Methanol synthesis plant

Abstract

This application discloses a methanol synthesis apparatus, belonging to the field of methanol preparation technology. The methanol synthesis apparatus includes a hydrogen preparation device, a carbon dioxide preparation device, and a first heat exchanger. The hydrogen preparation device includes a solid oxide electrolysis cell, a flash evaporator connected to the solid oxide electrolysis cell, and a water inlet pipe connected to the flash evaporator. The carbon dioxide preparation device includes a combustion furnace and a flue gas outlet pipe connected to the combustion furnace. The first heat exchanger is connected to both the flue gas outlet pipe and the water inlet pipe, and the flue gas outlet pipe and the water inlet pipe exchange heat through the first heat exchanger. This application, by setting up a first heat exchanger, enables the flue gas outlet pipe to exchange heat with the water inlet pipe. The heat carried in the discharged flue gas can heat the water in the water inlet pipe, realizing the utilization of waste heat in the flue gas, reducing energy consumption in the subsequent steam preparation process, and improving energy utilization efficiency.

Description

Technical Field

[0001] This application belongs to the field of methanol manufacturing technology, specifically relating to methanol synthesis equipment. Background Technology

[0002] Solid oxide electrolyzers can efficiently electrolyze water vapor at high temperatures to produce high-purity hydrogen and oxygen. Combustion furnaces, on the other hand, can produce the carbon dioxide needed for methanol production.

[0003] However, the flue gas discharged from the combustion furnace has a high temperature, meaning that some of the heat from the combustion furnace is wasted as energy is discharged with the flue gas. Utility Model Content

[0004] Purpose of this utility model: This application provides a methanol synthesis device to solve the technical problem of energy waste in the process of carbon dioxide production.

[0005] Technical solution: This application provides a methanol synthesis apparatus, comprising:

[0006] A hydrogen production apparatus, comprising a solid oxide electrolytic cell, a flash evaporator, a water inlet pipeline, and a hydrogen outlet pipeline, wherein the first gas inlet of the solid oxide electrolytic cell is connected to the steam outlet of the flash evaporator, the water inlet pipeline is connected to the water inlet of the flash evaporator, and the hydrogen outlet pipeline is connected to the hydrogen outlet of the solid oxide electrolytic cell.

[0007] A carbon dioxide preparation device, comprising a combustion furnace and a flue gas outlet main path, wherein the flue gas outlet main path is connected to the flue gas outlet of the combustion furnace;

[0008] A methanol preparation apparatus, wherein the hydrogen outlet pipeline and the flue gas outlet main pipeline are respectively connected to the mixed gas inlet of the methanol preparation apparatus;

[0009] The first heat exchanger is connected to the main flue gas outlet and the water inlet pipe, and the main flue gas outlet and the water inlet pipe exchange heat through the first heat exchanger.

[0010] In some embodiments,

[0011] The carbon dioxide preparation device further includes a first circulation branch, one end of which is connected to the circulating gas inlet of the combustion furnace, and the other end is connected in parallel to the flue gas outlet main path.

[0012] In some embodiments,

[0013] The end of the first circulation branch furthest from the circulating gas inlet is connected between the first heat exchanger and the combustion furnace.

[0014] In some embodiments,

[0015] The carbon dioxide production apparatus further includes:

[0016] A crusher, wherein the discharge port of the crusher is connected to the feed port of the combustion furnace;

[0017] The second circulation branch has one end connected in parallel to the main flue gas outlet and the other end connected to the drying gas inlet of the crusher.

[0018] In some embodiments,

[0019] The end of the second circulation branch furthest from the drying gas inlet is connected between the first heat exchanger and the methanol preparation device.

[0020] In some embodiments,

[0021] The hydrogen production apparatus further includes:

[0022] A hydrogen inlet pipe, wherein the hydrogen inlet pipe is connected to the first gas inlet;

[0023] The methanol synthesis equipment further includes a second heat exchanger, which is connected to the hydrogen inlet pipeline and the hydrogen outlet pipeline. The hydrogen inlet pipeline and the hydrogen outlet pipeline exchange heat through the second heat exchanger.

[0024] The hydrogen production apparatus further includes a tail gas outlet pipeline, which connects the tail gas outlet of the solid oxide electrolysis cell and the tail gas inlet of the combustion furnace.

[0025] In some embodiments,

[0026] The hydrogen production apparatus further includes an air inlet pipe, which is connected to the second air inlet of the solid oxide electrolytic cell;

[0027] The methanol synthesis equipment further includes a third heat exchanger, which is connected to the air inlet pipe and the exhaust gas outlet pipe. The air inlet pipe and the exhaust gas outlet pipe exchange heat through the third heat exchanger.

[0028] In some embodiments,

[0029] The hydrogen production apparatus further includes a second compressor, which is disposed in the air inlet pipeline and the outlet of the second compressor is connected to the third heat exchanger.

[0030] In some embodiments,

[0031] The methanol synthesis equipment also includes a fourth heat exchanger;

[0032] The methanol preparation apparatus further includes:

[0033] A reactor having the gas mixture inlet;

[0034] A mixed gas inlet pipeline, one end of which is connected to the mixed gas inlet, and the other end of which is connected to the end of the hydrogen outlet pipeline away from the hydrogen outlet and the end of the flue gas outlet main pipeline away from the flue gas outlet, respectively. The fourth heat exchanger is connected to the mixed gas inlet pipeline.

