Hydrogen production and suspension magnetization roasting coupling device and method

Abstract

The invention discloses a hydrogen production and suspension magnetization roasting coupling device and method. The hydrogen production and suspension magnetization roasting coupling device comprises a hydrogen production device, a suspension magnetization roasting device and a coupling connection assembly. According to the device, reduction gas with carbon monoxide and hydrogen as effective components is generated through an oxidation reaction under the pressurized non-catalytic condition, hematite, limonite and siderite are converted into ferromagnetic magnetite or maghemite under the reducing agent atmosphere condition, then high-grade and high-recovery-rate iron ore concentrate is obtained through magnetic separation, and efficient utilization of resources is achieved. The process flow is short, the load is convenient to increase and decrease, the operation flexibility is high, high fusion coupling of a hydrogen production system and a hydrogen-based mineral phase conversion system is realized, the method has the characteristics of wide raw material range, low gas production cost, low carbon, environment friendliness, high heat energy recycling rate, wide application range and the like, and a new way is provided for effectively developing and utilizing refractory ore resources.

Description

Technical Field

[0001] The invention relates to the technical field of chemical hydrogen production and metallurgical suspended magnetization roasting, and in particular to a hydrogen production and suspended magnetization roasting coupling device and method. Background Art

[0002] Suspended magnetization roasting technology is one of the most effective, successful and economically efficient magnetization roasting technologies for treating refractory iron ore resources. In recent years, suspended magnetization roasting technology has been industrially applied in treating refractory iron ore powder. The reaction mechanism of this technology is to use the heat storage to use the reducing agent CO or H2 to reduce the weakly magnetic refractory iron oxide at a certain temperature to generate strongly magnetic magnetite. This technology can effectively exploit and utilize refractory ore resources, expand domestic iron ore resource reserves, effectively reduce import dependence, achieve resource self-sufficiency, realize low-cost deep processing of refractory ores, replace some high-cost imported high-quality ores, and effectively reduce the cost of steel production. Through the mineral phase transformation suspended magnetization technology, refractory ores can be turned into selectable ores, and non-selectable ores can be turned into selectable ores. It plays a pivotal role in solving the strategic security of my country's iron ore resources, has broad market prospects, and is crucial to ensuring national resource security and economic sustainable development.

[0003] At present, the reduction reaction of suspended magnetization technology used in industry mainly uses CO as a reducing agent. The CO reducing agent is mainly obtained through two production methods. One is to produce coal gas through a gasifier to provide a reducing agent for the reduction reaction. The other is to use the blast furnace gas, a byproduct of blast furnace ironmaking in the metallurgical plant, to provide a reducing agent for the reduction reaction system of the suspended magnetization roasting furnace. Both of the above situations have relatively large limitations. First, using CO as a reducing agent will produce a large amount of CO2, which will produce a greenhouse effect; second, due to environmental protection reasons, many places do not allow the construction of gasifiers; third, many difficult-to-select ore mining areas do not have supporting steel smelting and no byproduct gas.

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

[0005] The purpose of the present invention is to provide a hydrogen production and suspended magnetization roasting coupling device and method in view of the deficiencies in the prior art, using hydrogen as a reducing agent, and realizing ore phase transformation by adjusting the reaction temperature, reaction concentration and reaction time, etc. The device has a compact process flow, a small footprint, a wide range of applications, safety and reliability, energy saving and environmental protection, and provides a new way for low-carbon and efficient utilization and green processing of difficult-to-select iron ore mineral resources.

[0006] To achieve the above object, the technical solution adopted by the present invention is:

[0007] A hydrogen production and suspension magnetization roasting coupling device, comprising a hydrogen production device, a suspension magnetization roasting device and a coupling connection component, wherein the hydrogen production device comprises a reformer, a boiler, a heat exchanger, a first heat exchanger, a second heat exchanger, an emergency conversion reactor, an emergency cooler, a liquid separation tank, a water seal box, a slurry tank, and 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 induced draft fan, a chimney, a feeding system, a cooling system, a slurry tank, and a slurry pump; the coupling connection component comprises a reformer synthesis gas outlet component, a boiler ... outlet assembly, boiler steam outlet assembly, heat exchanger steam inlet assembly, first heat exchanger steam inlet assembly, second heat exchanger steam inlet assembly, emergency conversion cooling and emptying assembly, reduction gas main pipeline assembly, reduction gas branch pipeline assembly, combustion gas pipeline assembly; a combustion chamber is provided on the top of the reformer, the synthesis gas outlet at the bottom of the reformer is connected with the synthesis gas inlet of the boiler through the reformer synthesis gas outlet assembly, the steam outlet of the boiler is respectively connected 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, and the raw gas outlet of the first heat exchanger is connected with the steam inlet of the reformer combustion chamber. The raw gas inlet and the compressed air outlet of the second heat exchanger are connected to the compressed air inlet of the reformer combustion chamber, the synthesis gas outlet of the boiler is respectively connected to 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 connected to the feed port of the cooling system through a one-way air lock valve, the discharge port of the cooling system is connected to the slurry tank, the cooling system is provided with a cold air inlet pipe, the exhaust port of the reduction reaction fluidized bed is connected to the air inlet of the cyclone dust collector, the ash lowering pipe at the bottom of the cyclone dust collector is connected to the inside of the reduction reaction fluidized bed, the exhaust port of the cyclone dust collector is connected to the air inlet at the bottom of the suspension roasting main furnace The main burner and the ignition burner are connected in sequence below the lower air inlet of the suspension roasting main furnace. The flue gas outlet at the top of the suspension roasting main furnace is connected with the flue gas inlet of the cyclone heater. The feed pipe at the bottom of the cyclone heater is connected with the feed port of the reduction reaction fluidized bed through a material sealing valve. The flue gas outlet of the cyclone heater is connected to the flue gas inlet of the cyclone preheater through an ascending flue. The discharge port of the feeding system is connected with the ascending flue. The flue gas outlet of the cyclone preheater is connected to the flue gas inlet of the dust collector. The flue gas outlet of the dust collector is connected to the chimney through an induced draft fan. The feed pipe at the bottom of the cyclone preheater is connected to the feed port of the suspension roasting main furnace.

[0008] Preferably, the combustion chamber at the top of the converter is connected to the first nitrogen replacement pipeline, a permanent lamp is provided in the combustion chamber, and the converter synthesis gas outlet assembly includes a zirconium oxide analyzer, a first pressure transmitter and a first temperature transmitter.

[0009] Preferably, a boiler steam outlet assembly is provided on the pipeline connected to the steam outlet of the boiler, and the boiler steam outlet assembly includes a second pressure transmitter and a second temperature transmitter; a boiler synthesis gas outlet assembly is provided on the pipeline connected to the synthesis gas outlet of the boiler, and the boiler synthesis gas outlet assembly includes a third pressure transmitter, a third temperature transmitter, H2 and CO analyzers, a first manual valve and a first pressure regulating valve.

[0010] Preferably, a first heat exchanger steam inlet assembly is provided on the pipeline connected to the steam inlet of the first heat exchanger, the first heat exchanger steam inlet assembly includes a second manual valve and a second pressure regulating valve, a third manual valve, a third pressure regulating valve and a fourth pressure transmitter are provided on the pipeline connected to the raw gas inlet of the first heat exchanger, a fifth pressure transmitter, a fourth temperature transmitter and a first quick-cut valve are provided on the pipeline connected to the raw gas outlet of the first heat exchanger, a second nitrogen replacement pipeline is connected between the third pressure regulating valve and the fourth pressure transmitter, a fourth manual valve and a first gas shut-off valve are provided on the second nitrogen replacement pipeline, the steam condensate outlet of the first heat exchanger is connected to the slurry tank, and the slurry tank outlet is connected to the slurry tank through a slurry pump.

