Offshore green ammonia production platform and production system based on offshore new energy power

Abstract

The application discloses a kind of offshore green ammonia production platform and production system based on offshore new energy power, it is related to offshore new energy technical field, including platform one, be provided with synthetic section module on the platform one.The flow of nozzle device in the application can be mechanically adjusted, the reciprocating motion of nozzle device is driven in the axial direction of heat exchange tube inside waste heat boiler by traction piece, so that nozzle device can spray cleaning fluid on the surface of heat exchange tube, the flow of nozzle device can be dynamically adjusted in the process of nozzle device movement by the setting of driving piece, so that nozzle device can spray different unit quantity of cleaning fluid according to the different degree of fouling of heat exchange tube surface, while the offshore green ammonia production process system provided by the application is simple, investment and running cost is low, under low load condition, the catalyst bed temperature of first ammonia synthesis tower and second ammonia synthesis tower is maintained by using the reaction heat of first ammonia synthesis tower and second ammonia synthesis tower itself.

Description

Technical Field

[0001] This invention relates to the field of marine new energy technology, and in particular to a marine green ammonia production platform and system based on marine new energy power. Background Technology

[0002] In recent years, the development of green power generation industries such as offshore wind and solar power has entered a period of rapid growth, with the installed capacity continuously increasing. However, due to the mismatch between the unstable characteristics of green electricity and the demand for power consumption, the current operating load of offshore green electricity is relatively low, resulting in significant wind and solar curtailment and a waste of renewable energy. To solve the problem of offshore green electricity consumption, the use of green electricity to electrolyze water to produce hydrogen, which is then converted into methanol, ammonia, and other green secondary energy sources, can achieve sustainable development of offshore renewable energy development and utilization. Ammonia, as a basic chemical raw material and fuel, is an ideal hydrogen storage carrier. The nitrogen gas used in its synthesis can be continuously obtained from the air. In addition, the green attributes of the synthesis method bring a premium, which has broad application prospects.

[0003] Traditional ammonia synthesis processes require a stable power supply, with operating loads typically ranging from 50% to 110%. Onshore power from the grid generally ensures continuous and stable production. However, green electricity produced using renewable energy equipment exhibits significant fluctuations and intermittency, causing frequent start-ups and shutdowns of chemical synthesis units, which can lead to equipment system failures or accidents. Most onshore ammonia plants planned to use green electricity rely on large-capacity hydrogen storage systems to ensure a stable gas supply and consider energy storage batteries or grid power to ensure the stable operation of the ammonia synthesis system. However, offshore platforms offer limited space for such arrangements, making conventional onshore practices either impractical or prohibitively expensive. Furthermore, during the waste heat recovery stage of ammonia synthesis gas, scale buildup occurs on the heat exchange tubes due to high temperatures. Currently, when spraying cleaning fluid to remove scale, the flow rate cannot be dynamically adjusted based on the degree of scale buildup, resulting in waste of the cleaning fluid. Summary of the Invention

[0004] In view of the problems existing in the above and / or existing offshore green ammonia production platforms based on offshore new energy power, the present invention is proposed.

[0005] Therefore, the problem to be solved by this invention is how to address the scaling that occurs on the heat exchange tubes due to high temperatures during the waste heat recovery stage of ammonia synthesis gas. Currently, when spraying cleaning fluid to remove scaling, it is impossible to dynamically adjust the flow rate of the cleaning fluid according to the degree of scaling, which leads to the waste of cleaning fluid.

[0006] To solve the above-mentioned technical problems, the present invention provides the following technical solution: a marine green ammonia production platform based on marine new energy power, comprising platform one and platform two. Platform one is equipped with an emergency generator room, a high-voltage switchboard room, a central control room, a low-voltage switchboard room, a hydrogen compressor unit, an air compressor unit, a PSA tank group unit, a TSA tank group unit, a cooler, a start-up boiler, a circulating cooling equipment, a steam turbine generator set, a seawater desalination unit, an energy storage battery room, and a transformer room. Platform two is equipped with an electrolysis water hydrogen production module, an ammonia synthesis section module, an ammonia refrigeration section module, a liquid cargo handling equipment, a flare tower, a liquid ammonia storage tank one, a liquid ammonia storage tank two, a nitrogen purification equipment, and a synthesis section module.

[0007] As a preferred embodiment of the offshore green ammonia production platform based on offshore new energy power as described in this invention, the synthesis section module further includes a waste heat boiler, a gas tank, a traction component, a spraying component, and a driving component. The waste heat boiler is installed on platform one, the gas tank is mounted on the waste heat boiler, the traction component is located inside the waste heat boiler, the spraying component includes a main frame, a nozzle device, and a base, the nozzle device is mounted on the main frame via the base, the main frame is located inside the waste heat boiler and connected to the traction component, and the driving component is installed between the waste heat boiler and the nozzle device to adjust the flow rate of the nozzle device when the nozzle device moves vertically.

