Zero-carbon glass kiln system

Abstract

The utility model discloses a zero-carbon glass kiln system which comprises a photovoltaic power generation device, an air separation device, a water electrolysis hydrogen production device, a mixer, a methanation device, a waste heat boiler I, a reforming device, a glass kiln, a waste heat boiler II and a dust removal and desulfurization device. The device is driven by green electricity to produce green oxygen, green nitrogen and green hydrogen; the flue gas of the glass kiln is cyclically enriched into high-concentration carbon dioxide (95.0 v% or above), the high-concentration carbon dioxide and green hydrogen are subjected to a methanation reaction to produce methane, and the methane, the carbon dioxide and water vapor are subjected to a reforming reaction to produce carbon monoxide and hydrogen; carbon monoxide and hydrogen are used as fuel of the glass kiln, green oxygen and carbon dioxide are mixed to form carbon-based oxygen-enriched combustion which is used as a combustion improver of the glass kiln, carbon-based oxygen-enriched combustion of the glass kiln is carried out, and redundant carbon dioxide is sold. According to the utility model, the purposes of greenness, energy conservation, almost no nitrogen oxide and zero carbon are realized.

Description

TECHNICAL FIELD

[0001] The utility model relates to glass kiln technical field, concretely relates to a zero carbon glass kiln system. BACKGROUND

[0002] With global climate warming touches ecological safety, water resource safety and food safety etc. every aspect, aggravates the risk of extreme climate disaster occurrence, seriously threatens human's living environment. And greenhouse gas emission is the most main factor that causes global climate warming, and the greenhouse effect of carbon dioxide produces accounts for more than 70v% of all greenhouse gases, therefore carbon dioxide's emission reduction is a problem that urgently to be solved, and it is important to control greenhouse effect, slow down global warming.

[0003] Although the carbon emission of domestic glass industry accounts for a small share at present, but it belongs to high energy consumption, high emission industry, and CO2 emission situation is not optimistic. CONTENT OF THE UTILITY MODEL

[0004] The utility model aims at providing a zero carbon glass kiln system to solve the deficiency of prior art.

[0005] To achieve the above-mentioned purpose, the utility model adopts the following technical scheme:

[0006] A zero carbon glass kiln system, comprising photovoltaic power generation device, air separation device, water electrolysis hydrogen production device, mixer, methanation device, waste heat boiler I, reforming device, glass kiln, waste heat boiler II and dust removal desulfurization device;

[0007] Photovoltaic power generation device is used for producing green electricity and providing electric energy for air separation device and water electrolysis hydrogen production device;

[0008] Air separation device is used for producing oxygen and nitrogen;

[0009] Water electrolysis hydrogen production device is used for producing hydrogen and oxygen;

[0010] Mixer is used for mixing oxygen sent by air separation device, oxygen sent by water electrolysis hydrogen production device and circulating flue gas sent by glass kiln into carbon-based oxygen-enriched;

[0011] Methanation device is used for carrying out methanation reaction on hydrogen sent by water electrolysis hydrogen production device and circulating flue gas sent by dust removal desulfurization device;

[0012] Waste heat boiler I is used for recovering waste heat of methane (containing saturated water vapor) sent by methanation device and byproduct production steam;

[0013] Reforming device is used for carrying out methane reforming reaction on methane (containing saturated water vapor) sent by waste heat boiler I and part circulating flue gas sent by glass kiln;

[0014] Glass furnace, which is fueled by carbon monoxide and hydrogen sent from reformer and combusted by carbon-based oxygen-rich sent from mixer, produces glass liquid;

[0015] Waste heat boiler II, which is used to recover waste heat from circulating flue gas sent from glass furnace and produce steam as by-product;

[0016] Dust and desulfurization device, which is used to remove dust and desulfurize circulating flue gas sent from waste heat boiler II;