[0011] Preferably, a second heat exchanger steam inlet assembly is provided on the pipeline connected to the steam inlet of the second heat exchanger, and the second heat exchanger steam inlet assembly includes a fifth manual valve and a fourth pressure regulating valve, a sixth manual valve, a fifth pressure regulating valve and a sixth pressure transmitter are provided on the pipeline connected to the compressed air inlet of the second heat exchanger, and a seventh pressure transmitter, a fifth temperature transmitter and a second quick-cut valve are provided on the pipeline connected to the compressed air outlet of the second heat exchanger, and the steam condensate outlet of the second heat exchanger is connected to the slurry tank, and the slurry tank outlet is connected to the slurry tank through a slurry pump.

[0012] Preferably, a heat exchanger steam inlet assembly is provided on the pipe connected to the steam inlet of the heat exchanger, and the heat exchanger steam inlet assembly includes a seventh manual valve and a sixth pressure regulating valve. The heat exchanger is also provided with a cold air inlet pipe and a warm air outlet pipe, and the warm air outlet pipe is respectively connected to the pipe of the flue gas inlet at the bottom of the suspended roasting main furnace and the ascending flue. The steam condensate outlet of the heat exchanger is connected to the slurry tank, and the slurry tank outlet is connected to the slurry tank through a slurry pump.

[0013] Preferably, the boiler synthesis gas outlet is connected to the synthesis gas main pipeline, and the emergency conversion cooling and emptying assembly is connected to the synthesis gas main pipeline through the emergency conversion cooling and emptying pipeline. The emergency conversion cooling and emptying pipeline is sequentially provided with an eighth manual valve, a third quick-cut valve, a first blind plate, an emergency conversion reactor, an emergency cooler, a liquid separator, an eighth pressure transmitter, a water seal box and a sixth temperature transmitter. The third nitrogen replacement pipeline is connected between the first blind plate and the third quick-cut valve. The third nitrogen replacement pipeline is provided with a ninth manual valve and a second gas shut-off valve. The emergency cooler and the water seal box are both provided with a water supply pipeline. The return water outlets of the emergency cooler, the liquid separator and the water seal box are connected to the return water main pipe, and the return water main pipe outlet is connected to the slurry tank, and the slurry tank outlet is connected to the slurry tank through a slurry pump.

[0014] Preferably, the syngas outlet of the boiler is connected to the combustion gas inlet of the suspended roasting main furnace through a combustion gas pipeline assembly, the combustion gas pipeline assembly includes a combustion gas pipeline, the combustion gas pipeline is provided with a tenth manual valve, a fourth quick-cut valve, a second blind plate, a first orifice flowmeter, a ninth pressure transmitter, a seventh temperature transmitter and a seventh pressure regulating valve, a fourth nitrogen replacement pipeline is connected between the fourth quick-cut valve and the second blind plate, and the fourth nitrogen replacement pipeline is provided with an eleventh manual valve and a third gas shut-off valve; the syngas outlet of the boiler is connected to the reducing gas branch pipeline assembly through the reducing gas main pipeline assembly, and then through the reducing gas main pipeline assembly. The branch pipeline assembly is connected to the reducing gas inlet of the reduction reaction fluidized bed, the reducing gas main pipeline assembly includes a reducing gas main pipeline, the reducing gas main pipeline is provided with a tenth hand valve, a fifth quick-cut valve, a third blind plate, an eighth pressure regulating valve, a second orifice flowmeter, a tenth pressure transmitter and an eighth temperature transmitter, the fifth nitrogen replacement pipeline is connected between the fifth quick-cut valve and the third blind plate, the fifth nitrogen replacement pipeline is provided with a thirteenth hand valve and a fourth gas shut-off valve; the reducing gas branch pipeline assembly includes a reducing gas branch pipeline, the reducing gas branch pipeline is provided with a third orifice flowmeter and a sixth quick-cut valve.

[0015] Preferably, the reduction reaction fluidized bed is tilted from high to low from the feed inlet to the discharge outlet, an eleventh pressure transmitter is provided on the top of the reduction reaction fluidized bed, a ninth temperature transmitter is provided inside the reduction reaction fluidized bed, an outlet flue O2 analyzer is provided on the pipeline between the exhaust port of the reduction reaction fluidized bed and the air inlet of the cyclone dust collector, and an O2 analyzer is provided on the pipeline between the exhaust port of the cyclone separation dust collector and the lower air inlet of the suspension roasting main furnace. 2、 H2, CO analyzers and regulating butterfly valves; the flue gas outlet at the top of the cooling system is connected to the flue gas inlet at the bottom of the suspension roasting main furnace, a starting burner is provided on the pipe connected to the flue gas outlet of the cooling system, a tenth temperature transmitter is provided on the pipe connected to the flue gas inlet of the suspension roasting main furnace, and an eleventh temperature transmitter is provided above the frustum section of the suspension roasting main furnace.

[0016] A method for using a hydrogen production and suspended magnetization roasting coupling device comprises the following steps:

[0017] S1. System startup: First, start the induced draft fan at a frequency of 12-18 Hz, then start the startup burner at the flue gas outlet of the cooling system, and increase the temperature at a rate of 20-30°C / min. When the inlet temperature of the flue gas inlet at the bottom of the suspension roasting main furnace reaches 350°C, start the ignition burner of the suspension roasting main furnace, and control the temperature rise of the suspension roasting main furnace by adjusting the combustion regulating valve of the main burner. When the top temperature in the suspension roasting main furnace is ≥550°C, the charging requirement of the suspension roasting main furnace is met. When the bottom temperature in the suspension roasting main furnace reaches 605°C, the start-up conditions of the converter are met.

[0018] S2, Nitrogen replacement:

[0019] S21. Fill fine-grained materials 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 manual valve and the third pressure regulating valve at the raw gas inlet of the first heat exchanger are in a closed state, and the first quick-cut valve at the raw gas outlet of the first heat exchanger is in an open state; confirm that the sixth manual valve and the fifth pressure regulating valve at the compressed air inlet of the second heat exchanger are in a closed state, and the second quick-cut valve at the compressed air outlet of the second heat exchanger is in a closed state; confirm that the water seal of the water seal box is sealed; open the first manual valve and the first pressure regulating valve, and open the emergency conversion cooling drain The eighth hand valve, the third quick-cut valve, and the first blind plate on the 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 tenth hand valve, the fifth quick-cut valve, the third blind plate, and the eighth pressure regulating valve on the reduction gas main pipeline, open the sixth quick-cut valve on the reduction gas branch pipeline, open the return gas valve of the reduction reaction fluidized bed, open the hand valve and the gas shut-off valve of the first nitrogen replacement pipeline on the top of the converter, open the fourth hand valve and the first gas shut-off valve of the second nitrogen replacement pipeline, and start nitrogen replacement of the pipelines and equipment of the entire coupled connection assembly;

[0020] S22, nitrogen enters the reduction reaction fluidized bed through the pipeline, and the pressure on the top of the reduction reaction fluidized bed is maintained at 0-3KPa by controlling the butterfly valve until the O2 analyzer and O 2、 If the O2 content detected by H2 and CO analyzers is less than 0.5%, the replacement is considered qualified;

[0021] S23, after 10 minutes of nitrogen replacement, the first quick-cut valve, the first gas shut-off valve, the fourth quick-cut valve, the seventh pressure regulating valve, the third quick-cut valve, the regulating butterfly valve and the gas shut-off valve of the first nitrogen replacement pipeline are synchronously closed;

[0022] S24. After the first nitrogen replacement of the system is completed, the nitrogen pressure maintenance of the pipeline and the system is continuously observed. The nitrogen pressure of the main suspension roasting furnace, the reduction reaction fluidized bed and the emergency conversion cooling and emptying pipeline is maintained at 0.3-3 KPa by opening and closing the thirteenth manual valve and the fourth gas shut-off valve on the fifth nitrogen replacement pipeline and the ninth manual valve and the second gas shut-off valve on the third nitrogen replacement pipeline in stages. The manual valve and the gas shut-off valve on the first nitrogen replacement pipeline, the fourth manual valve and the first gas shut-off valve on the second nitrogen replacement pipeline, and the eleventh manual valve and the third gas shut-off valve on the fourth nitrogen replacement pipeline are maintained at 3-20 KPa by opening and closing the manual valve and the gas shut-off valve on the first nitrogen replacement pipeline, the fourth manual valve and the first gas shut-off valve on the second nitrogen replacement pipeline, and the eleventh manual valve and the third gas shut-off valve on the fourth nitrogen replacement pipeline.

