Therefore, there is an urgent need for a device and method for producing syngas from organic solid waste using a molten iron bath with a pre-pyrolysis process, which can directly put into production without the need to crush thin and soft organic solid waste into less than 3mm, and without drying organic solid waste and water-containing oil sludge mixed with water-containing impurities. There is no drying tail gas, no tail gas emission throughout the entire process, and it is easy to realize automated production. Summary of the Invention

[0004] The purpose of this invention is to address the aforementioned problems in the prior art by providing an organic solid waste molten iron bath syngas production device with a pre-pyrolysis process.

[0005] To achieve the above-mentioned objectives, the present invention employs the following technical solution: An organic solid waste molten iron bath syngas production device with a pre-pyrolysis process comprises:

[0006] The molten pool gasifier is equipped with a first feed pipe, a second feed pipe, and a syngas outlet pipe, and contains molten iron inside, which is used to produce syngas from organic solid waste molten iron bath.

[0007] A cooler, connected to the syngas outlet pipe, is used to cool the syngas to a first set temperature;

[0008] A rake-type pyrolysis machine, connected to a cooler, is used to pyrolyze organic solid waste or water-containing oily sludge after primary crushing using syngas cooled to a first set temperature as a heat source to produce pyrolysis gas and pyrolysis semi-coke.

[0009] The condenser is connected to the pyrolysis gas outlet of the rake pyrolysis machine and is used to condense the pyrolysis gas into a mixture of non-condensable gas and oil.

[0010] An oil-water separator, connected to a condenser, is used to separate oil-water mixtures into oil and water. The oil is then pressurized by a high-pressure oil pump and vaporized by a vaporizer before being fed into an ejector as a primary high-pressure fluid.

[0011] The heat exchanger is connected to the pyrolysis non-condensable gas outlet and the heat exchange steam outlet of the condenser. It is used to heat the non-condensable gas to a second set temperature using the heat exchange steam of the condenser as a heat source, and input it into the ejector as a secondary low-pressure fluid.

[0012] The ejector is connected to the second feed pipe, the vaporizer and the heat exchanger respectively, and is used to drive the primary high-pressure fluid to the secondary low-pressure fluid into the molten iron in the molten pool gasifier for further cracking and gasification.

[0013] Working principle and beneficial effects: 1. Compared with the existing technology, this application generates pyrolysis gas and pyrolysis semi-coke by pyrolyzing organic solid waste or water-containing oil sludge after simple primary crushing. The heat source is the cooled syngas. In this way, there is no need to crush the organic solid waste multiple times or dry it. The water-containing oil sludge can be put into production directly. The whole process can recycle energy, which greatly reduces energy consumption and treatment costs, and further improves processing efficiency. Thus, the whole process is free of exhaust gas emissions and is easy to automate.

[0014] 2. Compared with the prior art, the heat source of the rake pyrolysis machine, condenser and vaporizer in this application all come from the processing process, realizing the recycling of energy. Moreover, the primary high-pressure fluid is pushed into the molten iron in the molten pool gasifier by the ejector to be cracked and gasified again. The substances generated in the whole process can be completely treated for energy, and the required syngas is effectively retained, thus achieving no drying tail gas and no tail gas emission in the whole process.

[0015] Furthermore, the heat exchange steam inlet of the vaporizer is connected to the heat exchange steam outlet of the cooler, so as to utilize the heat energy of the initial cooling process of the syngas as the heat source for vaporization.

[0016] Furthermore, the initial set temperature is 500℃. Since organic solid waste pyrolyzes within the temperature range of 450℃ to 500℃, further increasing the pyrolysis machine temperature would increase non-condensable gases and decrease pyrolysis oils in the pyrolysis products. Less pyrolysis oil is less conducive to subsequent pressurization, vaporization, and ejection. Therefore, the pyrolysis machine is set at 500℃.

[0017] Furthermore, the second set temperature is 350℃ or close to 350℃. This is because the temperature of the pyrolysis non-condensable gas entering the ejector must be close to that of the primary high-pressure fluid (vaporized pyrolysis oil), otherwise it will affect the pressure after ejection. At this point, the vaporized temperature of the pyrolysis oil is exactly around 350℃.

[0018] Furthermore, the size of the organic solid waste after primary crushing is 10cm or close to 10cm. This is because, after multiple verifications, setting the feed size of the pyrolysis machine to 10cm is a relatively economical size after crushing, and it does not require excessive pretreatment of the organic solid waste, thus greatly reducing costs.