[0017] Photovoltaic power generation device is connected with air separation device and water electrolysis hydrogen production device respectively; nitrogen outlet of air separation device is connected with tin tank of glass furnace and nitrogen product storage tank respectively, and a pressure reducing valve is arranged on the connecting pipeline of nitrogen outlet of air separation device and tin tank of glass furnace; oxygen outlet of air separation device and oxygen outlet of water electrolysis hydrogen production device are connected with mixer, a pressure reducing valve is arranged on the connecting pipeline of oxygen outlet of water electrolysis hydrogen production device and mixer, and flow detection instrument, temperature detection instrument, pressure detection instrument, oxygen purity detection instrument and flow regulating valve are arranged on the connecting pipeline of oxygen outlet of air separation device, oxygen outlet of water electrolysis hydrogen production device and mixer; hydrogen outlet of water electrolysis hydrogen production device is connected with methanation device; carbon-based oxygen-rich outlet of mixer is connected with heat storage grid A / B of glass furnace, and then connected with glass furnace; methane outlet of methanation device is connected with waste heat boiler I; methane outlet of waste heat boiler I is connected with heat storage grid A / B of reformer, and then connected with reformer, a pressure reducing valve is arranged on the connecting pipeline of methane outlet of waste heat boiler I and heat storage grid A / B of reformer, steam outlet of waste heat boiler I is connected with steam utilization device; carbon monoxide + hydrogen outlet of reformer is connected with glass furnace; circulating flue gas outlet of glass furnace is connected with heat storage grid B / A of glass furnace, and then connected with waste heat boiler II, mixer, heat storage grid A / B of reformer and heat storage grid B / A of reformer, respectively, and then connected with dust and desulfurization device, a booster is arranged on the connecting pipeline of heat storage grid B / A of glass furnace and waste heat boiler II and mixer, flow detection instrument, temperature detection instrument, pressure detection instrument, carbon dioxide purity detection instrument and flow regulating valve are arranged on the connecting pipeline of heat storage grid B / A of glass furnace and mixer, a booster is arranged on the connecting pipeline of glass furnace and heat storage grid A / B of reformer and heat storage grid B / A of reformer, and a pressure reducing valve is arranged on the connecting pipeline of heat storage grid B / A of reformer and dust and desulfurization device; circulating flue gas outlet of waste heat boiler II is connected with dust and desulfurization device; circulating flue gas outlet of dust and desulfurization device is connected with methanation device and CO2 product storage tank respectively, and a booster is arranged on the connecting pipeline of circulating flue gas outlet of dust and desulfurization device and methanation device.

[0018] Further, the dust and desulfurization device is composed of two parts, one is high-temperature dust collector, and the other is dry desulfurization equipment; the high-temperature dust collector adopts cyclone separation dust removal, and the dry desulfurization equipment adopts zinc oxide desulfurization.

[0019] The utility model discloses the beneficial effect has:

[0020] 1, the utility model discloses the green electricity driving air separation device production green oxygen and green nitrogen of green electricity of photovoltaic power generation device production, drives water electrolysis hydrogen production device production green hydrogen and green oxygen, green environmental protection.

[0021] 2, the utility model discloses the green electricity driving air separation device production green oxygen and green nitrogen of photovoltaic power generation device production, drives water electrolysis hydrogen production device production green hydrogen and green oxygen, green environmental protection.

[0022] 3, the utility model discloses the carbon dioxide of 95.0v% above concentration of glass kiln's flue gas circulation enrichment, as the raw material of methanation, the raw material of reforming, the raw material of glass kiln carbon-based oxygen-rich combustion, and the excess carbon dioxide is sold as a product, and the zero carbon glass kiln is really realized.

[0023] 4, the utility model discloses the green hydrogen of water electrolysis hydrogen production device production and the high concentration carbon dioxide (95.0v% above) of flue gas enrichment as the raw material production methane of methanation, utilizes the waste carbon dioxide, improves the utilization of waste resources.

[0024] 5, the utility model discloses the methane of methanation device production, the high concentration carbon dioxide (95.0v% above) of flue gas enrichment and water vapor as raw material, produce carbon monoxide and hydrogen through reforming reaction, improve the calorific value of fuel, and reduce the consumption of fuel.

[0025] 6, the utility model discloses the high concentration carbon dioxide (95.0v% above) of flue gas enrichment replaces air and carries out carbon-based oxygen-rich combustion, can make almost no nitrogen oxides produce in the combustion process, and because carbon dioxide is greenhouse gas, improves the thermal efficiency of glass kiln.

[0026] 7, the utility model discloses the high concentration carbon dioxide (95.0v% above) of flue gas enrichment, creates conditions for low-cost carbon dioxide capture, creates the possibility for zero carbon glass kiln.

[0027] 8, the utility model discloses the methanation, reforming and glass kiln are combined, and the heat of glass kiln flue gas is fully utilized for raw gas heat exchange, and the heat utilization rate is improved. BRIEF DESCRIPTION OF DRAWINGS

[0028] Figure 1 Structure diagram of zero-carbon glass kiln system. DETAILED DESCRIPTION

[0029] In order to make the purpose, technical scheme and advantages of the present application clearer, the technical scheme in the embodiments of the present application will be described clearly and completely below in combination with the drawings in the embodiments of the present application. Obviously, the described embodiments are part of the embodiments of the present application, rather than all the embodiments of the present application. Therefore, the detailed description of the embodiments of the present application provided in the drawings below is not intended to limit the scope of the claimed present application, but only represents selected embodiments of the present application. Based on the embodiments in the present application, all other embodiments obtained by those skilled in the art without creative labor fall within the scope of the present application.

[0030] A zero-carbon glass kiln system, as shown in Figure 1 includes a photovoltaic power generation device, an air separation device, a water electrolysis hydrogen production device, a mixer, a methanation device, a waste heat boiler I, a reforming device, a glass kiln, a waste heat boiler II and a dust and desulfurization device.