[0035] A methanol outlet pipeline is provided, which is connected to the methanol outlet of the reactor. A fourth heat exchanger is connected to the methanol outlet pipeline, and the mixed gas inlet pipeline and the methanol outlet pipeline exchange heat through the fourth heat exchanger.

[0036] In some embodiments,

[0037] The methanol preparation apparatus further includes:

[0038] A separation component is disposed in the methanol outlet pipeline;

[0039] The third circulation branch connects the gas outlet of the separation component and the end of the mixed gas inlet pipe away from the mixed gas inlet.

[0040] The third circulation branch is equipped with an exhaust device.

[0041] Beneficial Effects: Compared with the prior art, the methanol synthesis equipment provided in this application includes a hydrogen preparation device, a carbon dioxide preparation device, a methanol preparation device, and a first heat exchanger. The hydrogen preparation device includes a solid oxide electrolysis cell, a flash evaporator, a water inlet pipeline, and a hydrogen outlet pipeline. The first gas inlet of the solid oxide electrolysis cell is connected to the steam outlet of the flash evaporator, the water inlet pipeline is connected to the water inlet of the flash evaporator, and the hydrogen outlet pipeline is connected to the hydrogen outlet of the solid oxide electrolysis cell. The carbon dioxide preparation device includes a combustion furnace and a main flue gas outlet pipeline, which is connected to the flue gas outlet of the combustion furnace. The hydrogen outlet pipeline and the main flue gas outlet pipeline are respectively connected to the mixed gas inlet of the methanol preparation device. The first heat exchanger is connected to the main flue gas outlet pipeline and the water inlet pipeline, and the main flue gas outlet pipeline and the water inlet pipeline exchange heat through the first heat exchanger. This application sets up a first heat exchanger so that the flue gas outlet pipe can exchange heat with the water inlet pipe. The heat carried in the discharged flue gas can heat the water in the water inlet pipe, realizing the utilization of waste heat in the flue gas, reducing energy consumption in the subsequent steam preparation process, and improving the energy utilization rate of the methanol synthesis equipment. Attached Figure Description

[0042] The technical solution and other beneficial effects of this application will become apparent from the following detailed description of specific embodiments in conjunction with the accompanying drawings.

[0043] Figure 1 This is a connection diagram of the methanol synthesis equipment provided in the embodiments of this application;

[0044] Figure 2 This is a connection diagram of the first heat exchanger in the methanol synthesis equipment provided in the embodiments of this application;

[0045] Figure 3 This is a schematic diagram of the connection of the first circulation pipeline in the methanol synthesis equipment provided in the embodiments of this application;

[0046] Figure 4 This is a schematic diagram of the connection of the second circulation pipeline in the methanol synthesis equipment provided in the embodiments of this application;

[0047] Figure 5 This is a schematic diagram of the connection of the fourth heat exchanger in the methanol synthesis equipment provided in the embodiments of this application.

[0048] Explanation of reference numerals in the attached figures:

[0049] 100-Hydrogen preparation device; 110-Solid oxide electrolysis cell; 120-Flash evaporator; 121-Steam outlet; 122-Water inlet; 123-Liquid outlet; 130-Water inlet pipeline; 131-First pressure reducing valve; 140-Hydrogen inlet pipeline; 141-First heater; 150-Hydrogen outlet pipeline; 151-First compressor; 160-Air inlet pipeline; 161-Second heater; 162-Second compressor; 163-Gas outlet; 170-Heat pump; 180-Tail gas outlet pipeline; 200-Carbon dioxide preparation device; 210-Combustion furnace; 211-Circulating gas inlet; 212-Feed inlet; 213-Steam outlet; 214-Tail gas inlet; 215-Flue gas outlet; 220-Main flue gas outlet; 222-Dust collector; 223-Desulfurization tower; 225-Adsorption device; 2 26-Third compressor; 230-First circulation branch; 240-Second circulation branch; 250-Crusher; 251-Drying gas inlet; 252-Discharge outlet; 260-Turbine; 270-Generator; 300-Methanol preparation unit; 310-Reactor; 311-Methanol outlet; 320-Mixed gas inlet pipeline; 330-Methanol outlet pipeline; 332-Separation component; 333-High-pressure separator; 334-Second pressure reducing valve; 335-Low-pressure separator; 337-Third circulation branch; 338-Exhaust device; 339-Fourth compressor; 340-Solution pump; 350-Distillation column; 360-Gas-liquid separator; 370-Mixed gas inlet; 380-Gas outlet; 400-First heat exchanger; 500-Second heat exchanger; 600-Third heat exchanger; 700-Fourth heat exchanger. Detailed Implementation

[0050] The technical solutions of the embodiments of this application will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only a part of the embodiments of this application, and not all of them. All other embodiments obtained by those skilled in the art based on the embodiments of this application without creative effort are within the scope of protection of this application.

