Apparatus for adjusting the ratio of methanol reforming products, synthesis apparatus and synthesis method

Abstract

This invention relates to a ratio adjustment device, synthesis apparatus, and synthesis method for methanol reforming products, relating to the field of product synthesis. The device includes: a buffer tank with an annular branch pipe disposed on the outer side of its central portion, connected to the buffer tank via at least one channel, and the annular branch pipe having an outlet; a methanol reforming product inlet disposed on the bottom side of the buffer tank; a baffle disposed on the inner wall of the buffer tank, the bottom of the baffle being lower than the methanol reforming product inlet, the angle between the baffle and the inner wall being acute, and the lowest point of the baffle being higher than the highest point of the methanol reforming product inlet; the methanol reforming product inlet being connected to the annular branch pipe via a branch pipe, the branch pipe being equipped with a valve; and an outlet at the top and bottom of the buffer tank. The ratio adjustment device provided by this invention can flexibly supply raw materials with different ratios of carbon dioxide / hydrogen, carbon monoxide / hydrogen, and carbon dioxide / carbon monoxide / hydrogen.

Description

Technical Field

[0001] This invention relates to the field of product synthesis technology, specifically to a ratio adjustment device, synthesis apparatus, and synthesis method for methanol reforming products, and more particularly to a ratio adjustment device for methanol reforming products, a synthesis apparatus based on methanol reforming, and a synthesis method. Background Technology

[0002] Currently, in order to promote the goal of carbon neutrality, the use of renewable biomass gasification to produce syngas and the downstream production of green chemicals have become key research directions, especially the conversion of biomass energy into liquid fuels. However, biomass gasification technology and equipment are still in the research and development stage.

[0003] If the purpose is only to conduct subsequent chemical synthesis experiments, the source of syngas may be the coal gasification process. Syngas produced by this process is relatively low-cost and the technology is mature. However, the problem is that the syngas produced by coal gasification contains sulfur of different components, which will cause catalyst poisoning in subsequent chemical synthesis and affect the performance evaluation of the catalyst.

[0004] Based on this, the commonly used chemical pilot-scale experimental system is the methanol reforming gasification system, which uses syngas, carbon dioxide-rich syngas hydrogenation, and pure carbon dioxide hydrogenation as raw materials. By adjusting the reaction between methanol and water, a variety of raw materials with different ratios can be supplied, and the technology is relatively mature.

[0005] For example, CN100406375C describes a method for producing hydrogen from methanol through reforming, belonging to the field of industrial gas preparation technology. The method involves mixing methanol and water, pressurizing the mixture, and feeding it into a vaporization superheater. Once the reaction temperature is reached, the mixture enters a converter, where it is reformed under the action of a catalyst to generate reformed gas. This reformed gas is then cooled to room temperature. The key feature is that the reformed gas is purified and then fed into a pressure swing adsorption (PSA) decarbonization unit containing a decarbonization adsorbent to remove carbon dioxide, yielding decarbonized crude hydrogen containing H2, CO, and CH4. This decarbonized crude hydrogen is then fed into a PSA hydrogen extraction unit using molecular sieves as the main adsorbent to remove all impurities, yielding product hydrogen. The tail gas from the hydrogen extraction unit is pressurized and incorporated into a methanol-water mixture from the vaporization superheater before entering the converter. The tail gas from the decarbonization unit is directly discharged.

[0006] It is known that the product gas obtained from existing methanol reforming contains a certain amount of carbon dioxide, which is usually emitted as waste gas. Furthermore, chemical synthesis experiments involving carbon dioxide or carbon dioxide-rich hydrogenation have strict requirements for carbon dioxide feedstocks. If carbon dioxide is obtained through biomass combustion, it will involve numerous processes, including raw material processing, utilization of combustion heat, and carbon dioxide purification. In addition, if carbon dioxide is obtained through capture in coal-fired power plants, similar issues arise regarding low-cost capture, transportation, and large-capacity storage. In short, these processes will significantly increase the investment in experimental research, hindering demonstration and pilot-scale chemical synthesis experiments. Summary of the Invention

[0007] In view of the problems existing in the prior art, the purpose of the present invention is to provide a ratio adjustment device, a synthesis device and a synthesis method for methanol reforming products, so as to solve the defect of poor utilization effect of existing methanol reforming products.

