Integrated Energy Supply System Based on the Hydrogen Energy Storage System Using the Exhaust Smoke of Gas Engines

Abstract

The invention discloses an integrated energy supply system based on a gas engine waste smoke hydrogen energy storage system, which relates to the field of energy supply. The total amount of waste smoke of the gas engine is calculated, and the first amount of flue gas required by the chilled and hot water unit is calculated. When the total amount of waste smoke of the gas engine is less than or equal to the first amount of flue gas required by the chilled and hot water unit, all the flue gas is introduced into the lithium bromide absorption type chilled and hot water unit. If it is greater than the first amount of flue gas required by the lithium bromide absorption type chilled and hot water unit, the remaining flue gas is introduced into the waste smoke boiler to generate steam. The second amount of flue gas discharged from the hydrogenation reaction combustion furnace and entering the waste smoke boiler is determined, the total amount of flue gas entering the waste smoke boiler is calculated, the amount of natural gas raw material required is calculated according to the mass flow rate of steam and the total carbon flow rate in natural gas, and natural gas is introduced into the hydrogenation reaction combustion furnace according to the amount of natural gas raw material. The invention integrates the cold, heat and power cogeneration of natural gas reforming hydrogen production equipment, waste smoke boilers, gas engines, etc. and can be directly applied to building energy supply, and forms an effective recycling.

Description

Technical Field

[0001] The present invention relates to the technical field of energy supply, and in particular to an integrated energy supply system based on a gas engine flue gas hydrogen energy storage system. Background Art

[0002] As a clean and carbon-free new energy, hydrogen energy will play an increasingly important role in the building field in the foreseeable future. At present, the general equipment for conventional natural gas reforming to produce hydrogen is large in size and is mostly used in industry. There is no perfect, feasible and implementable solution for how to apply it to the building field.

[0003] At the same time, there is no effective recycling mechanism for the flue gas waste heat generated during the power generation process of gas engines. While causing secondary energy waste, it also increases the embodied carbon emissions of the system. How to effectively combine gas engine power generation, waste heat recovery, hydrogen energy storage and buildings will become a topic to be solved. Summary of the Invention

[0004] Aiming at the deficiencies in the prior art, the present invention provides an integrated energy supply system based on a gas engine flue gas hydrogen energy storage system that is effectively combined with a building energy supply system. It integrates cold, heat and power cogeneration such as natural gas reforming hydrogen production equipment, flue gas boilers and gas engines, and can be directly applied to building energy supply to form an effective recycling.

[0005] The integrated energy supply system based on a gas engine flue gas hydrogen energy storage system includes a gas engine, a reforming hydrogen production device and a lithium bromide absorption type cold and hot water unit. Among them,

[0006] The input end of the lithium bromide absorption type cold and hot water unit is connected to the high-temperature flue gas channel of the gas engine, and its output end is connected to the cold and hot water pipes for building air conditioning;

[0007] The reforming hydrogen production device includes a flue gas boiler, a hydrogenation reaction combustion furnace and a medium temperature shift furnace. The first input end of the flue gas boiler is connected to the high-temperature flue gas pipeline of the gas engine, and the second input end of the flue gas boiler is connected to the flue gas channel of the hydrogenation reaction combustion furnace; the medium temperature shift furnace is connected to the rear end of the hydrogenation reaction combustion furnace; the hydrogen output end at the end of the reforming hydrogen production device is connected to a hydrogen fuel cell;

[0008] Calculate the total gas engine exhaust volume per unit time, and calculate the required first flue gas volume of the lithium bromide absorption type cold and hot water unit per unit time;

[0009] When the total gas engine exhaust volume is less than or equal to the required first flue gas volume of the lithium bromide absorption type cold and hot water unit, all the flue gas is introduced into the lithium bromide absorption type cold and hot water unit;

[0010] When the total exhaust gas volume of the gas engine is greater than the first flue gas volume required by the lithium bromide absorption type cold and hot water unit, the lithium bromide absorption type cold and hot water unit is fully introduced with the flue gas volume required by the lithium bromide absorption type cold and hot water unit, and the remaining flue gas is introduced into the surplus flue gas boiler to generate steam; the second flue gas volume discharged from the hydrogenation reaction combustion furnace and entering the surplus flue gas boiler is determined according to the working state of the hydrogenation reaction combustion furnace; the total flue gas inlet volume of the surplus flue gas boiler is calculated according to the total exhaust gas volume, the first flue gas volume and the second flue gas volume.

[0011] The mass flow rate of the generated steam is calculated according to the total flue gas inlet volume, the required natural gas raw material volume is calculated according to the mass flow rate of the steam, and natural gas is introduced into the hydrogenation reaction combustion furnace according to the natural gas raw material volume.

[0012] The beneficial effects include: 1) Compared with the existing waste heat recovery and hydrogen production devices, some of the existing devices only complete the production of steam through waste heat recovery technology, and then combine with natural gas for a mixed reaction to obtain hydrogen. The purpose of the present invention is to effectively utilize the waste heat and surplus flue gas of the gas engine combined cooling, heating and power supply system and organically combine it with the natural gas reforming hydrogen production method. When the building cooling and heating load demand is insufficient in the transitional season of the gas engine combined cooling, heating and power supply system, the sufficient surplus flue gas of the gas engine can be effectively recovered through the surplus flue gas boiler to produce high-temperature steam for hydrogenation reaction in natural gas reforming hydrogen production. On the one hand, it effectively reduces the hydrogen production cost of the conventional natural gas reforming hydrogen production method, mainly saving the fuel cost of the steam used for hydrogen production to a great extent. On the other hand, it also effectively avoids the waste of the surplus flue gas and waste heat of the gas engine when the building cooling and heating load demand is small. In terms of surplus flue gas utilization, in addition to using the high-temperature surplus flue gas of the gas engine, the present invention also effectively integrates and utilizes the flue gas in the hydrogenation reaction combustion furnace, further saving the heating raw material cost of hydrogen production, and can save the raw material cost by 30% - 50%. In addition, when the present energy supply device and method are applied to actual buildings, through the method of the present application, according to the hourly cooling, heating and power loads of different buildings, the hourly hydrogen production volume and the required natural gas raw material volume can be accurately calculated and predicted.

[0013] 2) When natural gas reforming hydrogen production can be miniaturized and modularized, through the system proposed in the present application, only the modularized small-scale natural gas reforming hydrogen production equipment, surplus flue gas boiler and gas engine combined cooling, heating and power supply need to be directly combined on the construction site of the building to be directly used on the building, which has practical engineering application value.