[0031] The photovoltaic power generation device is used to produce green power (green electricity) and provide electric energy for the air separation device and the water electrolysis hydrogen production device. The main principle of photovoltaic power generation is the photoelectric effect of semiconductors. When electromagnetic waves with a frequency higher than a certain specific frequency (the frequency is called the limiting frequency) irradiate, some substances inside the electronic absorption energy escape to form an electric current, i.e. photoelectricity. Photovoltaic power generation has the advantages of safety and reliability, no noise, no pollution emission, absolute cleanliness and no public hazards.

[0032] The air separation device uses green electricity provided by the photovoltaic power generation device as electric energy to produce oxygen and nitrogen. The air separation device produces oxygen and nitrogen. First, air is compressed, cooled, and liquefied. Oxygen and nitrogen components are separated by contacting gas and liquid on the rectification tower plate, exchanging mass and heat, condensing oxygen component with high boiling point from steam into liquid, and continuously transferring nitrogen component with low boiling point into steam, so as to continuously increase the nitrogen content in the rising steam and the oxygen content in the downward liquid, thereby separating oxygen and nitrogen. The purity of the oxygen produced by the air separation device is 99.6v% or more, the temperature is normal, and the pressure is 0.2-0.3 MPa. The purity of the nitrogen produced by the air separation device is 99.9v% or more, the temperature is normal, and the pressure is 0.2-0.3 MPa. Since the air separation device uses green electricity produced by the photovoltaic power generation device as electric energy, the oxygen produced is green oxygen, and the nitrogen produced is green nitrogen. The oxygen produced by the air separation device is mixed with oxygen from the water electrolysis hydrogen production device and circulating flue gas (carbon dioxide concentration is 95.0v% or more) from the glass kiln to form carbon-based oxygen-enriched gas for combustion support in the glass kiln. The nitrogen produced by the air separation device is partially decompressed to 0.05 MPa and then sent to the tin tank of the glass kiln as protective gas, and the rest is sold externally.

[0033] The water electrolysis hydrogen production device uses green electricity provided by the photovoltaic power generation device as electric energy to produce hydrogen and oxygen. Water electrolysis hydrogen production is a relatively convenient method for producing hydrogen. Direct current is passed into an electrolytic cell filled with electrolyte, and water molecules undergo electrochemical reaction on the electrode to decompose into nitrogen and oxygen. The purity of the hydrogen produced by the water electrolysis hydrogen production device is 99.8v% or more, the temperature is 90-100℃, and the pressure is 2.5-3.0 MPa. The purity of the oxygen produced by the water electrolysis hydrogen production device is 99.0v% or more, the temperature is 90-100℃, and the pressure is 2.5-3.0 MPa. Since the water electrolysis hydrogen production device uses green electricity produced by the photovoltaic power generation device as electric energy, the hydrogen produced is green hydrogen, and the oxygen produced is green oxygen. The hydrogen produced by the water electrolysis hydrogen production device is sent to the methanation device for methanation reaction. The oxygen produced by the water electrolysis hydrogen production device is decompressed to 0.2-0.3 MPa and then mixed with oxygen from the air separation device and circulating flue gas (carbon dioxide concentration is 95.0v% or more) from the glass kiln in a mixer to form carbon-based oxygen-enriched gas as a combustion support agent for combustion support in the glass kiln.

[0034] Water electrolysis hydrogen production reaction equation: 2H2O→2H2+O2

[0035] A mixer is used to mix oxygen from the air separation unit, oxygen from the water electrolysis hydrogen production unit and circulating flue gas from the glass furnace into carbon-based oxygen-enriched gas, which is used as a combustion-supporting agent for the glass furnace. The oxygen from the air separation unit has a purity of 99.6 vol% or more, a normal temperature and a pressure of 0.2-0.3 MPa. The oxygen from the water electrolysis hydrogen production unit has a purity of 99.0 vol% or more, a temperature of 90-100°C and a pressure of 0.2-0.3 MPa. The circulating flue gas from the glass furnace has a carbon dioxide concentration of 95.0 vol% or more, a temperature of 550-650°C and a pressure of 0.15-0.25 MPa. The oxygen from the air separation unit, the oxygen from the water electrolysis hydrogen production unit and the circulating flue gas from the glass furnace are mixed into carbon-based oxygen-enriched gas for use as a combustion-supporting agent for the glass furnace after the flow rates of the three are adjusted by adjusting valves. The carbon-based oxygen-enriched gas has an oxygen content of 21-30 vol%, a temperature of 460-480°C and a pressure of 0.05-0.10 MPa. The oxygen concentration is adjusted according to the requirements of different glass furnaces.

