Hydrogen production and suspension magnetization roasting coupling device and method

Abstract

The application discloses a hydrogen production and suspension magnetization roasting coupling device and method, which comprises a hydrogen production device, a suspension magnetization roasting device and a coupling connection assembly. The device generates reducing gas with carbon monoxide and hydrogen as effective components through oxidation reaction under pressurized non-catalytic conditions, so that hematite, limonite and siderite are converted into magnetite or maghemite which is strongly magnetic under the condition of reducing agent atmosphere, and then high-grade and high-recovery iron concentrate is obtained through magnetic separation, thereby realizing efficient utilization of resources. The process flow is short, load increase and decrease is convenient, operation flexibility is large, the hydrogen production system and the hydrogen-based mineral phase conversion system are highly fused and coupled, raw materials are wide, gas production is low in cost, low-carbon environmental protection, heat energy recycling rate is high, and the application scope is wide, and the like, thereby providing a new way for effective development and utilization of refractory ore resources.

Description

TECHNICAL FIELD

[0001] The present application relates to the field of chemical hydrogen production and metallurgical suspension magnetization roasting, in particular to a hydrogen production and suspension magnetization roasting coupling device and method. BACKGROUND

[0002] Suspension magnetization roasting technology is one of the most effective, most successful and best economic benefit magnetization roasting technologies for processing refractory iron ore resources. In recent years, suspension magnetization roasting technology has been applied in the processing of refractory powder iron ore, and the reaction mechanism of the technology is to use the reducing agent CO or H2 at a certain temperature to reduce the weak magnetic refractory iron oxide to generate strong magnetic magnetite. This technology can effectively exploit and utilize refractory ore resources, expand domestic iron ore reserves, effectively reduce dependence on imports, achieve resource self-sufficiency, realize low-cost deep processing of refractory ores, replace part of high-cost imported high-quality ores, and effectively reduce steel production costs. Through the suspension magnetization technology of mineral phase conversion, the refractory ore can be changed into a mineable ore, and the non-mineable ore can be changed into a mineable ore, which plays a crucial role in solving the strategic security of iron ore resources in China and has a broad market prospect. It is of great importance to ensure national resource security and sustainable economic development.

[0003] The reduction reaction of the currently used industrial suspension magnetization technology mainly uses CO as the reducing agent. The CO reducing agent is mainly obtained by two production methods, one of which is to produce coal gas through a coal gas generator to provide a reducing agent for the reduction reaction, and the other is to use the byproduct blast furnace gas of the blast furnace ironmaking in the metallurgical plant to provide a reducing agent for the reduction reaction system of the suspension magnetization roasting furnace. The above two cases have relatively large limitations, one of which is that the use of CO as the reducing agent will produce a large amount of CO2, resulting in greenhouse effect; the second is that due to environmental protection reasons, many places do not allow the construction of coal gas generators; and the third is that many refractory ore mining areas do not have supporting steel smelting and byproduct gas.

[0004] Therefore, it is necessary to provide a hydrogen production and suspension magnetization roasting coupling device and method to solve the above technical problems. SUMMARY

[0005] The present application aims at the deficiencies of the prior art, and provides a hydrogen production and suspension magnetization roasting coupling device and method, which uses hydrogen as a reducing agent, adjusts the reaction temperature, reaction concentration and reaction time, etc., realizes mineral phase conversion, has compact process flow, small land occupation, wide application range, safety and reliability, energy saving and environmental protection, and provides a new way for low-carbon and efficient utilization and green processing of refractory iron ore resources.

[0006] To achieve the above purpose, the technical scheme adopted by the present application is:

[0007] The application discloses a hydrogen production and suspension magnetization roasting coupling device, which comprises a hydrogen production device, a suspension magnetization roasting device and a coupling connection assembly, wherein the hydrogen production device comprises a conversion furnace, a boiler, a heat exchanger, a first heat exchanger, a second heat exchanger, an emergency shift reactor, an emergency cooler, a liquid separator, a water seal tank, a slurry tank, a slurry pump; the suspension magnetization roasting device comprises a reduction reaction fluidized bed, a cyclone dust collector, a suspension roasting main furnace, a cyclone heater, a cyclone preheater, a dust collector, an air induction fan, a chimney, a feeding system, a cooling system, a slurry tank, a slurry pump; the coupling connection assembly comprises a conversion furnace synthesis gas outlet assembly, a boiler synthesis gas outlet assembly, a boiler steam outlet assembly, a heat exchanger steam inlet assembly, a first heat exchanger steam inlet assembly, a second heat exchanger steam inlet assembly, an emergency shift cooling and emptying assembly, a reduction gas main pipeline assembly, a reduction gas branch pipeline assembly and a combustion gas pipeline assembly; the top of the conversion furnace is provided with a combustion chamber, the synthesis gas outlet at the bottom of the conversion furnace is communicated with the synthesis gas inlet of the boiler through the conversion furnace synthesis gas outlet assembly, the steam outlet of the boiler is respectively communicated with the steam inlet of the first heat exchanger, the steam inlet of the second heat exchanger and the steam inlet of the heat exchanger, the raw material gas outlet of the first heat exchanger is communicated with the raw material gas inlet of the combustion chamber of the conversion furnace, the compressed air outlet of the second heat exchanger is communicated with the compressed air inlet of the combustion chamber of the conversion furnace, the synthesis gas outlet of the boiler is respectively communicated with the combustion gas inlet of the suspension roasting main furnace and the reduction gas inlet of the reduction reaction fluidized bed, the discharge port of the reduction reaction fluidized bed is communicated with the feeding port of the cooling system through a one-way air lock valve, the discharge port of the cooling system is communicated with the slurry tank, the cooling system is provided with a cold air inlet pipe, the exhaust port of the reduction reaction fluidized bed is communicated with the air inlet port of the cyclone dust collector, the ash pipe at the bottom of the cyclone dust collector is communicated with the inside of the reduction reaction fluidized bed, the exhaust port of the cyclone dust collector is communicated with the air inlet port of the lower part of the suspension roasting main furnace, the main burner and the ignition burner are sequentially arranged below the air inlet port of the lower part of the suspension roasting main furnace, the flue gas outlet at the top of the suspension roasting main furnace is communicated with the flue gas inlet of the cyclone heater, the discharge pipe at the bottom of the cyclone heater is communicated with the feeding port of the reduction reaction fluidized bed through a material seal valve, the flue gas outlet of the cyclone heater is connected with the flue gas inlet of the cyclone preheater through an ascending flue, the discharge port of the feeding system is communicated with the ascending flue, the flue gas outlet of the cyclone preheater is communicated with the flue gas inlet of the dust collector, the flue gas outlet of the dust collector is communicated with the chimney through the air induction fan, and the discharge pipe at the bottom of the cyclone preheater is communicated with the feeding port of the suspension roasting main furnace.

[0008] Preferably, the combustion chamber at the top of the conversion furnace is communicated with a first nitrogen replacement pipeline, a long-lasting lamp is arranged in the combustion chamber, and the conversion furnace synthesis gas outlet assembly comprises a zirconia analyzer, a first pressure transmitter and a first temperature transmitter.

[0009] Preferably, a boiler steam outlet assembly is arranged on the pipeline communicating with the steam outlet of the boiler, the boiler steam outlet assembly comprising a second pressure transmitter and a second temperature transmitter; a boiler synthesis gas outlet assembly is arranged on the pipeline communicating with the synthesis gas outlet of the boiler, the boiler synthesis gas outlet assembly comprising a third pressure transmitter, a third temperature transmitter, an H2 and CO analyzer, a first hand valve and a first pressure regulating valve.

[0010] Preferably, a first heat exchanger steam inlet assembly is arranged on the pipeline communicating with the steam inlet of the first heat exchanger, the first heat exchanger steam inlet assembly comprising a second hand valve and a second pressure regulating valve; a third hand valve, a third pressure regulating valve and a fourth pressure transmitter are arranged on the pipeline communicating with the raw material gas inlet of the first heat exchanger; a fifth pressure transmitter, a fourth temperature transmitter and a first quick cut valve are arranged on the pipeline communicating with the raw material gas outlet of the first heat exchanger; a second nitrogen replacement pipeline is arranged between the third pressure regulating valve and the fourth pressure transmitter, and a fourth hand valve and a first gas valve are arranged on the second nitrogen replacement pipeline; the steam condensate outlet of the first heat exchanger is communicated with a slurry tank, and the outlet of the slurry tank is communicated with a slurry tank through a slurry pump.