[0008] As a preferred embodiment of the offshore green ammonia production platform based on offshore new energy power as described in this invention, the waste heat boiler includes an air inlet pipe fixedly connected to one end of the waste heat boiler and an exhaust pipe fixedly connected to the other end of the waste heat boiler. The waste heat boiler is vertically equipped with a downcomer pipe and a heat exchange pipe. The nozzle device is arranged on one side of the heat exchange pipe to spray cleaning liquid on its surface.

[0009] As a preferred embodiment of the offshore green ammonia production platform based on offshore new energy power as described in this invention, the downcomer and the top end are connected to the inside of the gas tank. The gas tank includes a water inlet pipe fixedly connected to one end of the gas tank and a steam outlet pipe fixedly connected to the top of the gas tank. A steam-water separator is installed inside the gas tank, and the top end of the heat exchange tube is connected to the input end of the steam-water separator.

[0010] As a preferred embodiment of the offshore green ammonia production platform based on offshore new energy power according to the present invention, the traction component includes a motor fixedly installed on the outer wall of the waste heat boiler and a main shaft connected to the output shaft of the motor. The main frame is vertically slidably connected to the inner wall of the waste heat boiler. A sliding groove is provided on the main frame. A swing arm is fixedly connected to one end of the main shaft. A traction rod is fixedly connected to one end of the swing arm. One end of the traction rod is slidably connected inside the sliding groove.

[0011] As a preferred embodiment of the offshore green ammonia production platform based on offshore new energy power according to the present invention, the nozzle device includes a shell, a drug inlet and a push rod. The push rod is axially slidably connected inside the shell, the drug inlet is fixedly connected to the top of the shell, the inner wall of one end of the shell is set as a second conical surface, and the outer wall of one end of the push rod is set as a first conical surface.

[0012] As a preferred embodiment of the offshore green ammonia production platform based on offshore new energy power as described in this invention, the driving component includes a traction plate connected to multiple push rods, and the traction plate is horizontally slidably connected to the main frame.

[0013] As a preferred embodiment of the offshore green ammonia production platform based on offshore new energy power according to the present invention, the main frame is rotatably connected to a drive shaft, the drive shaft is provided with a spiral adjustment groove, a protrusion is fixedly provided on the traction plate, the traction plate is axially slidably connected to the drive shaft, and the protrusion is slidably connected in the adjustment groove.

[0014] As a preferred embodiment of the offshore green ammonia production platform based on offshore new energy power as described in this invention, the waste heat boiler is internally fixedly equipped with a linear guide rail and a rack, one end of the drive shaft is coaxially fixedly connected to a gear, the drive shaft meshes with the rack, and the slider of the linear guide rail is fixedly connected to the main frame.

[0015] The beneficial effects of this invention are: The flow rate of the nozzle device in this invention can be mechanically adjusted. The nozzle device is driven by a traction component to reciprocate along the axial direction of the heat exchange tube inside the waste heat boiler, so that the nozzle device can spray cleaning liquid onto the surface of the heat exchange tube. The flow rate of the nozzle device can be dynamically adjusted during the movement of the nozzle device, so that the nozzle device can spray different unit amounts of cleaning liquid according to the different degrees of scaling on the surface of the heat exchange tube, thereby achieving the purpose of saving resources.

[0016] In view of the problems existing in the above and / or a certain existing production system, the present invention is proposed.

[0017] Therefore, the problem to be solved by this invention is how to address the limited layout space available on offshore platforms, and the fact that conventional land-based practices are either impossible or too costly to implement at sea.

[0018] To solve the above-mentioned technical problems, the present invention provides the following technical solution: a production system comprising a water electrolysis hydrogen production module, a PSA tank group, an ammonia synthesis section module, and an ammonia refrigeration section module. The water electrolysis hydrogen production module includes a hydrogen purification device and a hydrogen buffer tank, which are connected. The PSA tank group includes a nitrogen compressor unit, a nitrogen purification device, and a nitrogen buffer tank, which are connected to the nitrogen compressor unit. The nitrogen compressor unit is connected to the nitrogen purification device. The ammonia synthesis section module includes a syngas compressor unit, a circulating gas compressor unit, an oil-water separator, a first ammonia synthesis tower, a second ammonia synthesis tower, a first waste heat boiler, a second waste heat boiler, a water cooler, a cold exchanger, a primary ammonia cooler, a secondary ammonia cooler, a non-condensable gas ammonia cooler, a primary ammonia separator, a secondary ammonia separator, a low-pressure flash evaporator, an atmospheric pressure flash evaporator, an ammonia washing tower, a hydrogen recovery device, a heat exchanger, and a non-condensable gas separator. The syngas compressor unit is connected to the nitrogen purification device and the oil-water separator. The system is connected to a hydrogen recovery unit, which is connected to an ammonia washing tower and a cold exchanger. The cold exchanger is connected to a primary ammonia separator and a secondary ammonia separator. A primary ammonia cooler and a secondary ammonia cooler are sequentially connected between the primary and secondary ammonia separators. Both the primary and secondary ammonia separators are connected to a low-pressure flash tank, which is connected to an atmospheric flash tank. The atmospheric flash tank is connected to a non-condensable gas separator. A circulating gas compressor unit is connected between the cold exchanger and an oil-water separator. The oil-water separator is simultaneously connected to a first ammonia synthesis tower and a second ammonia synthesis tower. The first ammonia synthesis tower is connected to a first waste heat boiler, and the second ammonia synthesis tower is connected to a second waste heat boiler. Both the first and second waste heat boilers are connected to a heat exchanger, which is connected to a water cooler. A non-condensable gas ammonia cooler is connected between the ammonia refrigeration section module and the non-condensable gas separator. The ammonia refrigeration section module is simultaneously connected to the primary ammonia cooler, the secondary ammonia cooler, and the atmospheric flash tank.