[0008] To achieve this objective, the present invention adopts the following technical solution:

[0009] In a first aspect, the present invention provides a ratio adjustment device for methanol reforming products, the ratio adjustment device comprising:

[0010] A buffer tank, wherein an annular diversion pipe is provided on the outer side of the middle part of the buffer tank, the annular diversion pipe is connected to the buffer tank through at least one channel, and the annular diversion pipe is provided with a first outlet and a second outlet;

[0011] The bottom side of the buffer tank is provided with a methanol reforming product inlet. A baffle is provided on the inner wall of the buffer tank for the methanol reforming product inlet. The bottom of the baffle is lower than the methanol reforming product inlet. The angle between the baffle and the inner wall where the methanol reforming product inlet is located is an acute angle. The lowest point of the top of the baffle is higher than the highest point of the top of the methanol reforming product inlet.

[0012] The methanol reforming product inlet is connected to an annular branch pipe via a branch pipe, and a first valve is installed on the branch pipe;

[0013] The buffer tank has a third outlet at the top and a fourth outlet at the bottom.

[0014] The proportioning adjustment device provided by this invention can flexibly supply raw materials with different proportions of carbon dioxide / hydrogen, carbon monoxide / hydrogen, and carbon dioxide / carbon monoxide / hydrogen, rapidly promote pilot-scale green chemical experimental research, and facilitate experimental verification research on carbon dioxide hydrogenation, carbon dioxide-rich syngas, and syngas chemical preparation.

[0015] As a preferred embodiment of the present invention, both the third outlet and the fourth outlet are equipped with control valves.

[0016] Secondly, the present invention provides a methanol reforming-based synthesis apparatus, the methanol reforming-based synthesis apparatus comprising:

[0017] It includes a methanol reforming unit, a proportioning adjustment device as described in the first aspect, and a synthesis unit connected in sequence.

[0018] The product outlet of the methanol reforming unit is connected to the methanol reforming product inlet;

[0019] The feed inlet of the synthesis unit is connected to either the first outlet or the second outlet.

[0020] As a preferred embodiment of the present invention, the methanol reforming unit includes a methanol-water storage device, a first pump, a first heat exchanger, a second heat exchanger, and a reforming reactor connected in sequence.

[0021] As a preferred embodiment of the present invention, a second valve is provided on the pipeline between the first pump and the first heat exchanger.

[0022] As a preferred embodiment of the present invention, the top side outlet of the reforming reactor is sequentially connected to a second heat exchanger, a first heat exchanger, a second pump, and a heating device.

[0023] As a preferred embodiment of the present invention, the outlet of the heating device is connected to the bottom side inlet of the reforming reactor.

[0024] Preferably, the product outlet of the reforming reactor is connected to the methanol reforming product inlet.

[0025] As a preferred embodiment of the present invention, the synthesis unit includes a synthesis reactor and a heat exchange device.

[0026] Preferably, a third pump is provided between the synthesis reactor and the heat exchange equipment.

[0027] Thirdly, the present invention provides a synthesis method based on methanol reforming, the synthesis method based on methanol reforming comprising:

[0028] A methanol-water reforming reaction is carried out, and the proportions of the materials obtained from the methanol-water reforming reaction are adjusted before being fed into the synthesis unit for synthesis.

[0029] As a preferred technical solution of the present invention, the matching of raw material gas and synthetic product is achieved by adjusting the ratio adjustment device during the synthesis.

[0030] Preferably, the synthesis includes the hydrogenation of carbon dioxide to produce aromatics, methanol, olefins, or aviation kerosene.

[0031] Compared with existing technical solutions, the present invention has the following beneficial effects:

[0032] (1) The device provided by the present invention uses a methanol steam reforming unit to prepare raw material gas for chemical synthesis in situ. The amount and composition of the raw material gas are adjustable, avoiding the transportation and storage of hazardous chemical hydrogen. The device is simple to operate and has low energy consumption, making it suitable for pilot-scale chemical synthesis systems. The raw material gas obtained by methanol steam reforming has high purity and no toxic substances, which can improve the stability of chemical catalysts and facilitate the preparation of chemicals for subsequent pilot-scale projects.