[0011] Preferably, a second heat exchanger steam inlet assembly is arranged on the pipeline communicating with the steam inlet of the second heat exchanger, the second heat exchanger steam inlet assembly comprising a fifth hand valve and a fourth pressure regulating valve; a sixth hand valve, a fifth pressure regulating valve and a sixth pressure transmitter are arranged on the pipeline communicating with the compressed air inlet of the second heat exchanger; a seventh pressure transmitter, a fifth temperature transmitter and a second quick cut valve are arranged on the pipeline communicating with the compressed air outlet of the second heat exchanger; the steam condensate outlet of the second heat exchanger is communicated with a slurry tank, and the outlet of the slurry tank is communicated with a slurry tank through a slurry pump.

[0012] Preferably, a heat exchanger steam inlet assembly is arranged on the pipeline communicating with the steam inlet of the heat exchanger, the heat exchanger steam inlet assembly comprising a seventh hand valve and a sixth pressure regulating valve; the heat exchanger further comprises a cold air inlet pipeline and a warm air outlet pipeline, and the warm air outlet pipeline is respectively communicated with the pipeline of the bottom flue gas inlet of the suspension calcination main furnace and the rising flue; the steam condensate outlet of the heat exchanger is communicated with a slurry tank, and the outlet of the slurry tank is communicated with a slurry tank through a slurry pump.

[0013] Preferably, the boiler synthesis gas outlet is connected to a synthesis gas main pipeline, the emergency shift cooling and emptying assembly is connected to the synthesis gas main pipeline through an emergency shift cooling and emptying pipeline, and the eighth hand valve, the third quick cut valve, the first blind plate, the emergency shift reactor, the emergency cooler, the liquid separation tank, the eighth pressure transmitter, the water seal tank and the sixth temperature transmitter are sequentially arranged on the emergency shift cooling and emptying pipeline. The third nitrogen replacement pipeline is connected between the first blind plate and the third quick cut valve, and the ninth hand valve and the second gas valve are arranged on the third nitrogen replacement pipeline. The emergency cooler and the water seal tank are both provided with a water supplement pipeline. The water outlet of the emergency cooler, the liquid separation tank and the water seal tank is communicated with a water return main pipeline. The water return main pipeline is communicated with a slurry tank through a slurry pump.

[0014] Preferably, the synthesis gas outlet of the boiler is communicated with the combustion gas inlet of the suspension calcination main furnace through a combustion gas pipeline assembly. The combustion gas pipeline assembly comprises a combustion gas pipeline, and the tenth hand valve, the fourth quick cut valve, the second blind plate, the first orifice plate flowmeter, the ninth pressure transmitter, the seventh temperature transmitter and the seventh pressure regulating valve are arranged on the combustion gas pipeline. The fourth nitrogen replacement pipeline is connected between the fourth quick cut valve and the second blind plate, and the eleventh hand valve and the third gas valve are arranged on the fourth nitrogen replacement pipeline. The synthesis gas outlet of the boiler is connected to a reduction gas main pipeline assembly through a reduction gas main pipeline assembly, and then connected to the reduction gas inlet of the reduction reaction fluidized bed through a reduction gas branch pipeline assembly. The reduction gas main pipeline assembly comprises a reduction gas main pipeline, and the twelfth hand valve, the fifth quick cut valve, the third blind plate, the eighth pressure regulating valve, the second orifice plate flowmeter, the tenth pressure transmitter and the eighth temperature transmitter are arranged on the reduction gas main pipeline. The fifth nitrogen replacement pipeline is connected between the fifth quick cut valve and the third blind plate, and the thirteenth hand valve and the fourth gas valve are arranged on the fifth nitrogen replacement pipeline. The reduction gas branch pipeline assembly comprises a reduction gas branch pipeline, and the third orifice plate flowmeter and the sixth quick cut valve are arranged on the reduction gas branch pipeline.

[0015] Preferably, the reduction reaction fluidized bed is arranged from high to low from the feeding port to the discharging port. The eleventh pressure transmitter is arranged on the top of the reduction reaction fluidized bed. The ninth temperature transmitter is arranged in the reduction reaction fluidized bed. The flue gas O2 analyzer is arranged on the pipeline between the gas outlet of the reduction reaction fluidized bed and the gas inlet of the cyclone dust collector. The O2 analyzer and the regulating butterfly valve are arranged on the pipeline between the gas outlet of the cyclone dust collector and the lower gas inlet of the suspension calcination main furnace. 2、 The flue gas outlet of the top of the cooling system is communicated with the flue gas inlet of the bottom of the suspension calcination main furnace. The start-up burner is arranged on the pipeline connected to the flue gas outlet of the cooling system. The tenth temperature transmitter is arranged on the pipeline connected to the flue gas inlet of the suspension calcination main furnace. The eleventh temperature transmitter is arranged above the conical section of the suspension calcination main furnace.

[0016] A use method of a hydrogen production and suspension magnetization calcination coupling device, comprising the following steps:

[0017] S1, system start: first start the induced draft fan at a frequency of 12-18hz, then start the start-up burner at the outlet of the cooling system flue gas, and raise the temperature at a rate of 20-30℃ / min, when the inlet temperature of the suspension calcination main furnace bottom flue gas inlet reaches 350℃, start the ignition burner of the suspension calcination main furnace, control the temperature rise of the suspension calcination main furnace by adjusting the combustion adjusting valve of the main burner, when the top temperature in the suspension calcination main furnace is ≥550℃, the feeding requirement of the suspension calcination main furnace is reached, when the bottom temperature in the suspension calcination main furnace reaches 605℃, the start-up condition of the conversion furnace is reached;

[0018] S2, nitrogen replacement:

[0019] S21, fill fine particles in the one-way air lock valve and material seal valve, and confirm that the one-way air lock valve and material seal valve are sealed; confirm that the third hand valve and the third pressure regulating valve of the first heat exchanger raw material gas inlet are in the closed state, the first quick cut valve of the first heat exchanger raw material gas outlet is in the open state; confirm that the sixth hand valve and the fifth pressure regulating valve of the second heat exchanger compressed air inlet are in the closed state, the second quick cut valve of the second heat exchanger compressed air outlet is in the closed state; confirm that the water seal of the water seal box is sealed; open the first hand valve and the first pressure regulating valve, open the eighth hand valve, the third quick cut valve, and the first blind plate on the emergency change cooling emptying pipeline, open the tenth hand valve, the fourth quick cut valve, the second blind plate, and the seventh pressure regulating valve on the combustion gas pipeline, open the twelfth hand valve, the fifth quick cut valve, the third blind plate, and the eighth pressure regulating valve on the main pipeline of the reduction gas, open the sixth quick cut valve on the branch pipeline of the reduction gas, open the gas return valve of the reduction reaction fluidized bed, open the hand valve and the gas valve of the first nitrogen replacement pipeline on the top of the conversion furnace, open the fourth hand valve and the first gas valve of the second nitrogen replacement pipeline, and start nitrogen replacement of the pipelines and equipment of the entire coupling assembly;

[0020] S22, nitrogen enters the reduction reaction fluidized bed through the pipeline, and the bed top pressure of the reduction reaction fluidized bed is maintained at 0-3KPa by controlling the adjusting butterfly valve, until the O2 content detected by the O2, H2, and CO analyzers is lower than 0.5%, which is considered to be qualified for replacement; 2、 H2, CO analyzer detects O2 content lower than 0.5%, considered as replacement qualified;

[0021] S23, after 10 minutes of nitrogen replacement, simultaneously close the first quick cut valve, the first gas valve, the fourth quick cut valve, the seventh pressure regulating valve, the third quick cut valve, the adjusting butterfly valve, and the gas valve of the first nitrogen replacement pipeline;

[0022] S24, after the first time nitrogen replacement of the system is completed, continuous observation pipeline, the nitrogen pressure of the system, through the stage of opening, closing the thirteenth hand valve and the fourth gas valve on the fifth nitrogen replacement pipeline and the ninth hand valve and the second gas valve on the third nitrogen replacement pipeline, the suspension calcination main furnace, the reduction reaction fluidized bed and the emergency change cooling empty pipeline for nitrogen pressure, keep the nitrogen pressure at 0.3-3KPa, through the stage of opening, closing the hand valve and the gas valve on the first nitrogen replacement pipeline, the fourth hand valve and the first gas valve on the second nitrogen replacement pipeline and the eleventh hand valve and the third gas valve on the fourth nitrogen replacement pipeline, the conversion furnace, the boiler synthesis gas outlet connected pipeline, the combustion gas pipeline and the raw material gas import, export pipeline for nitrogen pressure, keep the nitrogen pressure at 3-20KPa;