[0023] S3, reformer start-up: ignite the long-burning lamp in the reformer combustion chamber, turn on the zirconium oxide analyzer at the reformer synthesis gas outlet and put it into interlock, open the third manual valve at the raw gas inlet of the first heat exchanger and the sixth manual valve at the compressed air inlet of the second heat exchanger, adjust the opening of the third pressure regulating valve at the raw 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 spray gun at the top combustion chamber of the reformer, and the reformer starts to produce synthesis gas;

[0024] S4, heat exchange: the synthesis gas with a temperature of 1000-1300°C in the converter is sent to the boiler through the converter synthesis gas outlet assembly, and is sent to the direction of the suspension magnetization roasting device after cooling to 400-550°C through indirect heat exchange with the desalted cooling water fed into the boiler. The high-temperature steam of 400-500°C generated by the boiler is sent to the first heat exchanger, the second heat exchanger and the heat exchanger respectively, for indirect preheating of the raw gas and compressed air, so that the preheating temperature of the raw gas and compressed air reaches 200-350°C. The high-temperature steam is indirectly heat-exchanged with the cold air through the heat exchanger to generate warm air of 150-300°C. The warm air is connected to the pipe of the flue gas inlet at the bottom of the suspension roasting main furnace and the ascending flue through the warm air outlet pipe. The steam condensate after heat exchange is discharged into the slurry pool and sent to the slurry tank through the slurry pump, and used as auxiliary supplementary water for slurry adjustment of the slurry tank;

[0025] S5. Use of synthesis gas: The synthesis gas produced by the reformer is sent to the reduction reaction fluidized bed through a pipeline as gas for the mineral phase conversion of the reduction reaction and the fluidization of the fluidized bed. The production of synthesis gas is adjusted by controlling the intake of raw gas and compressed air into the reformer. For the reduction reaction fluidized bed, whether it is an empty bed or a full bed, gas accumulation operation is required to ensure that the cross-sectional fluidization velocity of the reduction reaction fluidized bed meets the fluidization requirements. The cross-sectional fluidization velocity is controlled at 0.10-0.15ms. -1During the gas accumulation period, the synthesis gas produced by the converter is sent to the suspension roasting main furnace through the combustion gas pipeline for combustion, providing heating heat for the suspension roasting main furnace, and according to the gas accumulation of the reduction reaction fluidized bed, the combustion gas supply of the main burner of the suspension roasting main furnace is reduced simultaneously. When the combustion gas volume is accumulated to meet the fluidization gas volume required for the reduction gas, the supply of combustion gas to the suspension roasting furnace is quickly stopped, and the withdrawn combustion gas is fed into the reduction reaction fluidized bed as fluidized bed reduction and fluidization gas. In order to ensure the normal fluidization and bed discharge of the reduction reaction fluidized bed, the disturbance wind speed of the wind cap hole of the reduction reaction fluidized bed is controlled at 50-90m.s -1 , the reducing 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 roasted 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 stop operation:

[0027] S61, degassing of reduction reaction fluidized bed:

[0028] S611, planned gas withdrawal: reduce the combustion load of the reformer, open the tenth manual valve, the fourth quick-cut valve, the second blind plate and the seventh pressure regulating valve on the combustion gas pipeline, adjust the intake 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 for combustion through the combustion gas pipeline;

[0029] S612, emergency gas withdrawal: quickly cut off the reducing gas source, and the synthetic gas is transported to the main suspension roasting furnace for combustion through the combustion gas pipeline;

[0030] S62, suspension roasting main furnace ignition burner shutdown: 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 shut-off valve on 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 nitrogen purge and replace the reducing gas main pipeline and the combustion gas pipeline; synchronously close the first quick-cut valve at the raw gas outlet of the first heat exchanger and the second quick-cut valve at the compressed air outlet of the second heat exchanger, the gas shut-off valve of the first nitrogen replacement pipeline on the top of the converter is automatically interlocked and opened, and nitrogen purge and replace the converter and its synthesis gas pipeline, and the mixed gas of the purged nitrogen and the synthesis gas is discharged into the atmosphere through the exhaust pipe after emergency conversion cooling treatment;

[0031] S63, converter shutdown: the converter interlock closes the first quick-cut valve at the raw gas outlet of the first heat exchanger and the second quick-cut valve at the compressed air outlet of the second heat exchanger, and the gas shut-off valve interlock of the first nitrogen replacement pipeline on the top of the converter automatically opens, and nitrogen is purged and replaced in the converter, the reducing gas main pipeline, the reducing gas branch pipeline and the reduction reaction fluidized bed.

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

[0033] 1. The present invention provides a device and method for coupling hydrogen production and suspended magnetization roasting, which can transform hematite, limonite and siderite into strongly magnetic magnetite or magnetic hematite under reducing agent atmosphere conditions, and then obtain high-grade and high-recovery iron concentrate through magnetic separation, thereby realizing efficient utilization of resources.

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

[0035] 3. Compared with traditional ore dressing technology, this technology can improve the iron grade by 5-10 percentage points and the iron recovery rate by 10-30 percentage points, and the production indicators are more excellent. For every 1 percentage point increase in the grade of the iron concentrate entering the furnace, the carbon dioxide emissions in the ironmaking process can be reduced by about 20kg. It can significantly improve the economic value of the product and reduce carbon emissions in the downstream metallurgical industry.

[0036] 4. The present invention uses the internal heat of the oxidation reaction to carry out the steam reforming reaction of hydrocarbons, does not require external heating, has high thermal efficiency, and the combustion reactants are the raw materials for the reforming reaction, does not require the addition of steam, does not require carbon supplementation, does not require desulfurization and deoiling before reforming, is not restricted by carbon deposition, and does not have the problem of catalyst deactivation.

[0037] 5. The present invention has a wide range of raw materials and can simultaneously process a variety of gaseous (liquid) hydrocarbons and other organic substances without the need for refining the raw materials.

[0038] 6. The H2 / CO ratio of the synthesis gas of the present invention is in the range of 0.9-2.2, with a high conversion rate, which is superior to the gas components of traditional conversion technologies, suitable for the hydrogen-carbon ratio of the raw gas required for various synthesis reactions, and has low hydrogen-carbon ratio adjustment costs and low gas production costs.

[0039] 7. The present invention converts the reaction heat to produce high-quality steam as a by-product, and the high-temperature heat recovery system has high heat recovery efficiency, sufficient heat recovery, high thermal energy utilization rate, and realizes efficient use of energy.

[0040] 8. The process flow and equipment structure of the present invention are simple, reliable and highly safe; they have great advantages in terms of conversion efficiency of hydrocarbon organic matter, outstanding advantages in large-scale equipment and small-scale synthesis gas production, convenient load increase and decrease, and great operational flexibility.

[0041] 9. The present invention can process a variety of gaseous hydrocarbons and liquid hydrocarbons at the same time, with flexible raw materials, and can generate synthesis gas: H2+CO from multiple organic matters. It can be applied to the clean and high-value utilization of natural gas, coke oven gas, waste gas, hydrocarbon-containing tail gas, organic waste liquid, etc.