[0033] (2) The proportioning adjustment device provided by the present invention can freely adjust the proportion of carbon dioxide, carbon monoxide and hydrogen components in the raw gas, meet the needs of subsequent preparation of monocyclic aromatic hydrocarbons, simplify separation equipment, and reduce separation energy consumption and separation cost.

[0034] (3) The synthesis apparatus provided by this invention is based on the endothermic and exothermic characteristics of chemical reactions in chemical synthesis. The reaction heat recovery system can realize the recovery and optimized use of reaction heat, thereby reducing carbon emissions. At the same time, the system can provide solutions for energy optimization in engineering projects and can predict the economics of projects. Attached Figure Description

[0035] Figure 1 This is a schematic diagram of the proportioning adjustment device for methanol reforming products provided in an embodiment of the present invention;

[0036] Figure 2 This is a schematic diagram showing the position of the baffle in an embodiment of the present invention;

[0037] Figure 3 This is a schematic diagram of the annular shunt pipe in an embodiment of the present invention;

[0038] Figure 4 This is a schematic diagram of a methanol reforming-based synthesis apparatus provided in an embodiment of the present invention.

[0039] In the diagram: 100 - Proportioning adjustment device, 110 - Methanol reforming product inlet, 111 - Baffle, 120 - Diverter branch pipe, 121 - First valve, 130 - Annular diverter pipe, 131 - First outlet, 132 - Second outlet, 133 - First channel, 134 - Second channel, 135 - Third channel, 140 - Third outlet, 150 - Fourth outlet;

[0040] 200-Methanol-Water Storage Equipment, 300-First Pump, 400-Second Valve, 500-Reform Reactor, 510-First Heat Exchanger, 520-Second Heat Exchanger, 530-Second Pump, 540-Heating Equipment, 600-Synthesis Reactor, 610-Third Pump, 620-Heat Exchange Equipment.

[0041] The present invention will now be described in further detail. However, the examples described below are merely simplified examples of the present invention and do not represent or limit the scope of protection of the present invention. The scope of protection of the present invention is determined by the claims. Detailed Implementation

[0042] To better illustrate the present invention and facilitate understanding of its technical solutions, typical but non-limiting embodiments of the present invention are as follows:

[0043] This embodiment provides a device for adjusting the proportions of methanol reforming products, such as... Figure 1 As shown, the proportioning adjustment device 100 includes:

[0044] A buffer tank, wherein an annular diversion pipe 130 is provided on the outer side of the middle part of the buffer tank, the annular diversion pipe 130 is connected to the buffer tank through at least one channel, and the annular diversion pipe 130 is provided with a first outlet 131 and a second outlet 132.

[0045] A methanol reforming product inlet 110 is provided on the bottom side of the buffer tank. A baffle 111 is installed on the inner wall of the buffer tank above the methanol reforming product inlet 110. The bottom of the baffle 111 is lower than the methanol reforming product inlet 110, and the angle between the baffle 111 and the inner wall of the methanol reforming product inlet 110 is an acute angle. The lowest point of the top of the baffle 111 is higher than the highest point of the top of the methanol reforming product inlet 110. Figure 2 As shown;

[0046] The methanol reforming product inlet 110 is connected to the annular branch pipe 130 through the branch pipe 120, and the branch pipe 120 is equipped with a first valve 121.

[0047] The buffer tank is provided with a third outlet 140 at the top and a fourth outlet 150 at the bottom.

[0048] Both the third outlet 140 and the fourth outlet 150 are equipped with control valves.

[0049] A compression pump is connected to either the first outlet 131 or the second outlet 132.

[0050] An acute angle is defined as an angle greater than 0° and less than 90°.

[0051] In this embodiment, the separation principle of the proportioning adjustment device 100 is as follows:

[0052] The raw material gas mixture of H2 / CO / CO2 is input from methanol reforming product inlet 110. After passing through baffle 111, the flow direction of the raw material gas changes to promote the stratification of H2 and CO / CO2 (this has two stratification effects: first, it enables the mixed gas to flow upward and to both sides of the buffer, and the heavy fluid sinks during the upward and lateral flow; second, it prevents the raw material from mixing with the sinking CO / CO2). After stratification, the denser component CO / CO2 accumulates in the lower half of the buffer tank, especially in the narrower bottom hemispherical tank area, while the lighter component H2 accumulates in the upper half of the buffer tank, with the middle area being the mixture of H2 and CO / CO2.