[0019] Furthermore, the cooler uses a first fan to input syngas at a first set temperature into the hollow outer wall interlayer of the rake pyrolysis machine, so as to serve as a heat source for the pyrolysis of organic solid waste or water-containing oily sludge.

[0020] Furthermore, the rake pyrolysis machine is equipped with a second feed lock hopper at the feed inlet. The top of the second feed lock hopper is equipped with a first hopper, and the side is evacuated by a second vacuum pump. Pneumatic valves are provided between the second feed lock hopper and the first hopper, as well as between the second feed lock hopper and the feed inlet.

[0021] Furthermore, the condenser uses a second fan to introduce non-condensable gas into the heat exchanger for heat exchange.

[0022] Furthermore, the bottom of the rake pyrolysis machine is provided with a pyrolysis semi-coke outlet, which is equipped with a blower and a second hopper or material conveyor for receiving the pyrolysis semi-coke. After being discharged from the pyrolysis semi-coke outlet, the pyrolysis semi-coke re-enters the first feed lock hopper of the molten pool gasifier for further cracking and gasification.

[0023] A method for producing syngas from organic solid waste using a molten iron bath with a pre-pyrolysis process, employing the aforementioned syngas-producing apparatus from organic solid waste using a molten iron bath with a pre-pyrolysis process, includes the following steps:

[0024] Material is added to the molten pool gasifier through the first feed lock hopper above the first feed pipe;

[0025] Close the first and third pneumatic valves on the first feed hopper, and turn on the first vacuum pump to evacuate the first feed hopper until the evacuation is complete.

[0026] Open the third pneumatic valve and introduce oxygen through the oxygen inlet on the first feed pipe. The material is sent into the molten iron to be cracked and gasified to generate syngas.

[0027] Syngas is fed into a cooler through a syngas outlet pipe and cooled to a first set temperature. Syngas at the first set temperature is then fed into the hollow outer wall interlayer of the rake pyrolysis machine by a first fan.

[0028] Close the fourth pneumatic valve between the first hopper and the second feed lock hopper of the rake pyrolysis machine, open the seventh pneumatic valve between the second feed lock hopper and the feed inlet of the rake pyrolysis machine, and turn on the second vacuum pump to evacuate the second feed lock hopper and the rake pyrolysis machine until the evacuation is complete.

[0029] Close the seventh pneumatic valve, open the fourth pneumatic valve, feed through the second feed hopper, and start the rake pyrolysis machine;

[0030] Close the fourth and seventh pneumatic valves, start the second vacuum pump to evacuate again until the evacuation is complete;

[0031] Open the seventh pneumatic valve so that the vacuumed material can enter the rake pyrolysis machine for pyrolysis, producing pyrolysis gas and pyrolysis semi-coke;

[0032] Pyrolysis gas is fed into the condenser through the pyrolysis gas outlet, and pyrolysis semi-coke is discharged into the second hopper through the pyrolysis semi-coke outlet. Pyrolysis semi-coke is then added into the first feed lock hopper through the second hopper.

[0033] The pyrolysis gas is condensed in the condenser to form a mixture of non-condensable gas and oil. The non-condensable gas is fed into the heat exchanger through the pyrolysis non-condensable gas outlet and the second fan for heat exchange. The oil mixture enters the oil-water separator through the liquid collection tank between the oil and water separators for oil-water separation.

[0034] The heat exchanger heats the non-condensable gas to a second set temperature to serve as a secondary low-pressure fluid for the ejector.

[0035] The oil-water separator separates an oil-liquid mixture into oil and water. The oil is pressurized by a high-pressure oil pump and then enters a vaporizer for vaporization, serving as the primary high-pressure fluid for the ejector.

[0036] The ejector causes the primary high-pressure fluid to carry the secondary low-pressure fluid into the molten iron in the molten pool gasifier for further cracking and gasification. Attached Figure Description

[0037] Figure 1 This is a schematic diagram of the structure of the present invention;

[0038] Figure 2 This is a process flow diagram of the present invention.

