In-situ dehydration high-conversion-rate methanol synthesis system

Abstract

The utility model discloses an in-situ dehydration high-conversion-rate methanol synthesis system, and relates to the technical field of fuel synthesis equipment. In the in-situ dehydration high-conversion-rate methanol synthesis system, an inlet of a synthesis tower A and an inlet of a synthesis tower B are communicated with an outlet of a gas raw material supply assembly, so that gas raw materials required by reaction are input into the synthesis tower A and the synthesis tower B; an outlet of the synthesis tower A and an outlet of the synthesis tower B are communicated with an inlet of the methanol discharge assembly so as to discharge methanol; the first switch valve A is arranged between an inlet of the synthesis tower A and an outlet of the gas raw material supply assembly, and the second switch valve A is arranged between an outlet of the synthesis tower A and an inlet of the methanol discharge assembly; the first switch valve B is arranged between the inlet of the synthesis tower B and the outlet of the gas raw material supply assembly, and the second switch valve B is arranged between the outlet of the synthesis tower B and the inlet of the methanol discharge assembly. By using the methanol synthesis system, the conversion rate of methanol synthesis reaction can be increased.

Description

Technical Field

[0001] This application relates to the field of fuel synthesis equipment technology, and more specifically, to an in-situ dehydration high-conversion methanol synthesis system. Background Technology

[0002] The hydrogenation of carbon dioxide into methanol is an environmentally friendly reaction, and since methanol is a fuel, it not only helps address the problem of excessive carbon dioxide emissions but also reduces the consumption of fossil resources. The most common method for producing methanol is to utilize... This synthesis catalyst catalyzes the hydrogenation of carbon dioxide to synthesize methanol under high temperature and high pressure, but it suffers from low conversion rate. Currently, the following methods exist to improve the conversion rate: unreacted gaseous feedstock is recycled back to the reactor inlet so that it can participate in the methanol synthesis process again. However, this will lead to higher operating energy consumption.

[0003] In conclusion, improving the conversion rate of methanol synthesis is a problem that urgently needs to be solved by those skilled in the art. Utility Model Content

[0004] In view of this, the purpose of this application is to provide an in-situ dehydration high-conversion methanol synthesis system, which can improve the conversion rate of methanol synthesis reaction.

[0005] To achieve the above objectives, this application provides the following technical solution:

[0006] A high-conversion methanol synthesis system with in-situ dehydration includes: a gas feedstock supply component, a synthesis tower A, a synthesis tower B, a methanol discharge component, a first switching valve A, a second switching valve A, a first switching valve B, and a second switching valve B.

[0007] The inlet of synthesis tower A and the inlet of synthesis tower B are both connected to the outlet of the gas feedstock supply assembly, so as to input the gas feedstock required for the reaction into synthesis tower A and synthesis tower B;

[0008] The outlets of synthesis tower A and synthesis tower B are both connected to the inlet of the methanol discharge assembly to discharge methanol.

[0009] The first switching valve A is located between the inlet of the synthesis tower A and the outlet of the gas feedstock supply component, and the second switching valve A is located between the outlet of the synthesis tower A and the inlet of the methanol discharge component.

[0010] The first switching valve B is located between the inlet of the synthesis tower B and the outlet of the gas feedstock supply component, and the second switching valve B is located between the outlet of the synthesis tower B and the inlet of the methanol discharge component.

[0011] Preferably, both the interior of synthesis tower A and the interior of synthesis tower B are equipped with water adsorbent;

[0012] The in-situ dehydration high-conversion methanol synthesis system also includes a hydraulic pump, a third switching valve A, a third switching valve B, a fourth switching valve A, and a fourth switching valve B.

[0013] The steam outlet of the synthesis tower A is connected to the steam inlet of the bottom ring pipe of the synthesis tower B, and the third switching valve A is located at the steam outlet of the synthesis tower A and the steam inlet of the bottom ring pipe of the synthesis tower B.

[0014] The steam outlet of the synthesis tower B is connected to the steam inlet of the bottom ring pipe of the synthesis tower A, and the third switching valve B is located at the steam outlet of the synthesis tower B and the steam inlet of the bottom ring pipe of the synthesis tower A.

[0015] The inlet of the hydraulic pump is connected to the boiler outlet, and the outlet of the hydraulic pump is connected to the steam inlet of the synthesis tower A and the steam inlet of the synthesis tower B. The fourth switch valve A is located between the outlet of the hydraulic pump and the steam inlet of the synthesis tower A, and the fourth switch valve B is located between the outlet of the hydraulic pump and the steam inlet of the synthesis tower B.

[0016] Preferably, the in-situ dehydration high-conversion methanol synthesis system further includes a steam drum, a fifth switching valve A, and a fifth switching valve B;

[0017] The water inlet of the steam drum is used to connect to the boiler outlet;

[0018] The first steam port of the steam drum is connected to the steam outlet of the synthesis tower A, and the fifth switch valve A is located between the first steam port of the steam drum and the steam outlet of the synthesis tower A;

[0019] The second steam port of the steam drum is connected to the steam outlet of the synthesis tower B, and the fifth switch valve B is located between the first steam port of the steam drum and the steam outlet of the synthesis tower B.

[0020] The liquid outlet of the steam drum is connected to the liquid inlet of the hydraulic pump, and the steam outlet of the steam drum is connected to a steam delivery pipeline.

[0021] Preferably, the in-situ dehydration high-conversion methanol synthesis system further includes a sixth switching valve A and a sixth switching valve B. The inlet of the synthesis tower A and the inlet of the synthesis tower B are both connected to nitrogen delivery pipelines. The sixth switching valve A is located on the inlet side of the synthesis tower A, and the sixth switching valve B is located on the inlet side of the synthesis tower B.

[0022] Preferably, the methanol discharge assembly includes a cooler, a separator, and a flash tank;

[0023] The outlets of synthesis tower A and synthesis tower B are both connected to the inlet of the cooler. The second switch valve A is located between the outlet of synthesis tower A and the inlet of the cooler, and the second switch valve B is located between the outlet of synthesis tower B and the inlet of the cooler.

[0024] The outlet of the cooler is connected to the inlet of the separator, and the liquid phase outlet of the separator is connected to the inlet of the flash tank.

[0025] The outlet of the flash tank is connected to a methanol delivery pipeline, and the exhaust port of the flash tank is connected to a carbon dioxide delivery pipeline.