[0053] The intermediate material flows through the annular diversion pipe 130, which has a first outlet 131 and a second outlet 132 at both ends. The first outlet 131 and the second outlet 132 can be connected to a compressor pump to pressurize the mixture at the rear end. When the first outlet 131 is connected to the compressor pump, the H2 / CO / CO2 mixture is diverted in the annular channel. Some of the gas flows downward into the inlet pipe (here, due to the compressor pump drawing air, the gas in the annular channel is diverted to the inlet, and the annular channel also serves to divert the denser gas to the inlet pipe, increasing the content ratio of the lighter gas component). The remaining gas enters the compressor pump, and the opening of the first valve 121 is used to adjust the ratio of H2 to CO / CO2 mixture in the compressor pump. When the second outlet 132 is connected to the compressor pump, the annular channel receives the diverted gas from the inlet pipe (the diversion branch pipe 120 tends to divert the lighter gas upward, which can also increase the content ratio of the lighter gas component). Similarly, the gas ratio can be dynamically adjusted through the second valve 400.

[0054] Furthermore, a third outlet 140 is provided at the top of the buffer tank to discharge the light gas component H2 from the buffer tank. The outlet flow rate of the third outlet 140 can be adjusted by a control valve to reduce the proportion of the light gas component at the first outlet 131 or the second outlet 132.

[0055] Furthermore, a fourth outlet 150 is provided at the bottom of the buffer tank to discharge the CO / CO2 mixture, which is denser gas component, from the buffer tank. The outlet flow rate of the fourth outlet 150 can be adjusted by a control valve to increase the proportion of low-density gas component at the first outlet 131 or the second outlet 132.

[0056] In summary, although the product obtained at the bottom of the reforming reactor 500 is a mixture of H2 / CO / CO2, the controllable proportion of the H2 / CO / CO2 mixture raw material can be supplied to the subsequent chemical synthesis section under the combined effects of vertical stratification by the column buffer, circulation and accumulation of heavy gas components in the annular channel, bottom discharge of heavy gas components, and regulation by the light and heavy component control valve.

[0057] Therefore, the composition of the feed gas can be controlled using a proportioning adjustment device, allowing for the preparation of feed gas with different component ratios required for the synthesis of various high-value chemicals. The concentration error of the prepared feed gas is <10%, as shown in Table 1. Based on the endothermic and exothermic characteristics of the reaction process, a reaction heat recovery system can be matched to the synthesis system to achieve full utilization of energy.

[0058] Table 1

[0059]

[0060]

[0061] Furthermore, the annular diverter 130 is connected to the buffer tank through at least one channel, the specific connection to which can be selected based on the separation requirements. For example, if the annular diverter 130 is selected to connect to the buffer tank through three channels, then... Figure 3 As shown, the annular shunt pipe 130 is connected to the buffer tank via the first channel 133, the second channel 134, and the third channel 135.

[0062] Furthermore, this embodiment provides a synthesis apparatus based on methanol reforming, such as... Figure 4 As shown, the methanol reforming-based synthesis apparatus includes:

[0063] It includes a methanol reforming unit, a proportioning adjustment device 100 as described above, and a synthesis unit connected in sequence.

[0064] The product outlet of the methanol reforming unit is connected to the methanol reforming product inlet 110;

[0065] The feed inlet of the synthesis unit is connected to either the first outlet 131 or the second outlet 132.

[0066] Furthermore, the feed inlet of the synthesis unit is connected to either the first outlet 131 or the second outlet 132 via a compression pump.

[0067] In this invention, the methanol reforming unit includes equipment capable of realizing methanol steam reforming reaction and / or methanol reforming reaction.