[0036] A methanation device is used to cause methanation reaction of hydrogen from the water electrolysis hydrogen production unit and circulating flue gas from the dust removal and desulfurization device. The hydrogen from the water electrolysis hydrogen production unit has a purity of 99.8 vol% or more, a temperature of 90-100°C and a pressure of 2.5-3.0 MPa. The circulating flue gas from the dust removal and desulfurization device has a carbon dioxide concentration of 95.0 vol% or more, a temperature of 250-300°C and a pressure of 2.5-3.0 MPa. The two are sent into the methanation device at a ratio of H2:CO2=4:1. Under the action of the methanation nickel-based catalyst, the hydrogen and carbon dioxide are catalytically converted to generate methane, and a large amount of heat is released. The generated methane has a purity of 94.0 vol% or more (calculated based on dry gas), a temperature of 390-410°C and a pressure of 2.5-3.0 MPa. The methane (containing saturated water vapor) is sent to waste heat boiler I.

[0037] Methanation reaction equation: 4H2+CO2→CH4+2H2O

[0038] Waste heat boiler I is used to recover the waste heat of the methane (containing saturated water vapor) from the methanation device and produce steam as a byproduct. The methane (containing saturated water vapor) from the methanation device has a temperature of 390-410°C. After the waste heat is recovered by the waste heat boiler I, the temperature is reduced to 240-260°C, and 1.5 MPa steam is produced as a byproduct, which is used for external sales. Because the suitable pressure for the reforming reaction is 0.5-1.0 MPa, the methane (containing saturated water vapor) after waste heat recovery is reduced to 0.5-1.0 MPa before being sent to the reforming device.

[0039] The reformer is used for the methane (containing saturated water vapor) sent by waste heat boiler I and part of the circulating flue gas sent by the glass furnace to generate the methane reforming reaction. The methane (containing saturated water vapor) sent by waste heat boiler I has the methane purity of 94.0% or above (calculated by dry gas), the temperature of 240-260°C and the pressure of 0.5-1.0 MPa. The circulating flue gas sent by the glass furnace has the carbon dioxide concentration of 95.0% or above, the temperature of 1300-1400°C and the pressure of 0.5-1.0 MPa. The circulating flue gas sent by the glass furnace enters the reformer in two ways. One way is to enter the heat storage grid of one side of the reformer to provide heat for the heat storage grid. The next round of the heat storage grid provides heat for the raw material gas of the reformer. After heat exchange, the temperature of the circulating flue gas is reduced to 250-300°C. After the pressure is reduced to 0.1-0.2 MPa, the circulating flue gas is sent to the dust removal and desulfurization device. The other way is that the methane (containing saturated water vapor) sent by waste heat boiler I and the circulating flue gas are sent into the heat storage grid of the other side of the reformer according to the CH4: CO2 volume ratio of 2:1 (the heat storage grid has been heated by the circulating flue gas of the previous round, and the heat storage grids of the two sides work alternately). The heat storage grid is heated to 900-1000°C. Under the action of the nickel-based catalyst at the pressure of 0.5-1.0 MPa, the methane, carbon dioxide and water vapor generate carbon monoxide and hydrogen through the methane reforming reaction. The CO: H2 volume ratio is about 3:5. The outlet temperature is 700-800°C, and the pressure is 0.5-1.0 MPa. The carbon monoxide and hydrogen are sent to the glass furnace as fuel.

[0040] Reforming reaction equation: CH4+H2O→CO+3H2

[0041] CH4+CO2→2CO+2H2

[0042] The glass furnace uses the carbon monoxide and hydrogen sent by the reformer as fuel (natural gas is used as fuel in the initial production period) and uses the carbon-based oxygen-rich sent by the mixer as a combustion aid to produce glass liquid. The carbon monoxide and hydrogen sent by the reformer have the CO: H2 volume ratio of about 3:5, the temperature of 700-800°C and the pressure of 0.5-1.0 MPa. The oxygen content of the carbon-based oxygen-rich sent by the mixer is 21-30%, the temperature is 460-480°C, and the pressure is 0.05-0.10 MPa. The carbon-based oxygen-rich sent by the mixer is heated to 700-800°C by the heat storage grid of one side of the glass furnace (the heat storage grid has been heated by the circulating flue gas of the previous round, and the heat storage grids of the two sides work alternately) and then sent into the glass furnace. The volume ratio of the fuel (carbon monoxide and hydrogen sent by the reformer) to the combustion aid (carbon-based oxygen-rich sent by the mixer) is about 1:2. In the glass furnace, the carbon monoxide and hydrogen are combusted under the combustion aid of the carbon-based oxygen-rich to provide heat for the glass furnace to produce glass liquid.