[0042] 10. The converter of the present invention has a wide pressure adaptability range, which can reach up to 7MPa, and can match the subsequent reduction pressure requirements.

[0043] 11. The process flow and equipment structure of the present invention are simple, the hydrogen production system and the hydrogen-based mineral phase conversion system are highly coupled and integrated, the process is short, the investment is low, there is no need to replace the catalyst, and it can operate stably for a long period of time. BRIEF DESCRIPTION OF THE DRAWINGS

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

[0045] Among them, 1-converter, 2-boiler, 3-heat exchanger, 4-first heat exchanger, 5-second heat exchanger, 6-emergency conversion reactor, 7-emergency cooler, 8-liquid separation tank, 9-water seal box, 10-slurry tank, 11-slurry pump, 12-reduction reaction fluidized bed, 13-cyclone dust collector, 14-suspension roasting 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-lasting lamp, 27-zirconia 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 air shut-off 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 manual valve, 57- sixth pressure regulating valve, 58- cold air inlet pipe, 59- warm air outlet pipe, 60- rising flue, 61- synthesis gas main pipeline, 62- emergency conversion cooling and exhaust pipeline, 63- combustion gas inlet, 64- eighth manual 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 manual valve, 71- second gas shut-off valve, 72- return water main pipe, 73- combustion gas pipeline, 74- tenth manual valve, 75- fourth quick-cut valve, 76- second blind plate, 77- first orifice flowmeter, 78- ninth pressure transmitter, 7 9-the seventh temperature transmitter, 80-the seventh pressure regulating valve, 81-the fourth nitrogen replacement pipeline, 82-the eleventh manual valve, 83-the third gas shut-off valve, 84-the main pipeline of reducing gas, 85-the tenth hand valve, 86-the fifth quick-cut valve, 87-the third blind plate, 88-the eighth pressure regulating valve, 89-the second orifice flowmeter, 90-the tenth pressure transmitter, 91-the eighth temperature transmitter, 92-the fifth nitrogen replacement pipeline, 93-the thirteenth manual valve, 94-the fourth gas shut-off valve, 95-the reducing gas branch pipeline, 96-the third orifice flowmeter, 97-the sixth quick-cut valve, 98-the eleventh pressure transmitter, 99-the ninth temperature transmitter, 100-the exhaust flue O2 analyzer, 101-the lower ash pipe, 102-O 2、H2, CO analyzer, 103-adjusting butterfly valve, 104-one-way air lock valve, 105-start burner, 106-cold air inlet pipe, 107-10th temperature transmitter, 108-11th temperature transmitter, 109-main burner, 110-ignition burner, 111-material sealing valve DETAILED DESCRIPTION

[0046] The present invention is further explained below in conjunction with the accompanying drawings and specific embodiments. It should be understood that these embodiments are only used to illustrate the present invention and are not used to limit the scope of the present invention. After reading the present invention, various equivalent forms of modifications to the present invention by those skilled in the art all fall within the scope defined by the claims attached to this application.

[0047] In the present invention, unless otherwise clearly stipulated and limited, the terms such as "installation", "setting", "connection", "fixed connection" and the like should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection or an indirect connection through an intermediate medium; it can be the internal connection of two elements or the interaction relationship between two elements. Unless otherwise clearly defined, ordinary technicians in this field can understand the specific meanings of the above terms in the present invention according to the specific circumstances.

[0048] In the present invention, the directions or positional relationships indicated by terms such as "upper", "lower", "bottom", "top", etc. are based on the directions or positional relationships shown in the accompanying drawings. They are relational words determined only for the convenience of describing the structural relationships of the various parts or elements of the present invention. They do not specifically refer to any part or element in the present invention and cannot be understood as limitations on the present invention.

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

[0050] A combustion chamber 24 is provided at the top of the reformer 1, and the combustion chamber at the top of the reformer is connected to the first nitrogen replacement pipeline 25. A permanent lamp 26 is provided in the combustion chamber. The synthesis gas outlet at the bottom of the reformer is connected to the synthesis gas inlet of the boiler through the reformer synthesis gas outlet assembly. The reformer synthesis gas outlet assembly includes a zirconium oxide analyzer 27, a first pressure transmitter 28 and a first temperature transmitter 29.

[0051] The steam outlet of the boiler is connected to the steam inlet of the first heat exchanger, the steam inlet of the second heat exchanger and the steam inlet of the heat exchanger respectively through the boiler steam outlet assembly, the boiler steam outlet assembly includes a second pressure transmitter 30 and a second temperature transmitter 31, and a boiler synthesis gas outlet assembly is provided on the synthesis gas main pipeline connected to the synthesis gas outlet of the boiler, and the boiler synthesis gas outlet assembly includes a third pressure transmitter 32, a third temperature transmitter 33, H2 and CO analyzers 34, a first manual valve 35 and a first pressure regulating valve 36;

[0052] A first heat exchanger steam inlet assembly is provided on the pipeline connected to the steam inlet of the first heat exchanger, and the first heat exchanger steam inlet assembly includes a second manual valve 37 and a second pressure regulating valve 38. A third manual valve 39, a third pressure regulating valve 40 and a fourth pressure transmitter 41 are provided on the pipeline connected to the raw 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 provided on the pipeline connected to the raw gas outlet of the first heat exchanger. The raw gas outlet of the first heat exchanger is connected to the raw gas inlet of the combustion chamber of the reformer. A second nitrogen replacement pipeline 45 is connected between the third pressure regulating valve and the fourth pressure transmitter. A fourth manual valve 46 and a first gas shut-off valve 47 are provided on the second nitrogen replacement pipeline. The steam condensate outlet of the first heat exchanger is connected to the slurry tank, and the slurry tank outlet is connected to the slurry tank through a slurry pump.

[0053] The pipeline connected to the steam inlet of the second heat exchanger is provided with a second heat exchanger steam inlet assembly, and the second heat exchanger steam inlet assembly includes a fifth manual valve 48 and a fourth pressure regulating valve 49. The pipeline connected to the compressed air inlet of the second heat exchanger is provided with a sixth manual valve 50, a fifth pressure regulating valve 51 and a sixth pressure transmitter 52. The pipeline connected to the compressed air outlet of the second heat exchanger is provided with a seventh pressure transmitter 53, a fifth temperature transmitter 54 and a second quick-cut valve 55. The compressed air outlet of the second heat exchanger is connected to the compressed air inlet of the combustion chamber of the reformer. The steam condensate outlet of the second heat exchanger is connected to the slurry tank, and the slurry tank outlet is connected to the slurry tank through a slurry pump.

[0054] A heat exchanger steam inlet assembly is provided on the pipeline connected to the steam inlet of the heat exchanger, and the heat exchanger steam inlet assembly includes a seventh hand valve 56 and a sixth pressure regulating valve 57. The heat exchanger is also provided with a cold air inlet pipeline 58 and a warm air outlet pipeline 59. The warm air outlet pipeline is respectively connected to the pipeline of the flue gas inlet at the bottom of the suspension roasting main furnace and the ascending flue 60. The steam condensate outlet of the heat exchanger is connected to the slurry tank, and the slurry tank outlet is connected to the slurry tank through a slurry pump.