[0051] In the description of this application, it should be noted that, unless otherwise expressly specified and limited, the terms "connected" and "linked" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection, an electrical connection, or a connection that allows for mutual communication; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two elements or the interaction between two elements. Those skilled in the art can understand the specific meaning of the above terms in this application according to the specific circumstances. In the description of this application, "multiple" means two or more, unless otherwise expressly and specifically limited. Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of indicated technical features. Thus, features defined with "first" and "second" may explicitly or implicitly include one or more features.

[0052] The following disclosure provides many different implementations or examples for carrying out different structures of this application. To simplify the disclosure of this application, the components and arrangements of specific examples are described below. Of course, these are merely examples and are not intended to limit this application.

[0053] The solid oxide electrolyzer 110 can efficiently electrolyze water vapor at high temperatures to produce high-purity hydrogen and oxygen. The combustion furnace 210 can produce carbon dioxide needed for methanol production.

[0054] However, the flue gas discharged from the combustion furnace 210 has a high temperature, meaning that some of the heat from the combustion furnace 210 is wasted as energy is discharged with the flue gas.

[0055] To address the technical problem of energy waste caused by heat being discharged with the flue gas in the aforementioned combustion furnace 210, the first embodiment of this application provides a methanol synthesis apparatus. Please refer to [link to relevant documentation]. Figure 1 and Figure 2The methanol synthesis equipment includes a hydrogen production unit 100, a carbon dioxide production unit 200, a methanol production unit 300, and a first heat exchanger 400. The hydrogen production unit 100 includes a solid oxide electrolysis cell 110, a flash evaporator 120, a water inlet pipe 130, and a hydrogen outlet pipe 150. The first gas inlet 111 of the solid oxide electrolysis cell 110 is connected to the steam outlet 121 of the flash evaporator 120, the water inlet pipe 130 is connected to the water inlet 122 of the flash evaporator 120, and the hydrogen outlet pipe 150 is connected to the first gas outlet 111 of the solid oxide electrolysis cell 110. Hydrogen outlet 112 is connected; carbon dioxide preparation device 200 includes combustion furnace 210 and flue gas outlet main line 220, flue gas outlet main line 220 is connected to flue gas outlet 215 of combustion furnace 210; hydrogen outlet pipeline 150 and flue gas outlet main line 220 are respectively connected to mixed gas inlet 370 of methanol preparation device 300; first heat exchanger 400 is connected to flue gas outlet main line 220 and first heat exchanger 400 is connected to water inlet pipeline 130, and flue gas outlet main line 220 and water inlet pipeline 130 exchange heat through first heat exchanger 400.

[0056] Specifically, the water inlet pipe 130 is used to introduce water into the flash evaporator 120, and the water inlet pipe 130 is connected to the first heat exchanger 400, which means that the water introduced into the flash evaporator 120 needs to enter the first heat exchanger 400 before entering the flash evaporator 120.

[0057] Since the flue gas outlet main path 220 is used to remove the flue gas from the combustion furnace 210, and the temperature of the flue gas is relatively high, the temperature of the flue gas outlet main path 220 is also relatively high. Therefore, when the flue gas outlet main path 220 and the water inlet pipe 130 exchange heat in the first heat exchanger 400, the heat flows from the higher temperature flue gas outlet main path 220 to the lower temperature water inlet pipe 130, so as to raise the temperature of the water in the water inlet pipe 130.

[0058] In some embodiments, the combustion furnace 210 is an oxygen-enriched combustion furnace 210.

[0059] In the above embodiments, firstly, by setting a first heat exchanger 400, the water that has not yet entered the flash evaporator 120 is preheated with high-temperature flue gas to increase the water temperature and reduce the energy consumption required for the flash evaporator 120 to heat the water; secondly, since the heat used to increase the water temperature in the first heat exchanger 400 comes from the waste heat of the flue gas, the water is heated by the first heat exchanger 400, utilizing the waste heat that would otherwise be wasted, reducing the overall energy consumption of the methanol synthesis equipment and improving the overall energy utilization rate of the methanol synthesis equipment.

[0060] In some embodiments, a first pressure reducing valve 131 is also connected between the flash evaporator 120 and the water inlet pipe 130 to reduce pressure and promote flash evaporation, thereby meeting the process requirements of the flash evaporator 120.

[0061] In some embodiments, the flash evaporator 120 includes a steam outlet 121 and a liquid outlet 123. The steam outlet 121 is connected to the first air inlet 111 of the solid oxide electrolysis cell 110, and the liquid outlet 123 is connected to a heat pump 170. The heat pump 170 is connected to a first heat exchanger 400, and the outlet of the heat pump 170 is connected to a water inlet pipe 130. The heat pump 170 is used to heat the low-pressure liquid separated by the flash evaporator 120, and then send the heated liquid into the water inlet pipe 130. After being heated by the first heat exchanger 400, the liquid re-enters the flash evaporator 120 for flash evaporation.

[0062] In some embodiments, please refer to Figure 1 and Figure 3 The carbon dioxide preparation device 200 also includes a first circulation branch 230, one end of which is connected to the circulating gas inlet 211 of the combustion furnace 210, and the other end is connected in parallel to the flue gas outlet main path 220.