[0068] Specifically, methanol steam can be reformed to produce a mixed feed gas containing CO2, CO, and H2. By adjusting the ratio of methanol to water, temperature, and type of catalyst, feed gas with different compositions can be obtained, which can then be used to synthesize various chemicals. The main chemical reactions occurring in the methanol reforming reactor 500 are as follows:

[0069] CH3OH + H2O → CO2 + 3H2

[0070] CH3OH→CO+2H2

[0071] When the methanol / water molar ratio is less than or equal to 1:1, the mixed gas theoretically consists mainly of CO2 and H2, with a molar ratio close to 1:3. When the methanol / water molar ratio is greater than 1:1, the mixed gas theoretically contains CO2, CO, and H2, with a (CO2+CO) / H2 molar ratio between 1:3 and 1:2. When the feedstock is only methanol, the mixed gas theoretically consists mainly of CO and H2, with a CO / H2 molar ratio around 1:2. In summary, by changing the molar ratio of methanol and water, the carbon-hydrogen molar ratio in the feedstock gas can be controlled within the range of 1:3 to 1:2.

[0072] Furthermore, when the composition of the raw material gas required for the synthesis of chemicals is not within the above range, the mixed gas prepared above can be appropriately separated to obtain a mixed gas with a specific composition for subsequent chemical preparation.

[0073] For example, the methanol reforming unit includes a methanol-water storage device 200, a first pump 300, a first heat exchanger 510, a second heat exchanger 520, and a reforming reactor 500 connected in sequence.

[0074] A second valve 400 is installed on the pipeline between the first pump 300 and the first heat exchanger 510.

[0075] The top side outlet of the reforming reactor 500 is sequentially connected to the second heat exchanger 520, the first heat exchanger 510, the second pump 530, and the heating device 540.

[0076] The outlet of the heating device 540 is connected to the bottom side inlet of the reforming reactor 500.

[0077] The product outlet of the reforming reactor 500 is connected to the methanol reforming product inlet 110.

[0078] The synthesis unit includes a synthesis reactor 600 and a heat exchange device 620.

[0079] A third pump 610 is configured between the synthesis reactor 600 and the heat exchange device 620.

[0080] Furthermore, this embodiment provides a synthesis method based on methanol reforming, the synthesis method based on methanol reforming comprising:

[0081] A methanol-water reforming reaction is carried out, and the proportions of the materials obtained from the methanol-water reforming reaction are adjusted before being fed into the synthesis unit for synthesis.

[0082] In the synthesis process, the matching of raw material gas and synthesized product is achieved by adjusting the ratio adjustment device.

[0083] The synthesis includes the hydrogenation of carbon dioxide to produce aromatics, methanol, olefins, or aviation kerosene.

[0084] Furthermore, to illustrate the excellent adjustment effect achievable by the proportioning adjustment device provided by the present invention, the following practical example is used for explanation:

[0085] The device is as follows:

[0086] It includes a methanol reforming unit, a proportioning adjustment device 100 as described above, and a synthesis unit connected in sequence.

[0087] The product outlet of the methanol reforming unit is connected to the methanol reforming product inlet 110;

[0088] The feed inlet of the synthesis unit is connected to either the first outlet 131 or the second outlet 132.

[0089] The feed inlet of the synthesis unit is connected to either the first outlet 131 or the second outlet 132 via a compression pump.

[0090] The methanol reforming unit includes a methanol-water storage device 200, a first pump 300, a first heat exchanger 510, a second heat exchanger 520, and a reforming reactor 500 connected in sequence. A second valve 400 is installed on the pipeline between the first pump 300 and the first heat exchanger 510. The top side outlet of the reforming reactor 500 is connected in sequence to the second heat exchanger 520, the first heat exchanger 510, the second pump 530, and a heating device 540. The outlet of the heating device 540 is connected to the bottom side inlet of the reforming reactor 500. The product outlet of the reforming reactor 500 is connected to the methanol reforming product inlet 110.