[0043] Carbon-based oxygen-enriched combustion reaction equation: 2CO + O2 + CO2 → 3CO2

[0044] 2H2 + O2 + CO2 → 2H2O + CO2

[0045] After the flue gas of the glass furnace is circulated and enriched for 3-5 hours, the carbon dioxide concentration reaches equilibrium, the carbon dioxide concentration is 95.0v% or more, the temperature is 1300-1400℃, and the pressure is 0.01-0.05MPa. The circulating flue gas is divided into two paths, one of which passes through the regenerator on the other side of the glass furnace to provide heat for the regenerator, and the next round of the regenerator provides heat for the carbon-based oxygen-enriched mixture sent by the mixer. After heat exchange, the circulating flue gas in this path is cooled to 550-650℃, pressurized to 0.15-0.25MPa, and sent to the mixer and waste heat boiler II. The other path does not pass through the regenerator of the glass furnace, the temperature is 1300-1400℃, the pressure is pressurized to 0.5-1.0MPa, and the reforming device is sent.

[0046] The waste heat boiler II is used to recover the waste heat of the circulating flue gas sent by the glass furnace and produce steam. The circulating flue gas sent by the glass furnace has a carbon dioxide concentration of 95.0v% or more, a temperature of 550-650℃, and a pressure of 0.15-0.25MPa. After waste heat recovery by the waste heat boiler II, the temperature is reduced to 250-300℃, the pressure is 0.1-0.2MPa, and 1.5-4.0MPa steam is produced as a byproduct for sale. The circulating flue gas after waste heat recovery is sent to the dust removal and desulfurization device.

[0047] The dust removal and desulfurization device is used to remove dust and desulfurize the circulating flue gas sent by the waste heat boiler II. The dust removal and desulfurization device consists of two parts, a high-temperature dust collector and a dry desulfurization equipment. The high-temperature dust collector uses cyclone separation for dust removal, and the dry desulfurization equipment uses zinc oxide desulfurization. The circulating flue gas first passes through the high-temperature dust collector to remove dust, and then passes through the dry desulfurization equipment to remove hydrogen sulfide. The circulating flue gas sent by the waste heat boiler II has a carbon dioxide concentration of 95.0v% or more, a temperature of 250-300℃, and a pressure of 0.1-0.2MPa. After dust removal and desulfurization, the circulating flue gas has a carbon dioxide concentration of 95.0v% or more, a temperature of 250-300℃, and a pressure of 0.05-0.10MPa. Part of it is pressurized to 2.5-3.0MPa and sent to the methanation device, and the rest is cooled and sold as carbon dioxide products.

[0048] Dry desulfurization reaction equation: ZnO + H2S → ZnS + H2O

[0049] The photovoltaic power generation device is connected with the air separation device and the water electrolysis hydrogen production device respectively; the nitrogen outlet of the air separation device is connected with the tin tank of the glass kiln and the nitrogen product storage tank respectively, and a pressure reducing valve is arranged on the connecting pipeline of the nitrogen outlet of the air separation device and the tin tank of the glass kiln; the oxygen outlet of the air separation device and the oxygen outlet of the water electrolysis hydrogen production device are connected with the mixer, a pressure reducing valve is arranged on the connecting pipeline of the oxygen outlet of the water electrolysis hydrogen production device and the mixer, and a flow detector F, a temperature detector T, a pressure detector P, a gas (oxygen) purity detector C and a flow regulating valve FIC are arranged on the connecting pipeline of the oxygen outlet of the air separation device, the oxygen outlet of the water electrolysis hydrogen production device and the mixer; the hydrogen outlet of the water electrolysis hydrogen production device is connected with the methanation device; the carbon-based oxygen-rich outlet of the mixer is connected with the regenerative grid A / B of the glass kiln and then connected to the glass kiln; the methane outlet of the methanation device is connected with the waste heat boiler I; the methane outlet of the waste heat boiler I is connected with the regenerative grid A / B of the reforming device and then connected to the reforming device, a pressure reducing valve is arranged on the connecting pipeline of the methane outlet of the waste heat boiler I and the regenerative grid A / B of the reforming device, and the steam outlet of the waste heat boiler I is connected with the steam utilization device; the carbon monoxide + hydrogen outlet of the reforming device is connected with the glass kiln; the circulating flue gas outlet of the glass kiln is connected with the regenerative grid B / A of the glass kiln and then connected to the waste heat boiler II, the mixer, the regenerative grid A / B of the reforming device and the regenerative grid B / A of the reforming device, respectively, and then connected to the reforming device, the dust and desulfurization device, respectively, a booster is arranged on the connecting pipeline of the regenerative grid B / A of the glass kiln and the waste heat boiler II, the mixer, the regenerative grid A / B of the reforming device and the regenerative grid B / A of the reforming device, flow detectors F, temperature detectors T, pressure detectors P, gas (carbon dioxide) purity detectors C and flow regulating valves FIC are arranged on the connecting pipeline of the regenerative grid B / A of the glass kiln and the mixer, and a pressure reducing valve is arranged on the connecting pipeline of the regenerative grid B / A of the reforming device and the dust and desulfurization device; the circulating flue gas outlet of the waste heat boiler II is connected with the dust and desulfurization device; the circulating flue gas outlet of the dust and desulfurization device is connected with the methanation device and the CO2 product storage tank, respectively, and a booster is arranged on the connecting pipeline of the circulating flue gas outlet of the dust and desulfurization device and the methanation device.