[0026] The gas phase outlet of the separator is connected to the first end of the circulating mixed gas pipeline, and the second end of the circulating mixed gas pipeline is connected to the inlet of the synthesis tower A and the inlet of the synthesis tower B.

[0027] Preferably, the gas feedstock supply assembly includes a heat exchanger, a fresh gas compressor, and a recirculating gas compressor;

[0028] The second end of the circulating mixed gas pipeline is connected to the inlet of the circulating gas compressor, and the inlet of the fresh gas compressor is connected to the fresh mixed gas pipeline.

[0029] The shell-side inlet of the heat exchanger is connected to the outlet of the fresh gas compressor and the outlet of the circulating gas compressor, and the shell-side outlet of the heat exchanger is connected to the inlet of the synthesis tower A and the inlet of the synthesis tower B.

[0030] The tube-side inlet of the heat exchanger is connected to the outlet of synthesis tower A and the outlet of synthesis tower B, and the tube-side outlet of the heat exchanger is connected to the inlet of the cooler.

[0031] Preferably, the in-situ dehydration high-conversion methanol synthesis system further includes an absorption heat exchanger, a seventh switching valve A, and a seventh switching valve B;

[0032] The inlet of the absorption heat exchanger is connected to the outlet of the synthesis tower A and the outlet of the synthesis tower B. The seventh switch valve A is located between the outlet of the synthesis tower A and the absorption heat exchanger, and the seventh switch valve B is located between the outlet of the synthesis tower B and the absorption heat exchanger.

[0033] Preferably, the exhaust volume of the fresh gas compressor is in the range of 15,000-18,000. The compression ratio range of the fresh gas compressor is 3.375-4, and the fresh gas compressor is used to transport hydrogen and carbon dioxide at a molar ratio of 1 / 3 and a temperature of 30°C. Fresh air mixture;

[0034] The displacement range of the recirculating air compressor is 30,000-36,000. The compression ratio range of the circulating gas compressor is 1 / 34-1 / 3, and the circulating gas compressor is used to transport gases at a temperature of 40°C. A circulating mixture with a recirculation ratio range of 2;

[0035] The heat exchanger is used to heat the circulating mixed gas to a target temperature, wherein the target temperature range is 220-230°C. ;

[0036] The water adsorbent is a resin adsorbent.

[0037] Preferably, the exhaust volume of the fresh gas compressor is in the range of 50,000-60,000. The compression ratio range of the fresh gas compressor is 4.625-5.25, and the fresh gas compressor is used to transport hydrogen and carbon dioxide at a molar ratio of 1 / 3 and a temperature of 30°C. The mixture of gases;

[0038] The displacement range of the recirculating gas compressor is 120,000-140,000. The compression ratio range of the circulating gas compressor is 1 / 9-1 / 4, and the circulating gas compressor is used to transport gases at a temperature of 40°C. The recirculation ratio is within the range of 2-3 for the circulating gas;

[0039] The heat exchanger is used to heat the circulating gas to a target temperature, and the target temperature range is 240-260°C. ;

[0040] The water adsorbent is a molecular sieve adsorbent.

[0041] Preferably, the in-situ dehydration high-conversion methanol synthesis system further includes a controller, a water vapor content sensor A, and a water vapor content sensor B;

[0042] The water vapor content acquisition device A is used to acquire the water vapor content in the reaction gas discharged from the outlet of the synthesis tower A, and the water vapor content acquisition device B is used to acquire the water vapor content in the reaction gas discharged from the outlet of the synthesis tower B.

[0043] The controller signal is connected to the first switching valve A, the second switching valve A, the third switching valve A, the fourth switching valve A, the fifth switching valve A, the sixth switching valve A, the seventh switching valve A, the first switching valve B, the second switching valve B, the third switching valve B, the fourth switching valve B, the fifth switching valve B, the sixth switching valve B, the seventh switching valve B, the water vapor content acquisition device A, and the water vapor content acquisition device B. It is used to receive water vapor content data and control the opening and closing of the first switching valve A, the second switching valve A, the third switching valve A, the fourth switching valve A, the fifth switching valve A, the sixth switching valve A, the seventh switching valve A, the first switching valve B, the second switching valve B, the third switching valve B, the fourth switching valve B, the fifth switching valve B, the sixth switching valve B, and the seventh switching valve B.

[0044] In this application, the methanol synthesis system is equipped with two synthesis towers, namely synthesis tower A and synthesis tower B. A gas feedstock supply assembly is connected to the inlet of synthesis tower A and the inlet of synthesis tower B, enabling methanol synthesis through synthesis towers A and B. A methanol discharge assembly is connected to the outlet of synthesis tower A and the outlet of synthesis tower B, allowing the methanol generated through synthesis towers A and B to be discharged. A first switching valve A is installed at the inlet side of synthesis tower A, and a second switching valve A is installed at the outlet side of synthesis tower A. Similarly, a first switching valve B is installed at the inlet side of synthesis tower B, and a second switching valve B is installed at the outlet side of synthesis tower A, allowing selection of either synthesis tower A or synthesis tower B for methanol synthesis.

[0045] In use, optionally, the first switch valve A and the second switch valve A are opened, and the first switch valve B and the second switch valve B are closed. Then, the gas raw material supply component supplies gas raw material to the synthesis tower A. The gas raw material refers to a mixture of hydrogen and carbon dioxide gas. Methanol synthesis can be achieved through the synthesis tower A.

[0046] Optionally, by opening the first switch valve B and the second switch valve B, and closing the first switch valve A and the second switch valve A, the gas feedstock supply component supplies gas feedstock to the synthesis tower B. The gas feedstock refers to a mixture of hydrogen and carbon dioxide gas, which enables methanol synthesis through the synthesis tower B.

[0047] Since either synthesis tower A or synthesis tower B can be selected to synthesize methanol, and when using either synthesis tower A or synthesis tower B to synthesize methanol, the water vapor content in the other tower can be reduced by means of water vapor discharge or water adsorbent, so that the conversion rate of the methanol synthesis reaction can be guaranteed when the synthesis tower with reduced water vapor content is used continuously to synthesize methanol. Attached Figure Description

[0048] To more clearly illustrate the technical solutions in the embodiments of this application or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only embodiments of this application. For those skilled in the art, other drawings can be obtained based on the provided drawings without creative effort.