[0014] This application selects a hydrogen fuel cell that can effectively utilize hydrogen nearby. Applying the hydrogen fuel cell in this system can directly supply power to the building, and secondly, it can effectively recover the waste heat of the hydrogen fuel cell and generate heat for the hot water storage tank used in the building. The innovative design of this system takes into account that if the generated hydrogen is transported over a long distance, its economy is poor, and only when the generated hydrogen is directly utilized nearby can higher economic benefits be achieved. Through improvements in structure and method, this invention realizes the integrated supply of cooling, heating, and electricity of the reforming hydrogen production equipment, waste gas boiler, gas engine, etc. to supply comprehensive energy to the entire building or building park.

[0015] As a preferred implementation, a method for calculating the required natural gas raw material quantity according to the mass flow rate of water vapor and the total carbon flow rate in natural gas includes:

[0016] Calculate the total carbon flow rate in natural gas according to the proportion of each component gas in natural gas;

[0017] Determine the water-carbon ratio of natural gas reforming to hydrogen production. According to the water-carbon ratio calculation formula, combined with the total carbon flow rate in natural gas and the mass flow rate of water vapor, calculate the volume flow rate of natural gas;

[0018] According to the chemical reaction formula of natural gas reforming to hydrogen production, combined with the total carbon flow rate in natural gas and the mass flow rate of water vapor generated by the waste gas boiler, calculate the required natural gas raw material quantity to be introduced.

[0019] As a preferred implementation, a method for calculating the total exhaust gas volume of a gas engine per unit time includes the following steps:

[0020] Determine the hourly electricity load demand of the building. According to the green power generation amount of the building, the power generation amount of the hydrogen fuel cell, and the rated power generation amount of the gas engine under full load, calculate the hourly power generation amount of the actual gas engine, as shown in the following formula;

[0021]

[0022] Where P engine (kW) is the power generation amount of the gas engine, E FL (kW) is the rated power generation amount of the gas engine under full load, E L (kW) is the hourly electricity load of the building, E P (kW) is the green power generation amount, E FC (kW) is the power generation amount of the hydrogen fuel cell;

[0023] Among them, green power includes solar energy or wind energy connected to the building;

[0024] Then, determine the total exhaust gas volume of the gas engine generated by the gas engine's power generation per hour according to the hourly power generation amount of the gas engine.

[0025] As a preferred implementation, the total inlet flue gas volume M (kg / h) of the residual flue gas boiler is calculated based on the total exhaust gas volume, the first flue gas volume, and the second flue gas volume, as shown in the following formula: smoke (kg / h), as shown in the following formula:

[0026]

[0027] In the formula, M T (kg / h) is the total exhaust gas volume of the gas engine per unit time, M C / H (kg / h) is the first flue gas volume required for cooling or heating of the lithium bromide absorption chiller, M b (kg / h) is the second flue gas volume that enters the residual flue gas boiler after being discharged from the hydrogenation reaction combustion furnace.

[0028] As a preferred implementation, the mass flow rate of the generated water vapor is calculated based on the total inlet flue gas volume, and is achieved through the following formula:

[0029]

[0030] M steam —The mass flow rate of the water vapor generated by the residual flue gas boiler (kg / h);

[0031] ΔQ—The recoverable flue gas residual heat of the residual flue gas boiler (kJ / h);

[0032] h1—The enthalpy value of water vapor during hydrogen reaction (kJ / kg);

[0033] h2—The enthalpy value of industrial water at room temperature (kJ / kg);

[0034] C—The mass specific heat capacity of the flue gas (kJ / (kg·°C));

[0035] M smoke —The flue gas volume entering the residual flue gas boiler (kg / h);

[0036] t1—The average temperature of the flue gas at the inlet of the residual flue gas boiler (°C);

[0037] t0—The average temperature of the flue gas at the outlet of the residual flue gas boiler (°C);;

[0038] α—The flue gas heat loss coefficient.

[0039] As a preferred implementation, according to the chemical reaction formula of natural gas to hydrogen, combined with the total carbon flow in natural gas and the mass flow rate of the water vapor generated by the residual flue gas boiler, the amount of natural gas raw material to be introduced is calculated, specifically through the following formula:

[0040] The total carbon flow in natural gas is calculated as follows:

[0041] ∑V carbon =γ CH4 +γC2H6 ×2 + γ C3H8 ×3 + γ C4H10 ×4,

[0042] where ∑V carbon is the total carbon flow in natural gas, and γ CH4 is the volume percentage of methane in natural gas, γ C2H6 is the volume percentage of ethane, γ C3H8 is the volume percentage of propane, γ C4H10 is the volume percentage of butane;

[0043] Determine the water-carbon ratio for hydrogen production from natural gas. Calculate the natural gas volume flow according to the water-carbon ratio calculation formula in combination with the total carbon flow and steam volume flow in natural gas as follows:

[0044]

[0045] where ξ is the water-carbon ratio, determined as a constant according to experience, and V natural is the natural gas volume flow (Nm 3 / h), and V steam is the steam volume flow (Nm 3 / h).

[0046] As a preferred embodiment, the reforming hydrogen production device further includes a natural gas pipeline, a desulfurizer, a desulfurized natural gas and steam mixer, a gas-liquid separator, a hydrogen purification device, and an exhaust gas collector. Among them,

[0047] The first input end of the desulfurized natural gas and steam mixer is connected to the steam output end of the residual heat boiler, and the output end of the desulfurized natural gas and steam mixer is connected to the hydrogenation reaction combustion furnace;

[0048] The first output end of the natural gas pipeline is connected to the desulfurizer, and the output end of the desulfurizer is connected to the second input end of the desulfurized natural gas and steam mixer;

[0049] The hydrogenation reaction combustion furnace includes a high-temperature reaction furnace and a flue gas channel. The input end of the high-temperature reaction furnace is connected to the output end of the desulfurized natural gas and steam mixer, and the flue gas output end of the flue gas channel is connected to the residual heat boiler; the output end of the high-temperature reaction furnace is connected to the input end of the medium-temperature shift furnace, the output end of the medium-temperature shift furnace is connected to the input end of the gas-liquid separator, and the output end of the gas-liquid separator is connected to the input end of the hydrogen purification device;

[0050] The first output end of the hydrogen purification device is connected to the hydrogen energy power generation device, the second output end of the hydrogen purification device is connected to the exhaust gas collector, and the output end of the exhaust gas collector is connected to the natural gas pipeline.