[0019] The beneficial effects of this invention are: The marine green ammonia production process system provided by this invention is simple, with low investment and operating costs, and operational flexibility of 10% to 110%. Under low load conditions, the reaction heat of the first and second ammonia synthesis towers is used to maintain the catalyst bed temperature, eliminating the need for a heating furnace. Under high load conditions, the heat from the ammonia synthesis gas is recovered for power generation and reuse. The system recovers approximately 5% of the hydrogen through a hydrogen recovery device, resulting in significant overall energy savings and efficiency improvements. Furthermore, key equipment in the system is designed for parallel operation or backup, facilitating uninterrupted maintenance at sea. Dangerous and safe zones are rationally separated, and each operating system is modularly arranged, resulting in low investment costs. Attached Figure Description

[0020] To more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings used in the following description of the embodiments will be briefly introduced. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0021] Figure 1 This is a top-view structural diagram of Platform 1 in an offshore green ammonia production platform based on offshore new energy power.

[0022] Figure 2 This is a top view of Platform 2 in a marine green ammonia production platform based on marine renewable energy power.

[0023] Figure 3 This is a side view of Platform 1 and Platform 2 in a marine green ammonia production platform based on marine new energy power.

[0024] Figure 4 This is a schematic diagram of the main structure of a waste heat boiler in an offshore green ammonia production platform based on offshore new energy power.

[0025] Figure 5 This is a cross-sectional schematic diagram of a waste heat boiler in an offshore green ammonia production platform based on offshore renewable energy power.

[0026] Figure 6 This is a schematic diagram of the main structure of the traction component in an offshore green ammonia production platform based on offshore new energy power.

[0027] Figure 7 This is a top view schematic diagram of the spraying component in an offshore green ammonia production platform based on offshore new energy power.

[0028] Figure 8 This is a cross-sectional structural diagram of the outer shell of a marine green ammonia production platform based on marine renewable energy power.

[0029] Figure 9 This is a schematic diagram of the connection structure between the drive shaft and the traction plate in a marine green ammonia production platform based on marine new energy power.

[0030] Figure 10 This is a system block diagram of a production system.

[0031] In the diagram: 1. Platform One; 2. Platform Two; 3. Emergency Generator Room; 4. High-Voltage Switchboard Room; 5. Central Control Room; 6. Low-Voltage Switchboard Room; 7. Hydrogen Compressor Unit; 8. Air Compressor Equipment; 9. PSA Tank Group Equipment; 901. Nitrogen Compressor Unit; 902. Nitrogen Purification Unit; 903. Nitrogen Buffer Tank; 10. TSA Tank Group Equipment; 11. Cooler; 12. Start-up Boiler; 13. Circulating Cooling Equipment; 14. Steam Turbine Generator Unit; 15. Seawater Desalination Equipment; 16. Energy Storage Battery Room; 17. Transformer Room; 18. Electrolytic Water Hydrogen Production Module; 1801. Hydrogen purification unit; 1802, Hydrogen buffer tank; 19, Ammonia synthesis section module; 1901, Syngas compressor unit; 1902, Circulating gas compressor unit; 1903, Oil-water separator; 1904, First ammonia synthesis tower; 1905, Second ammonia synthesis tower; 1906, First waste heat boiler; 1907, Second waste heat boiler; 1908, Water cooler; 1909, Cold exchanger; 1910, Primary ammonia cooler; 1911, Secondary ammonia cooler; 1912, Non-condensable gas ammonia cooler; 1913, Primary ammonia separator; 1914, Secondary ammonia separator; 1915, Low-pressure flash evaporator; 1 916. Atmospheric flash evaporator; 1917. Ammonia washing tower; 1918. Hydrogen recovery unit; 1919. Heat exchanger; 1920. Non-condensable gas separator; 20. Ammonia refrigeration section module; 21. Liquid cargo handling equipment; 22. Flare tower; 23. Liquid ammonia storage tank one; 24. Liquid ammonia storage tank two; 25. Nitrogen purification equipment; 26. Synthesis section module; 261. Waste heat boiler; 2611. Inlet pipe; 2612. Exhaust pipe; 2613. Downcomer; 2614. Heat exchanger tube; 262. Gas drum; 2621. Water inlet pipe; 2622. Steam output pipe; 2623. Steam-water separator; 2 63. Traction component; 2631. Motor; 2632. Main shaft; 2633. Swing arm; 2634. Traction rod; 2635. Slide groove; 2636. Linear guide rail; 264. Spraying component; 2641. Main frame; 2642. Nozzle device; 26421. Housing; 26422. Drug inlet; 26423. Push rod; 26424. First conical surface; 26425. Second conical surface; 2643. Base; 265. Driving component; 2651. Rack; 2652. Gear; 2653. Drive shaft; 2654. Traction plate; 2655. Adjustment groove; 2656. Protrusion. Detailed Implementation