[0049] Figure 1 This is a schematic diagram illustrating the principle of a specific embodiment provided in this application;

[0050] Figure 2 This is a schematic diagram illustrating the state of methanol production using synthesis tower A in a specific embodiment provided in this application;

[0051] Figure 3 This is a schematic diagram illustrating the state of methanol production using synthesis tower B, as provided in a specific embodiment of this application.

[0052] Figure label:

[0053] 1-Gas feedstock supply assembly; 101-Heat exchanger; 102-Fresh gas compressor; 103-Circulating gas compressor; 104-Fresh mixed gas pipeline; 2-Synthesis tower A; 3-Synthesis tower B; 4-Methanol discharge assembly; 401-Cooler; 402-Separator; 403-Flash tank; 404-Methanol delivery pipeline; 405-Carbon dioxide delivery pipeline; 406-Circulating mixed gas pipeline; 5-First switching valve A; 6-Second switching valve A; 7-The 8-Second switch valve B; 9-Third switch valve A; 10-Third switch valve B; 11-Steam drum; 12-Hydraulic pump; 13-Fourth switch valve A; 14-Fourth switch valve B; 15-Fifth switch valve A; 16-Fifth switch valve B; 17-Steam transmission pipeline; 18-Sixth switch valve A; 19-Sixth switch valve B; 20-Nitrogen transmission pipeline; 21-Absorption heat exchanger; 22-Seventh switch valve A; 23-Seventh switch valve B. Detailed Implementation

[0054] 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 some embodiments of this application, and not all embodiments. Based on the embodiments of this application, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the scope of protection of this application.

[0055] The core of this application is to provide an in-situ dehydration high-conversion methanol synthesis system.

[0056] This application provides an in-situ dehydration high-conversion methanol synthesis system, including a gas feedstock supply assembly 1, a synthesis tower A2, a synthesis tower B3, a methanol discharge assembly 4, a first switching valve A5, a second switching valve A6, a first switching valve B7, and a second switching valve B8; wherein,

[0057] The inlet of synthesis tower A2 and the inlet of synthesis tower B3 are both connected to the outlet of gas feedstock component 1, so as to input the gas feedstock required for the reaction into synthesis tower A2 and synthesis tower B3.

[0058] The outlets of synthesis tower A2 and synthesis tower B3 are both connected to the inlet of methanol discharge assembly 4 to discharge methanol.

[0059] The first switching valve A5 is located between the inlet of the synthesis tower A2 and the outlet of the gas feedstock component 1, and the second switching valve A6 is located between the outlet of the synthesis tower A2 and the inlet of the methanol discharge component 4.

[0060] The first switching valve B7 is located between the inlet of the synthesis tower B3 and the outlet of the gas feedstock component 1, and the second switching valve B8 is located between the outlet of the synthesis tower B3 and the inlet of the methanol discharge component 4.

[0061] refer to Figure 1 The methanol synthesis system is equipped with two synthesis towers, namely synthesis tower A2 and synthesis tower B3. A gas feedstock supply assembly 1 is connected to the inlet of synthesis tower A2 and the inlet of synthesis tower B3, enabling methanol synthesis through both towers. A methanol discharge assembly 4 is connected to the outlet of synthesis tower A2 and the outlet of synthesis tower B3, allowing the methanol produced in both towers to be discharged. A first switching valve A5 is installed at the inlet of synthesis tower A2, and a second switching valve A6 is installed at the outlet of synthesis tower A2. Similarly, a first switching valve B7 is installed at the inlet of synthesis tower B3, and a second switching valve B8 is installed at the outlet of synthesis tower A2, allowing selection of either synthesis tower A2 or synthesis tower B3 for methanol synthesis.

[0062] In use, optionally, the first switch valve A5 and the second switch valve A6 are opened, and the first switch valve B7 and the second switch valve B8 are closed. Then, the gas raw material supply component 1 supplies gas raw material to the synthesis tower A2. The gas raw material refers to a mixture of hydrogen and carbon dioxide gas. Methanol synthesis can be achieved through the synthesis tower A2.

[0063] Optionally, by opening the first switch valve B7 and the second switch valve B8, and closing the first switch valve A5 and the second switch valve A6, the gas feedstock supply component 1 supplies gas feedstock to the synthesis tower B3. The gas feedstock refers to a mixture of hydrogen and carbon dioxide gas, which enables methanol synthesis through the synthesis tower B3.

[0064] Since either synthesis tower A2 or synthesis tower B3 can be selected to synthesize methanol, and when using either synthesis tower A2 or synthesis tower B3 to synthesize methanol, the water vapor content in the other tower can be reduced by means of water vapor discharge or water adsorbent, so that the conversion rate of the methanol synthesis reaction can be guaranteed when the synthesis tower with reduced water vapor content is used continuously to synthesize methanol.

[0065] Based on the above embodiments, both synthesis tower A2 and synthesis tower B3 are equipped with water adsorbents;

[0066] The in-situ dehydration high-conversion methanol synthesis system also includes hydraulic pump 12, third switch valve A9, third switch valve B10, fourth switch valve A13, and fourth switch valve B14.

[0067] The steam outlet of synthesis tower A2 is connected to the steam inlet of the bottom ring pipe of synthesis tower B3, and the third switching valve A9 is located at the steam outlet of synthesis tower A2 and the steam inlet of the bottom ring pipe of synthesis tower B3.

[0068] The steam outlet of synthesis tower B3 is connected to the steam inlet of the bottom ring pipe of synthesis tower A2, and the third switching valve B10 is located at the steam outlet of synthesis tower B3 and the steam inlet of the bottom ring pipe of synthesis tower A2.

[0069] The inlet of the hydraulic pump 12 is connected to the boiler outlet, and the outlet of the hydraulic pump 12 is connected to the steam inlet of the synthesis tower A2 and the steam inlet of the synthesis tower B3. The fourth switch valve A13 is located between the outlet of the hydraulic pump 12 and the steam inlet of the synthesis tower A2, and the fourth switch valve B14 is located between the outlet of the hydraulic pump 12 and the steam inlet of the synthesis tower B3.