[0039] In the diagram, 1. First pneumatic valve; 2. First feed hopper; 3. Second pneumatic valve; 4. First vacuum pump; 5. Third pneumatic valve; 6. Oxygen inlet; 7. First feed pipe; 8. Molten pool gasifier; 9. Molten iron; 10. Syngas outlet pipe; 11. Cooler; 12. First cooling water inlet; 13. First heat exchange steam outlet; 14. First blower; 15. First hopper; 16. Fourth pneumatic valve; 17. Second feed hopper; 18. Second vacuum pump; 19. Fifth pneumatic valve; 20. Seventh pneumatic valve; 21. Feed inlet; 22. Rake pyrolysis machine; 23. Heat... 24. Semi-coke outlet; 25. Second hopper; 26. Airlock fan; 27. Reducer; 28. Motor; 29. ​​Syngas outlet; 30. Pyrolysis gas outlet; 31. Drain outlet; 32. Oil-water separator; 33. High-pressure oil pump; 34. Liquid collection tank; 35. Second cooling water inlet; 36. Condenser; 37. Pyrolysis non-condensable gas outlet; 38. Second heat exchange steam outlet; 39. Heat exchanger; 40. Condensate outlet; 41. Vaporizer; 42. Heat exchange steam inlet; 43. Cooling water outlet; 44. Ejector; 45. Second feed pipe; 46. Molten slag. Detailed Implementation

[0040] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. All other embodiments obtained by those skilled in the art based on the embodiments of the present invention are within the scope of protection of the present invention.

[0041] Those skilled in the art should understand that, in the disclosure of this invention, the terms "longitudinal," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," and "outer," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are only for the convenience of describing this invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, the above terms should not be construed as limiting this invention.

[0042] like Figure 1 As shown, this organic solid waste molten iron bath syngas production device with pre-pyrolysis process includes:

[0043] The molten pool gasifier 8 is equipped with a first feed pipe 7, a second feed pipe 45, and a syngas outlet pipe 10, and is equipped with molten iron 9 inside, which is used to produce syngas from organic solid waste molten iron bath.

[0044] The molten iron pool gasifier 8 contains molten iron liquid 9 and molten slag liquid 46 located on the molten iron liquid 9.

[0045] The first feed pipe 7 is equipped with an oxygen inlet 6 for introducing oxygen.

[0046] The first feed pipe 7 is also connected to a first feed lock hopper 2 for feeding and a third pneumatic valve 5 located between the first feed lock hopper 2 and the first feed pipe 7. The first feed lock hopper 2 is equipped with a first pneumatic valve 1, a second pneumatic valve 3 and a first vacuum pump 4, and the first vacuum pump 4 is used to achieve vacuuming.

[0047] Cooler 11 is connected to syngas outlet pipe 10 and is used to cool syngas to a first set temperature.

[0048] The cooler 11 is also provided with a first cooling water inlet 12 and a first heat exchange steam outlet 13.

[0049] The rake-type pyrolysis machine 22 is connected to the cooler 11 and is used to pyrolyze the organic solid waste (10cm or close to 10cm) or water-containing oil sludge after initial crushing using syngas cooled to the first set temperature (500℃) as a heat source to produce pyrolysis gas and pyrolysis semi-coke.

[0050] Among them, after multiple verifications, setting the feed size of the pyrolysis machine to 10cm is a relatively economical size after crushing, and it does not require excessive pretreatment of organic solid waste, which greatly reduces costs.

[0051] Because organic solid waste decomposes within a temperature range of 450℃ to 500℃, further increasing the pyrolysis machine temperature increases the amount of non-condensable gases and decreases the amount of pyrolysis oils in the pyrolysis products. Less pyrolysis oil is less conducive to subsequent pressurization, vaporization, and ejection. Therefore, the pyrolysis machine is set at 500℃.

[0052] In this embodiment, a second feed lock hopper 17 is provided on the feed inlet 21 of the rake pyrolysis machine 22. The top of the second feed lock hopper 17 is provided with a first hopper 15. The side is evacuated by a second vacuum pump 18. Pneumatic valves (a fourth pneumatic valve 16 and a seventh pneumatic valve 20) are provided between the second feed lock hopper 17 and the first hopper 15, as well as between the second feed lock hopper 17 and the feed inlet 21.

[0053] A fifth pneumatic valve 19 is provided between the second vacuum pump 18 and the second feed hopper 17.

[0054] In this embodiment, the bottom of the rake pyrolysis machine 22 is provided with a pyrolysis semi-coke outlet 23. The pyrolysis semi-coke outlet 23 is provided with a blower 25 and a second hopper 24 or material conveyor for receiving the pyrolysis semi-coke. After the pyrolysis semi-coke is discharged from the pyrolysis semi-coke outlet 23, it re-enters the first feed lock hopper 2 of the molten pool gasifier 8 for further cracking and gasification.