[0032] To make the above-mentioned objects, features and advantages of the present invention more apparent and understandable, the specific embodiments of the present invention will be described in detail below with reference to the accompanying drawings.

[0033] Many specific details are set forth in the following description in order to provide a full understanding of the invention. However, the invention may also be practiced in other ways different from those described herein, and those skilled in the art can make similar extensions without departing from the spirit of the invention. Therefore, the invention is not limited to the specific embodiments disclosed below.

[0034] Secondly, the term "one embodiment" or "embodiment" as used herein refers to a specific feature, structure, or characteristic that may be included in at least one implementation of the present invention. The phrase "in one embodiment" appearing in different places in this specification does not necessarily refer to the same embodiment, nor is it a single or selective embodiment that is mutually exclusive with other embodiments.

[0035] Example 1, please refer to Figures 1 to 3 This is the first embodiment of the present invention, which provides an offshore green ammonia production platform based on offshore new energy power, including platform 1 and platform 2. Platform 1 is equipped with an emergency generator room 3, a high-voltage switchboard room 4, a central control room 5, a low-voltage switchboard room 6, a hydrogen compressor unit 7, an air compressor unit 8, a PSA tank group unit 9, a TSA tank group unit 10, a cooler 11, a start-up boiler 12, a circulating cooling equipment 13, a steam turbine generator set 14, a seawater desalination unit 15, an energy storage battery room 16, and a transformer room 17. Platform 2 is equipped with an electrolysis water hydrogen production module 18, an ammonia synthesis section module 19, an ammonia refrigeration section module 20, a liquid cargo handling equipment 21, a flare tower 22, a liquid ammonia storage tank 1 23, a liquid ammonia storage tank 2 24, a nitrogen purification equipment 25, and a synthesis section module 26.

[0036] Platform 1 and Platform 2 obtain their power directly from the offshore booster station, including power generated by offshore new energy wind power, photovoltaic, and wave power generation devices, as well as stable power from the onshore power grid. They are equipped with steam turbine generators to recover the heat energy of steam generated by the waste heat boiler of the ammonia production system. In addition, Platform 1 is also equipped with an energy storage battery room 16 and an emergency generator room 3 to ensure short-term power supply to the operating system in the event of an emergency, so as to ensure the safe and orderly shutdown of the green ammonia production system.

[0037] The water electrolysis hydrogen production module 18 includes water electrolysis hydrogen production system equipment, as well as supporting hydrogen production transformers, hydrogen production power supplies and auxiliary equipment. The water electrolysis hydrogen production module 18 is equipped with a wall structure, and the structure facing the hazardous area meets the explosion-proof requirements. The seawater desalination equipment 15, circulating cooling equipment 13, cooler 11, air compressor equipment 8, PSA tank group equipment 9, TSA tank group equipment 10, hydrogen compressor group 7, steam turbine generator group 14, and start-up boiler 12 are arranged in the open or semi-open area of ​​platform 1, which is a safe area. The nitrogen purification equipment 25, synthesis section module 26, ammonia synthesis section module 19, ammonia refrigeration section module 20, liquid cargo handling equipment 21, flare tower 22, liquid ammonia storage tank 1 23 and liquid ammonia storage tank 24 are arranged on the open deck of platform 2, which is a hazardous area.

[0038] Example 2, please refer to Figures 4 to 9 This is the second embodiment of the present invention.

[0039] The synthesis section module 26 of this embodiment also includes a waste heat boiler 261, an air tank 262, a traction component 263, a spraying component 264, and a driving component 265. The waste heat boiler 261 is installed on platform 1, the air tank 262 is assembled on the waste heat boiler 261, the traction component 263 is disposed inside the waste heat boiler 261, the spraying component 264 includes a main frame 2641, a nozzle device 2642, and a base 2643. The nozzle device 2642 is installed on the main frame 2641 through the base 2643. The main frame 2641 is disposed inside the waste heat boiler 261 and connected to the traction component 263. The driving component 265 is installed between the waste heat boiler 261 and the nozzle device 2642 to adjust the flow rate of the nozzle device 2642 when the nozzle device 2642 moves vertically.