[0055] The boiler synthesis gas outlet is connected to the synthesis gas main pipeline 61, and the synthesis gas main pipeline is connected to the emergency conversion cooling and emptying pipeline 62, the combustion gas inlet 63 of the suspension roasting main furnace and the reduction gas inlet of the reduction reaction fluidized bed;

[0056] The emergency conversion cooling and emptying assembly is connected to the synthesis gas main pipeline through the emergency conversion cooling and emptying pipeline, and the emergency conversion cooling and emptying pipeline is provided with an eighth manual valve 64, a third quick-cut valve 65, a first blind plate 66, an emergency conversion reactor 6, an emergency cooler 7, a liquid separator 8, an eighth pressure transmitter 67, a water seal box 9 and a sixth temperature transmitter 68 in sequence. The third nitrogen replacement pipeline 69 is connected between the first blind plate and the third quick-cut valve. The third nitrogen replacement pipeline is provided with a ninth manual valve 70 and a second gas shut-off valve 71. The emergency cooler and the water seal box are both provided with water supply pipelines. The return water outlets of the emergency cooler, the liquid separator and the water seal box are connected to the return water main pipe 72, and the return water main pipe outlet is connected to the slurry tank, and the slurry tank outlet is connected to the slurry tank through a slurry pump;

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

[0058] The synthesis gas main pipeline is connected to the reduction gas branch pipeline assembly through the reduction gas main pipeline assembly, and then 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 includes a reduction gas main pipeline 84, on which a 12nd hand valve 85, a 5th quick-cut valve 86, a 3rd blind plate 87, an 8th pressure regulating valve 88, a 2nd orifice plate flowmeter 89, a 10th pressure transmitter 90 and an 8th temperature transmitter 91 are provided. A 5th nitrogen replacement pipeline 92 is connected between the 5th quick-cut valve and the 3rd blind plate, and a 13th hand valve 93 and a 4th gas shut-off valve 94 are provided on the 5th nitrogen replacement pipeline; the reduction gas branch pipeline assembly includes a reduction gas branch pipeline 95, on which a 3rd orifice plate flowmeter 96 and a 6th quick-cut valve 97 are provided;

[0059] The reduction reaction fluidized bed is inclined from high to low from the feed port to the discharge port, and the inclination slope is 4°. An eleventh pressure transmitter 98 is provided on the top of the reduction reaction fluidized bed, and a ninth temperature transmitter 99 is provided inside the reduction reaction fluidized bed. The exhaust port of the reduction reaction fluidized bed is connected with the air inlet of the cyclone dust collector, and an exhaust flue O2 analyzer 100 is provided on the pipeline between the exhaust port of the reduction reaction fluidized bed and the air inlet of the cyclone dust collector. The ash lowering pipe 101 at the bottom of the cyclone dust collector is connected with the fifth air chamber inside the reduction reaction fluidized bed, the exhaust port of the cyclone dust collector is connected with the air inlet of the lower part of the suspension roasting main furnace, and the exhaust port of the cyclone separation dust collector is connected with the air inlet of the lower part of the suspension roasting main furnace. 2、 H2, CO analyzer 102 and regulating butterfly valve 103, the discharge port of the reduction reaction fluidized bed is connected to the feed port of the cooling system through a one-way air lock valve 104;

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

[0061] A tenth temperature transmitter 107 is provided on the pipeline connected to the flue gas inlet of the suspension roasting main furnace, an eleventh temperature transmitter 108 is provided above the frustum section of the suspension roasting main furnace, a main burner 109 and an ignition burner 110 are provided in sequence below the lower air inlet of the suspension roasting main furnace, the flue gas outlet at the top of the suspension roasting main furnace is connected to the flue gas inlet of the cyclone heater, the feed pipe at the bottom of the cyclone heater is connected to the feed port of the reduction reaction fluidized bed through a material sealing valve 111, the flue gas outlet of the cyclone heater is connected to the flue gas inlet of the cyclone preheater through an ascending flue, the discharge port of the feeding system is connected to the ascending flue, the flue gas outlet of the cyclone preheater is connected to the flue gas inlet of the dust collector, the flue gas outlet of the dust collector is connected to the chimney through an induced draft fan, and the feed pipe at the bottom of the cyclone preheater is connected to the feed port of the suspension roasting main furnace.

[0062] A method for using a hydrogen production and suspended magnetization roasting coupling device comprises the following steps:

[0063] S1. System startup: First, start the induced draft fan at a frequency of 15 Hz, then start the startup burner at the flue gas outlet of the cooling system, and heat it up at a rate of 24°C / min. When the inlet temperature of the flue gas inlet at the bottom of the suspension roasting main furnace reaches 350°C, start the ignition burner of the suspension roasting main furnace, and control the temperature rise of the suspension roasting main furnace by adjusting the combustion regulating valve of the main burner. When the top temperature in the suspension roasting main furnace is ≥550°C, the charging requirement of the suspension roasting main furnace is met. When the bottom temperature in the suspension roasting main furnace reaches 605°C, the start-up conditions of the converter are met.

[0064] S2, Nitrogen replacement:

[0065] S21. Fill fine-grained materials 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 manual valve and the third pressure regulating valve at the raw gas inlet of the first heat exchanger are in a closed state, and the first quick-cut valve at the raw gas outlet of the first heat exchanger is in an open state; confirm that the sixth manual valve and the fifth pressure regulating valve at the compressed air inlet of the second heat exchanger are in a closed state, and the second quick-cut valve at the compressed air outlet of the second heat exchanger is in a closed state; confirm that the water seal of the water seal box is sealed; open the first manual valve and the first pressure regulating valve, and open the emergency conversion cooling drain The eighth hand valve, the third quick-cut valve, and the first blind plate on the 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 tenth hand valve, the fifth quick-cut valve, the third blind plate, and the eighth pressure regulating valve on the reduction gas main pipeline, open the sixth quick-cut valve on the reduction gas branch pipeline, open the return gas valve of the reduction reaction fluidized bed, open the hand valve and the gas shut-off valve of the first nitrogen replacement pipeline on the top of the converter, open the fourth hand valve and the first gas shut-off valve of the second nitrogen replacement pipeline, and start nitrogen replacement of the pipelines and equipment of the entire coupled connection assembly;

[0066] S22, nitrogen enters the reduction reaction fluidized bed through the pipeline, and the top pressure of the reduction reaction fluidized bed is maintained at 2KPa by controlling the butterfly valve until the O2 analyzer and O 2、 If the O2 content detected by H2 and CO analyzers is less than 0.5%, the replacement is considered qualified;

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

[0068] S24. After the first nitrogen replacement of the system is completed, the nitrogen pressure maintenance of the pipeline and the system is continuously observed. The nitrogen pressure of the main furnace for suspension roasting, the reduction reaction fluidized bed and the emergency conversion cooling and emptying pipeline is maintained at 2.5 KPa by opening and closing the thirteenth manual valve and the fourth gas shut-off valve on the fifth nitrogen replacement pipeline and the ninth manual valve and the second gas shut-off valve on the third nitrogen replacement pipeline in stages. The manual valve and the gas shut-off valve on the first nitrogen replacement pipeline, the fourth manual valve and the first gas shut-off valve on the second nitrogen replacement pipeline, and the eleventh manual valve and the third gas shut-off valve on the fourth nitrogen replacement pipeline are maintained at 15 KPa by opening and closing the manual valve and the gas shut-off valve on the first nitrogen replacement pipeline, the fourth manual valve and the first gas shut-off valve on the second nitrogen replacement pipeline, and the eleventh manual valve and the third gas shut-off valve on the fourth nitrogen replacement pipeline.