[0055] The rake pyrolysis machine 22 operates by a motor 27 driving a reducer 26 to drive the internal spiral structure. The pyrolysis machine is also equipped with a syngas outlet 28 for discharging syngas.

[0056] In this embodiment, the cooler 11 inputs syngas at 500°C into the hollow outer wall interlayer of the rake pyrolysis machine 22 via the first fan 14, so as to serve as a heat source for the pyrolysis of organic solid waste or water-containing oil sludge.

[0057] The condenser 35 is connected to the pyrolysis gas outlet 29 of the rake pyrolysis machine 22 and is used to condense the pyrolysis gas to form a mixture of non-condensable gas and oil.

[0058] The non-condensable gas after passing through the condenser 35 is introduced into the heat exchanger 39 by the second fan 37 for heat exchange. The condenser 35 is also provided with a second cooling water inlet 34 and a second heat exchange steam outlet 38.

[0059] The oil-water separator 31 is connected to the condenser 35 and is used to separate the oil-liquid mixture into oil and water. The oil is pressurized by the high-pressure oil pump 32 and vaporized by the vaporizer 41 before being fed into the ejector 44 as a primary high-pressure fluid.

[0060] The oil-water separator 31 is also equipped with a drain outlet 30.

[0061] The heat exchange steam inlet 42 of the vaporizer 41 is connected to the heat exchange steam outlet of the cooler 11 to utilize the heat energy of the initial cooling process of the syngas as the heat source for vaporization; and the vaporizer 41 is also provided with a cooling water outlet 43 and a heat exchange steam inlet 42.

[0062] The heat exchanger 39 is connected to the pyrolysis non-condensable gas outlet 36 and the heat exchange steam outlet of the condenser 35. It is used to heat the non-condensable gas to a second set temperature (350°C or close to 350°C) using the heat exchange steam of the condenser 35 as a heat source, and input it to the ejector 44 as a secondary low-pressure fluid. The heat exchanger 39 is also provided with a condensate outlet 40.

[0063] The non-condensable gas from pyrolysis needs to be close in temperature to the vaporized pyrolysis oil in the primary high-pressure fluid after entering the ejector 44, otherwise it will affect the pressure after ejection. At this point, the vaporized temperature of the pyrolysis oil is approximately 350°C.

[0064] The ejector 44 is connected to the second feed pipe 45, the vaporizer 41 and the heat exchanger 39 respectively, and is used to drive the primary high-pressure fluid to enter the molten iron 9 of the molten pool gasifier 8 for further cracking and gasification.

[0065] Example 2

[0066] A method for producing syngas from organic solid waste using a molten iron bath with a pre-pyrolysis process, employing the aforementioned syngas-producing apparatus from organic solid waste using a molten iron bath with a pre-pyrolysis process, includes the following steps:

[0067] Material is added to the molten pool gasifier 8 through the first feed lock hopper 2 above the first feed pipe 7;

[0068] Close the first pneumatic valve 1 and the third pneumatic valve 5 on the first feed hopper 2, and turn on the first vacuum pump 4 to evacuate the first feed hopper 2 until the evacuation is complete.

[0069] Open the third pneumatic valve 5, and oxygen is introduced through the oxygen inlet 6 on the first feed pipe 7. The material is sent into the molten iron 9 for cracking and gasification to generate syngas.

[0070] Syngas is fed into cooler 11 through syngas outlet pipe 10 and cooled to 500°C. Syngas at 500°C is then fed into the hollow outer wall interlayer of rake pyrolysis machine 22 by first fan 14.

[0071] Close the fourth pneumatic valve 16 between the first hopper 15 and the second feed lock hopper 17 of the rake pyrolysis machine 22, open the seventh pneumatic valve 20 between the second feed lock hopper 17 and the feed inlet 21 of the rake pyrolysis machine 22, and turn on the second vacuum pump 18 to evacuate the second feed lock hopper 17 and the rake pyrolysis machine 22 until the evacuation is complete.