[0023] S3, the conversion furnace starts: ignite the pilot light in the combustion chamber of the conversion furnace, open the zirconia analyzer of the conversion furnace synthesis gas outlet and put into the interlock, open the third hand valve of the raw material gas import of the first heat exchanger and the sixth hand valve of the compressed air import of the second heat exchanger, adjust the opening of the third pressure regulating valve of the raw material gas import of the first heat exchanger and the fifth pressure regulating valve of the compressed air import of the second heat exchanger, ignite the lance of the top combustion chamber of the conversion furnace, the conversion furnace starts to produce synthesis gas;

[0024] S4, heat exchange: the synthesis gas in the conversion furnace with the temperature of 1000-1300℃ is sent to the boiler through the conversion furnace synthesis gas outlet assembly, and is indirectly heated with the desalted cooling water fed into the boiler, and is sent to the direction of the suspension magnetization roasting device after being cooled to 400-550℃. The high temperature steam produced by the boiler with the temperature of 400-500℃ is respectively sent to the first heat exchanger, the second heat exchanger and the heat exchanger, and is used for indirectly preheating the raw material gas and the compressed air, so that the preheating temperature of the raw material gas and the compressed air reaches 200-350℃. The high temperature steam is indirectly heated with the cold air through the heat exchanger to produce warm air with the temperature of 150-300℃. The warm air is connected with the pipeline of the flue gas import of the suspension calcination main furnace bottom and the rising flue through the warm air outlet pipeline respectively. The condensed liquid of the heated steam is discharged into the slurry pool and is sent to the slurry tank through the slurry pump as the auxiliary water for the slurry preparation of the slurry tank;

[0025] S5, the use of synthesis gas: the synthesis gas produced by the conversion furnace is sent into the reduction reaction fluidized bed through the pipeline as the gas for the reduction reaction mineral phase conversion and the fluidization of the fluidized bed. The gas production of the synthesis gas is adjusted by controlling the gas import of the raw material gas and the compressed air into the conversion furnace. For the reduction reaction fluidized bed, whether it is empty bed feeding or full bed feeding, it needs to be operated to accumulate gas to ensure that the cross section fluidization velocity of the reduction reaction fluidized bed meets the fluidization requirements, and the cross section fluidization velocity is controlled at 0.10-0.15m.s -1, the converter produces synthesis gas through the combustion gas pipeline into the suspension calcination main furnace combustion, to provide heating for the suspension calcination main furnace, and according to the gas accumulation amount of the reduction reaction fluidized bed, the combustion gas supply of the suspension calcination main furnace main burner is reduced synchronously, when the combustion gas amount accumulates to the flow state gas amount required by the reducing gas, the supply of combustion gas to the suspension calcination furnace is stopped quickly, the withdrawn combustion gas is fed into the reduction reaction fluidized bed as the fluidized bed reduction and flow state gas, in order to ensure the flow state of the reduction reaction fluidized bed and the normal discharge of the bed, the wind cap hole disturbance wind speed of the reduction reaction fluidized bed is controlled at 50-90m / s -1 , the reduction gas inlet pressure of the reduction reaction fluidized bed is controlled at 50-100KPa, in order to ensure the safety of the system and the quality of the calcined sand product, the bed pressure of the reduction reaction fluidized bed is controlled at 0-3KPa, the reducing agent concentration of the reduction reaction is controlled at 25%-55%, the reaction time is controlled at 25-50min, and the reduction reaction temperature is controlled at 500-600℃;

[0026] S6, gas stopping operation:

[0027] S61, reduction reaction fluidized bed gas withdrawal:

[0028] S611, planned gas withdrawal: reduce the combustion load of the converter, open the tenth hand valve, the fourth quick cut valve, the second blind plate and the seventh pressure regulating valve on the combustion gas pipeline, adjust the inlet amount of combustion gas by adjusting the seventh pressure regulating valve, and send low load synthesis gas to the suspension calcination main furnace through the combustion gas pipeline for combustion;

[0029] S612, emergency gas withdrawal: quickly cut off the reduction gas source, and send synthesis gas through the combustion gas pipeline to the suspension calcination main furnace for combustion;

[0030] S62, suspension calcination main furnace ignition burner shutdown: cut off the fifth quick cut valve of the reduction gas main pipeline and the fourth quick cut valve of the combustion gas pipeline, and synchronously interlock and automatically open the third gas closing valve of the fourth nitrogen replacement pipeline and the first gas closing valve of the second nitrogen replacement pipeline for nitrogen blowing replacement of the reduction gas main pipeline and the combustion gas pipeline; synchronously close the first quick cut valve of the first heat exchanger raw material gas outlet and the second quick cut valve of the second heat exchanger compressed air outlet, and the gas closing valve of the first nitrogen replacement pipeline at the top of the converter is interlocked and automatically opened for nitrogen blowing replacement of the converter and its synthesis gas pipeline; the mixed gas of the blowing nitrogen and synthesis gas is treated by emergency shift cooling and then discharged into the atmosphere through the emptying pipe;

[0031] S63, converter shutdown: the first quick cut valve of the first heat exchanger raw material gas outlet and the second quick cut valve of the second heat exchanger compressed air outlet are interlocked and closed, and the gas closing valve of the first nitrogen replacement pipeline at the top of the converter is interlocked and automatically opened for nitrogen blowing replacement of the converter, the reduction gas main pipeline, the reduction gas branch pipeline and the reduction reaction fluidized bed.

[0032] Compared with the prior art, the present application has the following advantages:

[0033] 1. The present application provides a hydrogen production and suspension magnetization roasting coupling device and method, which can convert hematite, limonite and siderite into magnetite or maghemite under the condition of a reducing agent atmosphere, and then obtain high-grade and high-recovery iron concentrate through magnetic separation, thereby realizing efficient utilization of resources.

[0034] 2. The hydrogen production and suspension magnetization roasting coupling device and method provided by the present application have the advantages of low carbon environmental protection, high mass and heat transfer efficiency, low reduction temperature, and uniform product quality, and the energy consumption is 0.9-1.2 GJ / t, which is more than 20% lower than the energy consumption per ton of concentrate in conventional roasting.

[0035] 3. Compared with traditional beneficiation technology, the present application can increase the iron grade by 5-10 percentage points and the iron recovery rate by 10-30 percentage points, and the production index is more excellent. When the grade of iron concentrate powder entering the furnace is increased by 1 percentage point, about 20 kg of carbon dioxide emission can be reduced in the ironmaking process. The economic value of the product can be significantly improved, and the carbon emission in the downstream metallurgical industry can be reduced.

[0036] 4. The present application uses oxidation reaction internal heat to carry out hydrocarbon steam conversion reaction, without external heating, high thermal efficiency, and the combustion reactants are the conversion reaction raw materials, without the need for steam addition and carbon supplement, without the need for desulfurization and oil removal before conversion, without the limitation of carbon deposition, and without catalyst deactivation problems.

[0037] 5. The present application can simultaneously treat various gaseous (liquid) hydrocarbons and other organic matters, and the raw materials do not need to be refined.

[0038] 6. The present application has a synthesis gas H2 / CO ratio in the range of 0.9-2.2, high conversion rate, and better gas components than traditional conversion technology, which is suitable for the hydrogen-carbon ratio of raw gas required for various synthesis reactions, and has low hydrogen-carbon ratio adjustment cost and low gas production cost.

[0039] 7. The present application produces high-quality steam as a byproduct of the conversion reaction, and the heat recovery efficiency of the high-temperature heat recovery system is high, the heat recovery is sufficient, the heat energy utilization rate is high, and the energy is used efficiently.

[0040] 8. The process flow and equipment structure of the present application are simple, reliable and safe, and have great advantages in the conversion efficiency of hydrocarbon organic matter and other aspects, and are outstanding in device large-scale and small-scale synthesis gas production, load increase and decrease, and operation flexibility.

[0041] 9. The present application can simultaneously treat various gaseous hydrocarbons and liquid hydrocarbons, and the raw materials are flexible, and the multi-organic matter can generate synthesis gas: H2+CO, which can be applied to natural gas, coke oven gas, raw coal gas, hydrocarbon-containing tail gas, organic waste liquid and other clean and high-value utilization.

[0042] 10. The reformer pressure adaptation range of the present application is wide, and can reach 7 MPa at the highest, which can match the subsequent reduction pressure needs.