[0091] The proportioning adjustment device 100 includes: a buffer tank, an annular diversion pipe 130 disposed on the outer side of the middle part of the buffer tank, the annular diversion pipe 130 being connected to the buffer tank through three channels, such as a first channel 133, a second channel 134, and a third channel 135; the annular diversion pipe 130 being provided with a first outlet 131 and a second outlet 132; a methanol reforming product inlet 110 disposed on the bottom side of the buffer tank, the methanol reforming product inlet 110 being provided with a baffle 111 on the inner wall of the buffer tank; the baffle 111... The baffle 111 is positioned below the methanol reforming product inlet 110. The angle between the baffle 111 and the inner wall of the methanol reforming product inlet 110 is 45°. The lowest point of the top of the baffle 111 is higher than the highest point of the top of the methanol reforming product inlet 110. The methanol reforming product inlet 110 is connected to the annular branch pipe 130 through a branch pipe 120. A first valve 121 is installed on the branch pipe 120. A third outlet 140 is provided at the top of the buffer tank, and a fourth outlet 150 is provided at the bottom. Both the third outlet 140 and the fourth outlet 150 are equipped with control valves.

[0092] The synthesis unit includes a synthesis reactor 600 and a heat exchange device 620; a third pump 610 is configured between the synthesis reactor 600 and the heat exchange device 620.

[0093] Example 1

[0094] Taking a pilot project with an annual production of 100 tons of monocyclic aromatic hydrocarbons as an example, the required feed gas is a mixture of CO2 and H2, with a molar ratio of CO2 to H2 of 1:6, a CO2 conversion rate of 40%, an aromatic hydrocarbon selectivity of 60%, and a required feed gas consumption of 1750 tons, of which 1375 tons are CO2 and 375 tons are H2.

[0095] A mixture of CO2 and H2 is prepared by a methanol reforming unit. The feed molar ratio of green methanol to water vapor is 1:1, resulting in a CO2 to H2 molar ratio of approximately 1:3 in the mixture. This mixture undergoes partial separation via a methanol reforming product proportioning adjustment device, yielding 1750 tons (V) of feed gas from either the first or second outlet. CO2 / V H2 =1:6, including 375 tons of H2 and 1375 tons of CO2), the fourth outlet yields a CO2 enriched mixture (CO2 concentration of about 75%), which can be further used to synthesize other green chemicals.

[0096] The reforming reaction is carried out at a temperature of 250℃ and a pressure of 1.5MPa. The methanol reforming unit can provide a continuous and stable gas source for the pilot-scale aromatics preparation system, ensuring the smooth operation of the pilot project.

[0097] The raw material gas prepared above is introduced into the synthesis unit to prepare aromatics. This is a reaction of CO2 plus H2 to produce aromatics, with methanol as the intermediate product. The first reaction, CO2 plus H2 to produce methanol, is a low-temperature (250°C) reaction, followed by the methanol to aromatics synthesis process, which is a high-temperature (350°C) process. The reaction heat recovery system can control different temperature ranges by recovering and utilizing energy, thereby achieving efficient energy utilization while improving reaction conversion rate and selectivity.

[0098] Example 2

[0099] Taking a pilot project with an annual production capacity of 100 tons of methane as an example, the required feed gas is a mixture of CO and H2, with a molar ratio of CO to H2 of 1:3. The CO conversion rate is 100%, the selectivity is 95%, and the required feed gas consumption is approximately 223.7 tons, of which 184.2 tons are CO and 39.5 tons are H2.

[0100] A mixture of CO and H2 is produced by a methanol reforming unit. The feedstock is green methanol, resulting in a CO to H2 molar ratio of approximately 1:2. This mixture undergoes partial separation via a methanol reforming product proportioning adjustment device, yielding 223.7 tons (V) of feed gas at the first outlet. CO / V H2 =1:3, including 39.5 tons of H2 and 184.2 tons of CO), the fourth outlet yields a CO-enriched mixture (CO concentration of approximately 60%), which can be further used to synthesize other green chemicals.

[0101] The reforming reaction is carried out at a temperature of 250℃ and a pressure of 1.5 MPa. The methanol reforming unit can provide a continuous and stable gas source for the pilot-scale methane production system, ensuring the smooth operation of the pilot project.

[0102] The prepared feed gas was introduced into the synthesis unit to produce methane at a reaction temperature of 350°C and a reaction pressure of 3.0 MPa. This reaction is exothermic, and the reaction heat recovery system can preheat and deheat the feed gas and reactor by recovering and utilizing energy, thus ensuring stable reaction operation.