[0051] As a preferred embodiment, it further includes a hydrogen compressor and a natural gas compressor,

[0052] The input end of the hydrogen compressor is connected to the hydrogen purification device, and the output end of the hydrogen compressor is connected to the hydrogen energy power generation device;

[0053] The input end of the natural gas compressor is connected to the natural gas pipeline, and the output end of the natural gas compressor is connected to the input end of the desulfurizer.

[0054] As a preferred implementation, it further includes a first heat exchanger, which is installed in the connecting pipeline between the high-temperature reactor and the desulfurized natural gas and steam mixer;

[0055] A second heat exchanger, which includes a first cooling channel and a second cooling channel. The first cooling channel is installed in the connecting pipeline between the desulfurizer and the high-temperature reactor, and the second cooling channel is installed in the connecting pipeline between the compressor and the intermediate shift furnace;

[0056] A third heat exchanger, which is installed in the connecting pipeline between the gas-liquid separator and the intermediate shift furnace.

[0057] As a preferred implementation, it further includes a hot water storage tank. One end of the third heat exchanger is the cooling water input end, and the other end outputs to one of the input ends of the hot water storage tank. The other input end of the hot water storage tank is connected to the heat energy output end of the hydrogen energy power generation device. Description of the Drawings

[0058] In order to more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the following will briefly introduce the drawings required for use in the description of the embodiments or the prior art. Obviously, the following drawings are only some embodiments of the present invention. For those of ordinary skill in the art, without creative efforts, other drawings can also be obtained based on these drawings.

[0059] Figure 1 is the overall structure diagram of the integrated energy supply system based on the waste smoke hydrogen energy storage system of the gas engine;

[0060] Figure 2 is the total carbon flow and natural gas hydrogen production calculation flow chart;

[0061] Figure 3 is the flow chart of natural gas raw material quantity calculation and hydrogen production quantity calculation. Detailed Embodiments

[0062] The following further elaborates on the present invention in conjunction with the embodiments. The following embodiments are explanations of the present invention, and the present invention is not limited to the following embodiments. Any changes or substitutions within the technical scope disclosed by the present invention should be covered within the protection scope of the present invention.

[0063] The integrated energy supply system based on the waste smoke hydrogen energy storage system of the gas engine, refer to Figure 1, including a gas engine, a reforming hydrogen production device, and a lithium bromide absorption chiller-heater, where

[0064] The input end of the lithium bromide absorption chiller-heater is connected to the high-temperature flue gas channel of the gas engine, and its output end is connected to the chilled and hot water pipes for building air conditioning;

[0065] The reforming hydrogen production device includes a surplus flue gas boiler, a hydrogenation reaction combustion furnace, and a medium temperature shift furnace. The first input end of the surplus flue gas boiler is connected to the high-temperature flue gas pipeline of the gas engine, and the second input end of the surplus flue gas boiler is connected to the flue gas channel of the hydrogenation reaction combustion furnace; the medium temperature shift furnace is connected to the rear end of the hydrogenation reaction combustion furnace; the hydrogen output end at the end of the reforming hydrogen production device is connected to a hydrogen fuel cell;

[0066] Calculate the total amount of flue gas discharged by the gas engine per unit time, and calculate the required first amount of flue gas for the lithium bromide absorption chiller-heater per unit time;

[0067] When the total amount of flue gas discharged by the gas engine is less than or equal to the required first amount of flue gas for the lithium bromide absorption chiller-heater, then all the flue gas is introduced into the lithium bromide absorption chiller-heater;

[0068] When the total amount of flue gas discharged by the gas engine is greater than the required first amount of flue gas for the lithium bromide absorption chiller-heater, then the required amount of flue gas for the lithium bromide absorption chiller-heater is introduced into it in full, and the remaining flue gas is introduced into the surplus flue gas boiler to generate steam; determine the second amount of flue gas discharged from the hydrogenation reaction combustion furnace and entering the surplus flue gas boiler according to the working state of the hydrogenation reaction combustion furnace; calculate the total amount of flue gas entering the surplus flue gas boiler based on the total amount of flue gas discharged, the first amount of flue gas, and the second amount of flue gas;

[0069] Calculate the mass flow rate of the generated steam based on the total amount of flue gas entering, calculate the hydrogen production amount based on the mass flow rate of the steam, calculate the required amount of natural gas raw material based on the hydrogen production amount, and introduce natural gas into the hydrogenation reaction combustion furnace according to the amount of natural gas raw material.

[0070] Combined with reference Figure 2 and Figure 3 Understand the following disclosure.

[0071] (1) Calculate the total amount of flue gas discharged by the gas engine per unit time, with the following formula:

[0072] The gas engine can use natural gas to generate electricity and produce high-temperature flue gas simultaneously. The calculation methods for electricity generation and heat are as follows:

[0073] P engine =V engine ×Q gas ×η engine / 3.6 (1)

[0074]

[0075] In the formula, Pengine (kW) is the power generation of the gas engine, V engine (m 3 / h) is the natural gas consumption of the gas engine, Q gas (MJ / m 3 ) is the calorific value of natural gas, η engine is the power generation efficiency of the gas engine, Q engine (kW) is the heat recovered by the waste heat boiler from the high-temperature waste smoke of the gas engine, η L is the heat loss rate of the gas engine.

[0076] Specifically, the method for calculating the total waste smoke volume of the gas engine per unit time is to determine the hourly electricity load demand of the building, calculate the hourly power generation of the actual gas engine based on the green power generation, hydrogen fuel cell power generation and the rated power generation of the gas engine at full load in the building, and then determine the total flue gas volume M T (kg / h) generated by the gas engine during power generation.

[0077] Among them, green power includes solar energy or wind energy connected to the building.

[0078] The calculation method of the hourly power generation of the gas engine is as follows:

[0079] First of all, the power generation P engine (kwh / h) of the gas engine is determined according to the performance of the equipment and the power supply configuration method set in this study, that is, in order to operate safely, the load rate of the gas engine needs to be maintained at 50% - 100%. After the gas engine supplies power to the building, the power is then supplied by solar and wind power. If the power is still insufficient, commercial power is supplied. Therefore, the power generation P engine (kWh / h) of the gas engine can be inferred to be determined by the following formula:

[0080]

[0081] In the formula, P engine (kW) is the power generation of the gas engine, E FL (kW) is the rated power generation of the gas engine at full load, E L (kW) is the hourly electricity load of the building, E P (kW) is the green power generation, E FC (kW) is the power generation of the hydrogen fuel cell. For the safe operation of the gas engine, its operating load generally needs to be maintained above 50%. When the power generation of the gas engine is known, the natural gas consumption of the gas engine can be calculated using the aforementioned formula (1).