[0050] The zero-carbon glass kiln system is used to carry out a zero-carbon glass kiln process, which comprises the following steps:

[0051] (1) The photovoltaic power generation unit produces green electricity to power the air separation unit and the water electrolysis hydrogen production unit. The air separation unit uses the green electricity provided by the photovoltaic power generation unit to produce oxygen and nitrogen. The oxygen purity is above 99.6% (v%), at room temperature and a pressure of 0.2–0.3 MPa; the oxygen is sent to the mixer. The nitrogen purity is above 99.9% (v%), at room temperature and a pressure of 0.2–0.3 MPa. Some of the nitrogen is depressurized to 0.05 MPa and sent to the tin bath of the glass furnace as a protective gas; the remainder is sold externally. The water electrolysis hydrogen production unit uses the green electricity provided by the photovoltaic power generation unit to produce hydrogen and oxygen. The hydrogen purity is above 99.8% (v%), at a temperature of 90–100℃ and a pressure of 2.5–3.0 MPa; the hydrogen is sent to the methanation unit. The oxygen purity is above 99.0% (v%), at a temperature of 90–100℃ and a pressure of 2.5–3.0 MPa.

[0052] 3.0 MPa, oxygen pressure reduced to 0.2-0.3 MPa before being sent to the mixer.

[0053] (2) The mixer mixes the oxygen from the air separation unit and the water electrolysis unit with the circulating flue gas from the glass furnace to form a carbon-based oxygen-enriched mixture, which serves as the combustion aid for the glass furnace. The oxygen from the air separation unit has a purity of ≥99.6% at room temperature and a pressure of 0.2–0.3 MPa. The oxygen from the water electrolysis unit has a purity of ≥99.0% at a temperature of 90–100℃ and a pressure of 0.2–0.3 MPa. The circulating flue gas from the glass furnace has a carbon dioxide concentration of ≥95.0% at a temperature of 550–650℃ and a pressure of 0.15–0.25 MPa. The oxygen from the air separation unit, the oxygen from the water electrolysis hydrogen production unit, and the circulating flue gas from the glass furnace are all regulated by regulating valves. The resulting carbon-based oxygen-enriched mixture has a content of 21-30% v%, a temperature of 460-480℃, and a pressure of 0.05-0.10 MPa. The oxygen concentration is adjusted according to the requirements of different glass furnaces.

[0054] (3) The methanation unit reacts hydrogen from the water electrolysis hydrogen production unit with circulating flue gas from the dust removal and desulfurization unit. The hydrogen from the water electrolysis hydrogen production unit has a purity of ≥99.8 vol%, a temperature of 90–100 °C, and a pressure of 2.5–3.0 MPa. The circulating flue gas from the dust removal and desulfurization unit has a carbon dioxide concentration of ≥95.0 vol%, a temperature of 250–300 °C, and a pressure of 2.5–3.0 MPa. The two are fed into the methanation unit at a volume ratio of H2:CO2 = 4:1. Under the action of the nickel-based methanation catalyst, hydrogen and carbon dioxide are catalytically converted into methane, releasing a large amount of heat. The generated methane has a purity of ≥94.0 vol% (dry gas), a temperature of 390–410 °C, and a pressure of 2.5–3.0 MPa. The methane (containing saturated water vapor) is sent to waste heat boiler I.

[0055] (4) Waste heat boiler I recovers waste heat from the methane (containing saturated water vapor) sent by the methanation device and produces steam as a byproduct. The temperature of the methane (containing saturated water vapor) sent by the methanation device is 390-410°C, and after waste heat recovery by the waste heat boiler I, the temperature is reduced to 240-260°C, and 1.5 MPa steam is produced as a byproduct, which is sold externally. The methane (containing saturated water vapor) after waste heat recovery is reduced to 0.5-1.0 MPa and sent to the reformer.

[0056] (5) The reformer carries out a methane reforming reaction on the methane (containing saturated water vapor) sent by the waste heat boiler I and part of the circulating flue gas sent by the glass furnace. The methane (containing saturated water vapor) sent by the waste heat boiler I has a methane purity of 94.0% or more (calculated on dry gas), a temperature of 240-260°C, and a pressure of 0.5-1.0 MPa. The circulating flue gas sent by the glass furnace has a carbon dioxide concentration of 95.0% or more, a temperature of 1300-1400°C, and a pressure of 0.5-1.0 MPa. The circulating flue gas sent by the glass furnace is divided into two paths and enters the reformer. One path enters a heat storage chamber on one side of the reformer to provide heat for the heat storage chamber, which in the next round provides heat for the raw material gas of the reformer. After heat exchange, the temperature of the circulating flue gas is reduced to 250-300°C, and after being reduced to 0.1-0.2 MPa, it is sent to the dust removal and desulfurization device. The other path and the methane (containing saturated water vapor) sent by the waste heat boiler I are sent to the heat storage chamber on the other side of the reformer (the heat storage chamber has been heated by the circulating flue gas in the previous round, and the two heat storage chambers work alternately) at a CH4:CO2 volume ratio of 2:1. After heat exchange by the heat of the heat storage chamber, the temperature is raised to 900-1000°C. Under the action of a nickel-based catalyst at a pressure of 0.5-1.0 MPa, methane, carbon dioxide, and water vapor undergo a methane reforming reaction to generate carbon monoxide and hydrogen, with a CO:H2 volume ratio of about 3:5. The outlet temperature is 700-800°C, and the pressure is 0.5-1.0 MPa. The mixture is sent to the glass furnace as fuel.