[0103] Example 3

[0104] Taking a pilot project with an annual production capacity of 200 tons of butyraldehyde as an example, the required feed gas is a mixture of CO and H2, with a CO / H2 molar ratio of 1:1, a CO conversion rate of 90%, and a selectivity of 100%. The required propylene and feed gas consumption are 130 tons and 92 tons, respectively, of which the feed gas contains approximately 86 tons of CO and 6 tons of H2.

[0105] A mixture of CO and H2 is prepared by a methanol reforming unit using green methanol as feedstock. The resulting mixture has a CO to H2 molar ratio of approximately 1:2. This mixture undergoes partial separation via a methanol reforming product proportioning adjustment device, yielding 92 tons (V) of feedstock gas from either the first or second outlet. CO / V H2 =1:1, 6 tons of H2 and 86 tons of CO), the third outlet can produce a concentrated H2 mixture (H2 concentration of about 80%), which can be further used to synthesize other green chemicals.

[0106] The reforming reaction is carried out at a temperature of 250℃ and a pressure of 1.5MPa. The methanol reforming unit can provide a continuous and stable gas source for the pilot-scale aliphatic aldehyde preparation system, ensuring the smooth operation of the pilot project.

[0107] The prepared feed gas is introduced into the synthesis unit to react with propylene to produce butyraldehyde. The reaction temperature is 100℃ and the reaction pressure is 1.8MPa. This reaction process is exothermic. The reaction heat recovery system can preheat and deheat the feed gas and reactor by recovering and utilizing energy, so as to achieve stable and continuous operation of the reaction.

[0108] Example 4

[0109] Taking a pilot project with an annual production of 100 tons of methanol as an example, the required feed gas is a mixture of CO2, CO and H2, with a molar ratio of 1:6:13. The required feed gas consumption is approximately 315 tons, of which CO2 accounts for 58.3 tons, CO accounts for approximately 222.4 tons, and H2 accounts for 34.3 tons.

[0110] A mixture of CO2, CO, and H2 is prepared by a methanol reforming unit. The feed molar ratio of green methanol to water vapor is 7:1, resulting in a CO2:CO:H2 molar ratio of 1:6:15 in the mixture. This mixture undergoes partial separation via a methanol reforming product proportioning adjustment device, yielding 315 tons (V) of feed gas from either the first or second outlet. CO2 / V CO / V H2 =1:6:13, including 34.3 tons of H2, 222.4 tons of CO and 58.3 tons of CO2), the third outlet can obtain H2 concentrated gas mixture (H2 concentration of about 74%), which can be further used to synthesize other green chemicals.

[0111] The reforming reaction is carried out at a temperature of 250℃ and a pressure of 1.5MPa. The methanol reforming unit can provide a continuous and stable gas source for the pilot-scale methanol preparation system, ensuring the smooth operation of the pilot project.

[0112] The prepared feed gas was introduced into the synthesis unit to produce methanol at a reaction temperature of 250°C and a reaction pressure of 6.0 MPa. This reaction process is a reversible exothermic reaction with reduced volume. The reaction heat recovery system can preheat and deheat the feed and reactor by recovering and utilizing energy, thus achieving stable operation of the reaction.

[0113] Example 5

[0114] Taking a pilot project with an annual production of 100 tons of methanol as an example, the required feed gas is a mixture of CO2, CO and H2, with a molar ratio of 1:6:17. The required feed gas consumption is approximately 325.6 tons, of which CO2 accounts for 58.3 tons, CO accounts for approximately 222.4 tons, and H2 accounts for 44.9 tons.

[0115] The raw CO2, CO, and H2 mixture was prepared by a methanol reforming unit with a feed molar ratio of 4:1 for green methanol and water vapor. The resulting mixture had a CO2:CO:H2 molar ratio of 2:6:18. This mixture underwent partial separation via a methanol reforming product proportioning adjustment device, yielding 325.6 tons (V) of raw gas from either the first or second outlet. CO2 / V CO / V H2 =1:6:17, including 44.9 tons of H2, 222.4 tons of CO and 58.3 tons of CO2), the third outlet can produce a concentrated H2 mixture (H2 concentration of 81%), and the fourth outlet can produce a concentrated CO2 mixture (CO2 concentration of 15%). The concentrated H2 mixture and the concentrated CO2 mixture can be used to synthesize other green chemicals respectively.