[0082] Specifically, taking solar power generation as an example of green power, renewable energy solar power generation E is preferentially used in building power supply P(kW). Since the load factor of the gas engine needs to be maintained above 50%, when E L -E P -E FC ≤E FL ×50%, the power generation of the gas engine is E FL ×50%; when E FL ×50% < E L -E P -E FC ≤E FC at this time, the power generation of the gas engine is E L -E P -E FC ; when E L -E P -E FC >E FL at this time, the power generation of the gas engine is the total rated power generation E FL under full load operation. When E L - P engine - E P -E FC ≤0, that is, when the sum of the power generation of the gas engine, solar power generation and hydrogen fuel cell power generation cannot cover the electrical load demand of the building, the insufficient power is all supplemented by commercial power EC. If there is surplus power generation, the surplus power is all used to provide the stable power load required for compressing gas by hydrogen or natural gas compressors. Among them, the solar power generation and the power generation of the hydrogen fuel cell can be obtained by the corresponding formulas (5) and (6), and the hourly electrical load E L (kW) of the building can be obtained by combining the building historical data and survey data.

[0083] The method for calculating the total exhaust gas volume of the gas engine according to the power generation of the gas engine is as follows: According to the analysis of the gas engine equipment performance data provided by the equipment manufacturer, the flue gas volume M T (kg / h) of the gas engine is calculated as shown in formula (4).

[0084]

[0085] In the formula, M T (kg / h) is the total exhaust gas volume of the gas engine, is the load factor of the gas engine, and the load factor of the gas engine is the ratio of the actual power generation of the gas engine to the rated full load power generation, and E TGE (kW) is the rated full load power generation.

[0086] Among them, regarding green power, in this application, taking solar panels as an example, the solar power generation calculation formula is as follows:

[0087] E P = HA ×S×K1×K2 (5)

[0088] In the formula, E p is the power generation of the solar panel (kW), H A is the solar radiation per unit area (kW / m 2 ), S is the area of the solar panel (m 2 ), K1 is the component conversion efficiency (generally 16 - 18%, 17% is taken in this application); K2 is the overall system efficiency (generally 75% - 85%, 80% is taken in this application). In addition, H A (kW / m 2 ) data is obtained from the surveyed climate data.

[0089] Among them, the calculation of the power generation of the hydrogen fuel cell is specifically as follows in Formula (6) and Formula (7):

[0090] E FC = V H2 ×Q H2 ×η EFC / 3.6 (6)

[0091] Q FC = V H2 ×Q H2 ×η WFC / 3.6 (7)

[0092] In the formula, E FC (W) is the power generation of the hydrogen fuel cell, V H2 (Nm 3 / h) is the hydrogen volume entering the hydrogen fuel cell for power generation, Q H2 (MJ / m 3 ) is the calorific value of hydrogen, η EFC is the power generation efficiency of the hydrogen fuel cell, η WFC is the heat recovery efficiency of the hydrogen fuel cell.

[0093] According to the total exhaust gas volume M T (kg / h) of the gas engine, the first flue gas volume M C / H (kg / h) and the second flue gas volume M b (kg / h), calculate the total flue gas inlet volume M smoke (kg / h) of the economizer boiler through the following formula (8): M smoke

[0094]

[0095] In the formula, M T (kg / h) is the total exhaust gas volume of the gas engine, M C / HM (kg / h) is the first flue gas volume required for cooling or heating by the lithium bromide absorption chiller / heater. b M (kg / h) is the second flue gas volume that enters the afterheat boiler after being discharged from the hydrogenation reaction combustion furnace.

[0096] When the building has heating and cooling load requirements, a part of the gas engine flue gas volume enters the lithium bromide absorption chiller / heater to produce chilled and hot water for building air conditioning, that is, the first flue gas volume M (kg / h). C / H The remaining gas engine flue gas volume M T - M C / H (kg / h) all enters the afterheat boiler to be used for producing steam for hydrogen production.

[0097] The total incoming flue gas volume M (kg / h) that enters the afterheat boiler to produce steam, in addition to that from the gas engine, also includes the second flue gas volume M (kg / h) that is discharged from the hydrogenation reaction combustion furnace and enters the afterheat boiler. When M smoke - M b (kg / h) < 0, it means that the flue gas volume produced by the gas engine is only enough to fully meet the heating and cooling load requirements of the building. At this time, the flue gas volume that enters the afterheat boiler to produce steam for hydrogen production is only M (kg / h) from the hydrogenation reaction furnace; when M T - M C / H ≥0, it means that in addition to meeting the heating and cooling load requirements of the building, the flue gas volume produced by the gas engine has a surplus. At this time, the total incoming flue gas volume M (kg / h) of the afterheat boiler flue is M b - M T + M C / H . If the current hydrogenation reaction burner is in operation, the total incoming flue gas volume includes the second flue gas volume M smoke (kg / h), and if the current hydrogenation reaction burner is not in operation, the second flue gas volume M T - M C / H + M b . If the current hydrogenation reaction burner is in operation, the total incoming flue gas volume includes the second flue gas volume M b (kg / h), and if the current hydrogenation reaction burner is not in operation, the second flue gas volume M b is 0.

[0098] A more specific description shows that the first flue gas volume required to produce chilled and hot water for building air conditioning by the lithium bromide absorption chiller / heater can be calculated by the following formula (9).

[0099]

[0100] where M (kg / h) is the flue gas volume required for cooling or heating by the lithium bromide absorption chiller / heater, h C / H (kJ / kg) is the flue gas enthalpy value that enters the lithium bromide absorption chiller / heater, h in (kJ / kg) is the flue gas enthalpy value that leaves the lithium bromide absorption chiller / heater, and COP out (kJ / kg) C / His the coefficient of performance (COP) of the lithium bromide absorption type cold and hot water unit, and this value is a constant. Q C / H (kWh / h) is the hourly cooling load or heating load of different types of buildings. Through investigation, the hourly cooling load or heating load values of different types of buildings can be obtained, and these values are the product of the daily cooling or heating load value and the hourly load percentage. Among them, h in (kJ / kg) and h out (kJ / kg) are calculated through the following formula (10).

[0101] h S = 11.157×t - 306.2 (10)

[0102] In the formula, h S (kJ / kg) is the flue gas enthalpy value, and t (℃) is the flue gas temperature. This formula is summarized by the applicant based on the flue gas enthalpy value table of the gas engine. h in and h out can be determined according to the flue gas temperature when entering and the flue gas temperature when leaving by substituting into formula (10).