[0043] 11. The process flow and equipment structure of the present application are simple, the hydrogen production system and the hydrogen-based mineral phase conversion system are highly coupled and fused, the flow is short, the investment is low, no catalyst needs to be replaced, and long-period stable operation can be realized. BRIEF DESCRIPTION OF DRAWINGS

[0044] Figure 1 is a structural schematic diagram of a hydrogen production and suspension magnetization roasting coupling device of the present application;

[0045] Wherein, 1 - converter, 2 - boiler, 3 - heat exchanger, 4 - first heat exchanger, 5 - second heat exchanger, 6 - emergency shift reactor, 7 - emergency cooler, 8 - liquid separation tank, 9 - water seal tank, 10 - slurry tank, 11 - slurry pump, 12 - reduction reaction fluidized bed, 13 - cyclone dust collector, 14 - suspension calcination main furnace, 15 - cyclone heater, 16 - cyclone heater, 17 - dust collector, 18 - induced draft fan, 19 - chimney, 20 - feeding system, 21 - cooling system, 22 - slurry tank, 23 - slurry pump, 24 - combustion chamber, 25 - first nitrogen replacement pipeline, 26 - long light, 27 - zirconium oxide analyzer, 28 - first pressure transmitter, 29 - first temperature transmitter, 30 - second pressure transmitter, 31 - second temperature transmitter, 32 - third pressure transmitter, 33 - third temperature transmitter, 34 - H2 and CO analyzer, 35 - first hand valve, 36 - first pressure regulating valve, 37 - second hand valve, 38 - second pressure regulating valve, 39 - third hand valve, 40 - third pressure regulating valve, 41 - fourth pressure transmitter, 42 - fifth pressure transmitter, 43 - fourth temperature transmitter, 44 - first quick cut valve, 45 - second nitrogen replacement pipeline, 46 - fourth hand valve, 47 - first gas valve, 48 - fifth hand valve, 49 - fourth pressure regulating valve, 50 - sixth hand valve, 51 - fifth pressure regulating valve, 52 - sixth pressure transmitter, 53 - seventh pressure transmitter, 54 - fifth temperature transmitter, 55 - second quick cut valve, 56 - seventh hand valve, 57 - sixth pressure regulating valve, 58 - cold air inlet pipeline, 59 - warm air outlet pipeline, 60 - updraft flue, 61 - synthesis gas main pipeline, 62 - emergency shift cooling emptying pipeline, 63 - combustion gas inlet, 64 - eighth hand valve, 65 - third quick cut valve, 66 - first blind plate, 67 - eighth pressure transmitter, 68 - sixth temperature transmitter, 69 - third nitrogen replacement pipeline, 70 - ninth hand valve, 71 - second gas valve, 72 - water return main pipe, 73 - combustion gas pipeline, 74 - tenth hand valve, 75 - fourth quick cut valve, 76 - second blind plate, 77 - first orifice flowmeter, 78 - ninth pressure transmitter, 79 - seventh temperature transmitter, 80 - seventh pressure regulating valve, 81 - fourth nitrogen replacement pipeline, 82 - eleventh hand valve, 83 - third gas valve, 84 - reduction gas main pipeline, 85 - twelfth hand valve, 86 - fifth quick cut valve, 87 - third blind plate, 88 - eighth pressure regulating valve, 89 - second orifice flowmeter, 90 - tenth pressure transmitter, 91 - eighth temperature transmitter, 92 - fifth nitrogen replacement pipeline, 93 - thirteenth hand valve, 94 - fourth gas valve, 95 - reduction gas branch pipeline, 96 - third orifice flowmeter, 97 - sixth quick cut valve, 98 - eleventh pressure transmitter, 99 - ninth temperature transmitter, 100 - flue gas O2 analyzer, 101 - ash pipe, 102 - O 2、H2, CO analyzer, 103 - regulating butterfly valve, 104 - one-way lock valve, 105 - starting burner, 106 - cold gas inlet pipe, 107 - tenth temperature transmitter, 108 - eleventh temperature transmitter, 109 - main burner, 110 - ignition burner, 111 - material seal valve DETAILED DESCRIPTION

[0046] The present application is further illustrated by the following description and examples with reference to the accompanying drawings, in which the embodiments merely for illustrating the present application and are not used to limit the scope of the present application, and various modifications of the present application made by one skilled in the art after reading the present application fall within the scope defined by the appended claims.

[0047] In the present application, unless otherwise explicitly specified and limited, the terms "mounting", "setting", "connecting", "fixing" and the like should be understood in a broad sense, for example, can be fixed connection, can also be detachable connection, or integrated; can be mechanical connection, can also be electrical connection; can be directly connected, can also be indirectly connected through an intermediate medium, can be the internal communication of two elements or the interaction relationship of two elements, unless otherwise explicitly limited, the above-mentioned terms in the present application can be understood according to the specific meaning in the present application by the person skilled in the art.

[0048] In the present application, the terms such as "upper", "lower", "bottom", "top" and the like indicate the orientation or positional relationship based on the orientation or positional relationship shown in the drawings, which is only a relationship word determined for the purpose of describing the structural relationship of the components or elements of the present application, and cannot be understood as a limitation of the present application.

[0049] As shown in Figure 1 A hydrogen production and suspension magnetization roasting coupling device, which comprises a hydrogen production device, a suspension magnetization roasting device and a coupling connection assembly. The hydrogen production device comprises a conversion furnace 1, a boiler 2, a heat exchanger 3, a first heat exchanger 4, a second heat exchanger 5, an emergency shift reactor 6, an emergency cooler 7, a liquid separation tank 8, a water seal tank 9, a slurry tank 10, a slurry pump 11. The suspension magnetization roasting device comprises a reduction reaction fluidized bed 12, a cyclone dust collector 13, a suspension roasting main furnace 14, a cyclone heater 15, a cyclone preheater 16, a dust collector 17, an induced draft fan 18, a chimney 19, a feeding system 20, a cooling system 21, a slurry tank 22, a slurry pump 23. The coupling connection assembly comprises a conversion furnace synthesis gas outlet assembly, a boiler synthesis gas outlet assembly, a boiler steam outlet assembly, a heat exchanger steam inlet assembly, a first heat exchanger steam inlet assembly, a second heat exchanger steam inlet assembly, an emergency shift cooling and emptying assembly, a reduction gas main pipeline assembly, a reduction gas branch pipeline assembly, a combustion gas pipeline assembly.

[0050] The top of the reformer 1 is provided with a combustion chamber 24, the combustion chamber at the top of the reformer is communicated with a first nitrogen replacement pipeline 25, a long-lasting lamp 26 is arranged in the combustion chamber, a syngas outlet at the bottom of the reformer is communicated with a syngas inlet of the boiler through a reformer syngas outlet assembly, the reformer syngas outlet assembly comprises a zirconia analyzer 27, a first pressure transmitter 28 and a first temperature transmitter 29;

[0051] A steam outlet of the boiler is communicated with a steam inlet of the first heat exchanger, a steam inlet of the second heat exchanger and a steam inlet of the heat exchanger through a boiler steam outlet assembly respectively, the boiler steam outlet assembly comprises a second pressure transmitter 30 and a second temperature transmitter 31, a boiler syngas outlet assembly is arranged on a syngas main pipeline communicated with the syngas outlet of the boiler, the boiler syngas outlet assembly comprises a third pressure transmitter 32, a third temperature transmitter 33, an H2 and CO analyzer 34, a first hand valve 35 and a first pressure regulating valve 36;

[0052] A first heat exchanger steam inlet assembly is arranged on a pipeline communicated with the steam inlet of the first heat exchanger, the first heat exchanger steam inlet assembly comprises a second hand valve 37 and a second pressure regulating valve 38, a third hand valve 39, a third pressure regulating valve 40 and a fourth pressure transmitter 41 are arranged on a pipeline communicated with a raw material gas inlet of the first heat exchanger, a fifth pressure transmitter 42, a fourth temperature transmitter 43 and a first quick cut valve 44 are arranged on a pipeline communicated with a raw material gas outlet of the first heat exchanger, the raw material gas outlet of the first heat exchanger is communicated with a raw material gas inlet of the combustion chamber of the reformer, a second nitrogen replacement pipeline 45 is communicated between the third pressure regulating valve and the fourth pressure transmitter, a fourth hand valve 46 and a first gas valve 47 are arranged on the second nitrogen replacement pipeline, a steam condensate outlet of the first heat exchanger is communicated with a slurry tank, an outlet of the slurry tank is communicated with a slurry tank through a slurry pump;