[0063] Understandably, since the first circulation branch 230 is connected to the flue gas outlet main branch 220, the first circulation branch 230 can reintroduce some of the flue gas into the combustion furnace 210.

[0064] In the above embodiment, by reintroducing a portion of the flue gas into the combustion furnace 210, oxygen is replenished to enhance the turbulent mixing effect, optimize temperature distribution, improve the turbulent mixing effect of the combustion furnace 210, and promote the complete combustion of unburned fuel, thereby improving the efficiency of the combustion furnace 210. Simultaneously, the improved combustion efficiency also reduces emissions of carbon monoxide and carbon particles, making the combustion furnace 210 more environmentally friendly.

[0065] In some embodiments, please refer to Figure 1 and Figure 3 The end of the first circulation branch 230 away from the circulating gas inlet 211 is connected between the first heat exchanger 400 and the combustion furnace 210.

[0066] In some embodiments, please refer to Figure 1 The carbon dioxide production device 200 also includes a dust collector 222 and a desulfurization tower 223 installed in the main flue gas outlet 220. The desulfurization tower 223 is connected to the flue gas outlet 215 of the combustion furnace 210. The dust collector 222 is connected between the desulfurization tower 223 and the combustion furnace 210. The end of the first circulation branch 230 away from the circulating gas inlet 211 is connected between the desulfurization tower 223 and the first heat exchanger 400. Part of the flue gas discharged from the combustion furnace 210 passes through the dust collector 222 and the desulfurization tower 223 in sequence before flowing to the first heat exchanger 400. Part of the flue gas discharged from the combustion furnace 210 passes through the dust collector 222 and the desulfurization tower 223 in sequence before flowing through the first circulation branch 230 to the circulating gas inlet 211 of the combustion furnace 210.

[0067] Understandably, the temperature of the flue gas will decrease after passing through the first heat exchanger 400.

[0068] In the above embodiment, since the first circulation branch 230 is connected between the combustion furnace 210 and the first heat exchanger 400, that is, the first circulation branch 230 is located upstream of the first heat exchanger 400, the flue gas in the first circulation branch 230 has not yet entered the first heat exchanger 400 for heat exchange and still has a high temperature. The first circulation branch 230 can introduce the high-temperature flue gas into the combustion furnace 210, so that the high-temperature flue gas can be used to form a turbulent mixing effect, reducing the possibility that the temperature drop in the combustion furnace 210 will be too large due to the introduction of gas from the outside, resulting in a significant reduction in the combustion effect, and improving the performance of the combustion furnace 210.

[0069] In some embodiments, flue gas is injected into the combustion furnace 210 in stages from the first circulation branch 230.

[0070] In some embodiments, please refer to Figure 1 and Figure 4 The carbon dioxide preparation device 200 also includes a second circulation branch 240 and a crusher 250. The discharge port 252 of the crusher 250 is connected to the feed port 212 of the combustion furnace 210. One end of the second circulation branch 240 is connected in parallel to the flue gas outlet main road 220, and the other end is connected to the drying gas inlet 251 of the crusher 250.

[0071] In some embodiments, the fuel for the combustion furnace 210 is biomass fuel. The combustion efficiency of the combustion furnace 210 can be improved by setting a crusher 250 upstream of the combustion furnace 210 to crush the biomass fuel.

[0072] In some embodiments, please refer to Figure 1 and Figure 4 The second circulation branch 240 is connected downstream of the dust collector 222 and the desulfurization tower 223. That is, the flue gas in the second circulation branch 240 is the flue gas after being treated by the dust collector 222 and the desulfurization tower 223, which can prevent particulate matter and sulfides from accumulating in the second circulation branch 240.

[0073] In the first aspect, in the above embodiment, flue gas is input into the crusher 250 through the second circulation branch 240 so that the flue gas can be used as a carrier gas for biomass fuel to transport biomass fuel and send biomass fuel into the combustion furnace 210.

[0074] Secondly, as the flue gas carries biomass fuel into the combustion furnace 210, the ratio of the flue gas to oxygen can be adjusted by changing the flue gas circulation rate, thereby controlling the oxygen concentration and making the combustion furnace 210 more convenient to use. Specifically, increasing the flue gas circulation rate can decrease the oxygen concentration, and decreasing the flue gas circulation rate can increase the oxygen concentration.

[0075] Thirdly, the flue gas can enter the combustion furnace 210 to dilute the nitrogen in the combustion furnace 210, reduce the heat loss caused by nitrogen absorption, and also reduce the formation of nitrides.

[0076] Fourthly, the circulating flue gas contains carbon dioxide, which has a high specific heat capacity. When the flue gas enters the combustion furnace 210 as a carrier gas, the carbon dioxide absorbs the heat released during combustion, lowering the flame temperature. Simultaneously, the flue gas dilutes the oxygen content, reducing the possibility of localized overheating within the combustion furnace 210. Furthermore, reducing the possibility of localized overheating also decreases the formation of nitrogen oxides, making the combustion furnace 210 more environmentally friendly during operation.