[0116] The reforming reaction is carried out at a temperature of 250℃ and a pressure of 1.5MPa. The methanol reforming unit can provide a continuous and stable gas source for the pilot-scale methanol preparation system, ensuring the smooth operation of the pilot project.

[0117] The preferred embodiments of the present invention have been described in detail above. However, the present invention is not limited to the specific details in the above embodiments. Within the scope of the technical concept of the present invention, various simple modifications can be made to the technical solution of the present invention, and these simple modifications all fall within the protection scope of the present invention.

[0118] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner without contradiction. In order to avoid unnecessary repetition, the present invention will not describe the various possible combinations separately.

[0119] Furthermore, various different embodiments of the present invention can be combined in any way, as long as they do not violate the spirit of the present invention, they should also be regarded as the content disclosed by the present invention.

Claims

1. A device for adjusting the proportions of methanol reforming products, characterized in that, The proportioning adjustment device includes: A buffer tank, wherein an annular diversion pipe is provided on the outer side of the middle part of the buffer tank, the annular diversion pipe is connected to the buffer tank through at least one channel, and the annular diversion pipe is provided with a first outlet and a second outlet; The bottom side of the buffer tank is provided with a methanol reforming product inlet. A baffle is provided on the inner wall of the buffer tank for the methanol reforming product inlet. The bottom of the baffle is lower than the methanol reforming product inlet. The angle between the baffle and the inner wall where the methanol reforming product inlet is located is an acute angle. The lowest point of the top of the baffle is higher than the highest point of the top of the methanol reforming product inlet. The methanol reforming product inlet is connected to an annular branch pipe via a branch pipe, and a first valve is installed on the branch pipe; The buffer tank has a third outlet at the top and a fourth outlet at the bottom.

2. The proportioning adjustment device for methanol reforming products as described in claim 1, characterized in that, Both the third and fourth outlets are equipped with control valves; Preferably, the first outlet or the second outlet is connected to a compression pump.

3. A synthesis apparatus based on methanol reforming, characterized in that, The methanol reforming-based synthesis apparatus includes: It includes a methanol reforming unit, a proportioning adjustment device as described in claim 1 or 2, and a synthesis unit connected in sequence; The product outlet of the methanol reforming unit is connected to the methanol reforming product inlet; The feed inlet of the synthesis unit is connected to either the first outlet or the second outlet.

4. The methanol reforming-based synthesis apparatus as described in claim 3, characterized in that, The methanol reforming unit includes a methanol-water storage device, a first pump, a first heat exchanger, a second heat exchanger, and a reforming reactor connected in sequence.

5. The methanol reforming-based synthesis apparatus as described in claim 4, characterized in that, A second valve is installed on the pipeline between the first pump and the first heat exchanger.

6. The methanol reforming-based synthesis apparatus as described in claim 4 or 5, characterized in that, The top side outlet of the reforming reactor is connected in sequence to the second heat exchanger, the first heat exchanger, the second pump, and the heating equipment.

7. The methanol reforming-based synthesis apparatus as described in claim 6, characterized in that, The outlet of the heating equipment is connected to the bottom side inlet of the reforming reactor; Preferably, the product outlet of the reforming reactor is connected to the methanol reforming product inlet.

8. The methanol reforming-based synthesis apparatus according to any one of claims 3-7, characterized in that, The synthesis unit includes a synthesis reactor and a heat exchange device; Preferably, a third pump is provided between the synthesis reactor and the heat exchange equipment.

9. A synthesis method based on methanol reforming, characterized in that, The methanol reforming-based synthesis method includes: A methanol-water reforming reaction is carried out, and the proportions of the materials obtained from the methanol-water reforming reaction are adjusted before being fed into the synthesis unit for synthesis.

10. The synthesis method based on methanol reforming as described in claim 9, characterized in that, The matching of raw material gas and synthetic product is achieved by adjusting the ratio adjustment device in the synthesis process. Preferably, the synthesis includes the hydrogenation of carbon dioxide to produce aromatics, methanol, olefins, or aviation kerosene.

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