[0040] It should be noted that the high-temperature synthesis gas from the first and second ammonia synthesis towers enters the waste heat boiler 261, and room-temperature water enters the waste heat boiler 261 through the gas chamber 262 to exchange heat with the synthesis gas. After heat exchange, the room-temperature water is converted into steam and discharged from the gas chamber 262, while the synthesis gas after heat exchange is discharged through the waste heat boiler 261. In the above process, the main frame 2641 drives the nozzle device 2642 to reciprocate vertically under the drive of the traction component 263. At the same time, the nozzle device 2642 cooperates with the drive component 265 during movement to realize the dynamic adjustment of the flow rate of the nozzle device 2642 during the spraying of cleaning liquid.

[0041] Specifically, the waste heat boiler 261 includes an air inlet pipe 2611 fixedly connected to one end of the waste heat boiler 261, and an exhaust pipe 2612 fixedly connected to the other end of the waste heat boiler 261. Inside the waste heat boiler 261, a downcomer pipe 2613 and a heat exchange pipe 2614 are vertically arranged. A nozzle device 2642 is arranged on one side of the heat exchange pipe 2614 to spray cleaning liquid on its surface.

[0042] The high-temperature synthesis gas from the first and second ammonia synthesis towers enters the waste heat boiler 261 through the inlet pipe 2611 and is finally discharged from the exhaust pipe 2612. The ambient temperature water moves to the heat exchange tube 2614 through the downcomer 2613. Inside the waste heat boiler 261, after the high-temperature synthesis gas from the first and second ammonia synthesis towers comes into contact with the heat exchange tube 2614, the high-temperature synthesis gas can exchange heat with the ambient temperature water in the downcomer 2613 and the heat exchange tube 2614, so that the ambient temperature water is finally turned into water vapor and enters the gas drum 262.

[0043] Specifically, the downcomer 2613 and its top end are connected to the inside of the gas chamber 262. The gas chamber 262 includes a water inlet pipe 2621 fixedly connected to one end of the gas chamber 262 and a steam outlet pipe 2622 fixedly connected to the top of the gas chamber 262. A steam-water separator 2623 is installed inside the gas chamber 262, and the top end of the heat exchange tube 2614 is connected to the input end of the steam-water separator 2623.

[0044] Room temperature water enters the downcomer 2613 through the inlet pipe 2621, and after heat exchange in the heat exchange tube 2614, it is converted into water vapor and then enters the steam-water separator 2623. After water removal, the high temperature water vapor is finally discharged through the steam outlet pipe 2622 so that the high temperature steam can be utilized.

[0045] It should be noted that the steam-water separator 2623 is used to separate steam and water in high-temperature steam to remove moisture from the high-temperature steam. Its specific structure and working principle are well known to those skilled in the art and will not be described in detail here.

[0046] Specifically, the traction component 263 includes a motor 2631 fixedly installed on the outer wall of the waste heat boiler 261, and a main shaft 2632 connected to the output shaft of the motor 2631. The main frame 2641 is vertically slidably connected to the inner wall of the waste heat boiler 261. A sliding groove 2635 is provided on the main frame 2641. A swing arm 2633 is fixedly connected to one end of the main shaft 2632. A traction rod 2634 is fixedly connected to one end of the swing arm 2633. One end of the traction rod 2634 is slidably connected inside the sliding groove 2635.

[0047] The motor 2631 can drive the main shaft 2632 to rotate. When the main shaft 2632 rotates, it can drive the swing arm 2633 to rotate synchronously. At this time, the other end of the swing arm 2633 can drive the traction rod 2634 to revolve. Since the traction rod 2634 is always located in the slide groove 2635, when the traction rod 2634 revolves, it can drive the main frame 2641 to reciprocate vertically through the slide groove 2635. This allows the main frame 2641 to drive multiple nozzle devices 2642 to move synchronously through the base 2643. Since the movement direction of the nozzle devices 2642 is along the axial direction of the heat exchange tube 2614, the nozzle devices 2642 can thoroughly clean the scale on the heat exchange tube 2614.

[0048] Specifically, the nozzle device 2642 includes a housing 26421, a drug inlet 26422, and a push rod 26423. The push rod 26423 is axially slidably connected inside the housing 26421. The drug inlet 26422 is fixedly connected to the top of the housing 26421. The inner wall of one end of the housing 26421 is configured as a second conical surface 26425, and the outer wall of one end of the push rod 26423 is configured as a first conical surface 26424. The driving component 265 includes a traction plate 2654 connected to multiple push rods 26423. The traction plate 2654 is horizontally slidably connected to the main frame 2641. A drive shaft 2653 is rotatably connected to the main frame 2641. A spiral adjustment groove 2655 is provided on the drive shaft 2653. A protrusion 2656 is fixedly provided on the traction plate 2654. The traction plate 2654 is axially slidably connected to the drive shaft 2653, and the protrusion 2656 is slidably connected in the adjustment groove 2655.