[0070] To increase the forward rate of the methanol synthesis reaction, refer to Figure 1 As explained, the outlet of hydraulic pump 12 is connected to the steam inlet of synthesis tower A2, so that hydraulic pump 12 can input coolant into synthesis tower A2 to absorb the heat generated during the methanol synthesis reaction in synthesis tower A2. A fourth switching valve A13 is installed between the steam inlet of synthesis tower A2 and the outlet of hydraulic pump 12. The fourth switching valve A13 can control the opening and closing of the steam inlet of synthesis tower A2, that is, control whether coolant can be input into synthesis tower A2. Furthermore, the steam outlet of synthesis tower A2 is connected to the steam inlet of synthesis tower B3, so that heat can be provided for the dehydration of water adsorbent in synthesis tower B3. After the water adsorbent in synthesis tower B3 is dehydrated, water vapor will be discharged from the bottom outlet of synthesis tower B3.

[0071] Similarly, the outlet of hydraulic pump 12 is also connected to the steam inlet of synthesis tower B3, so hydraulic pump 12 can input coolant into synthesis tower B3 to absorb the heat generated during the methanol synthesis reaction in synthesis tower B3. A fourth switching valve B14 is installed between the steam inlet of synthesis tower B3 and the outlet of hydraulic pump 12. The opening and closing of the steam inlet of synthesis tower B3 can be controlled by the fourth switching valve B14, that is, whether coolant can be input into synthesis tower B3. Furthermore, the steam outlet of synthesis tower B3 is connected to the steam inlet of synthesis tower A2, so it can provide heat for the dehydration of water adsorbent in synthesis tower A2. After the water adsorbent in synthesis tower A2 is dehydrated, water vapor will be discharged from the bottom outlet of synthesis tower A2.

[0072] In operation, open the third switch valve A9 and the fourth switch valve A13, and close the third switch valve B10 and the fourth switch valve B14. Methanol can be synthesized through synthesis tower A2, and the water adsorbent in synthesis tower B3 can be dehydrated. Conversely, open the third switch valve B10 and the fourth switch valve B14, and close the third switch valve A9 and the fourth switch valve A13. Methanol can be synthesized through synthesis tower B3, and the water adsorbent in synthesis tower A2 can be dehydrated.

[0073] This embodiment ensures that the conversion rate of the methanol synthesis reaction is maintained when the synthesis tower with reduced water vapor content is used continuously to synthesize methanol.

[0074] Based on the above embodiments, the in-situ dehydration high-conversion methanol synthesis system also includes a steam drum 11, a fifth switching valve A15, and a fifth switching valve B16.

[0075] The water inlet of steam drum 11 is used to connect to the boiler outlet;

[0076] The first steam port of the steam drum 11 is connected to the steam outlet of the synthesis tower A2, and the fifth switch valve A15 is located between the first steam port of the steam drum 11 and the steam outlet of the synthesis tower A2.

[0077] The second steam port of the steam drum 11 is connected to the steam outlet of the synthesis tower B3, and the fifth switch valve B16 is located between the first steam port of the steam drum 11 and the steam outlet of the synthesis tower B3.

[0078] The liquid outlet of the steam drum 11 is connected to the liquid inlet of the hydraulic pump 12, and the steam outlet of the steam drum 11 is connected to the steam delivery pipeline 17.

[0079] refer to Figure 1 As explained, the methanol synthesis system is equipped with a steam drum 11 to provide coolant for absorbing the reaction heat of the synthesis tower. During operation, water is added to the steam drum 11 from the boiler. In some embodiments, when using synthesis tower A2 for methanol synthesis, please refer to... Figure 2Open the fourth switch valve A13, the third switch valve A9, and the fifth switch valve B16, and close the fourth switch valve B14, the third switch valve B10, and the fifth switch valve A15. Water in the steam drum 11 is pumped into the synthesis tower A2 by the hydraulic pump 12, where it absorbs the heat generated by the reaction in the synthesis tower A2 and is converted into steam. The steam enters the shell side of the synthesis tower B3 through the pipeline, providing heat energy for the dehydration and regeneration process of the water adsorbent in the synthesis tower B3. The remaining steam is returned to the steam drum 11 for recycling.

[0080] Conversely, in some embodiments, when using synthesis tower B3 for methanol synthesis, please refer to... Figure 3 Close the fourth switch valve A13, the third switch valve A9, and the fifth switch valve B16, and open the fourth switch valve B14, the third switch valve B10, and the fifth switch valve A15. Water in the steam drum 11 is pumped into the synthesis tower B3 by the hydraulic pump 12, where it absorbs the heat generated by the reaction in the synthesis tower B3 and is converted into steam. The steam enters the shell side of the synthesis tower A2 through the pipeline, providing heat energy for the dehydration and regeneration process of the water adsorbent in the synthesis tower A2. The remaining steam is returned to the steam drum 11 for recycling.

[0081] Based on the above embodiments, the in-situ dehydration high-conversion methanol synthesis system also includes a sixth switching valve A18 and a sixth switching valve B19. The inlet of synthesis tower A2 and the inlet of synthesis tower B3 are both connected to nitrogen delivery pipelines 20. The sixth switching valve A18 is located on the inlet side of synthesis tower A2, and the sixth switching valve B19 is located on the inlet side of synthesis tower B3.

[0082] refer to Figure 1 As explained, the inlets of synthesis tower A2 and synthesis tower B3 are both connected to nitrogen delivery pipeline 20. A sixth switch valve A18 is installed on the nitrogen delivery pipeline 20 connected to the inlet of synthesis tower A2. The valve can control the opening and closing of the inlet of synthesis tower A2, that is, control whether nitrogen can be input into synthesis tower A2. Similarly, a sixth switch valve B19 is installed on the nitrogen delivery pipeline 20 connected to the inlet of synthesis tower B3. The valve can control the opening and closing of the inlet of synthesis tower B3, that is, control whether nitrogen can be input into synthesis tower B3.

[0083] In some embodiments, when using synthesis tower A2 for methanol synthesis, please refer to [the relevant documentation / reference]. Figure 2 Open the sixth switch valve B19 to continuously supply low-pressure nitrogen gas into the synthesis tower B3, so as to carry away the water vapor removed during the regeneration of the water adsorbent from the bottom outlet of the synthesis tower B3; conversely, in some embodiments, when using the synthesis tower B3 for methanol synthesis, please refer to... Figure 3 Open the sixth switch valve A18 to continuously input low-pressure nitrogen into the synthesis tower A2, so as to carry away the water vapor removed by the water adsorbent regeneration from the bottom outlet of the synthesis tower A2.