[0057] (6) The glass furnace uses carbon monoxide and hydrogen sent by the reformer as fuel (natural gas is used as fuel in the initial stage of production), and carbon-based oxygen-rich mixture sent by the mixer as a combustion aid to produce glass liquid. The carbon monoxide and hydrogen sent by the reformer have a CO:H2 volume ratio of about 3:5, a temperature of 700-800°C, and a pressure of 0.5-1.0 MPa. The oxygen content of the carbon-based oxygen-rich mixture sent by the mixer is 21-30%, the temperature is 460-480°C, and the pressure is 0.05-0.10 MPa. The carbon-based oxygen-rich mixture sent by the mixer is first heated to 700-800°C by a heat storage chamber on one side of the glass furnace (the heat storage chamber has been heated by the circulating flue gas in the previous round, and the two heat storage chambers work alternately). After heat exchange, the temperature is raised to 700-800°C, and the pressure is reduced to 0.05-0.10 MPa. The mixture is then sent to the glass furnace as a combustion aid.

[0058] 800℃ after sending into the glass kiln. Fuel (carbon monoxide and hydrogen from the reformer) : combustion-supporting agent (carbon-based oxygen-rich mixture from the mixer) volume ratio = about 1:2. In the glass kiln, carbon monoxide and hydrogen are combusted under the combustion-supporting of carbon-based oxygen-rich mixture to provide heat for the glass kiln to produce glass liquid.

[0059] After 3-5 hours of circulating enrichment, the carbon dioxide concentration of the flue gas of the glass kiln reaches equilibrium, the carbon dioxide concentration is 95.0v% or more, the temperature is 1300-1400℃, and the pressure is 0.01-0.05MPa. The circulating flue gas is divided into two paths, one path passes through the other side of the glass kiln regenerator to provide heat for the regenerator, and the next round of the regenerator provides heat for the carbon-based oxygen-rich mixture from the mixer. After heat exchange, the circulating flue gas in this path is cooled to 550-650℃, pressurized to 0.15-0.25MPa, and sent to the mixer and waste heat boiler II; the other path does not pass through the glass kiln regenerator, the temperature is 1300-1400℃, and the pressure is pressurized to 0.5-1.0MPa, and is sent to the reformer.

[0060] (7) The waste heat boiler II recovers the waste heat of the circulating flue gas from the glass kiln and produces steam as a byproduct. The circulating flue gas from the glass kiln has a carbon dioxide concentration of 95.0v% or more, a temperature of 550-650℃, and a pressure of 0.15-0.25MPa. After waste heat recovery in the waste heat boiler II, the temperature is reduced to 250-300℃, the pressure is 0.1-0.2MPa, and 1.5-4.0MPa steam is produced as a byproduct for sale. The circulating flue gas after waste heat recovery is sent to the dust removal and desulfurization device.

[0061] (8) The dust removal and desulfurization device removes dust and desulfurizes the circulating flue gas from the waste heat boiler II. The circulating flue gas first passes through the high-temperature dust remover in the dust removal and desulfurization device to remove dust, and then passes through the dry desulfurization equipment in the dust removal and desulfurization device to remove hydrogen sulfide. The circulating flue gas from the waste heat boiler II has a carbon dioxide concentration of 95.0v% or more, a temperature of 250-300℃, and a pressure of 0.1-0.2MPa. After dust removal and desulfurization, the circulating flue gas has a carbon dioxide concentration of 95.0v% or more, a temperature of 250-300℃, and a pressure of 0.05-0.10MPa. Part of it is pressurized to 2.5-3.0MPa and sent to the methanation device, and the rest is cooled and sold as carbon dioxide product.

[0062] In the initial stage, the glass kiln uses natural gas as fuel and air as combustion-supporting agent. After the flue gas is generated, carbon-based oxygen-rich mixture composed of flue gas and oxygen (produced by air separation device and water electrolysis hydrogen production device) gradually replaces air for combustion-supporting. After 3-5 hours of circulating enrichment, the carbon dioxide concentration in the circulating flue gas reaches equilibrium, the carbon dioxide concentration is 95.0v% or more, and the methanation device, reformer, waste heat boiler I, waste heat boiler II, and dust removal and desulfurization device are all put into use, and the system enters normal operating state.