[0053] A second heat exchanger steam inlet assembly is arranged on a pipeline communicated with the steam inlet of the second heat exchanger, the second heat exchanger steam inlet assembly comprises a fifth hand valve 48 and a fourth pressure regulating valve 49, a sixth hand valve 50, a fifth pressure regulating valve 51 and a sixth pressure transmitter 52 are arranged on a pipeline communicated with a compressed air inlet of the second heat exchanger, a seventh pressure transmitter 53, a fifth temperature transmitter 54 and a second quick cut valve 55 are arranged on a pipeline communicated with a compressed air outlet of the second heat exchanger, the compressed air outlet of the second heat exchanger is communicated with a compressed air inlet of the combustion chamber of the reformer, a steam condensate outlet of the second heat exchanger is communicated with a slurry tank, an outlet of the slurry tank is communicated with a slurry tank through a slurry pump;

[0054] A pipe communicating with the steam inlet of the heat exchanger is provided with a heat exchanger steam inlet assembly, which comprises a seventh hand valve 56 and a sixth pressure regulating valve 57. The heat exchanger is also provided with a cold air inlet pipe 58 and a warm air outlet pipe 59, which respectively communicate with a pipe of the flue gas inlet at the bottom of the suspension calcination main furnace and an ascending flue 60. The steam condensate outlet of the heat exchanger communicates with a slurry tank, and the outlet of the slurry tank communicates with a slurry tank through a slurry pump;

[0055] The boiler synthesis gas outlet is connected with a synthesis gas main pipe 61, which respectively communicates with an emergency shift cooling and emptying pipe 62, a combustion gas inlet 63 of the suspension calcination main furnace and a reducing gas inlet of the reduction reaction fluidized bed.

[0056] The emergency shift cooling and emptying assembly is connected with the synthesis gas main pipe through the emergency shift cooling and emptying pipe, which is sequentially provided with an eighth hand valve 64, a third quick cut valve 65, a first blind plate 66, an emergency shift reactor 6, an emergency cooler 7, a liquid separation tank 8, an eighth pressure transmitter 67, a water seal tank 9 and a sixth temperature transmitter 68. A third nitrogen replacement pipe 69 is connected between the first blind plate and the third quick cut valve, and the third nitrogen replacement pipe is provided with a ninth hand valve 70 and a second gas shut-off valve 71. The emergency cooler and the water seal tank are both provided with a water supply pipe. The water outlets of the emergency cooler, the liquid separation tank and the water seal tank communicate with a water return main pipe 72, and the outlet of the water return main pipe communicates with a slurry tank. The outlet of the slurry tank communicates with a slurry tank through a slurry pump.

[0057] The synthesis gas main pipe is connected with the combustion gas inlet of the suspension calcination main furnace through a combustion gas pipe assembly, which comprises a combustion gas pipe 73, which is provided with a tenth hand valve 74, a fourth quick cut valve 75, a second blind plate 76, a first orifice plate flowmeter 77, a ninth pressure transmitter 78, a seventh temperature transmitter 79 and a seventh pressure regulating valve 80. A fourth nitrogen replacement pipe 81 is connected between the fourth quick cut valve and the second blind plate, and the fourth nitrogen replacement pipe is provided with an eleventh hand valve 82 and a third gas shut-off valve 83.

[0058] The synthesis gas main pipe is connected with the reducing gas branch pipe assembly through a reducing gas main pipe assembly, and is connected with the reducing gas inlet of the reduction reaction fluidized bed through the reducing gas branch pipe assembly. The reducing gas main pipe assembly comprises a reducing gas main pipe 84, which is provided with a twelfth hand valve 85, a fifth quick cut valve 86, a third blind plate 87, an eighth pressure regulating valve 88, a second orifice plate flowmeter 89, a tenth pressure transmitter 90 and an eighth temperature transmitter 91. A fifth nitrogen replacement pipe 92 is connected between the fifth quick cut valve and the third blind plate, and the fifth nitrogen replacement pipe is provided with a thirteenth hand valve 93 and a fourth gas shut-off valve 94. The reducing gas branch pipe assembly comprises a reducing gas branch pipe 95, which is provided with a third orifice plate flowmeter 96 and a sixth quick cut valve 97.

[0059] The reducing reaction fluidized bed is arranged from high to low in the feeding port to the discharging port, and the inclination slope is 4°. The top of the reducing reaction fluidized bed is provided with the eleventh pressure transmitter 98. The inside of the reducing reaction fluidized bed is provided with the ninth temperature transmitter 99. The exhaust port of the reducing reaction fluidized bed is communicated with the air inlet of the cyclone dust collector. The pipeline between the exhaust port of the reducing reaction fluidized bed and the air inlet of the cyclone dust collector is provided with the outlet flue gas O2 analyzer 100. The ash pipe 101 at the bottom of the cyclone dust collector is communicated with the fifth air chamber in the reducing reaction fluidized bed. The exhaust port of the cyclone dust collector is communicated with the air inlet of the lower part of the suspension roasting main furnace. The pipeline between the exhaust port of the cyclone dust collector and the air inlet of the lower part of the suspension roasting main furnace is provided with the O 2、 H2, CO analyzer 102 and regulating butterfly valve 103. The discharging port of the reducing reaction fluidized bed is communicated with the feeding port of the cooling system through the one-way air lock valve 104.

[0060] The flue gas outlet at the top of the cooling system is communicated with the flue gas inlet at the bottom of the suspension roasting main furnace. The pipeline connected with the flue gas outlet of the cooling system is provided with the start-up burner 105. The discharging port of the cooling system is communicated with the slurry tank. The cooling system is provided with the cold air inlet pipe 106.

[0061] The pipeline connected with the flue gas inlet of the suspension roasting main furnace is provided with the tenth temperature transmitter 107. The upper part of the suspension roasting main furnace is provided with the eleventh temperature transmitter 108. The lower part of the air inlet of the suspension roasting main furnace is sequentially provided with the main burner 109 and the ignition burner 110. The flue gas outlet at the top of the suspension roasting main furnace is communicated with the flue gas inlet of the cyclone heater. The ash pipe at the bottom of the cyclone heater is communicated with the feeding port of the reducing reaction fluidized bed through the material seal valve 111. The flue gas outlet of the cyclone heater is connected with the flue gas inlet of the cyclone preheater through the rising flue. The discharging port of the feeding system is communicated with the rising flue. The flue gas outlet of the cyclone preheater is communicated with the flue gas inlet of the dust remover. The flue gas outlet of the dust remover is communicated with the chimney through the induced draft fan. The ash pipe at the bottom of the cyclone preheater is communicated with the feeding port of the suspension roasting main furnace.

[0062] A use method of a hydrogen production and suspension magnetization roasting coupling device, comprising the following steps:

[0063] S1, system start-up: first, start the induced draft fan at a frequency of 15 hz, then start the start-up burner at the flue gas outlet of the cooling system, and heat at a rate of 24 ℃ / min. When the inlet temperature of the flue gas inlet at the bottom of the suspension roasting main furnace reaches 350 ℃, start the ignition burner of the suspension roasting main furnace. Control the temperature rise of the suspension roasting main furnace by adjusting the combustion adjusting valve of the main burner. When the top temperature in the suspension roasting main furnace is ≥550 ℃, the feeding requirement of the suspension roasting main furnace is reached. When the bottom temperature in the suspension roasting main furnace reaches 605 ℃, the start-up condition of the conversion furnace is reached.