[0084] Based on the above embodiments, the methanol discharge assembly 4 includes a cooler 401, a separator 402, and a flash tank 403;

[0085] The outlets of synthesis tower A2 and synthesis tower B3 are both connected to the inlet of cooler 401. The second switching valve A6 is located between the outlet of synthesis tower A2 and the inlet of cooler 401, and the second switching valve B8 is located between the outlet of synthesis tower B3 and the inlet of cooler 401.

[0086] The outlet of cooler 401 is connected to the inlet of separator 402, and the liquid phase outlet of separator 402 is connected to the inlet of flash tank 403.

[0087] The outlet of flash tank 403 is connected to methanol delivery pipeline 404, and the exhaust port of flash tank 403 is connected to carbon dioxide delivery pipeline 405.

[0088] The gas phase outlet of the separator 402 is connected to the first end of the circulating mixed gas pipeline 406, and the second end of the circulating mixed gas pipeline 406 is connected to the inlet of the synthesis tower A2 and the inlet of the synthesis tower B3.

[0089] refer to Figure 1 As explained, the inlet of cooler 401 is connected to the bottom outlet of synthesis tower A2 and synthesis tower B3 to cool the reaction output gases of synthesis tower A2 and synthesis tower B3. The outlet of cooler 401 is connected to the inlet of separator 402 to achieve gas-liquid separation. The liquid phase outlet of separator 402 is connected to the inlet of flash tank 403 for flash evaporation. A methanol delivery pipeline 404 is connected to the outlet of flash tank 403, and a carbon dioxide delivery pipeline 405 is connected to the exhaust port of flash tank 403 to remove dissolved carbon dioxide from the reaction gases. The carbon dioxide gas is then delivered through the carbon dioxide delivery pipeline 405, and the crude methanol is delivered through the methanol delivery pipeline 404. The gas phase outlet of separator 402 is connected to the circulating mixed gas pipeline 406 to return unreacted gases to synthesis tower A2 and synthesis tower B3.

[0090] Based on the above embodiments, the gas raw material supply assembly 1 includes a heat exchanger 101, a fresh gas compressor 102, and a circulating gas compressor 103.

[0091] The second end of the circulating mixed gas line 406 is connected to the inlet of the circulating gas compressor 103, and the inlet of the fresh gas compressor 102 is connected to the fresh mixed gas line 104.

[0092] The shell-side inlet of heat exchanger 101 is connected to the outlet of fresh gas compressor 102 and the outlet of circulating gas compressor 103, and the shell-side outlet of heat exchanger 101 is connected to the inlet of synthesis tower A2 and the inlet of synthesis tower B3.

[0093] The tube-side inlet of heat exchanger 101 is connected to the outlet of synthesis tower A2 and the outlet of synthesis tower B3, and the tube-side outlet of heat exchanger 101 is connected to the inlet of cooler 401.

[0094] refer to Figure 1 As explained, the inlet of the fresh gas compressor 102 is connected to the fresh mixed gas pipeline 104 to receive and compress fresh raw material gas. The upper end of the circulating mixed gas pipeline 406 is connected to the circulating mixed gas pipeline 406, and the lower end of the circulating mixed gas pipeline 406 is connected to the gas phase outlet of the separator 402 to receive the gas separated by the separator 402. The shell-side inlet of the heat exchanger 101 is connected to the outlet of the fresh gas compressor 102 and the outlet of the circulating gas compressor 103, so that the gas output from the fresh gas compressor 102 and the circulating gas compressor 103 can be transported into the shell side of the heat exchanger 101. The shell-side outlet of the heat exchanger 101 is connected to the inlet of the synthesis tower A2 and the synthesis tower B3, so that all the collected gas can be transported into the synthesis tower A2 and the synthesis tower B3.

[0095] The tube side inlet of heat exchanger 101 is connected to the outlet of synthesis tower A2 and synthesis tower B3, so that the gas produced by the reaction in synthesis tower A2 and synthesis tower B3 can be transported into the tube side of heat exchanger 101, so that the reaction gas can be initially cooled by heat exchanger 101. The tube side outlet of heat exchanger 101 is connected to cooler 401, so that the reaction gas can be further cooled by cooler 401.

[0096] Based on the above embodiments, the in-situ dehydration high-conversion methanol synthesis system also includes an absorption heat exchanger 21, a seventh switching valve A22, and a seventh switching valve B23.

[0097] The inlet of the absorption heat exchanger 21 is connected to the outlet of the synthesis tower A2 and the outlet of the synthesis tower B3. The seventh switch valve A22 is located between the outlet of the synthesis tower A2 and the absorption heat exchanger 21, and the seventh switch valve B23 is located between the outlet of the synthesis tower B3 and the absorption heat exchanger 21.

[0098] refer to Figure 1As explained, the methanol synthesis system is also equipped with an absorption heat exchanger 21. The outlets of synthesis tower A2 and synthesis tower B3 are both connected to the absorption heat exchanger 21. The gas in synthesis tower A2 and synthesis tower B3 can be transported to the absorption heat exchanger 21 through their bottom outlets. A seventh switch valve A22 is installed between the outlet of synthesis tower A2 and the absorption heat exchanger 21 to control whether the gas discharged from synthesis tower A2 can be transported to the absorption heat exchanger 21. A seventh switch valve B23 is installed between the outlet of synthesis tower B3 and the absorption heat exchanger 21 to control whether the gas discharged from synthesis tower B3 can be transported to the absorption heat exchanger 21. After the water vapor discharged from the bottom outlets of synthesis tower A2 and synthesis tower B3 is transported to the absorption heat exchanger 21, the water vapor is condensed into wastewater after the heat is recovered by the absorption heat exchanger 21, and the regenerated waste gas can be treated as tail gas.

[0099] Furthermore, a waste pipeline is connected to the gas phase outlet of the absorption heat exchanger 21 to transport and discharge the regenerated waste gas, and a wastewater pipe is connected to the liquid phase outlet of the absorption heat exchanger 21 to transport and discharge the condensate wastewater.

[0100] To improve the level of automation and ensure methanol production, based on the above embodiments, the in-situ dehydration high-conversion methanol synthesis system also includes a controller, a water vapor content acquisition device A, and a water vapor content acquisition device B.

[0101] Water vapor content sensor A is used to obtain the water vapor content in the reaction gas discharged from the outlet of synthesis tower A2, and water vapor content sensor B is used to obtain the water vapor content in the reaction gas discharged from the outlet of synthesis tower B3.