[0077] Fifthly, the circulating flue gas can reduce combustion instability caused by excessively rapid fuel oxidation, while also inhibiting coking and ash accumulation, and maintaining stable heat transfer efficiency in the furnace.

[0078] In some embodiments, please refer to Figure 1 and Figure 4 The end of the second circulation branch 240 away from the drying gas inlet 251 is connected between the first heat exchanger 400 and the methanol preparation device 300.

[0079] Since the end of the second circulation branch 240 furthest from the drying gas inlet 251 is connected between the first heat exchanger 400 and the methanol preparation device 300, the flue gas entering the second circulation branch 240 has already passed through the first heat exchanger 400 and been cooled. In other words, the flue gas in the second sub-pipe 224 has already been condensed in the first heat exchanger 400.

[0080] In the above embodiment, since the flue gas in the second circulation branch 240 has already been condensed in the first heat exchanger 400, the moisture content of the flue gas in the second circulation branch 240 is reduced, which can reduce the corrosion of the crusher 250 by the flue gas and extend the maintenance cycle and service life of the crusher 250. At the same time, since the flue gas needs to be used as the carrier gas for the crushed biomass fuel, the lower moisture content can also reduce the possibility of fuel caking after crushing, ensuring the combustion effect of the combustion furnace 210.

[0081] In some embodiments, please refer to Figure 1The hydrogen production apparatus 100 also includes a hydrogen inlet pipe 140, which is connected to the first gas inlet 111; the methanol synthesis apparatus also includes a second heat exchanger 500, which is connected to the hydrogen inlet pipe 140 and the hydrogen outlet pipe 150, and the hydrogen inlet pipe 140 and the hydrogen outlet pipe 150 exchange heat through the second heat exchanger 500.

[0082] It should be noted that, for ease of use Figure 1 The drawing shows a second heat exchanger 500 at the hydrogen outlet pipe 150 and the hydrogen inlet pipe 140. In fact, the hydrogen inlet pipe 140 and the hydrogen outlet pipe 150 are connected to the same second heat exchanger 500, that is, the hydrogen inlet pipe 140 and the hydrogen outlet pipe 150 exchange heat with the second heat exchanger 500.

[0083] Specifically, the gas temperature in the hydrogen outlet pipe 150 is higher, and the gas temperature in the hydrogen inlet pipe 140 is lower. In the second heat exchanger 500, the heat in the hydrogen outlet pipe 150 flows to the hydrogen inlet pipe 140.

[0084] In some embodiments, the output end of the hydrogen inlet pipe 140 is connected to the steam outlet 121 of the flash evaporator 120 and the input end of the first mixing device, and the output end of the first mixing device is connected to the first air inlet 111. The mixing device is capable of mixing hydrogen and steam.

[0085] In the first aspect, in the above embodiment, by setting the hydrogen inlet pipe 140 and the flash evaporator 120 to be connected to the first air inlet 111 at the same time, the hydrogen can be used as the carrier gas for the water vapor generated by the flash evaporator 120, and carry the water vapor into the solid oxide electrolysis cell 110.

[0086] Secondly, in the above embodiment, by setting up a second heat exchanger 500 to utilize the waste heat discharged from the solid oxide electrolysis cell 110 to heat the gas about to enter the solid oxide electrolysis cell 110, the waste heat of the solid oxide electrolysis cell 110 is reused, reducing the energy consumption for heating the gas in the hydrogen inlet pipe 140 and improving the energy utilization rate of the hydrogen production device 100. Simultaneously, heating the gas in the hydrogen inlet pipe 140 reduces the possibility of the gas in the hydrogen inlet pipe 140 mixing with water vapor and then cooling down and condensing, thus improving the effect of the gas in the hydrogen inlet pipe 140 in carrying water vapor.

[0087] In some embodiments, please refer to Figure 1The hydrogen inlet pipe 140 is connected to the first heater 141, and the steam outlet 121 is also connected to the first heater 141. The first heater 141 is connected to the first gas inlet 111 of the solid oxide electrolysis cell 110. That is, the gas in the hydrogen inlet pipe 140 is heated in the second heat exchanger 500 and then flows to the first heater 141 and is further heated before entering the solid oxide electrolysis cell 110.

[0088] In the above embodiment, the gas in the hydrogen inlet pipe 140 is first heated by the waste heat and then heated by the first heater 141, which reduces the energy consumption of the first heater 141.

[0089] In some embodiments, please refer to Figure 1 The carbon dioxide production apparatus 200 also includes a turbine 260 connected to the steam outlet 213 of the combustion furnace 210, and a generator 270 connected to the turbine 260, the turbine 260 being able to drive the generator 270 to rotate.

[0090] Specifically, the steam evaporated by combustion in the combustion furnace 210 can flow from the steam outlet 213 to the turbine 260 and drive the turbine 260 to rotate. The generator 270 connected to the turbine 260 can be driven by the turbine 260 to generate electricity.

[0091] In some embodiments, the electricity generated by the generator 270 can power one or more of the hydrogen production apparatus 100, carbon dioxide production apparatus 200, and methanol production apparatus 300.

[0092] In the above embodiments, by setting up turbine 260 and generator 270, the energy generated by combustion furnace 210 can be reused, thereby further reducing the energy consumption of carbon dioxide production device 200 or methanol synthesis device.