[0103] (2) Calculate the mass flow rate of the generated water vapor according to the total incoming flue gas volume, calculate the required natural gas raw material volume according to the mass flow rate of the water vapor and the total carbon flow rate in the natural gas, and introduce natural gas into the hydrogenation reaction combustion furnace according to the natural gas raw material volume.

[0104] When the flue gas volume M smoke (kg / h) entering the economizer is determined, the mass flow rate M steam (kg / h) of the hydrogen production water vapor generated by the corresponding economizer can be determined according to formula (11).

[0105]

[0106] M steam —The mass flow rate of the water vapor generated by the economizer (kg / h);

[0107] ΔQ—The recoverable flue gas waste heat of the economizer (kJ / h);

[0108] h1—The enthalpy value of the water vapor during the hydrogen reaction (kJ / kg);

[0109] h2—The enthalpy value of industrial water at room temperature (kJ / kg); For example, it can be set to 20℃ at room temperature;

[0110] C—The specific heat capacity of the flue gas (kJ / (kg·℃)); For example, in this embodiment, it is taken as 1.15 kJ / (kg·℃);

[0111] M smoke —The flue gas volume entering the economizer (kg / h);

[0112] t1—the average temperature of the flue gas at the inlet of the residual smoke boiler (°C);

[0113] t0—the average temperature of the flue gas at the outlet of the residual smoke boiler (°C); generally, it can be taken as 150 °C;

[0114] α—the coefficient of heat loss of the flue gas; usually taken as 0.9.

[0115] Among them, according to the actual situation of the equipment performance, it can be known that the exhaust gas temperature of the residual smoke boiler should generally not be lower than 150 °C, otherwise corrosion of the tail heating surface will occur. Then the recoverable flue gas residual heat ΔQ of the residual smoke boiler is as follows in formula (12):

[0116] ΔQ = C smoke ×M smoke ×(t1 - t0) × α (12)

[0117] In the formula, ΔQ represents the recoverable flue gas residual heat of the residual smoke boiler (kJ / h), C smoke is the specific heat capacity of the flue gas (kJ / (kg·°C)), and its value is 1.15 kJ / (kg·°C), M smoke is the mass flow rate of the flue gas entering the residual smoke boiler (kg / h), t1 is the average temperature of the flue gas at the inlet of the residual smoke boiler (°C), t0 is the average temperature of the flue gas at the outlet of the residual smoke boiler (°C), generally taken as 150 °C. Considering that the exhaust gas temperature of the residual smoke boiler should generally not be lower than 150 °C, otherwise corrosion of the tail heating surface will occur, α is the coefficient of heat loss of the flue gas, usually taken as 0.9.

[0118] Then, the mass flow rate M steam (kg / h) of the steam for hydrogen production can be determined by formula (13), and the hydrogen production amount V H2 (Nm 3 / h) is as follows in the formula:

[0119]

[0120] In the formula, V H2 (Nm 3 / h) is the actual hydrogen production amount; M steam (kg / h) is the mass flow rate of the steam generated by the residual smoke recovered by the residual smoke boiler for heating water, ρ steam is the density of the steam (kg / Nm 3 ). It should be particularly noted that in this application, the hydrogen production amount is determined by the recoverable residual heat of the residual smoke boiler, that is, hydrogen is determined by heat. When there is no residual smoke from the gas engine entering the residual smoke boiler to generate the steam required for the hydrogenation reaction, the hydrogen production amount is also 0 accordingly. Only when there is residual smoke waste heat for generating the steam required for the hydrogenation reaction, the hydrogen production will proceed, otherwise the hydrogen production will stop. This hydrogen production method can be used to calculate the power generation of the hydrogen fuel cell.

[0121] The main reactions during the hydrogen production process are as shown in the following formulas (14) to (16):

[0122] C m H n + mH2O → mCO + (n + 2m) / 2H2 (14)

[0123] ZnO + H2S → ZnS + H2O (15)

[0124] CO + H2O → CO2 + H2 (16)

[0125] The calculation process of the hydrogen production amount and carbon flow of the waste smoke from the gas engine is as Figure 2 shown. Natural gas mainly includes four gases, and each corresponding gas can produce hydrogen. In the first stage, the reactions of the four gases follow the following chemical formula: C m H n + mH2O → mCO + (n + 2m) / 2H2, which is an endothermic reaction. In the middle shift reaction of the second stage, the reaction follows the following chemical formula: CO + H2O → CO2 + H2, which is an exothermic reaction. To sum up, the chemical reactions of each gas in natural gas in the two stages are: C m H n + 2mH2O → mCO2 + (4m + n) / 2H2, where m can take 1, 2, 3, 4, and n can correspondingly take 4, 6, 8, 10, respectively representing four different gases in natural gas. The main component of natural gas is methane (CH4), accounting for 85% by volume, followed by ethane (C2H6) accounting for 9%, propane (C3H8) accounting for 3%, and butane (C4H 10 ) accounting for 1%. In addition, it also contains 2% nitrogen (N2) and trace amounts of hydrogen sulfide (H2S).

[0126] Based on the composition of natural gas, the calculation formula for the carbon atoms in the obtained natural gas in this application is as shown in formula (17):

[0127] ∑V carbon =γ CH4 +γ C2H6 ×2 + γ C3H8 ×3 + γ C4H10 ×4 (17)

[0128] In the formula, ∑V carbon is the total carbon atom content of natural gas, γ CH4 is the volume percentage of methane (CH4) in natural gas, γ C2H6 is the volume percentage of ethane (C2H6), γ C3H8 is the volume percentage of propane (C3H8), γ C4H10 is the volume percentage of butane (C4H 10) volume percentage.

[0129] Multiply the number of carbon atoms in each gas by the corresponding volume ratio to obtain the result of the carbon flow per unit of natural gas. There is 1 carbon atom in CH4, 2 carbon atoms in C2H6, 3 carbon atoms in C3H8, and 4 carbon atoms in C4H 10 There are 4 carbon atoms in [C4H], so the carbon flow per unit of natural gas is finally calculated to be 1.16. If there is 1 unit volume of natural gas, then it will contain 0.85 unit volume of methane, and this reaction requires 2 × 0.85 unit volume of water vapor, corresponding to 0.85 unit volume of CO2 and 4 × 0.85 unit volume of H2. The calculation process for the hydrogenation reaction of other gases is also as Figure 2 shown. The reaction of one unit volume of natural gas requires 2 × 0.85 + 4 × 0.09 + 6 × 0.03 + 8 × 0.01 = 2.32 unit volume of water vapor, and then 4 × 0.85 + 7 × 0.09 + 10 × 0.03 + 13 × 0.01 = 4.46 unit volume of hydrogen is produced. Therefore, 40 m 3 / h of natural gas will be able to output 40 × 4.46 = 178.4 m 3 / h of H2.