[0102] The controller signal is connected to the first switching valve A5, the second switching valve A6, the third switching valve A9, the fourth switching valve A13, the fifth switching valve A15, the sixth switching valve A18, the seventh switching valve A22, the first switching valve B7, the second switching valve B8, the third switching valve B10, the fourth switching valve B14, the fifth switching valve B16, the sixth switching valve B19, the seventh switching valve B23, the water vapor content acquisition device A, and the water vapor content acquisition device B. This is used to receive water vapor content data and control the opening and closing of the first switching valve A5, the second switching valve A6, the third switching valve A9, the fourth switching valve A13, the fifth switching valve A15, the sixth switching valve A18, the seventh switching valve A22, the first switching valve B7, the second switching valve B8, the third switching valve B10, the fourth switching valve B14, the fifth switching valve B16, the sixth switching valve B19, and the seventh switching valve B23.

[0103] In some embodiments, when used, such as Figure 2 As shown, the molar ratio of hydrogen to carbon dioxide is 1 / 3, and the temperature is 30°C. The fresh air mixture is compressed from 1.6 MPaG to 7-8 MPaG by the fresh air compressor, and the output flow rate of the fresh air mixture from the fresh air compressor ranges from 15,000 to 18,000. The circulation ratio is 2 and the temperature is 40. The recirculated gas mixture is compressed from 6~6.8 MPaG to 7~8 MPaG by the recirculated gas compressor, and the output flow rate of the recirculated gas mixture from the recirculated gas compressor ranges from 30000 to 36000. The fresh mixed gas discharged from the fresh gas compressor and the recirculated mixed gas discharged from the recirculated gas compressor are both sent to heat exchanger 101 for preheating to heat the gas to 220-230°C. This target temperature.

[0104] Opening the first switch valve A5, the second switch valve A6, the sixth switch valve B19, the seventh switch valve B23, the fifth switch valve A15, the third switch valve A9, and the fourth switch valve B14, and closing the first switch valve B7, the second switch valve B8, the sixth switch valve A18, the seventh switch valve A22, the fifth switch valve B16, the third switch valve B10, and the fourth switch valve A13, the preheated mixed gas will be transported to the synthesis tower A2 to achieve methanol synthesis. The gas will then be discharged through the methanol discharge component 4. During the methanol synthesis process, water vapor is adsorbed by the resin adsorbent to facilitate the methanol synthesis reaction. The process proceeds in the forward direction; simultaneously, the steam drum 11 transports boiler water to the synthesis tower A2, where it absorbs the heat released by the reaction and is converted into steam. This steam is then transported to the bottom ring pipe of the synthesis tower B3 to heat the adsorbent inside the synthesis tower B3, thereby accelerating the dehydration of the adsorbent. Nitrogen gas carries the steam out from the bottom tube outlet of the synthesis tower B3, thus enabling the adsorbent to be regenerated in the synthesis tower B3. The gas output from the bottom tube outlet of the synthesis tower B3 is discharged into the absorption heat exchanger 21. After the heat is recovered by the absorption heat exchanger 21, the steam is condensed into wastewater, and the regenerated waste gas can be treated as tail gas.

[0105] During the process of methanol being discharged through methanol discharge component 4, the gas discharged from synthesis tower A2 is first sent to heat exchanger 101 to recover part of the reaction heat through mixed gas, and then input into cooler 401 for further cooling. After further cooling, the gas-liquid two-phase reaction gas achieves gas-liquid separation in separator 402. The unreacted gaseous raw material is sent to the circulating gas compressor through the gas phase outlet of separator 402, while the crude methanol is discharged from the liquid phase outlet of separator 402 and enters flash tank 403 for flash evaporation to remove dissolved carbon dioxide.

[0106] The water vapor content in the gas discharged from the resynthesis tower A2 through its own outlet reaches a certain level. When mol, such as Figure 3As shown, the first switch valve A5, the second switch valve A6, the sixth switch valve B19, the seventh switch valve B23, the fifth switch valve A15, the third switch valve A9, and the fourth switch valve B14 are closed, while the first switch valve B7, the second switch valve B8, the sixth switch valve A18, the seventh switch valve A22, the fifth switch valve B16, the third switch valve B10, and the fourth switch valve A13 are opened. At this time, the preheated mixed gas is transported to the synthesis tower B3 to achieve methanol synthesis and is discharged through the methanol discharge component 4. At the same time, the adsorbent can be regenerated in the synthesis tower A2.

[0107] In this embodiment, the wastewater discharge flow rate is 3~3.6t / h, and the methanol production is 5~6t / h.

[0108] In other embodiments, when used, such as Figure 2 As shown, the molar ratio of hydrogen to carbon dioxide is 1 / 3, and the temperature is 30°C. The fresh air mixture is compressed from 1.6 MPaG to 9-10 MPaG by the fresh air compressor, and the output flow rate of the fresh air mixture from the fresh air compressor ranges from 50,000 to 60,000. The cycle ratio range is 2-3, and the temperature is 40°C. The recirculated gas mixture is compressed from 8-9 MPaG to 9-10 MPaG by the recirculated gas compressor, and the output flow rate of the recirculated gas mixture from the recirculated gas compressor ranges from 120,000 to 140,000. The fresh mixed gas discharged from the fresh gas compressor and the recirculated mixed gas discharged from the recirculated gas compressor are both sent to heat exchanger 101 for preheating to heat the gas to 40-260°C. This target temperature.

[0109] Opening the first switch valve A5, the second switch valve A6, the sixth switch valve B19, the seventh switch valve B23, the fifth switch valve A15, the third switch valve A9, and the fourth switch valve B14, and closing the first switch valve B7, the second switch valve B8, the sixth switch valve A18, the seventh switch valve A22, the fifth switch valve B16, the third switch valve B10, and the fourth switch valve A13, the preheated mixed gas will be transported to the synthesis tower A2 to achieve methanol synthesis. The gas will then be discharged through the methanol discharge component 4. During the methanol synthesis process, water vapor is adsorbed by the resin adsorbent to facilitate the methanol synthesis reaction. The process proceeds in the forward direction; simultaneously, the steam drum 11 transports boiler water to the synthesis tower A2, where it absorbs the heat released by the reaction and is converted into steam. This steam is then transported to the bottom ring pipe of the synthesis tower B3 to heat the adsorbent inside the synthesis tower B3, thereby accelerating the dehydration of the adsorbent. Nitrogen gas carries the steam out from the bottom tube outlet of the synthesis tower B3, thus enabling the adsorbent to be regenerated in the synthesis tower B3. The gas output from the bottom tube outlet of the synthesis tower B3 is discharged into the absorption heat exchanger 21. After the heat is recovered by the absorption heat exchanger 21, the steam is condensed into wastewater, and the regenerated waste gas can be treated as tail gas.