[0069] S3, reformer start-up: ignite the long-burning lamp in the reformer combustion chamber, turn on the zirconium oxide analyzer at the reformer synthesis gas outlet and put it into interlock, open the third manual valve at the raw gas inlet of the first heat exchanger and the sixth manual valve at the compressed air inlet of the second heat exchanger, adjust the opening of the third pressure regulating valve at the raw 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 spray gun at the top combustion chamber of the reformer, and the reformer starts to produce synthesis gas;

[0070] The main chemical equation for the generation of syngas is:

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

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

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

[0074] Among them, "+Q" indicates an endothermic reaction, and "-Q" indicates an exothermic reaction;

[0075] S4, heat exchange: the synthesis gas with a temperature of 1000-1300°C in the converter is sent to the boiler through the converter synthesis gas outlet assembly, and is sent to the direction of the suspension magnetization roasting device after being cooled to 450°C by indirect heat exchange with the desalted cooling water fed into the boiler. The high-temperature steam of 400°C generated by the boiler is sent to the first heat exchanger, the second heat exchanger and the heat exchanger respectively, and is used for indirect preheating of the raw gas and compressed air, so that the preheating temperature of the raw gas and compressed air reaches 200-350°C. The high-temperature steam is indirectly heat-exchanged with the cold air through the heat exchanger to generate warm air of 200°C. The warm air is connected to the pipe of the flue gas inlet at the bottom of the suspension roasting main furnace and the ascending flue through the warm air outlet pipe. The steam condensate after heat exchange is discharged into the slurry pool and sent to the slurry tank through the slurry pump, and is used as auxiliary supplementary water for slurry adjustment of the slurry tank;

[0076] S5. Use of synthesis gas: The synthesis gas produced by the reformer is sent to the reduction reaction fluidized bed through a pipeline as the gas for the mineral phase conversion of the reduction reaction and the fluidization of the fluidized bed. The production of synthesis gas is adjusted by controlling the intake of raw gas and compressed air into the reformer. For the reduction reaction fluidized bed, whether it is an empty bed or a full bed, gas accumulation operation is required to ensure that the cross-sectional fluidization velocity of the reduction reaction fluidized bed meets the fluidization requirements. The cross-sectional fluidization velocity is controlled at 0.12ms. -1During the gas accumulation period, the synthesis gas produced by the converter is sent to the suspension roasting main furnace through the combustion gas pipeline for combustion, providing heating heat for the suspension roasting main furnace, and according to the gas accumulation of the reduction reaction fluidized bed, the combustion gas supply of the main burner of the suspension roasting main furnace is reduced simultaneously. When the combustion gas volume is accumulated to meet the fluidization gas volume required for the reduction gas, the supply of combustion gas to the suspension roasting furnace is quickly stopped, and the withdrawn combustion gas is fed into the reduction reaction fluidized bed as fluidized bed reduction and fluidization gas. In order to ensure the normal fluidization and bed discharge of the reduction reaction fluidized bed, the disturbance wind speed of the wind cap hole of the reduction reaction fluidized bed is controlled at 70m.s -1 , the reducing gas inlet pressure of the reduction reaction fluidized bed is controlled at 50-100KPa. To ensure the safety of the system and the quality of the roasted sand product, the bed pressure of the reduction reaction fluidized bed is controlled at 2KPa, the reducing 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 stop operation:

[0078] S61, degassing of reduction reaction fluidized bed:

[0079] S611, planned degassing: when the reduction reaction fluidized bed needs degassing due to process requirements, the reducing 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, and the nitrogen purge of the combustion gas pipeline is completed simultaneously, and the tenth manual valve, the fourth quick-cut valve, the second blind plate and the seventh pressure regulating valve on the combustion gas pipeline are opened, and the intake amount of the combustion gas is adjusted by adjusting the seventh pressure regulating valve, and the low-load synthesis gas is sent to the suspension roasting main furnace for combustion through the combustion gas pipeline;

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

[0081] S62. Shutdown of the ignition burner of the suspended roasting main furnace: The roasting furnace system is shut down due to the interlocking shutdown of the induced draft fan, electricity, compressed air, nitrogen, natural gas, flame detection, valve status, reducing gas pressure, combustible gas detection of flue gas in the furnace, oxygen detection, flue gas temperature, etc., which triggers the shutdown of the suspended roasting main furnace, or the ignition burner failure triggers the interlocking shutdown of the suspended roasting main furnace. Under the above conditions, the fifth quick-cut valve of the reduction gas main pipeline and the fourth quick-cut valve of the combustion gas pipeline will both stop gas due to the interlocking of the quick-cut valves, and the third gas shut-off valve on the fourth nitrogen replacement pipeline and the first gas shut-off valve on the second nitrogen replacement pipeline will be automatically opened through synchronous interlocking, and the reduction gas main pipeline and the combustion gas pipeline will be purged and replaced with nitrogen; the first quick-cut valve at the outlet of the raw gas of the first heat exchanger and the second quick-cut valve at the outlet of the compressed air of the second heat exchanger will be closed synchronously, and the gas shut-off valve of the first nitrogen replacement pipeline on the top of the converter will be automatically opened through interlocking, and the converter and its synthesis gas pipeline will be purged and replaced with nitrogen, and the mixed gas of the purged nitrogen and the synthesis gas will be discharged into the atmosphere through the exhaust pipe after emergency conversion cooling treatment;

[0082] S63. Converter shutdown: If the converter's permanent lamp fails or the O2 content in the pipeline connected to the converter's synthesis gas outlet exceeds the standard, the converter interlocks and closes the first quick-cut valve at the first heat exchanger's raw gas outlet and the second quick-cut valve at the second heat exchanger's compressed air outlet. The gas shut-off valve interlock of the first nitrogen replacement pipeline on the converter's top automatically opens, and nitrogen is purged and replaced in the converter, the reducing gas main pipeline, the reducing gas branch pipeline and the reduction reaction fluidized bed.

[0083] The above description shows and describes the preferred embodiments of the present invention. As mentioned above, it should be understood that the present invention is not limited to the form disclosed herein, and 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 through the above teachings or the technology or knowledge of the relevant field. The changes and modifications made by those skilled in the art do not depart from the spirit and scope of the present invention, and should be within the scope of protection of the claims attached to the present invention.

Claims

1. A hydrogen production and suspension magnetization roasting coupling device, characterized in that: The invention comprises a hydrogen production device, a suspended magnetization roasting device and a coupling connection component, wherein the hydrogen production device comprises a reformer, a boiler, a heat exchanger, a first heat exchanger, a second heat exchanger, an emergency conversion reactor, an emergency cooler, a liquid separation tank, a water seal box, a slurry tank, and a slurry pump; the suspended magnetization roasting device comprises a reduction reaction fluidized bed, a cyclone dust collector, a suspended roasting main furnace, a cyclone heater, a cyclone preheater, a dust collector, an induced draft fan, a chimney, a feeding system, a cooling system, a slurry tank, and a slurry pump; the coupling connection component comprises a reformer synthesis gas outlet component, a boiler synthesis gas outlet component, a boiler steam outlet component A heat exchanger steam inlet component, a first heat exchanger steam inlet component, a second heat exchanger steam inlet component, an emergency conversion cooling and emptying component, a reduction gas main pipeline component, a reduction gas branch pipeline component, and a combustion gas pipeline component; a combustion chamber is provided on the top of the reformer, and the synthesis gas outlet at the bottom of the reformer is connected to the synthesis gas inlet of the boiler through the reformer synthesis gas outlet component, and the steam outlet of the boiler is respectively connected to 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 gas outlet of the first heat exchanger is connected to the raw gas inlet of the reformer combustion chamber, and the second The compressed air outlet of the heat exchanger is connected to the compressed air inlet of the combustion chamber of the reformer, the synthesis gas outlet of the boiler is respectively connected to 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 connected to the feed port of the cooling system through a one-way air lock valve, the discharge port of the cooling system is connected to the slurry tank, the cooling system is provided with a cold air inlet pipe, the exhaust port of the reduction reaction fluidized bed is connected to the air inlet of the cyclone dust collector, the ash lowering pipe at the bottom of the cyclone dust collector is connected to the inside of the reduction reaction fluidized bed, the exhaust port of the cyclone dust collector is connected to the air inlet at the bottom of the suspension roasting main furnace, and the cyclone dust collector is connected to the air inlet of the lower part of the suspension roasting main furnace. A main burner and an ignition burner are arranged in sequence below the lower air inlet of the floating roasting main furnace. The flue gas outlet at the top of the floating roasting main furnace is connected with the flue gas inlet of the cyclone heater. The feed pipe at the bottom of the cyclone heater is connected with the feed port of the reduction reaction fluidized bed through a material sealing valve. The flue gas outlet of the cyclone heater is connected to the flue gas inlet of the cyclone preheater through an ascending flue. The discharge port of the feeding system is connected with the ascending flue. The flue gas outlet of the cyclone preheater is connected to the flue gas inlet of the dust collector. The flue gas outlet of the dust collector is connected to the chimney through an induced draft fan. The feed pipe at the bottom of the cyclone preheater is connected to the feed port of the floating roasting main furnace.