[0130] According to Equation (17), the total number of carbon atoms in natural gas is calculated to be 1.16. The content of carbon atoms in natural gas is directly related to the amount of water vapor required for the hydrogenation reaction, and the residual heat of the flue gas entering the economizer directly determines the amount of water vapor produced.

[0131] When calculating the mass flow rate of water vapor required for hydrogen production in the hydrogenation reaction, it is necessary to measure the total carbon atom content in natural gas to calculate the water-carbon ratio. Under normal production conditions, controlling the water-carbon ratio of water and natural gas is the key to hydrogen production from natural gas. The water-carbon ratio for hydrogen production is generally 3 - 5, and the normal value of the water-carbon ratio is 3.5. If it deviates too much from this ratio, it may cause waste of water vapor. If the value is too small, it will cause carbon deposition on the hydrogenation reaction catalyst and deactivate it. According to previous research, the water-carbon ratio of this application is set to 3.5. The water-carbon ratio calculation formula is Equation (18), and the carbon flow is determined by the superposition of carbon-containing gases in natural gas:

[0132]

[0133] In the formula, ξ is the water-carbon ratio, with a value of 3.5 in this application, V natural is the natural gas volume flow rate (Nm 3 / h), V steam is the water vapor volume flow rate (Nm 3 / h), ∑V carbon is the total volume flow rate of carbon in natural gas (Nm 3 / h), and 1.16 is the total number of carbon atoms in natural gas calculated.

[0134] As can be seen from the above formula (17), the total number of carbon atoms in natural gas is 1.16. According to the above formula, the required volume flow rate of natural gas can be calculated through the volume flow rate of water vapor.

[0135] Exemplarily, if 40 Nm 3 / h of natural gas is used as the raw material for hydrogen production, the carbon flow rate of natural gas is the product of the volume flow rate and the total number of carbon atoms, resulting in 46.4 Nm 3 / h. Since the steam-carbon ratio is generally selected as 3.5, the steam flow rate required for the hydrogenation reaction of 40 Nm 3 / h of natural gas is 162.4 Nm 3 / h.

[0136] Among them, the reforming hydrogen production device further includes a natural gas pipeline, a desulfurizer, a desulfurized natural gas and steam mixer, a gas-liquid separator, a hydrogen purification device and an exhaust gas collector. Refer to Figure 1 , where

[0137] The first input end of the desulfurized natural gas and steam mixer is connected to the steam output end of the residual flue gas boiler, and the output end of the desulfurized natural gas and steam mixer is connected to the hydrogenation reaction combustion furnace;

[0138] The first output end of the natural gas pipeline is connected to the desulfurizer, and the output end of the desulfurizer is connected to the second input end of the desulfurized natural gas and steam mixer;

[0139] The hydrogenation reaction combustion furnace includes a high-temperature reaction furnace and a flue gas passage. The input end of the high-temperature reaction furnace is connected to the output end of the desulfurized natural gas and steam mixer, and the flue gas output end of the flue gas passage is connected to the residual flue gas boiler; the output end of the high-temperature reaction furnace is connected to the input end of the medium-temperature shift furnace, the output end of the medium-temperature shift furnace is connected to the input end of the gas-liquid separator, and the output end of the gas-liquid separator is connected to the input end of the hydrogen purification device;

[0140] The first output end of the hydrogen purification device is connected to the hydrogen energy power generation device, the second output end of the hydrogen purification device is connected to the exhaust gas collector, and the output end of the exhaust gas collector is connected to the natural gas pipeline.

[0141] The above structure innovatively incorporates the combustible gas remaining after hydrogen purification in natural gas reforming hydrogen production into the building gas supply pipeline, further effectively combining the residual flue gas hydrogen storage method in this application with building energy supply.

[0142] In a preferred structure, a hydrogen compressor and a natural gas compressor are further included.

[0143] The input end of the hydrogen compressor is connected to the hydrogen purification device, and the output end of the hydrogen compressor is connected to the hydrogen energy power generation device;

[0144] The input end of the natural gas compressor is connected to the natural gas pipeline, and the output end of the natural gas compressor is connected to the input end of the desulfurizer.

[0145] In a preferred structure, it further includes a first heat exchanger, which is installed in the connecting pipeline between the high-temperature reaction furnace and the mixer of desulfurized natural gas and water vapor;

[0146] A second heat exchanger, which includes a first cooling channel and a second cooling channel. The first cooling channel is installed in the connecting pipeline between the desulfurizer and the high-temperature reaction furnace, and the second cooling channel is installed in the connecting pipeline between the compressor and the intermediate shift furnace;

[0147] A third heat exchanger, which is installed in the connecting pipeline between the gas-liquid separator and the intermediate shift furnace.

[0148] It further includes a hot water storage tank. One end of the third heat exchanger is the cooling water input end, and the other end outputs to one input end of the hot water storage tank. The other input end of the hot water storage tank is connected to the heat energy output end of the hydrogen energy power generation device.

[0149] Above, the specific operation mode of the integrated energy supply system:

[0150] The gas engine uses natural gas as raw material for power generation. While generating electricity, it produces high-temperature flue gas, and the flue gas temperature can generally reach about 368 - 469 °C.

[0151] In summer and winter seasons, when the building has stable heating and cooling load demands, the flue gas of the gas engine can generate chilled water / hot water for building air conditioning through a lithium bromide absorption chiller to meet the building heating and cooling load demands. When there is no stable heating and cooling load demand in the building during the transition season, the flue gas of the gas engine can pass through the surplus flue gas boiler to generate high-temperature water vapor required for the hydrogen production reaction, avoiding waste of flue gas waste heat. The high-temperature water vapor generated by the surplus flue gas boiler is mixed with the natural gas desulfurized by the desulfurizer in the mixer of natural gas and water vapor, and then enters the high-temperature reaction furnace placed in the combustion furnace together for hydrogenation reaction. The reason why natural gas needs to be desulfurized is that the sulfides contained in it will cause the catalyst for the hydrogenation reaction to fail. Therefore, the natural gas in the natural gas pipeline needs to be compressed by the compressor and then preheated by the heat exchanger before entering the desulfurizer for desulfurization.