[0110] During the process of methanol being discharged through methanol discharge component 4, the gas discharged from synthesis tower A2 is first sent to heat exchanger 101 to recover part of the reaction heat through mixed gas, and then input into cooler 401 for further cooling. After further cooling, the gas-liquid two-phase reaction gas achieves gas-liquid separation in separator 402. The unreacted gaseous raw material is sent to the circulating gas compressor through the gas phase outlet of separator 402, while the crude methanol is discharged from the liquid phase outlet of separator 402 and enters flash tank 403 for flash evaporation to remove dissolved carbon dioxide.

[0111] The water vapor content in the gas discharged from the resynthesis tower A2 through its own outlet reaches a certain level. When mol, such as Figure 3 As shown, the first switch valve A5, the second switch valve A6, the sixth switch valve B19, the seventh switch valve B23, the fifth switch valve A15, the third switch valve A9, and the fourth switch valve B14 are closed, while the first switch valve B7, the second switch valve B8, the sixth switch valve A18, the seventh switch valve A22, the fifth switch valve B16, the third switch valve B10, and the fourth switch valve A13 are opened. At this time, the preheated mixed gas is transported to the synthesis tower B3 to achieve methanol synthesis and is discharged through the methanol discharge component 4. At the same time, the adsorbent can be regenerated in the synthesis tower A2.

[0112] In this embodiment, the wastewater discharge flow rate is 10-12 t / h, and the methanol production rate is 18-21 t / h.

[0113] It should be noted that the relational terms such as "first" and "second" mentioned above are only used to distinguish one entity from several other entities, and do not necessarily require or imply any such actual relationship or order between these entities; the terms "upper surface; lower surface; top; bottom" and the directional terms "upper; lower; left; right" mentioned above are defined based on the accompanying drawings in the specification.

[0114] The various embodiments in this specification are described in a progressive manner, with each embodiment focusing on the differences from other embodiments. The same or similar parts between the various embodiments can be referred to each other.

[0115] The above provides a detailed description of the in-situ dehydration high-conversion methanol synthesis system provided in this application. Specific examples have been used to illustrate the principles and implementation methods of this application. The descriptions of the above embodiments are merely for the purpose of helping to understand the method and core ideas of this application. It should be noted that those skilled in the art can make various improvements and modifications to this application without departing from its principles, and these improvements and modifications also fall within the protection scope of this application.

Claims

1. An in-situ dehydration high-conversion methanol synthesis system, characterized in that, include: Gas feedstock supply assembly (1), synthesis tower A (2), synthesis tower B (3), methanol discharge assembly (4), first switch valve A (5), second switch valve A (6), first switch valve B (7), second switch valve B (8); The inlet of the synthesis tower A (2) and the inlet of the synthesis tower B (3) are both connected to the outlet of the gas raw material supply component (1) to input the gas raw materials required for the reaction into the synthesis tower A (2) and the synthesis tower B (3); The outlets of the synthesis tower A (2) and the synthesis tower B (3) are both connected to the inlet of the methanol discharge assembly (4) to discharge methanol. The first switching valve A (5) is located between the inlet of the synthesis tower A (2) and the outlet of the gas raw material supply component (1), and the second switching valve A (6) is located between the outlet of the synthesis tower A (2) and the inlet of the methanol discharge component (4). The first switching valve B (7) is located between the inlet of the synthesis tower B (3) and the outlet of the gas raw material supply component (1), and the second switching valve B (8) is located between the outlet of the synthesis tower B (3) and the inlet of the methanol discharge component (4).

2. The in-situ dehydration high-conversion methanol synthesis system according to claim 1, characterized in that, Both the interior of synthesis tower A (2) and the interior of synthesis tower B (3) are equipped with water adsorbent; The in-situ dehydration high-conversion methanol synthesis system also includes a hydraulic pump (12), a third switch valve A (9), a third switch valve B (10), a fourth switch valve A (13), and a fourth switch valve B (14). The steam outlet of the synthesis tower A (2) is connected to the steam inlet of the bottom ring pipe of the synthesis tower B (3), and the third switching valve A (9) is located at the steam outlet of the synthesis tower A (2) and the steam inlet of the bottom ring pipe of the synthesis tower B (3). The steam outlet of the synthesis tower B (3) is connected to the steam inlet of the bottom ring pipe of the synthesis tower A (2), and the third switching valve B (10) is located at the steam outlet of the synthesis tower B (3) and the steam inlet of the bottom ring pipe of the synthesis tower A (2). The inlet of the hydraulic pump (12) is connected to the boiler outlet, and the outlet of the hydraulic pump (12) is connected to the steam inlet of the synthesis tower A (2) and the steam inlet of the synthesis tower B (3). The fourth switch valve A (13) is located between the outlet of the hydraulic pump (12) and the steam inlet of the synthesis tower A (2), and the fourth switch valve B (14) is located between the outlet of the hydraulic pump (12) and the steam inlet of the synthesis tower B (3).

3. The in-situ dehydration high-conversion methanol synthesis system according to claim 2, characterized in that, The in-situ dehydration high-conversion methanol synthesis system also includes a steam drum (11), a fifth switch valve A (15), and a fifth switch valve B (16). The water inlet of the steam drum (11) is used to connect to the boiler outlet; The first steam port of the steam drum (11) is connected to the steam outlet of the synthesis tower A (2), and the fifth switching valve A (15) is located between the first steam port of the steam drum (11) and the steam outlet of the synthesis tower A (2). The second steam port of the steam drum (11) is connected to the steam outlet of the synthesis tower B (3), and the fifth switching valve B (16) is located between the first steam port of the steam drum (11) and the steam outlet of the synthesis tower B (3). The liquid outlet of the steam drum (11) is connected to the liquid inlet of the hydraulic pump (12), and the steam outlet of the steam drum (11) is connected to a steam delivery pipeline (17).