[0049] Because the temperature on the heat exchange tube 2614 is not uniform but gradually increases from bottom to top, the scale on its surface also increases with the increase in temperature. Therefore, the amount of cleaning fluid sprayed by the nozzle device 2642 is not fixed but gradually increases as it moves from the end of the heat exchange tube 2614 to the top of the heat exchange tube 2614. When the nozzle device 2642 moves from the top of the heat exchange tube 2614 to the end of the heat exchange tube 2614, the amount of cleaning fluid sprayed gradually decreases.

[0050] Taking the movement of the nozzle device 2642 from the end to the top of the heat exchange tube 2614 as an example, the specific process is as follows: During the upward movement of the main frame 2641, the drive shaft 2653 can be driven to rotate. When the drive shaft 2653 rotates, it can drive the adjusting groove 2655 on its surface to rotate synchronously. Since the adjusting groove 2655 has a spiral structure, it can cooperate with the protrusion 2656 to drive the traction plate 2654 to move axially along the drive shaft 2653. By setting the spiral direction of the adjusting groove 2655, when the main frame 2641 moves upward, the traction plate 2654 gradually moves away from the nozzle. When the device 2642 and the traction plate 2654 move, they can drive the push rod 26423 to move synchronously. At this time, the push rod 26423 will drive the first conical surface 26424 away from the second conical surface 26425 inside the outer shell 26421. The distance between the first conical surface 26424 and the second conical surface 26425 will gradually increase as the outer shell 26421 rises. Therefore, the flow rate of the cleaning fluid will also increase. In this way, the higher the position on the heat exchange tube 2614, the more scale will be formed. The higher the position of the nozzle device 2642, the more cleaning fluid will be sprayed, thereby achieving the purpose of adjusting the flow rate of the cleaning fluid according to the degree of scaling.

[0051] It should be noted that the cleaning fluid enters the outer casing 26421 through the inlet 26422. The device for storing the cleaning fluid can be a storage tank placed in the external environment. The cleaning fluid is delivered to the inlet 26422 through a pump and a hose. In order to ensure the continuous delivery of the cleaning fluid, the hose is made of a high-temperature resistant material.

[0052] Specifically, the waste heat boiler 261 has a linear guide rail 2636 and a rack 2651 fixedly installed inside. One end of the drive shaft 2653 is coaxially fixedly connected to a gear 2652. The drive shaft 2653 meshes with the rack 2651. The slider of the linear guide rail 2636 is fixedly connected to the main frame 2641.

[0053] During the upward movement of the main frame 2641, the drive shaft 2653 can drive the gear 2652 to move synchronously. At this time, the gear 2652 can cooperate with the rack 2651 to realize the rotation of the drive shaft 2653. The linear guide rail 2636 can limit the range of motion of the main frame 2641 and reduce the friction between the main frame 2641 and the inner wall of the waste heat boiler 261.

[0054] Example 3, refer to Figure 10 This is the third embodiment of the present invention, which provides a production system including an electrolytic water hydrogen production module 18, a PSA tank group equipment 9, an ammonia synthesis section module 19, and an ammonia refrigeration section module 20.

[0055] Among them, the ammonia synthesis section module 19 adopts two sets of ammonia synthesis towers of different sizes connected in series and parallel, and is equipped with a parallel variable frequency compressor unit to meet the wide load variation of green power ammonia production.

[0056] Specifically, the water electrolysis hydrogen production module 18 includes multiple electrolyzers, gas-liquid separators, hydrogen purification devices 1801 and hydrogen buffer tanks 1802. The multiple electrolyzers, gas-liquid separators, hydrogen purification devices 1801 and hydrogen buffer tanks 1802 are connected in sequence to adapt to rapid adjustment of green electricity fluctuations.

[0057] Specifically, the PSA tank assembly 9 includes multiple air compressors, an adsorption tower containing carbon molecular sieves, a nitrogen compressor unit 9017, a nitrogen purification device 902, and a nitrogen buffer tank 903. The multiple air compressors are connected to the adsorption tower containing carbon molecular sieves, the adsorption tower containing carbon molecular sieves is connected to the nitrogen buffer tank 903, the nitrogen buffer tank 903 is connected to the nitrogen compressor unit 9017, and the nitrogen compressor unit 9017 is connected to the nitrogen purification device 902.

[0058] In this system, one adsorption tower is always in operation, which depressurizes and desorbs nitrogen and oxygen in turn. The nitrogen purification unit 902 is located after the nitrogen compressor and before the syngas compressor. It removes trace amounts of oxygen by adding an appropriate amount of hydrogen for catalytic removal. After cooling by a water condenser and removing water by a gas-water separator 2623, it is dried by TSA. The two adsorption drying towers are used alternately, one for adsorption and drying to remove water, and the other for heating, desorption, and drainage to obtain high-purity nitrogen with an oxygen content of ≤5ppm. Multiple air compressors can also provide the required compressed air for the system.