[0152] The first heat exchanger is built into the inner wall side of the flue gas channel in the combustion furnace. The mixture of desulfurized natural gas and water vapor first flows through the first heat exchanger in the combustion furnace for preheating to facilitate accelerating the hydrogenation reaction speed and the required reaction temperature. The hydrogenation reaction temperature in the high-temperature reaction furnace is about 735 °C. Therefore, it is necessary to use the natural gas in the natural gas pipeline as the heating fuel for combustion to raise the temperature. The natural gas in the natural gas pipeline burns with air oxygen to heat the high-temperature reaction furnace, and at the same time, the flue gas generated by the combustion circulates in the flue gas channel in the combustion furnace and finally enters the surplus flue gas boiler to generate high-temperature water vapor for hydrogen production.

[0153] The main component of natural gas is CH4. The main chemical equation for its hydrogenation reaction is CH4 + H2O → CO + 3H2, which is an endothermic process with a reaction temperature of about 735°C. After the hydrogenation reaction, the mixed gas flows out of the high-temperature reaction furnace and passes through the second heat exchanger to heat the natural gas to be desulfurized. Since the desulfurization reaction temperature is between 290 and 350°C, the natural gas to be desulfurized needs to be preheated first. The mixed gas entering the medium-temperature shift furnace needs to be cooled because the medium-temperature shift reaction is an exothermic reaction with a reaction temperature of only about 200 - 300°C. The main chemical equation for the reaction is CO + H2O → CO2 + H2. After the medium-temperature shift reaction, the mixed gas flows out of the medium-temperature shift furnace and passes through the third heat exchanger. After being cooled by cooling water, it is cooled down and enters the gas-liquid separator for gas-liquid separation. After passing through the heat exchanger, the cooling water is heated up and can be stored in the hot water storage tank for use as domestic hot water for buildings, and can effectively become the energy required by the building. After gas-liquid separation, the water vapor in the mixed gas is liquefied into water droplets at the bottom of the gas-liquid separator, and gases such as CO2, H2, CO, and CH4 rise to the PSA hydrogen purification device. In the PSA hydrogen compression adsorption purification equipment, hydrogen is separated and purified from other gases, and its purity will become 99.999Vol%. The other gases in the mixed gas are mainly CO and CO2, which will be stored in the waste gas collector. The combustible gases CO and a small part of CH4 gas in the waste gas collector can be mixed into the natural gas pipeline and transported to the building together as domestic gas, making the maximum use of the waste gas. The hydrogen purified by the PSA hydrogen purification device, after being compressed to a certain extent by the hydrogen compressor, can be directly used as the raw material of the hydrogen fuel cell device. The hydrogen fuel cell generates electricity to supply the building, and the accompanying waste heat can be used as the heat source of the hot water storage tank to heat domestic hot water for the building.

[0154] Compared with the existing waste heat recovery and utilization hydrogen production devices, some existing devices only complete the production of water vapor through waste heat recovery technology, and then combine with natural gas for a mixed reaction conversion to obtain hydrogen. The purpose of the present invention is to complete a gas engine combined cooling, heating and power generation device based on the basic technology of gas engine power supply. Under the condition that the hardware technology is mature, reduce the volume of the natural gas reforming hydrogen production equipment and directly connect it to the building for application, so that the waste smoke of the gas engine can be effectively utilized, including the direct application of hydrogen, the hot water of the heat exchanger generated by hydrogen production, the waste gas of the waste gas collector, etc., to achieve the maximum utilization of energy.

Claims

1. An integrated energy supply system based on a gas engine waste heat hydrogen energy storage system, characterized in that It includes a gas engine, a reforming hydrogen production device, and a lithium bromide absorption type cold and hot water unit. Among them, The input end of the lithium bromide absorption type cold and hot water unit is connected to the high-temperature flue gas channel of the gas engine, and its output end is connected to the cold and hot water pipes for building air conditioning; The reforming hydrogen production device includes a residual smoke boiler, a hydrogenation reaction combustion furnace, and a medium temperature shift furnace. The first input end of the residual smoke boiler is connected to the high-temperature flue gas pipeline of the gas engine, and the second input end of the residual smoke boiler is connected to the flue gas channel of the hydrogenation reaction combustion furnace; The medium temperature shift furnace is connected to the rear end of the hydrogenation reaction combustion furnace; The hydrogen output end at the end of the reforming hydrogen production device is connected to a hydrogen fuel cell; Calculate the total smoke emission of the gas engine per unit time, and calculate the required first flue gas volume of the lithium bromide absorption type cold and hot water unit per unit time; When the total smoke emission of the gas engine is less than or equal to the required first flue gas volume of the lithium bromide absorption type cold and hot water unit, all the flue gas is introduced into the lithium bromide absorption type cold and hot water unit; When the total smoke emission of the gas engine is greater than the required first flue gas volume of the lithium bromide absorption type cold and hot water unit, the required flue gas volume is introduced into the lithium bromide absorption type cold and hot water unit in sufficient quantity according to the required flue gas volume of the lithium bromide absorption type cold and hot water unit, and the remaining flue gas is introduced into the residual smoke boiler to generate water vapor; Determine the second flue gas volume discharged from the hydrogenation reaction combustion furnace and entering the residual smoke boiler according to the working state of the hydrogenation reaction combustion furnace; Calculate the total flue gas volume entering the residual smoke boiler according to the total smoke emission, the first flue gas volume, and the second flue gas volume; Calculate the mass flow rate of the generated water vapor according to the total flue gas volume entering, calculate the required natural gas raw material quantity according to the mass flow rate of the water vapor and the total carbon flow rate in the natural gas, and introduce natural gas into the hydrogenation reaction combustion furnace according to the natural gas raw material quantity.

2. The integrated energy supply system based on the hydrogen energy storage system using the waste heat of a gas engine as claimed in claim 1, wherein, The method for calculating the required natural gas raw material quantity according to the mass flow rate of the water vapor and the total carbon flow rate in the natural gas includes: Calculate the total carbon flow rate in the natural gas according to the proportion of each component gas in the natural gas; Determine the water-carbon ratio for natural gas hydrogen production, and calculate the natural gas volume flow rate according to the water-carbon ratio calculation formula in combination with the total carbon flow rate in the natural gas and the mass flow rate of the water vapor; According to the chemical reaction formula for natural gas hydrogen production, in combination with the total carbon flow rate in the natural gas and the mass flow rate of the water vapor generated by the residual smoke boiler, calculate the required natural gas raw material quantity to be introduced.