[0072] Close the seventh pneumatic valve 20, open the fourth pneumatic valve 16, feed through the second feed lock hopper 17, and start the rake pyrolysis machine 22;

[0073] Close the fourth pneumatic valve 16 and the seventh pneumatic valve 20, start the second vacuum pump 18 to evacuate the vacuum again until the evacuation is complete;

[0074] Open the seventh pneumatic valve 20 so that the vacuumed material can enter the rake pyrolysis machine 22 for pyrolysis, producing pyrolysis gas and pyrolysis semi-coke;

[0075] Pyrolysis gas is fed into condenser 35 through pyrolysis gas outlet 29, and pyrolysis semi-coke is discharged into second hopper 24 through pyrolysis semi-coke outlet 23. Pyrolysis semi-coke is then added into first feed lock hopper 2 through second hopper 24.

[0076] The pyrolysis gas is condensed by condenser 35 to form a mixture of non-condensable gas and oil. The non-condensable gas is fed into heat exchanger 39 through pyrolysis non-condensable gas outlet 36 and second fan 37 for heat exchange. The oil mixture enters oil-water separator 31 through liquid collection tank 33 between oil and water separators 31 for oil-water separation.

[0077] Heat exchanger 39 heats the 70°C non-condensable gas to about 350°C to serve as the secondary low-pressure fluid for ejector 44.

[0078] The oil-water separator 31 separates the oil mixture into oil and water. The oil is pressurized by the high-pressure oil pump 32 and then enters the vaporizer 41 for vaporization, so as to serve as a primary high-pressure fluid.

[0079] The ejector 44 causes the primary high-pressure fluid to carry the secondary low-pressure fluid into the molten iron 9 of the molten pool gasifier 8 for further cracking and gasification.

[0080] The parts of this invention not described in detail are prior art, therefore they are not described in detail here.

[0081] It is understood that the term "a" should be understood as "at least one" or "one or more", that is, in one embodiment, the number of an element can be one, while in another embodiment, the number of the element can be multiple, and the term "a" should not be understood as a limitation on the number.

[0082] Although this paper extensively uses the following components: first pneumatic valve 1, first feed hopper 2, second pneumatic valve 3, first vacuum pump 4, third pneumatic valve 5, oxygen inlet 6, first feed pipe 7, molten pool gasifier 8, molten iron 9, syngas outlet pipe 10, cooler 11, first cooling water inlet 12, first heat exchange steam outlet 13, first fan 14, first hopper 15, fourth pneumatic valve 16, second feed hopper 17, second vacuum pump 18, fifth pneumatic valve 19, seventh pneumatic valve 20, feed inlet 21, rake pyrolysis machine 22, pyrolysis semi-coke outlet 23, ... The terms 24, 25, 26, 27, 28, 29, 20, 30, 31, 32, 33, 34, 35, 36, 37, 38, 39, 30, 30, 31, 32, 33, 34, 35, 36, 37, 38, 39, 40, 41, 42, 43, 44, 45, 46, 46, etc., are used, but the possibility of using other terms is not excluded. These terms are used merely for the convenience of describing and explaining the essence of the invention; interpreting them as any additional limitation would be contrary to the spirit of the invention.

[0083] This invention is not limited to the preferred embodiments described above. Anyone can derive other products in various forms under the guidance of this invention. However, regardless of any changes made to their shape or structure, any technical solution that is the same as or similar to that of this application falls within the protection scope of this invention.

Claims

1. An organic solid waste molten iron bath syngas production device with pre-pyrolysis process, characterized in that, include: The molten pool gasifier is equipped with a first feed pipe, a second feed pipe, and a syngas outlet pipe, and contains molten iron inside, which is used to produce syngas from organic solid waste molten iron bath. A cooler, connected to the syngas outlet pipe, is used to cool the syngas to a first set temperature; A rake-type pyrolysis machine, connected to the cooler, is used to pyrolyze organic solid waste or water-containing oily sludge after initial crushing using syngas cooled to a first set temperature as a heat source to produce pyrolysis gas and pyrolysis semi-coke. A condenser, connected to the pyrolysis gas outlet of the rake pyrolysis machine, is used to condense the pyrolysis gas into a mixture of non-condensable gas and oil. An oil-water separator, connected to the condenser, is used to separate the oil-water mixture into oil and water. The oil is pressurized by a high-pressure oil pump and vaporized by a vaporizer before being fed into the ejector as a primary high-pressure fluid. The heat exchanger is connected to the pyrolysis non-condensable gas outlet and the heat exchange steam outlet of the condenser, and is used to heat the non-condensable gas to a second set temperature using the heat exchange steam of the condenser as a heat source, and input it into the ejector as a secondary low-pressure fluid. The ejector is connected to the second feed pipe, the vaporizer and the heat exchanger respectively, and is used to drive the secondary low-pressure fluid into the molten iron in the molten pool gasifier for re-cracking and gasification. The rake pyrolysis machine has a pyrolysis semi-coke outlet at its bottom. A blower and a second hopper or material conveyor are installed at the outlet to receive the pyrolysis semi-coke. After being discharged from the outlet, the pyrolysis semi-coke re-enters the first feed hopper of the molten pool gasifier for further pyrolysis and gasification. The cooler uses a first blower to input syngas at a first set temperature into the hollow outer wall interlayer of the rake pyrolysis machine as a heat source for the pyrolysis of organic solid waste or water-containing oil sludge. The condenser uses a second blower to input non-condensable gas into the heat exchanger for heat exchange.