[0059] Specifically, the ammonia synthesis section module 19 includes a synthesis gas compressor unit 1901, a circulating gas compressor unit 1902, an oil-water separator 1903, a first ammonia synthesis tower 1904, a second ammonia synthesis tower 1905, a first waste heat boiler 1906, a second waste heat boiler 1907, a water cooler 1908, a cold exchanger 1909, a primary ammonia cooler 1910, a secondary ammonia cooler 1911, a non-condensable gas ammonia cooler 1912, a primary ammonia separator 1913, and a secondary ammonia separator 1914. The system includes a primary ammonia separator 1914, a low-pressure flash evaporator 1915, an atmospheric flash evaporator 1916, an ammonia washing tower 1917, a hydrogen recovery unit 1918, and a heat exchanger 1919. A syngas compressor unit 1901 is connected to a nitrogen purification unit 902, an oil-water separator 1903, and a hydrogen recovery unit 1918. The hydrogen recovery unit 1918 is connected to the ammonia washing tower 1917 and a cold exchanger 1909. The cold exchanger 1909 is connected to the primary ammonia separator 1913 and the secondary ammonia separator 1919. A primary ammonia separator 1914 is connected to a secondary ammonia separator 1913, and a primary ammonia cooler 1910 and a secondary ammonia cooler 1911 are connected sequentially between them. Both the primary and secondary ammonia separators 1913 and 1914 are connected to a low-pressure flash tank 1915, which is connected to an atmospheric pressure flash tank 1916. The atmospheric pressure flash tank 1916 is connected to a non-condensable gas separator. A circulating gas compressor unit 1902 is connected to the heat exchanger. Between 1909 and oil-water separator 1903, oil-water separator 1903 is simultaneously connected to the first ammonia synthesis tower 1904 and the second ammonia synthesis tower 1905. The first ammonia synthesis tower 1904 is connected to the first waste heat boiler 1906. The second ammonia synthesis tower 1905 is connected to the second waste heat boiler 1907. The first waste heat boiler 1906 and the second waste heat boiler 1907 are both connected to heat exchanger 1919. Heat exchanger 1919 is connected to water cooler 1908.

[0060] The first ammonia synthesis tower 1904 and the second ammonia synthesis tower 1905 adopt an internally cooled reactor structure, equipped with heat exchangers and electric furnace devices. The bottom outlets of the first ammonia synthesis tower 1904 and the second ammonia synthesis tower 1905 are directly connected to the first waste heat boiler 1906 and the second waste heat boiler 1907, respectively, to avoid excessively high outlet pipe temperatures and pressures and to utilize by-product steam. Under high load conditions, the high-temperature gas in the catalyst layer of the first ammonia synthesis tower 1904 and the second ammonia synthesis tower 1905 exchanges heat with the cold synthesis gas in the heat exchange tubes 2614 buried in the catalyst layer to control the catalyst temperature. Under low load conditions, the hot synthesis gas in the heat exchange tubes 2614 buried in the catalyst layer transfers heat to the catalyst layer to maintain the catalyst temperature under low load conditions.

[0061] Syngas compressor unit 1901 and circulating gas compressor unit 1902 are each configured with at least two sets, which can be operated in parallel. At low load, only one compressor unit needs to be turned on. The syngas and circulating gas after being pressurized by the compressor unit enter the oil-water separator 1903 to mix and separate the entrained oil and water. Most of the gas enters the annulus of the second ammonia synthesis tower 1905. The remaining small amount of syngas mixes with the gas exiting the annulus and then undergoes heat exchange in the heat exchanger 1919. After that, it can enter the first ammonia synthesis tower 1904 and the second ammonia synthesis tower 1905 respectively. The reaction gas coming out of the bottom of the first ammonia synthesis tower 1904 can enter the second ammonia synthesis tower 1905 through pipelines and valve opening and closing settings to maintain the catalyst temperature in the second ammonia synthesis tower 1905. The syngas processing ratio of the first ammonia synthesis tower 1904 and the second ammonia synthesis tower 1905 is implemented at 4:6-3:7. When the first ammonia synthesis tower 1904 and the second ammonia synthesis tower 1905 are connected in parallel, the full load can reach 110% of the total operating load of the system.

[0062] After the reaction gas from the first waste heat boiler 1906 and the second waste heat boiler 1907 is mixed, it enters the heat exchanger 1919 to heat the gas entering the tower. Then, after passing through the water cooler 1908 and the cold exchanger 1909, it undergoes gas-liquid separation through the primary ammonia cooler 1910 and the secondary ammonia cooler 1911. The separated liquid ammonia is separated in the low-pressure flash tank 1915. The separated liquid ammonia product enters the atmospheric pressure flash tank 1916 for flash separation. The low-pressure flash gas is sent to the syngas compressor, and the liquid ammonia separated in the atmospheric pressure flash tank 1916 is sent to the liquid ammonia storage tank. The gaseous ammonia first passes through the non-condensable gas ammonia cooler 1912 to recover its cooling capacity before entering the ammonia refrigeration section module 20 for ammonia recovery.