[0093] In some embodiments, please refer to Figure 1 The hydrogen production apparatus 100 also includes a tail gas outlet pipe 180, which is connected to the tail gas outlet 113 of the solid oxide electrolysis cell 110 and the tail gas inlet 214 of the combustion furnace 210.

[0094] Understandably, the exhaust gas outlet pipe 180 is used to outlet the exhaust gas generated by the solid oxide electrolysis cell 110 during operation. The exhaust gas includes a large amount of oxygen, and the exhaust gas entering the combustion furnace 210 enables the combustion furnace 210 to achieve oxygen-enriched combustion.

[0095] In the above embodiment, by connecting the exhaust gas outlet pipe 180 to the combustion furnace 210, the exhaust gas containing a large amount of oxygen discharged from the solid oxide electrolysis cell 110 is introduced into the combustion furnace 210, thereby increasing the oxygen content in the combustion furnace 210. This couples SOEC technology with oxygen-enriched combustion technology, enabling the solid oxide electrolysis cell 110 to function as an air separation device, reducing the number of devices in the methanol synthesis equipment, and improving the combustion efficiency of the combustion furnace 210.

[0096] In some embodiments, please refer to Figure 1 The hydrogen production apparatus 100 also includes an air inlet pipe 160, which is connected to the second air inlet 114 of the solid oxide electrolysis cell 110; the methanol synthesis apparatus also includes a third heat exchanger 600, which is connected to the air inlet pipe 160 and the exhaust gas outlet pipe 180, and the air inlet pipe 160 and the exhaust gas outlet pipe 180 exchange heat through the third heat exchanger 600.

[0097] Understandably, the gas temperature in the exhaust gas outlet pipe 180 is higher than that in the air inlet pipe 160. In the third heat exchanger 600, the exhaust gas outlet pipe 180 can heat the air inlet pipe 160 to raise the gas temperature in the air inlet pipe 160.

[0098] In some embodiments, the solid oxide electrolytic cell 110 is also connected to a second heater 161, and the air inlet pipe 160 is connected to the second heater 161. That is, the gas in the air inlet pipe 160 is first heated in the third heat exchanger 600, then enters the second heater 161 for heating, and finally enters the solid oxide electrolytic cell 110.

[0099] In the above embodiment, by setting a third heat exchanger 600 to use the waste heat of the exhaust gas generated by the solid oxide electrolysis cell 110 to heat the air about to enter the solid oxide electrolysis cell 110, the waste heat is recovered and utilized, and the energy consumption of the solid oxide electrolysis cell 110 or the second heater 161 is reduced.

[0100] In some embodiments, please refer to Figure 1 The hydrogen production apparatus 100 also includes a second compressor 162, which is located in the air inlet pipe 160 and has its outlet 163 connected to the third heat exchanger 600. The second compressor 162 compresses air to increase the partial pressure of oxygen in the air, thereby improving the reaction efficiency of the solid oxide electrolysis cell 110. Simultaneously, the higher pressure also achieves positive pressure, preventing impurities from seeping in and improving the reliability of the hydrogen production apparatus 100.

[0101] Specifically, the second compressor 162 is located in the air inlet pipe 160, upstream of the third heat exchanger 600.

[0102] Understandably, the air passing through the second compressor 162 is compressed, its internal energy increases, and its temperature rises.

[0103] In the above embodiment, by placing the second compressor 162 upstream of the third heat exchanger 600 in the air inlet pipe 160, the energy obtained by the second compressor 162 can be transferred to the exhaust gas outlet pipe 180 in the third heat exchanger 600 to heat the exhaust gas outlet pipe 180, so that the energy consumed by the second compressor 162 can be utilized as much as possible, thereby improving the energy utilization rate of the entire methanol synthesis equipment.

[0104] In some embodiments, please refer to Figure 1 and Figure 5 The methanol synthesis equipment also includes a fourth heat exchanger 700. The methanol preparation device 300 also includes a reactor 310, a mixed gas inlet pipe 320, and a methanol outlet pipe 330. The reactor 310 has a mixed gas inlet 370. One end of the mixed gas inlet pipe 320 is connected to the mixed gas inlet 370, and the other end of the mixed gas inlet pipe 320 is connected to the end of the hydrogen outlet pipe 150 away from the hydrogen outlet 112 and the end of the flue gas outlet main pipe 220 away from the flue gas outlet 215, respectively. The fourth heat exchanger 700 is connected to the mixed gas inlet pipe 320. The methanol outlet pipe 330 is connected to the methanol outlet 311 of the reactor 310. The fourth heat exchanger 700 is connected to the methanol outlet pipe 330, and the mixed gas inlet pipe 320 and the methanol outlet pipe 330 exchange heat through the fourth heat exchanger 700.

[0105] Specifically, the temperature of the gas mixture inlet pipe 320 is lower, and the temperature of the methanol outlet pipe 330 is higher. The methanol outlet pipe 330 can heat the gas mixture inlet pipe 320 through the fourth heat exchanger 700.