Claims

1. A zero-carbon glass furnace system, characterized in that, It includes photovoltaic power generation equipment, air separation equipment, water electrolysis hydrogen production equipment, mixer, methanation equipment, waste heat boiler I, reforming equipment, glass furnace, waste heat boiler II, and dust removal and desulfurization equipment; Photovoltaic power generation devices are used to produce green electricity to power air separation units and water electrolysis hydrogen production units. Air separation unit, used to produce oxygen and nitrogen; A water electrolysis hydrogen production unit, used to produce hydrogen and oxygen; A mixer is used to mix oxygen from the air separation unit, oxygen from the water electrolysis hydrogen production unit, and circulating flue gas from the glass furnace into a carbon-based oxygen-enriched mixture. The methanation unit is used to react hydrogen from the water electrolysis hydrogen production unit and circulating flue gas from the dust removal and desulfurization unit with methanation. Waste heat boiler I is used to recover the waste heat of methane containing saturated water vapor from the methanation unit and produce steam as a byproduct. The reforming unit is used to reform methane containing saturated steam from waste heat boiler I and part of the circulating flue gas from the glass furnace into methane. Glass furnaces use carbon monoxide and hydrogen from the reforming unit as fuel and carbon-based oxygen-enriched gas from the mixer as a combustion aid to produce molten glass. Waste heat boiler II is used to recover the waste heat from the circulating flue gas sent from the glass kiln and produce steam as a by-product. The dust removal and desulfurization unit is used to remove dust and desulfurize the circulating flue gas sent from waste heat boiler II; The photovoltaic power generation unit is connected to the air separation unit and the water electrolysis hydrogen production unit, respectively. The nitrogen outlet of the air separation unit is connected to the tin bath and nitrogen product storage tank of the glass furnace, respectively. A pressure reducing valve is installed on the connecting pipe between the nitrogen outlet of the air separation unit and the tin bath of the glass furnace. The oxygen outlets of the air separation unit and the water electrolysis hydrogen production unit are both connected to a mixer. A pressure reducing valve is installed on the connecting pipe between the oxygen outlet of the water electrolysis hydrogen production unit and the mixer. Flow meters and temperature sensors are installed on the connecting pipes between the oxygen outlets of the air separation unit and the water electrolysis hydrogen production unit and the mixer. Detectors, pressure detectors, oxygen purity detectors, flow control valves; the hydrogen outlet of the water electrolysis hydrogen production unit is connected to the methanation unit; the carbon-based oxygen-enriched outlet of the mixer is connected to the A / B heat storage compartment of the glass furnace via a switching connection, and then connected to the glass furnace; the methane outlet of the methanation unit is connected to waste heat boiler I; the methane outlet of waste heat boiler I is connected to the A / B heat storage compartment of the reforming unit via a switching connection, and then connected to the reforming unit; a pressure reducing valve is installed on the connecting pipe between the methane outlet of waste heat boiler I and the A / B heat storage compartment of the reforming unit; the steam outlet of waste heat boiler I is connected to the steam utilization unit. Connections: The carbon monoxide + hydrogen outlet of the reforming unit is connected to the glass furnace; the circulating flue gas outlet of the glass furnace is connected to the heat storage cells B / A of the glass furnace via a switching connection, then to waste heat boiler II and the mixer, and to the heat storage cells A / B of the reforming unit via a switching connection, then to the reforming unit, and to the dust removal and desulfurization unit via a switching connection, with a booster compressor installed on the connecting pipes between the heat storage cells B / A of the glass furnace and waste heat boiler II and the mixer, and a flow meter and temperature sensor installed on the connecting pipes between the heat storage cells B / A of the glass furnace and the mixer. The system includes a temperature detector, a pressure detector, a carbon dioxide purity detector, a flow regulating valve, and booster compressors installed on the connecting pipes of the heat storage cells A / B of the glass furnace and the reforming unit, and the heat storage cells B / A of the reforming unit. Pressure reducing valves are installed on the connecting pipes of the heat storage cells B / A of the reforming unit and the dust removal and desulfurization unit. The circulating flue gas outlet of waste heat boiler II is connected to the dust removal and desulfurization unit. The circulating flue gas outlet of the dust removal and desulfurization unit is connected to the methanation unit and the CO2 product storage tank, respectively. A booster compressor is installed on the connecting pipe between the circulating flue gas outlet of the dust removal and desulfurization unit and the methanation unit.

2. The zero-carbon glass furnace system according to claim 1, characterized in that, The dust removal and desulfurization device consists of two parts: a high-temperature dust collector and a dry desulfurization device. The high-temperature dust collector uses cyclone separation for dust removal, and the dry desulfurization equipment uses zinc oxide desulfurization.

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