[0064] S2, nitrogen replacement:

[0065] S21, fill the fine particle material into the one-way air lock valve and the material seal valve, and confirm that the one-way air lock valve and the material seal valve are sealed; confirm that the third hand valve and the third pressure regulating valve at the raw material gas inlet of the first heat exchanger are in the closed state, the first quick cut valve at the raw material gas outlet of the first heat exchanger is in the open state; confirm that the sixth hand valve and the fifth pressure regulating valve at the compressed air inlet of the second heat exchanger are in the closed state, the second quick cut valve at the compressed air outlet of the second heat exchanger is in the closed state; confirm that the water seal of the water seal box is sealed; open the first hand valve and the first pressure regulating valve, open the eighth hand valve, the third quick cut valve and the first blind plate on the emergency shift cooling and emptying pipeline, open the tenth hand valve, the fourth quick cut valve, the second blind plate and the seventh pressure regulating valve on the combustion gas pipeline, open the twelfth hand valve, the fifth quick cut valve, the third blind plate and the eighth pressure regulating valve on the reducing gas main pipeline, open the sixth quick cut valve on the reducing gas branch pipeline, open the gas return valve of the reduction reaction fluidized bed, open the hand valve and the gas valve on the first nitrogen displacement pipeline at the top of the conversion furnace, open the fourth hand valve and the first gas valve on the second nitrogen displacement pipeline, and start nitrogen displacement of the pipelines and equipment of the entire coupling assembly;

[0066] S22, nitrogen enters the reduction reaction fluidized bed through the pipeline, and the bed top pressure of the reduction reaction fluidized bed is maintained at 2 KPa by controlling the regulating butterfly valve until the O2 analyzer and the O 2、 H2, CO analyzer detects that the O2 content is lower than 0.5%, which is considered to be qualified for displacement;

[0067] S23, after 10 minutes of nitrogen displacement, the first quick cut valve, the first gas valve, the fourth quick cut valve, the seventh pressure regulating valve, the third quick cut valve, the regulating butterfly valve and the gas valve on the first nitrogen displacement pipeline are closed synchronously;

[0068] S24, after the first nitrogen displacement of the system is completed, the nitrogen pressure maintaining of the pipelines and the system is continuously observed, the thirteenth hand valve and the fourth gas valve on the fifth nitrogen displacement pipeline and the ninth hand valve and the second gas valve on the third nitrogen displacement pipeline are opened and closed in stages to maintain the nitrogen pressure at 2.5 KPa, the hand valve and the gas valve on the first nitrogen displacement pipeline, the fourth hand valve and the first gas valve on the second nitrogen displacement pipeline and the eleventh hand valve and the third gas valve on the fourth nitrogen displacement pipeline are opened and closed in stages to maintain the nitrogen pressure at 15 KPa, and the pipelines connected with the conversion furnace and the boiler synthesis gas outlet, the combustion gas pipeline and the pipelines connected with the raw material gas inlet and outlet are nitrogen pressure maintained;

[0069] S3, start-up of the reformer: ignite the pilot light in the combustion chamber of the reformer, open the zirconia analyzer of the reformer syngas outlet and put into interlock, open the third hand valve of the raw material gas inlet of the first heat exchanger and the sixth hand valve of the compressed air inlet of the second heat exchanger, adjust the opening of the third pressure regulating valve of the raw material gas inlet of the first heat exchanger and the fifth pressure regulating valve of the compressed air inlet of the second heat exchanger, ignite the lance of the combustion chamber at the top of the reformer, and the reformer starts to produce syngas;

[0070] The main chemical equations for generating syngas are:

[0071] CH4+2O2=CO2+2H2O+Q

[0072] CH4+CO2=2H2+2CO-Q

[0073] CH4+H2O=3H2+CO-Q

[0074] Wherein, "+Q" represents an endothermic reaction, and "-Q" represents an exothermic reaction;

[0075] S4, heat exchange: the syngas in the reformer with a temperature of 1000-1300℃ is sent to the boiler through the reformer syngas outlet assembly, and is indirectly heated with the desalted cooling water supplied to the boiler, and then is sent to the direction of the suspension magnetization roasting device after being cooled to 450℃. The 400℃ high-temperature steam generated by the boiler is respectively sent to the first heat exchanger, the second heat exchanger and the heat exchanger, and is used for indirectly preheating the raw material gas and the compressed air, so that the preheating temperature of the raw material gas and the compressed air reaches 200-350℃. The high-temperature steam is indirectly heated with the cold air through the heat exchanger to generate 200℃ warm air. The warm air is respectively connected to the pipeline of the flue gas inlet at the bottom of the suspension roasting main furnace and the rising flue through the warm air outlet pipeline. The condensed steam after heat exchange is discharged into the slurry pool and is sent to the slurry tank through the slurry pump as auxiliary make-up water for slurry preparation of the slurry tank;

[0076] S5, use of syngas: the syngas produced by the reformer is sent to the reduction reaction fluidized bed through the pipeline as the gas for reduction reaction mineral phase conversion and fluidization of the fluidized bed. The production of syngas is adjusted by controlling the gas inlet amount of the raw material gas and the compressed air into the reformer. For the reduction reaction fluidized bed, whether it is empty bed feeding or full bed feeding, gas accumulation operation is needed to ensure that the cross-sectional fluidization velocity of the reduction reaction fluidized bed meets the fluidization requirements, and the cross-sectional fluidization velocity is controlled at 0.12m.s -1, during the gas accumulation period, the synthesis gas produced by the converter is sent to the suspension calcination main furnace through the combustion gas pipeline to provide heating heat for the suspension calcination main furnace, and according to the gas accumulation amount of the reduction reaction fluidized bed, the combustion gas supply of the suspension calcination main furnace main burner is reduced synchronously, when the combustion gas amount accumulates to meet the fluidization gas amount required by the reducing gas, the supply of combustion gas to the suspension calcination furnace is stopped quickly, the withdrawn combustion gas is fed into the reduction reaction fluidized bed as the fluidized bed reduction and fluidization gas, in order to ensure the fluidization of the reduction reaction fluidized bed and the normal discharge of the bed layer, the disturbance wind speed of the air cap hole of the reduction reaction fluidized bed is controlled at 70m / s -1 The reduction gas inlet pressure of the reduction reaction fluidized bed is controlled at 50-100KPa, in order to ensure the safety of the system and the quality of the calcined sand product, the bed layer pressure of the reduction reaction fluidized bed is controlled at 2KPa, the reduction agent concentration of the reduction reaction is controlled at 45%, the reaction time is controlled at 40min, and the reduction reaction temperature is controlled at 550℃;

[0077] S6, gas stopping operation:

[0078] S61, reduction reaction fluidized bed gas withdrawal:

[0079] S611, planned gas withdrawal: when the reduction reaction fluidized bed needs to be operated due to process needs, the reduction gas in the reduction reaction fluidized bed is gradually withdrawn, and the combustion load of the converter is reduced to make the converter run at low load, the nitrogen blowing of the combustion gas pipeline is completed synchronously, and the tenth hand valve, the fourth quick cut valve, the second blind plate and the seventh pressure regulating valve on the combustion gas pipeline are opened. Adjust the seventh pressure regulating valve to adjust the inlet amount of combustion gas, and send the low-load synthesis gas to the suspension calcination main furnace through the combustion gas pipeline for combustion;

[0080] S612, emergency gas withdrawal: when the reduction reaction fluidized bed needs to be shut down due to emergency reasons, the sixth quick cut valve is cut off, the reduction gas source is quickly cut off, and the synthesis gas is transported to the suspension calcination main furnace through the combustion gas pipeline for combustion;

[0081] S62, the suspension calcination main furnace ignition burner stops: the calcination furnace system stops because of the induced draft fan, power, compressed air, nitrogen, natural gas, flame detection, valve state, reducing gas pressure, flue gas combustible gas detection, oxygen detection, flue gas temperature interlock, trigger the suspension calcination main furnace stop, or trigger the suspension calcination main furnace interlock stop under the condition of ignition burner failure. Under the above conditions, the fifth quick cut valve of the reducing gas main pipeline and the fourth quick cut valve of the combustion gas pipeline will be cut off because of the interlock, the third gas shut-off valve of the fourth nitrogen replacement pipeline and the first gas shut-off valve of the second nitrogen replacement pipeline are synchronously interlocked and automatically opened, and the reducing gas main pipeline and the combustion gas pipeline are nitrogen purged and replaced; the first quick cut valve of the first heat exchanger raw material gas outlet and the second quick cut valve of the second heat exchanger compressed air outlet are synchronously closed, and the gas shut-off valve of the first nitrogen replacement pipeline at the top of the converter is interlocked and automatically opened, and the converter and its synthesis gas pipeline are nitrogen purged and replaced, and the mixed gas of the purged nitrogen and the synthesis gas is treated by emergency shift cooling and then discharged into the atmosphere through the emptying pipe;

[0082] S63, the converter stops: the converter stops because of the long-lasting light failure or the O2 content of the pipeline connected to the converter synthesis gas outlet exceeds the standard, the first quick cut valve of the first heat exchanger raw material gas outlet and the second quick cut valve of the second heat exchanger compressed air outlet are interlocked and closed by the converter, and the gas shut-off valve of the first nitrogen replacement pipeline at the top of the converter is interlocked and automatically opened, and the converter, the reducing gas main pipeline, the reducing gas branch pipeline and the reducing reaction fluidized bed are nitrogen purged and replaced.

[0083] The above description shows and describes the preferred embodiments of the present application, as previously described, it should be understood that the present application is not limited to the forms disclosed herein, should not be regarded as excluding other embodiments, but can be used in various other combinations, modifications and environments, and can be modified within the scope of the invention concept described herein, by the above teaching or related art or knowledge. The modifications and changes made by those skilled in the art without departing from the spirit and scope of the present application shall be within the scope of protection of the appended claims of the present application.