4. The in-situ dehydration high-conversion methanol synthesis system according to claim 3, characterized in that, The in-situ dehydration high-conversion methanol synthesis system also includes a sixth switch valve A (18) and a sixth switch valve B (19). The inlet of the synthesis tower A (2) and the inlet of the synthesis tower B (3) are both connected to nitrogen delivery pipelines (20). The sixth switch valve A (18) is located on the inlet side of the synthesis tower A (2), and the sixth switch valve B (19) is located on the inlet side of the synthesis tower B (3).

5. The in-situ dehydration high-conversion methanol synthesis system according to claim 4, characterized in that, The methanol discharge assembly (4) includes a cooler (401), a separator (402), and a flash tank (403). The outlets of the synthesis tower A (2) and the synthesis tower B (3) are both connected to the inlet of the cooler (401). The second switching valve A (6) is located between the outlet of the synthesis tower A (2) and the inlet of the cooler (401). The second switching valve B (8) is located between the outlet of the synthesis tower B (3) and the inlet of the cooler (401). The outlet of the cooler (401) is connected to the inlet of the separator (402), and the liquid phase outlet of the separator (402) is connected to the inlet of the flash tank (403). The outlet of the flash tank (403) is connected to a methanol delivery pipeline (404), and the exhaust port of the flash tank (403) is connected to a carbon dioxide delivery pipeline (405). The gas phase outlet of the separator (402) is connected to the first end of the circulating mixed gas pipeline (406), and the second end of the circulating mixed gas pipeline (406) is connected to the inlet of the synthesis tower A (2) and the inlet of the synthesis tower B (3).

6. The in-situ dehydration high-conversion methanol synthesis system according to claim 5, characterized in that, The gas feedstock supply assembly (1) includes a heat exchanger (101), a fresh gas compressor (102), and a circulating gas compressor (103). The second end of the circulating mixed gas line (406) is connected to the inlet of the circulating gas compressor (103), and the inlet of the fresh gas compressor (102) is connected to the fresh mixed gas line (104). The shell-side inlet of the heat exchanger (101) is connected to the outlet of the fresh gas compressor (102) and the outlet of the circulating gas compressor (103), and the shell-side outlet of the heat exchanger (101) is connected to the inlet of the synthesis tower A (2) and the inlet of the synthesis tower B (3). The tube side inlet of the heat exchanger (101) is connected to the outlet of the synthesis tower A (2) and the outlet of the synthesis tower B (3), and the tube side outlet of the heat exchanger (101) is connected to the inlet of the cooler (401).

7. The in-situ dehydration high-conversion methanol synthesis system according to claim 6, characterized in that, The in-situ dehydration high-conversion methanol synthesis system also includes an absorption heat exchanger (21), a seventh switch valve A (22), and a seventh switch valve B (23). The inlet of the absorption heat exchanger (21) is connected to the outlet of the synthesis tower A (2) and the outlet of the synthesis tower B (3). The seventh switch valve A (22) is located between the outlet of the synthesis tower A (2) and the absorption heat exchanger (21). The seventh switch valve B (23) is located between the outlet of the synthesis tower B (3) and the absorption heat exchanger (21).

8. The in-situ dehydration high-conversion methanol synthesis system according to claim 7, characterized in that, The displacement range of the fresh air compressor (102) is 15,000-18,000. The fresh gas compressor (102) has a compression ratio range of 3.375-4, and the fresh gas compressor (102) is used to transport hydrogen and carbon dioxide in a molar ratio of 1 / 3 at a temperature of 30°C. Fresh air mixture; The exhaust volume of the recirculating gas compressor (103) ranges from 30,000 to 36,000. The compression ratio range of the circulating gas compressor (103) is 1 / 34-1 / 3, and the circulating gas compressor (103) is used to transport gases at a temperature of 40°C. A circulating mixture with a recirculation ratio range of 2; The heat exchanger (101) is used to heat the circulating mixed gas to a target temperature, wherein the target temperature range is 220-230°C. ; The water adsorbent is a resin adsorbent.

9. The in-situ dehydration high-conversion methanol synthesis system according to claim 7, characterized in that, The displacement of the fresh air compressor (102) is in the range of 50,000-60,000. The fresh gas compressor (102) has a compression ratio range of 4.625-5.25, and the fresh gas compressor (102) is used to transport hydrogen and carbon dioxide in a molar ratio of 1 / 3 at a temperature of 30°C. The mixture of gases; The exhaust volume of the recirculating gas compressor (103) ranges from 120,000 to 140,000. The compression ratio range of the circulating gas compressor (103) is 1 / 9-1 / 4, and the circulating gas compressor (103) is used to deliver gas at a temperature of 40°C. The recirculation ratio is within the range of 2-3 for the circulating gas; The heat exchanger (101) is used to heat the circulating gas to a target temperature, wherein the target temperature range is 240-260°C. ; The water adsorbent is a molecular sieve adsorbent.

10. The in-situ dehydration high-conversion methanol synthesis system according to claim 8 or 9, characterized in that, The in-situ dehydration high-conversion methanol synthesis system also includes a controller, a water vapor content sensor A, and a water vapor content sensor B; The water vapor content acquisition device A is used to acquire the water vapor content in the reaction gas discharged from the outlet of the synthesis tower A (2), and the water vapor content acquisition device B is used to acquire the water vapor content in the reaction gas discharged from the outlet of the synthesis tower B (3). The controller signal is connected to the first switching valve A (5), the second switching valve A (6), the third switching valve A (9), the fourth switching valve A (13), the fifth switching valve A (15), the sixth switching valve A (18), the seventh switching valve A (22), the first switching valve B (7), the second switching valve B (8), the third switching valve B (10), the fourth switching valve B (14), the fifth switching valve B (16), the sixth switching valve B (19), the seventh switching valve B (23), the water vapor content acquisition device A, and the water vapor... Vapor content acquisition device B is used to receive water vapor content data and control the opening and closing of the first switch valve A (5), the second switch valve A (6), the third switch valve A (9), the fourth switch valve A (13), the fifth switch valve A (15), the sixth switch valve A (18), the seventh switch valve A (22), the first switch valve B (7), the second switch valve B (8), the third switch valve B (10), the fourth switch valve B (14), the fifth switch valve B (16), the sixth switch valve B (19), and the seventh switch valve B (23).

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