2. A 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, a permanent lamp is arranged in the combustion chamber, and the reformer synthesis gas outlet assembly comprises a zirconium oxide analyzer, a first pressure transmitter and a first temperature transmitter.

3. The hydrogen production and suspended magnetization roasting coupling device according to claim 1 is characterized in that: A boiler steam outlet assembly is provided on the pipeline connected to the steam outlet of the boiler, and the boiler steam outlet assembly includes a second pressure transmitter and a second temperature transmitter. A boiler synthesis gas outlet assembly is provided on the pipeline connected to the synthesis gas outlet of the boiler, and the boiler synthesis gas outlet assembly includes a third pressure transmitter, a third temperature transmitter, H2 and CO analyzers, a first manual valve and a first pressure regulating valve.

4. The hydrogen production and suspended magnetization roasting coupling device according to claim 1 is characterized in that: A first heat exchanger steam inlet assembly is provided on the pipeline connected to the steam inlet of the first heat exchanger, and the first heat exchanger steam inlet assembly includes a second manual valve and a second pressure regulating valve. A third manual valve, a third pressure regulating valve and a fourth pressure transmitter are provided on the pipeline connected to the raw gas inlet of the first heat exchanger. A fifth pressure transmitter, a fourth temperature transmitter and a first quick-cut valve are provided on the pipeline connected to the raw gas outlet of the first heat exchanger. A second nitrogen replacement pipeline is connected between the third pressure regulating valve and the fourth pressure transmitter. A fourth manual valve and a first gas shut-off valve are provided on the second nitrogen replacement pipeline. The steam condensate outlet of the first heat exchanger is connected to the slurry tank, and the slurry tank outlet is connected to the slurry tank through a slurry pump.

5. The hydrogen production and suspended magnetization roasting coupling device according to claim 1 is characterized in that: A second heat exchanger steam inlet assembly is provided on the pipeline connected to the steam inlet of the second heat exchanger, and the second heat exchanger steam inlet assembly includes a fifth manual valve and a fourth pressure regulating valve. A sixth manual valve, a fifth pressure regulating valve and a sixth pressure transmitter are provided on the pipeline connected to the compressed air inlet of the second heat exchanger. A seventh pressure transmitter, a fifth temperature transmitter and a second quick-cut valve are provided on the pipeline connected to the compressed air outlet of the second heat exchanger. The steam condensate outlet of the second heat exchanger is connected to the slurry tank, and the slurry tank outlet is connected to the slurry tank through a slurry pump.

6. The hydrogen production and suspended magnetization roasting coupling device according to claim 1 is characterized in that: A heat exchanger steam inlet assembly is provided on the pipe connected to the steam inlet of the heat exchanger, and the heat exchanger steam inlet assembly includes a seventh manual valve and a sixth pressure regulating valve. The heat exchanger is also provided with a cold air inlet pipe and a warm air outlet pipe. The warm air outlet pipe is respectively connected to the pipe of the flue gas inlet at the bottom of the suspended roasting main furnace and the ascending flue. The steam condensate outlet of the heat exchanger is connected to the slurry tank, and the slurry tank outlet is connected to the slurry tank through a slurry pump.

7. The hydrogen production and suspended magnetization roasting coupling device according to claim 1 is characterized in that: The boiler synthesis gas outlet is connected to the synthesis gas main pipeline, and the emergency conversion cooling and emptying component is connected to the synthesis gas main pipeline through the emergency conversion cooling and emptying pipeline. The emergency conversion cooling and emptying pipeline is sequentially provided with an eighth manual valve, a third quick-cut valve, a first blind plate, an emergency conversion reactor, an emergency cooler, a liquid separator, an eighth pressure transmitter, a water seal box and a sixth temperature transmitter. The third nitrogen replacement pipeline is connected between the first blind plate and the third quick-cut valve. The third nitrogen replacement pipeline is provided with a ninth manual valve and a second gas shut-off valve. The emergency cooler and the water seal box are both provided with a water supply pipeline. The return water outlets of the emergency cooler, the liquid separator and the water seal box are connected to the return water main pipe, and the return water main pipe outlet is connected to the slurry tank, and the slurry tank outlet is connected to the slurry tank through a slurry pump.

8. The hydrogen production and suspended magnetization roasting coupling device according to claim 1 is characterized in that: The syngas outlet of the boiler is connected to the combustion gas inlet of the suspended roasting main furnace through a combustion gas pipeline assembly, the combustion gas pipeline assembly includes a combustion gas pipeline, the combustion gas pipeline is provided with a tenth manual valve, a fourth quick-cut valve, a second blind plate, a first orifice flowmeter, a ninth pressure transmitter, a seventh temperature transmitter and a seventh pressure regulating valve, a fourth nitrogen replacement pipeline is connected between the fourth quick-cut valve and the second blind plate, and an eleventh manual valve and a third gas shut-off valve are provided on the fourth nitrogen replacement pipeline; the syngas outlet of the boiler is connected to the reducing gas branch pipeline assembly through the reducing gas main pipeline assembly, and then through the reducing gas branch pipeline The reducing gas pipeline assembly is connected to the reducing gas inlet of the reduction reaction fluidized bed, the reducing gas main pipeline assembly includes a reducing gas main pipeline, the reducing gas main pipeline is provided with a tenth hand valve, a fifth quick-cut valve, a third blind plate, an eighth pressure regulating valve, a second orifice flowmeter, a tenth pressure transmitter and an eighth temperature transmitter, a fifth nitrogen replacement pipeline is connected between the fifth quick-cut valve and the third blind plate, and the fifth nitrogen replacement pipeline is provided with a thirteenth hand valve and a fourth gas shut-off valve; the reducing gas branch pipeline assembly includes a reducing gas branch pipeline, the reducing gas branch pipeline is provided with a third orifice flowmeter and a sixth quick-cut valve.

9. The hydrogen production and suspended magnetization roasting coupling device according to claim 1, characterized in that: The reduction reaction fluidized bed is tilted from high to low from the feed inlet to the discharge outlet, an eleventh pressure transmitter is provided on the top of the reduction reaction fluidized bed, a ninth temperature transmitter is provided inside the reduction reaction fluidized bed, an outlet flue O2 analyzer is provided on the pipeline between the exhaust port of the reduction reaction fluidized bed and the air inlet of the cyclone dust collector, an O2 analyzer is provided on the pipeline between the exhaust port of the cyclone separation dust collector and the lower air inlet of the suspension roasting main furnace 2、 H2, CO analyzers and regulating butterfly valves; the flue gas outlet at the top of the cooling system is connected to the flue gas inlet at the bottom of the suspension roasting main furnace, a starting burner is provided on the pipe connected to the flue gas outlet of the cooling system, a tenth temperature transmitter is provided on the pipe connected to the flue gas inlet of the suspension roasting main furnace, and an eleventh temperature transmitter is provided above the frustum section of the suspension roasting main furnace.