Claims

1. A hydrogen production and suspension magnetized roasting coupling device, characterized in that: The application relates to a hydrogen production device, a suspension magnetization roasting device and a coupling assembly, wherein the hydrogen production device comprises a conversion furnace, a boiler, a heat exchanger, a first heat exchanger, a second heat exchanger, an emergency shift reactor, an emergency cooler, a liquid separator, a water seal tank, a slurry tank, a slurry pump; the suspension magnetization roasting device comprises a reduction reaction fluidized bed, a cyclone dust collector, a suspension roasting main furnace, a cyclone heater, a cyclone preheater, a dust remover, an air induction fan, a chimney, a feeding system, a cooling system, a slurry tank, a slurry pump; the coupling assembly comprises a conversion furnace synthesis gas outlet assembly, a boiler synthesis gas outlet assembly, a boiler steam outlet assembly, a heat exchanger steam inlet assembly, a first heat exchanger steam inlet assembly, a second heat exchanger steam inlet assembly, an emergency shift cooling and emptying assembly, a reduction gas main pipeline assembly, a reduction gas branch pipeline assembly and a combustion gas pipeline assembly; a combustion chamber is arranged at the top of the conversion furnace, a synthesis gas outlet at the bottom of the conversion furnace is communicated with a synthesis gas inlet of the boiler through the conversion furnace synthesis gas outlet assembly, a steam outlet of the boiler is communicated with a steam inlet of the first heat exchanger, a steam inlet of the second heat exchanger and a steam inlet of the heat exchanger respectively, a raw material gas outlet of the first heat exchanger is communicated with a raw material gas inlet of the combustion chamber of the conversion furnace, a compressed air outlet of the second heat exchanger is communicated with a compressed air inlet of the combustion chamber of the conversion furnace, a synthesis gas outlet of the boiler is communicated with a combustion gas inlet of the suspension roasting main furnace and a reduction gas inlet of the reduction reaction fluidized bed respectively, a discharge port of the reduction reaction fluidized bed is communicated with a feeding port of the cooling system through a one-way air lock valve, a discharge port of the cooling system is communicated with the slurry tank, the cooling system is provided with a cold air inlet pipe, an exhaust port of the reduction reaction fluidized bed is communicated with an air inlet port of the cyclone dust collector, a dust outlet pipe at the bottom of the cyclone dust collector is communicated with the inside of the reduction reaction fluidized bed, an exhaust port of the cyclone dust collector is communicated with an air inlet port of the lower part of the suspension roasting main furnace, a main burner and an ignition burner are sequentially arranged below the air inlet port of the lower part of the suspension roasting main furnace, a flue gas outlet at the top of the suspension roasting main furnace is communicated with a flue gas inlet of the cyclone heater, a discharge pipe at the bottom of the cyclone heater is communicated with a feeding port of the reduction reaction fluidized bed through a material seal valve, a flue gas outlet of the cyclone heater is connected with a flue gas inlet of the cyclone preheater through an ascending flue, a discharge port of the feeding system is communicated with the ascending flue, a flue gas outlet of the cyclone preheater is communicated with a flue gas inlet of the dust remover, a flue gas outlet of the dust remover is communicated with the chimney through the air induction fan, a discharge pipe at the bottom of the cyclone preheater is communicated with a feeding port of the suspension roasting main furnace. The boiler synthesis gas outlet is connected with a synthesis gas main pipeline, the emergency shift cooling and emptying assembly is connected with the synthesis gas main pipeline through an emergency shift cooling and emptying pipeline, an emergency shift reactor, an emergency cooler, a liquid separator, an eighth pressure transmitter, a water seal tank and a sixth temperature transmitter are sequentially arranged on the emergency shift cooling and emptying pipeline, the emergency cooler and the water seal tank are both provided with a water supplement pipeline, a backwater outlet of the emergency cooler, the liquid separator and the water seal tank is communicated with a backwater main pipeline, an outlet of the backwater main pipeline is communicated with the slurry tank, an outlet of the slurry tank is communicated with the slurry tank through a slurry pump.

2. The hydrogen production and suspension magnetization roasting coupling device according to claim 1, characterized in that: The combustion chamber at the top of the reformer is communicated with the first nitrogen replacement pipeline, and a permanent light is arranged in the combustion chamber.

3. The hydrogen production and suspension magnetization roasting coupling device according to claim 2, characterized in that: A boiler steam outlet assembly is arranged on the pipeline communicated with the steam outlet of the boiler, and the boiler steam outlet assembly comprises a second pressure transmitter and a second temperature transmitter.

4. The hydrogen production and suspension magnetization roasting coupling device according to claim 3, characterized in that: A first heat exchanger steam inlet assembly is arranged on the pipeline communicated with the steam inlet of the first heat exchanger, and the first heat exchanger steam inlet assembly comprises a second hand valve and a second pressure regulating valve.

5. The device according to claim 4, characterized in that: A second heat exchanger steam inlet assembly is arranged on the pipeline communicated with the steam inlet of the second heat exchanger, and the second heat exchanger steam inlet assembly comprises a fifth hand valve and a fourth pressure regulating valve.

6. The hydrogen production and suspension magnetization roasting coupling device according to claim 5, characterized in that: A heat exchanger steam inlet assembly is arranged on the pipeline communicated with the steam inlet of the heat exchanger, and the heat exchanger steam inlet assembly comprises a seventh hand valve and a sixth pressure regulating valve.

7. The hydrogen production and suspension magnetization roasting coupling device according to claim 6, characterized in that: The synthesis gas outlet of the boiler is connected to the combustion gas inlet of the suspension calcination main furnace through a combustion gas pipeline assembly, the combustion gas pipeline assembly comprises a combustion gas pipeline, and the combustion gas pipeline is provided with a tenth hand valve, a fourth quick cut valve, a second blind plate, a first orifice plate flowmeter, a ninth pressure transmitter, a seventh temperature transmitter and a seventh pressure regulating valve, the fourth quick cut valve and the second blind plate are connected to a fourth nitrogen replacement pipeline, the fourth nitrogen replacement pipeline is provided with an eleventh hand valve and a third gas shut-off valve; the synthesis gas outlet of the boiler is connected to a reduction gas branch pipeline assembly through a reduction gas main pipeline assembly, and the reduction gas branch pipeline assembly is connected to the reduction gas inlet of the reduction reaction fluidized bed through the reduction gas branch pipeline assembly, the reduction gas main pipeline assembly comprises a reduction gas main pipeline, and the reduction gas main pipeline is provided with a twelfth hand valve, a fifth quick cut valve, a third blind plate, an eighth pressure regulating valve, a second orifice plate flowmeter, a tenth pressure transmitter and an eighth temperature transmitter, the fifth quick cut valve and the third blind plate are connected to a fifth nitrogen replacement pipeline, and the fifth nitrogen replacement pipeline is provided with a thirteenth hand valve and a fourth gas shut-off valve; the reduction gas branch pipeline assembly comprises a reduction gas branch pipeline, and the reduction gas branch pipeline is provided with a third orifice plate flowmeter and a sixth quick cut valve.

8. The hydrogen production and suspension magnetization roasting coupling device according to claim 7, characterized in that: The reduction reaction fluidized bed is arranged from high to low in inclination from the feeding port to the discharging port, the top of the reduction reaction fluidized bed is provided with an eleventh pressure transmitter, the inside of the reduction reaction fluidized bed is provided with a ninth temperature transmitter, a gas flue O2 analyzer is arranged on the pipeline between the gas outlet of the reduction reaction fluidized bed and the gas inlet of the cyclone dust collector, O2, H2 and CO analyzers and an adjusting butterfly valve are arranged on the pipeline between the gas outlet of the cyclone dust collector and the lower gas inlet of the suspension calcination main furnace; the flue gas outlet at the top of the cooling system is connected to the flue gas inlet at the bottom of the suspension calcination main furnace, a start-up burner is arranged on the pipeline connected to the flue gas outlet of the cooling system, a tenth temperature transmitter is arranged on the pipeline connected to the flue gas inlet of the suspension calcination main furnace, and an eleventh temperature transmitter is arranged above the conical section of the suspension calcination main furnace.