[0106] Specifically, the methanol preparation apparatus 300 also includes a second gas mixing device, which is connected to the mixed gas inlet pipe 320. The output end of the hydrogen outlet pipe 150 and the output end of the flue gas outlet main pipe 220 are respectively connected to the input end of the second gas mixing device. After the hydrogen and flue gas are mixed by the second gas mixing device, they enter the input end of the mixed gas inlet pipe 320 from the output end of the second gas mixing device.

[0107] In some embodiments, the hydrogen outlet line 150 is provided with a first compressor 151, which is capable of compressing the gas in the hydrogen outlet line 150 to create a positive pressure.

[0108] In some embodiments, the flue gas outlet main duct 220 is provided with a third compressor 226, which is capable of compressing the gas in the flue gas outlet main duct 220 to create a positive pressure.

[0109] In some embodiments, the main flue gas outlet 220 is further provided with an adsorption device 225 to further filter impurities in the flue gas after it has been treated by the dust collector 222 and the desulfurization tower 223. Specifically, the adsorption device 225 is disposed between the first heat exchanger 400 and the third compressor 226.

[0110] In the above embodiment, by setting a fourth heat exchanger 700, the waste heat generated by the reactor 310 in the methanol outlet pipeline 330 can be recovered and reused, and the mixed gas inlet pipeline 320 can be heated, thereby reducing the energy consumption of the reactor 310 and improving the energy utilization rate of the methanol preparation device 300.

[0111] In some embodiments, please refer to Figure 1 The methanol preparation apparatus 300 also includes a separation component 332 and a third circulation branch 337. The separation component 332 is disposed in the methanol outlet pipeline 330. The third circulation branch 337 connects the gas outlet 380 of the separation component 332 and the end of the mixed gas inlet pipeline 320 away from the mixed gas inlet 370.

[0112] The separation component 332 includes a high-pressure separation tank 333, a second pressure reducing valve 334, and a low-pressure separation tank 335 connected in sequence. The high-pressure separation tank 333 is connected upstream of the low-pressure separation tank 335, and the second pressure reducing valve 334 is located between the high-pressure separation tank 333 and the low-pressure separation tank 335. The high-pressure separation tank 333 performs preliminary gas-liquid separation. The separated liquid is depressurized by the second pressure reducing valve 334 and then enters the low-pressure separation tank 335 for further gas-liquid separation. One end of the third circulation branch 337 is connected to the high-pressure gas outlet of the high-pressure separation tank 333 and the low-pressure gas outlet of the low-pressure separation tank 335, and the other end is connected to the mixed gas inlet pipeline 320 to collect the gas in the high-pressure separation tank 333 and the low-pressure separation tank 335 and guide it to the mixed gas inlet pipeline 320, thereby increasing the output rate of the methanol preparation unit 300.

[0113] In some embodiments, a fourth compressor 339 is connected to a third circulation branch 337 to compress the gas in the third circulation branch 337 before it enters the mixed gas inlet pipe 320, thereby creating a positive pressure.

[0114] In some embodiments, the methanol outlet pipeline 330 is further connected in sequence to a solution pump 340, a distillation column 350, and a gas-liquid separator 360. The solution pump 340 is used to provide power to the liquid in the fourth sub-pipeline 336, driving the liquid in the fourth sub-pipeline 336; the distillation column 350 is used to control the methanol concentration so that the produced methanol meets production requirements; the gas-liquid separator 360 is used to separate water or other impurities from the methanol.

[0115] In the above embodiment, a separation component 332 is provided to perform gas-liquid separation on the product of reactor 310. The third circulation branch 337 can continue to guide the separated gas to the mixed gas inlet pipe 320 for reaction again, thereby improving the yield of reactor 310.

[0116] In some embodiments, please refer to Figure 1 The third circulation branch 337 is equipped with an exhaust device 338.

[0117] Understandably, as the gas in the third circulation branch 337 continues to circulate, inert gas will gradually accumulate and continuously circulate in the third circulation branch 337, the mixed gas inlet pipe 320, the reactor 310, and the methanol outlet pipe 330, unable to be discharged. In some embodiments, the exhaust device 338 is one of a shut-off valve, a ball valve, a butterfly valve, etc.

[0118] In the above embodiment, by providing an exhaust device 338 in the third circulation branch 337, the operator can periodically release a portion of the gas in the third circulation branch 337 in the form of venting gas, thereby reducing the content of inert gas.

[0119] In some embodiments, the end of the third circulation line 227 away from the gas outlet 380 is connected to the input end of the second mixing device so as to fully mix the gas, hydrogen and oxygen in the third circulation line 227.

[0120] Accordingly, this application also provides a distributed energy system, including a methanol synthesis device as described in any of the above embodiments.

[0121] This distributed energy system can produce methanol fuel from biomass, hydrogen and other raw materials through methanol synthesis equipment, and then use methanol to generate electricity, heat or cool. At the same time, it can recover the waste heat in the operation of the system, so as to achieve efficient recycling of energy.

[0122] The methanol synthesis equipment provided in the embodiments of this application has been described in detail above. Specific examples have been used in this application to illustrate the principles and implementation methods of this application. The description of the above embodiments is only for the purpose of helping to understand the technical solutions and core ideas of this application. Those skilled in the art should understand that they can still modify the technical solutions described in the foregoing embodiments or make equivalent substitutions for some of the technical features. These modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of this application.