3. The integrated energy supply system based on the hydrogen energy storage system using the waste heat of a gas engine as claimed in claim 1, wherein, The method for calculating the total smoke emission of the gas engine per unit time includes the following steps: Determine the hourly electricity load demand of the building, and calculate the hourly generated electricity of the actual gas engine according to the green power generation amount of the building, the generated electricity amount of the hydrogen fuel cell, and the rated generated electricity amount under full load of the gas engine, as shown in the following formula; Where P engine is the power generation of the gas engine, in kW, E FL is the rated power generation of the gas engine under full load, in kW, E L is the hourly electricity load of the building, in kW, E P is the green power generation, in kW, E FC is the power generation of the hydrogen fuel cell, in kW; Among them, the green power includes solar energy or wind energy connected to the building; Then determine the total smoke emission of the gas engine generated along with the power generation according to the hourly generated electricity of the gas engine.

4. The integrated energy supply system based on the gas engine waste heat hydrogen energy storage system according to claim 3, wherein Method for calculating the total flue gas inlet volume M of the residual smoke boiler based on the total exhaust gas volume, the first flue gas volume and the second flue gas volume, with the unit of kg / h, as shown in the following formula: smoke ​ Where M T is the total exhaust gas volume of the gas engine per unit time, with the unit of kg / h, and M C / H is the first flue gas volume required for the lithium bromide absorption chiller to produce chilled or hot water for building refrigeration or heating, with the unit of kg / h, and M b is the second flue gas volume that enters the residual flue gas boiler after being discharged from the hydrogenation reaction combustion furnace, with the unit of kg / h.

5. The integrated energy supply system based on the gas engine residual flue gas hydrogen energy storage system according to claim 4, characterized in that, Calculate the mass flow rate of the generated water vapor according to the total flue gas volume entering, which is achieved through the following formula: M steam — Mass flow rate of water vapor generated by the residual smoke boiler, unit: kg / h; ΔQ—the recoverable flue gas residual heat of the residual smoke boiler, unit: kJ / h; h1—the enthalpy value of water vapor during hydrogen reaction, unit: kJ / kg; h2—the enthalpy value of industrial water at room temperature, unit: kJ / kg; C—the mass specific heat capacity of the flue gas, unit: kJ / (kg·℃); M smoke — The amount of flue gas entering the after-smoke boiler, in kg / h; t1—the average temperature of the flue gas at the inlet of the residual smoke boiler, unit: ℃; t0—the average temperature of the flue gas at the outlet of the residual smoke boiler, unit: ℃; α—the flue gas heat loss coefficient.

6. The integrated energy supply system based on the gas engine waste heat hydrogen energy storage system according to claim 2, characterized in that, According to the chemical reaction formula for hydrogen production from natural gas, combined with the total carbon flow rate in natural gas and the mass flow rate of steam generated by the residual heat boiler, calculate the amount of natural gas raw material to be introduced. The specific calculation is carried out through the following formula: The calculation formula for the total carbon flow rate in natural gas is as follows: ∑V carbon = γ CH4 + γ C2H6 × 2 + γ C3H8 × 3 + γ C4H10 × 4, where ∑V carbon is the total carbon flow rate in natural gas, γ CH4 is the volume percentage of methane in natural gas, γ C2H6 is the volume percentage of ethane, γ C3H8 is the volume percentage of propane, γ C4H10 is the volume percentage of butane; Determine the water-carbon ratio for hydrogen production from natural gas. According to the water-carbon ratio calculation formula, combined with the total carbon flow rate in natural gas and the steam volume flow rate, calculate the natural gas volume flow rate as follows: where ξ is the water-carbon ratio, determined as a constant according to experience, V natural is the natural gas volume flow rate, with the unit of Nm 3 / h, and V steam is the water vapor volume flow rate, with the unit of Nm 3 / h.

7. The integrated energy supply system based on the hydrogen energy storage system using the waste heat of a gas engine as claimed in claim 1, wherein The reforming hydrogen production device further includes a natural gas pipeline, a desulfurizer, a desulfurized natural gas and steam mixer, a gas-liquid separator, a hydrogen purification device, and an exhaust gas collector. Among them, The first input end of the desulfurized natural gas and steam mixer is connected to the steam output end of the residual heat boiler, and the output end of the desulfurized natural gas and steam mixer is connected to the hydrogenation reaction combustion furnace; The first output end of the natural gas pipeline is connected to the desulfurizer, and the output end of the desulfurizer is connected to the second input end of the desulfurized natural gas and steam mixer; The hydrogenation reaction combustion furnace includes a high-temperature reaction furnace and a flue gas passage. The input end of the high-temperature reaction furnace is connected to the output end of the desulfurized natural gas and steam mixer, and the flue gas output end of the flue gas passage is connected to the residual heat boiler; the output end of the high-temperature reaction furnace is connected to the input end of the medium-temperature shift furnace, the output end of the medium-temperature shift furnace is connected to the input end of the gas-liquid separator, and the output end of the gas-liquid separator is connected to the input end of the hydrogen purification device; The first output end of the hydrogen purification device is connected to the hydrogen energy power generation device, the second output end of the hydrogen purification device is connected to the exhaust gas collector, and the output end of the exhaust gas collector is connected to the natural gas pipeline.

8. The integrated energy supply system based on the gas engine residual smoke hydrogen energy storage system according to claim 7, characterized in that, It further includes a hydrogen compressor and a natural gas compressor, The input end of the hydrogen compressor is connected to the hydrogen purification device, and the output end of the hydrogen compressor is connected to the hydrogen energy power generation device; The input end of the natural gas compressor is connected to the natural gas pipeline, and the output end of the natural gas compressor is connected to the input end of the desulfurizer.

9. The integrated energy supply system based on the gas engine residual smoke hydrogen energy storage system according to claim 7, characterized in that, It further includes a first heat exchanger, which is installed on the connecting pipeline between the high-temperature reaction furnace and the desulfurized natural gas and steam mixer; A second heat exchanger, which includes a first cooling channel and a second cooling channel. The first cooling channel is installed on the connecting pipeline between the desulfurizer and the high-temperature reaction furnace, and the second cooling channel is installed on the connecting pipeline between the compressor and the medium-temperature shift furnace; A third heat exchanger, which is installed on the connecting pipeline between the gas-liquid separator and the medium-temperature shift furnace.

10. The integrated energy supply system based on the gas engine waste heat hydrogen energy storage system according to claim 9, characterized in that, It further includes a hot water storage tank. One end of the third heat exchanger is the cooling water input end, and the other end outputs to one input end of the hot water storage tank. The other input end of the hot water storage tank is connected to the heat energy output end of the hydrogen energy power generation device.

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