9. The use of a hydrogen production and suspension magnetization roasting coupling device according to claim 8, characterized in that, The method comprises the following steps: S1, system starting: first, start the induced draft fan at a frequency of 12-18 Hz, then start the start-up burner at the flue gas outlet of the cooling system and heat at a rate of 20-30 ℃ / min, when the inlet temperature of the flue gas inlet at the bottom of the suspension calcination main furnace reaches 350 ℃, start the ignition burner of the suspension calcination main furnace, control the temperature rise of the suspension calcination main furnace by adjusting the combustion adjusting valve of the main burner, when the top temperature in the suspension calcination main furnace is greater than or equal to 550 ℃, the feeding requirement of the suspension calcination main furnace is met, and when the bottom temperature in the suspension calcination main furnace reaches 605 ℃, the starting condition of the conversion furnace is met; S2, nitrogen replacement: S21, fill the fine particle material into the one-way air lock valve and the material seal valve, and confirm that the one-way air lock valve and the material seal valve are sealed; confirm that the third hand valve and the third pressure regulating valve at the raw material gas inlet of the first heat exchanger are in the closed state, the first quick cut valve at the raw material gas outlet of the first heat exchanger is in the open state; confirm that the sixth hand valve and the fifth pressure regulating valve at the compressed air inlet of the second heat exchanger are in the closed state, the second quick cut valve at the compressed air outlet of the second heat exchanger is in the closed state; confirm that the water seal of the water seal box is sealed; open the first hand valve and the first pressure regulating valve, open the eighth hand valve, the third quick cut valve, and the first blind plate on the emergency shift cooling and emptying pipeline, open the tenth hand valve, the fourth quick cut valve, the second blind plate, and the seventh pressure regulating valve on the combustion gas pipeline, open the twelfth hand valve, the fifth quick cut valve, the third blind plate, and the eighth pressure regulating valve on the reducing gas main pipeline, open the sixth quick cut valve on the reducing gas branch pipeline, open the gas return valve of the reduction reaction fluidized bed, open the hand valve and the gas valve on the first nitrogen displacement pipeline at the top of the conversion furnace, open the fourth hand valve and the first gas valve on the second nitrogen displacement pipeline, and start nitrogen displacement of the pipelines and equipment of the entire coupling assembly; S22, nitrogen enters the reduction reaction fluidized bed through the pipeline, and the bed top pressure of the reduction reaction fluidized bed is maintained at 0-3KPa by controlling the regulating butterfly valve until the O2 content detected by the O2 analyzer and the O2, H2, CO analyzers in the gas flue is lower than 0.5%, which is considered as qualified displacement; S23, after nitrogen displacement for 10 minutes, the first quick cut valve, the first gas valve, the fourth quick cut valve, the seventh pressure regulating valve, the third quick cut valve, the regulating butterfly valve, and the gas valve on the first nitrogen displacement pipeline are closed synchronously; S24, after the first nitrogen displacement of the system is completed, the nitrogen pressure maintaining of the pipelines and system is continuously observed, the thirteenth hand valve and the fourth gas valve on the fifth nitrogen displacement pipeline and the ninth hand valve and the second gas valve on the third nitrogen displacement pipeline are opened and closed periodically to maintain the nitrogen pressure at 0.3-3KPa, the hand valve and the gas valve on the first nitrogen displacement pipeline, the fourth hand valve and the first gas valve on the second nitrogen displacement pipeline, and the eleventh hand valve and the third gas valve on the fourth nitrogen displacement pipeline are opened and closed periodically to maintain the nitrogen pressure at 3-20KPa; S3, start the conversion furnace: ignite the pilot light in the combustion chamber of the conversion furnace, open the zirconia analyzer at the synthesis gas outlet of the conversion furnace and input the interlock, open the third hand valve at the raw material gas inlet of the first heat exchanger and the sixth hand valve at the compressed air inlet of the second heat exchanger, adjust the opening degree of the third pressure regulating valve at the raw material gas inlet of the first heat exchanger and the fifth pressure regulating valve at the compressed air inlet of the second heat exchanger, ignite the lance at the top of the conversion furnace, and the conversion furnace starts to produce synthesis gas; S4, heat exchange: the synthesis gas with temperature of 1000-1300℃ in the converter is sent to the boiler through the converter synthesis gas outlet assembly, and is indirectly exchanged with the desalted cooling water supplied to the boiler to reduce the temperature to 400-550℃, and then is sent to the direction of the suspension magnetization roasting device. The high temperature steam with temperature of 400-500℃ generated by the boiler is sent to the first heat exchanger, the second heat exchanger and the heat exchanger respectively, for indirectly preheating the raw material gas and the compressed air, so that the preheating temperature of the raw material gas and the compressed air reaches 200-350℃. The high temperature steam is indirectly exchanged with the cold air through the heat exchanger to generate warm air with temperature of 150-300℃. The warm air is connected to the pipeline of the flue gas inlet of the bottom of the suspension roasting main furnace and the rising flue through the warm air outlet pipeline respectively. The condensed steam after heat exchange is discharged into the slurry pool and is sent to the slurry tank through the slurry pump as auxiliary make-up water for the slurry tank; S5, use of synthesis gas: the synthesis gas produced by the converter is sent to the reduction reaction fluidized bed through the pipeline as the gas for reduction reaction mineral phase conversion and fluidization of the fluidized bed. The production of the synthesis gas is adjusted by controlling the gas inlet amount of the raw material gas and the compressed air into the converter. For the reduction reaction fluidized bed, whether the empty bed is fed or the full bed is fed, the gas accumulation operation is needed to ensure that the cross-sectional fluidization velocity of the reduction reaction fluidized bed meets the fluidization requirement, and the cross-sectional fluidization velocity is controlled at 0.10-0.15m.s-1. During the gas accumulation, the synthesis gas produced by the converter is sent to the suspension roasting main furnace through the combustion gas pipeline to provide heating heat for the suspension roasting main furnace. According to the gas accumulation amount of the reduction reaction fluidized bed, the combustion gas supply of the main burner of the suspension roasting main furnace is simultaneously reduced. When the combustion gas amount accumulates to the fluidization gas amount required by the reduction gas, the supply of the combustion gas to the suspension roasting furnace is quickly stopped. The withdrawn combustion gas is supplied to the reduction reaction fluidized bed as the gas for reduction and fluidization of the fluidized bed. In order to ensure the fluidization of the reduction reaction fluidized bed and the normal discharge of the bed layer, the disturbance wind speed of the air cap hole of the reduction reaction fluidized bed is controlled at 50-90m.s-1. The reduction gas inlet pressure of the reduction reaction fluidized bed is controlled at 50-100KPa. In order to ensure the system safety and the quality of the calcined sand product, the bed layer pressure of the reduction reaction fluidized bed is controlled at 0-3KPa. The reduction agent concentration of the reduction reaction is controlled at 25%-55%, the reaction time is controlled at 25-50min, and the reduction reaction temperature is controlled at 500-600℃. S6, gas stopping operation: S61, gas withdrawal of the reduction reaction fluidized bed: S611, planned gas withdrawal: reduce the combustion load of the converter, open the tenth hand valve, the fourth quick cut valve, the second blind plate and the seventh pressure regulating valve on the combustion gas pipeline, adjust the inlet amount of the combustion gas by adjusting the seventh pressure regulating valve, and send the low load synthesis gas to the suspension roasting main furnace through the combustion gas pipeline for combustion; S612, emergency gas withdrawal: quickly cut off the reduction gas source, and send the synthesis gas to the suspension roasting main furnace through the combustion gas pipeline for combustion; S62, suspension roasting main furnace ignition burner stop: cut off the fifth quick cut valve of the reducing gas main pipeline and the fourth quick cut valve of the combustion gas pipeline, the third gas valve on the fourth nitrogen replacement pipeline and the first gas valve on the second nitrogen replacement pipeline are synchronously opened, the first quick cut valve of the raw material gas outlet of the first heat exchanger and the second quick cut valve of the compressed air outlet of the second heat exchanger are synchronously closed, the gas valve of the first nitrogen replacement pipeline at the top of the conversion furnace is automatically opened, the conversion furnace and its synthesis gas pipeline are replaced by nitrogen blowing, and the mixed gas of the blowing nitrogen and the synthesis gas is treated by emergency shift cooling and then discharged into the atmosphere through the exhaust pipe; S63, conversion furnace shutdown: the first quick cut valve of the raw material gas outlet of the first heat exchanger and the second quick cut valve of the compressed air outlet of the second heat exchanger are closed by the conversion furnace, the gas valve of the first nitrogen replacement pipeline at the top of the conversion furnace is automatically opened, and the conversion furnace, the reducing gas main pipeline, the reducing gas branch pipeline and the reduction reaction fluidized bed are replaced by nitrogen blowing.

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