10. A method for using the hydrogen production and suspended magnetization roasting coupling device according to any one of claims 1 to 9, characterized in that: The following steps are involved: S1. System startup: First, start the induced draft fan at a frequency of 12-18 Hz, then start the startup burner at the flue gas outlet of the cooling system, and increase the temperature at a rate of 20-30°C / min. When the inlet temperature of the flue gas inlet at the bottom of the suspension roasting main furnace reaches 350°C, start the ignition burner of the suspension roasting main furnace, and control the temperature rise of the suspension roasting main furnace by adjusting the combustion regulating valve of the main burner. When the top temperature in the suspension roasting main furnace is ≥550°C, the charging requirement of the suspension roasting main furnace is met. When the bottom temperature in the suspension roasting main furnace reaches 605°C, the start-up conditions of the converter are met. S2, Nitrogen replacement: S21. Fill fine-grained materials 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 manual valve and the third pressure regulating valve at the raw gas inlet of the first heat exchanger are in a closed state, and the first quick-cut valve at the raw gas outlet of the first heat exchanger is in an open state; confirm that the sixth manual valve and the fifth pressure regulating valve at the compressed air inlet of the second heat exchanger are in a closed state, and the second quick-cut valve at the compressed air outlet of the second heat exchanger is in a closed state; confirm that the water seal of the water seal box is sealed; open the first manual valve and the first pressure regulating valve, and open the emergency conversion cooling drain The eighth hand valve, the third quick-cut valve, and the first blind plate on the 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 tenth hand valve, the fifth quick-cut valve, the third blind plate, and the eighth pressure regulating valve on the reduction gas main pipeline, open the sixth quick-cut valve on the reduction gas branch pipeline, open the return gas valve of the reduction reaction fluidized bed, open the hand valve and the gas shut-off valve of the first nitrogen replacement pipeline on the top of the converter, open the fourth hand valve and the first gas shut-off valve of the second nitrogen replacement pipeline, and start nitrogen replacement of the pipelines and equipment of the entire coupled connection assembly; S22, nitrogen enters the reduction reaction fluidized bed through the pipeline, and the pressure on the top of the reduction reaction fluidized bed is maintained at 0-3KPa by controlling the butterfly valve until the O2 analyzer and O 2、 If the O2 content detected by H2 and CO analyzers is less than 0.5%, the replacement is considered qualified; S23, after 10 minutes of nitrogen replacement, the first quick-cut valve, the first gas shut-off valve, the fourth quick-cut valve, the seventh pressure regulating valve, the third quick-cut valve, the regulating butterfly valve and the gas shut-off valve of the first nitrogen replacement pipeline are synchronously closed; S24. After the first nitrogen replacement of the system is completed, the nitrogen pressure maintenance of the pipeline and the system is continuously observed. The nitrogen pressure of the main suspension roasting furnace, the reduction reaction fluidized bed and the emergency conversion cooling and emptying pipeline is maintained at 0.3-3 KPa by opening and closing the thirteenth manual valve and the fourth gas shut-off valve on the fifth nitrogen replacement pipeline and the ninth manual valve and the second gas shut-off valve on the third nitrogen replacement pipeline in stages. The manual valve and the gas shut-off valve on the first nitrogen replacement pipeline, the fourth manual valve and the first gas shut-off valve on the second nitrogen replacement pipeline, and the eleventh manual valve and the third gas shut-off valve on the fourth nitrogen replacement pipeline are maintained at 3-20 KPa by opening and closing the manual valve and the gas shut-off valve on the first nitrogen replacement pipeline, the fourth manual valve and the first gas shut-off valve on the second nitrogen replacement pipeline, and the eleventh manual valve and the third gas shut-off valve on the fourth nitrogen replacement pipeline. S3, reformer start-up: ignite the long-burning lamp in the reformer combustion chamber, turn on the zirconium oxide analyzer at the reformer synthesis gas outlet and put it into interlock, open the third manual valve at the raw gas inlet of the first heat exchanger and the sixth manual valve at the compressed air inlet of the second heat exchanger, adjust the opening of the third pressure regulating valve at the raw 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 spray gun at the top combustion chamber of the reformer, and the reformer starts to produce synthesis gas; S4, heat exchange: the synthesis gas with a temperature of 1000-1300°C in the converter is sent to the boiler through the converter synthesis gas outlet assembly, and is sent to the direction of the suspension magnetization roasting device after cooling to 400-550°C through indirect heat exchange with the desalted cooling water fed into the boiler. The high-temperature steam of 400-500°C generated by the boiler is sent to the first heat exchanger, the second heat exchanger and the heat exchanger respectively, for indirect preheating of the raw gas and compressed air, so that the preheating temperature of the raw gas and compressed air reaches 200-350°C. The high-temperature steam is indirectly heat-exchanged with the cold air through the heat exchanger to generate warm air of 150-300°C. The warm air is connected to the pipe of the flue gas inlet at the bottom of the suspension roasting main furnace and the ascending flue through the warm air outlet pipe. The steam condensate after heat exchange is discharged into the slurry pool and sent to the slurry tank through the slurry pump, and used as auxiliary supplementary water for slurry adjustment of the slurry tank; S5. Use of synthesis gas: The synthesis gas produced by the reformer is sent to the reduction reaction fluidized bed through a pipeline as gas for the mineral phase conversion of the reduction reaction and the fluidization of the fluidized bed. The production of synthesis gas is adjusted by controlling the intake of raw gas and compressed air into the reformer. For the reduction reaction fluidized bed, whether it is an empty bed or a full bed, gas accumulation operation is required to ensure that the cross-sectional fluidization velocity of the reduction reaction fluidized bed meets the fluidization requirements. The cross-sectional fluidization velocity is controlled at 0.10-0.15ms. -1 During the gas accumulation period, the synthesis gas produced by the converter is sent to the suspension roasting main furnace through the combustion gas pipeline for combustion, providing heating heat for the suspension roasting main furnace, and according to the gas accumulation of the reduction reaction fluidized bed, the combustion gas supply of the main burner of the suspension roasting main furnace is reduced simultaneously. When the combustion gas volume is accumulated to meet the fluidization gas volume required for the reduction gas, the supply of combustion gas to the suspension roasting furnace is quickly stopped, and the withdrawn combustion gas is fed into the reduction reaction fluidized bed as fluidized bed reduction and fluidization gas. In order to ensure the normal fluidization and bed discharge of the reduction reaction fluidized bed, the disturbance wind speed of the wind cap hole of the reduction reaction fluidized bed is controlled at 50-90m.s -1 , the reducing 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 roasted 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℃; S6, gas stop operation: S61, degassing of reduction reaction fluidized bed: S611, planned gas withdrawal: reduce the combustion load of the reformer, open the tenth manual valve, the fourth quick-cut valve, the second blind plate and the seventh pressure regulating valve on the combustion gas pipeline, adjust the intake 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 for combustion through the combustion gas pipeline; S612, emergency gas withdrawal: quickly cut off the reducing gas source, and the synthetic gas is transported to the main suspension roasting furnace for combustion through the combustion gas pipeline; S62, suspension roasting main furnace ignition burner shutdown: 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 shut-off valve on 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 nitrogen purge and replace the reducing gas main pipeline and the combustion gas pipeline; synchronously close the first quick-cut valve at the raw gas outlet of the first heat exchanger and the second quick-cut valve at the compressed air outlet of the second heat exchanger, the gas shut-off valve of the first nitrogen replacement pipeline on the top of the converter is automatically interlocked and opened, and nitrogen purge and replace the converter and its synthesis gas pipeline, and the mixed gas of the purged nitrogen and the synthesis gas is discharged into the atmosphere through the exhaust pipe after emergency conversion cooling treatment; S63, converter shutdown: the converter interlock closes the first quick-cut valve at the raw gas outlet of the first heat exchanger and the second quick-cut valve at the compressed air outlet of the second heat exchanger, and the gas shut-off valve interlock of the first nitrogen replacement pipeline on the top of the converter automatically opens, and nitrogen is purged and replaced in the converter, the reducing gas main pipeline, the reducing gas branch pipeline and the reduction reaction fluidized bed.

Images