2. The organic solid waste molten iron bath syngas production device with pre-pyrolysis process according to claim 1, characterized in that, The heat exchange steam inlet of the vaporizer is connected to the heat exchange steam outlet of the cooler, so as to utilize the heat energy of the initial cooling process of the syngas as the heat source for vaporization.

3. The organic solid waste molten iron bath syngas production device with pre-pyrolysis process according to claim 1, characterized in that, The first set temperature is 500℃.

4. The organic solid waste molten iron bath syngas production device with pre-pyrolysis process according to claim 1, characterized in that, The second set temperature is 350°C.

5. The organic solid waste molten iron bath syngas production device with pre-pyrolysis process according to claim 1, characterized in that, The size of the organic solid waste after initial crushing is 10 cm.

6. The organic solid waste molten iron bath syngas production device with pre-pyrolysis process according to claim 1, characterized in that, The rake pyrolysis machine is equipped with a second feed lock hopper at the feed inlet. The top of the second feed lock hopper is equipped with a first hopper. The side is evacuated by a second vacuum pump. Pneumatic valves are provided between the second feed lock hopper and the first hopper, as well as between the second feed lock hopper and the feed inlet.

7. A method for producing syngas from organic solid waste via a molten iron bath with a pre-pyrolysis process, characterized in that, The organic solid waste molten iron bath syngas production apparatus with pre-pyrolysis process as described in any one of claims 1-6 includes the following steps: Material is added to the molten pool gasifier through the first feed lock hopper above the first feed pipe; Close the first and third pneumatic valves on the first feed hopper, and turn on the first vacuum pump to evacuate the first feed hopper until the evacuation is complete. Open the third pneumatic valve and introduce oxygen through the oxygen inlet on the first feed pipe. The material is sent into the molten iron to be cracked and gasified to generate syngas. Syngas is fed into a cooler through a syngas outlet pipe and cooled to a first set temperature. Syngas at the first set temperature is then fed into the hollow outer wall interlayer of the rake pyrolysis machine by a first fan. Close the fourth pneumatic valve between the first hopper and the second feed lock hopper of the rake pyrolysis machine, open the seventh pneumatic valve between the second feed lock hopper and the feed inlet of the rake pyrolysis machine, and turn on the second vacuum pump to evacuate the second feed lock hopper and the rake pyrolysis machine until the evacuation is complete. Close the seventh pneumatic valve, open the fourth pneumatic valve, feed through the second feed hopper, and start the rake pyrolysis machine; Close the fourth and seventh pneumatic valves, start the second vacuum pump to evacuate again until the evacuation is complete; Open the seventh pneumatic valve so that the vacuumed material can enter the rake pyrolysis machine for pyrolysis, producing pyrolysis gas and pyrolysis semi-coke; Pyrolysis gas is fed into the condenser through the pyrolysis gas outlet, and pyrolysis semi-coke is discharged into the second hopper through the pyrolysis semi-coke outlet. Pyrolysis semi-coke is then added into the first feed lock hopper through the second hopper. The pyrolysis gas is condensed in the condenser to form a mixture of non-condensable gas and oil. The non-condensable gas is fed into the heat exchanger through the pyrolysis non-condensable gas outlet and the second fan for heat exchange. The oil mixture enters the oil-water separator through the liquid collection tank between the oil and water separators for oil-water separation. The heat exchanger heats the non-condensable gas to a second set temperature to serve as a secondary low-pressure fluid for the ejector. The oil-water separator separates the oil mixture into oil and water. After being pressurized by a high-pressure oil pump, the oil enters the vaporizer for vaporization, serving as a primary high-pressure fluid. The ejector causes the primary high-pressure fluid to push the secondary low-pressure fluid into the molten iron in the molten pool gasifier for further cracking and gasification.

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