Claims

1. A methanol synthesis apparatus, characterized in that, include: A hydrogen production apparatus (100) includes a solid oxide electrolyzer (110), a flash evaporator (120), a water inlet pipe (130), and a hydrogen outlet pipe (150). The first gas inlet (111) of the solid oxide electrolyzer (110) is connected to the steam outlet (121) of the flash evaporator (120), the water inlet pipe (130) is connected to the water inlet (122) of the flash evaporator (120), and the hydrogen outlet pipe (150) is connected to the hydrogen outlet (112) of the solid oxide electrolyzer (110). A carbon dioxide preparation device (200) includes a combustion furnace (210) and a flue gas outlet main path (220), wherein the flue gas outlet main path (220) is connected to the flue gas outlet (215) of the combustion furnace (210); A methanol preparation apparatus (300) is provided, wherein the hydrogen outlet pipeline (150) and the flue gas outlet main pipeline (220) are respectively connected to the mixed gas inlet (370) of the methanol preparation apparatus (300); The first heat exchanger (400) is connected to the flue gas outlet main line (220) and the water inlet line (130). The flue gas outlet main line (220) and the water inlet line (130) exchange heat through the first heat exchanger (400).

2. The methanol synthesis equipment according to claim 1, characterized in that, The carbon dioxide preparation device (200) further includes a first circulation branch (230), one end of which is connected to the circulating gas inlet (211) of the combustion furnace (210), and the other end is connected in parallel to the flue gas outlet main path (220).

3. The methanol synthesis equipment according to claim 2, characterized in that, The end of the first circulation branch (230) away from the circulating gas inlet (211) is connected between the first heat exchanger (400) and the combustion furnace (210).

4. The methanol synthesis equipment according to claim 1, characterized in that, The carbon dioxide production apparatus (200) further includes: A crusher (250) is provided, the discharge port (252) of which is connected to the feed port (212) of the combustion furnace (210). The second circulation branch (240) has one end connected in parallel to the flue gas outlet main road (220) and the other end connected to the drying gas inlet (251) of the crusher (250).

5. The methanol synthesis equipment according to claim 4, characterized in that, The end of the second circulation branch (240) away from the drying gas inlet (251) is connected between the first heat exchanger (400) and the methanol preparation device (300).

6. The methanol synthesis equipment according to claim 1, characterized in that, The hydrogen production apparatus (100) further includes: Hydrogen inlet pipe (140), which is connected to the first gas inlet (111); The methanol synthesis equipment further includes a second heat exchanger (500), which is connected to the hydrogen inlet pipeline (140) and the hydrogen outlet pipeline (150). The hydrogen inlet pipeline (140) and the hydrogen outlet pipeline (150) exchange heat through the second heat exchanger (500). The hydrogen production apparatus (100) further includes a tail gas outlet pipe (180), which connects the tail gas outlet (113) of the solid oxide electrolysis cell (110) and the tail gas inlet (214) of the combustion furnace (210).

7. The methanol synthesis equipment according to claim 6, characterized in that, The hydrogen production apparatus (100) further includes an air inlet pipe (160), which is connected to the second air inlet (114) of the solid oxide electrolytic cell (110); The methanol synthesis equipment further includes a third heat exchanger (600), which is connected to the air inlet pipe (160) and the exhaust gas outlet pipe (180). The air inlet pipe (160) and the exhaust gas outlet pipe (180) exchange heat through the third heat exchanger (600).

8. The methanol synthesis equipment according to claim 7, characterized in that, The hydrogen production apparatus (100) further includes a second compressor (162), which is disposed in the air inlet pipe (160), and the outlet (163) of the second compressor (162) is connected to the third heat exchanger (600).

9. The methanol synthesis equipment according to claim 1, characterized in that, The methanol synthesis equipment also includes a fourth heat exchanger (700); The methanol preparation apparatus (300) further includes: The reactor (310) has the mixed gas inlet (370); A gas mixture inlet pipe (320) is provided, one end of which is connected to the gas mixture inlet (370), and the other end of which is connected to the end of the hydrogen outlet pipe (150) away from the hydrogen outlet (112) and the end of the flue gas outlet main pipe (220) away from the flue gas outlet (215), respectively. The fourth heat exchanger (700) is connected to the gas mixture inlet pipe (320). A methanol outlet pipeline (330) is connected to the methanol outlet (311) of the reactor (310). A fourth heat exchanger (700) is connected to the methanol outlet pipeline (330). The mixed gas inlet pipeline (320) and the methanol outlet pipeline (330) exchange heat through the fourth heat exchanger (700).

10. The methanol synthesis equipment according to claim 9, characterized in that, The methanol preparation apparatus (300) further includes: A separation component (332) is disposed in the methanol outlet pipeline (330); The third circulation branch (337) connects the gas outlet (380) of the separation component (332) and the end of the mixed gas inlet pipe (320) away from the mixed gas inlet (370); The third circulation branch (337) is equipped with an exhaust device (338).

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