[0063] It should be noted that since the argon in the PSA tank unit 9 cannot be removed, a large amount of argon will accumulate in the synthesis system. It is necessary to reduce the argon in the system by using purge gas. Inevitably, some hydrogen and nitrogen will be carried out. Hydrogen recovery is carried out on the synthesis purge gas. First, the ammonia in it is washed away by the ammonia washing tower 1917, and then the hydrogen is recovered by the hydrogen recovery device 1918. The recovered hydrogen-rich gas is returned to the ammonia synthesis loop, and the non-permeable gas is sent to the flare tower 22 for combustion.

[0064] Specifically, the ammonia refrigeration section module 20 is connected to the non-condensable gas separator 1920 via a non-condensable gas ammonia cooler 1912. The ammonia refrigeration section module 20 is also connected to the primary ammonia cooler 1910, the secondary ammonia cooler 1911, and the atmospheric flash tank 1916. The ammonia refrigeration section module 20 includes a multi-stage ammonia compressor and an ammonia receiving tank. The liquid ammonia separated from the ammonia receiving tank is sent to the ammonia cooler. The non-condensable gas separated from the ammonia receiving tank, carrying ammonia, is cooled by the gaseous ammonia from the atmospheric flash tank 1916 in the non-condensable gas ammonia cooler 1912. The condensed liquid ammonia is sent to the atmospheric flash tank, and the non-condensable gas is sent to the inlet of the syngas compressor.

[0065] It should be noted that when the new energy power supply exceeds 50% of the rated total power consumption, the power comes from the electricity obtained by the booster station from the offshore new energy power supply equipment and the power generated by the steam turbine generator set 14. The first ammonia synthesis tower 1904 and the second ammonia synthesis tower 1905 operate in parallel, and the synthesis gas compressor set 1901 and the circulating gas compressor set 1902 are all in operation. The gas supply is adjusted by regulating the variable frequency motor. When the new energy power supply is between 31% and 50% of the rated total power consumption, the power comes from the electricity obtained by the booster station from the offshore new energy power supply equipment and the power generated by the steam turbine generator set 14. The electricity supply is provided by the first ammonia synthesis tower 1904 and the second ammonia synthesis tower 1905, which operate in series and parallel. Specifically, the first ammonia synthesis tower 1904 is operating at full capacity, while the second ammonia synthesis tower 1905 operates at low load. Gas from the outlet of the first waste heat boiler 1906 is mixed with a small amount of syngas and enters the second ammonia synthesis tower 1905 for ammonia synthesis. The catalyst temperature in the second ammonia synthesis tower 1905 is maintained stable by the heat of reaction. The syngas compressor unit 1901 and the circulating gas compressor unit 1902 operate at half their configured capacity, and the gas supply is adjusted by regulating the variable frequency motor. When the new energy power supply is 10% of the rated total power consumption... %-30% of the electricity comes from the booster station's acquisition of power from offshore new energy power supply equipment and the power generated by steam turbine generator set 14. The first ammonia synthesis tower 1904 is in operation, and the second ammonia synthesis tower 1905 is in standby mode. Part of the gas exiting the first ammonia synthesis tower 1904 passes through the first waste heat boiler 1906, and the other part passes through a bypass pipeline into the catalyst bed of the second ammonia synthesis tower 1905 for heat preservation. The synthesis gas compressor unit 1901 and the circulating gas compressor unit 1902 operate as configured individual units, and the gas supply is adjusted by regulating the variable frequency motor. When the new energy power supply is less than the rated total consumption... 10% of the electricity is supplied by the booster station from the onshore power grid. The platform operates stably under 10% ammonia production conditions, and the process is consistent with the 10%-30% load operation. When power cannot be obtained from the booster station suddenly, including sudden power cable failure, booster station equipment failure, high-voltage power distribution system failure, etc., the electrolytic cell, compressor and other equipment will immediately stop. The energy storage battery room 16 and the emergency generator room 3 provide power for the system safety, including necessary pumps, valves, air system, ventilation system, etc., and provide power guarantee for the system to further purge nitrogen and vent hydrogen and reaction gas.

[0066] It should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention and are not intended to limit it. Although the present invention has been described in detail with reference to preferred embodiments, those skilled in the art should understand that modifications or equivalent substitutions can be made to the technical solutions of the present invention without departing from the spirit and scope of the technical solutions of the present invention, and all such modifications or substitutions should be covered within the scope of the claims of the present invention.

Claims

1. A marine green ammonia production platform based on offshore renewable energy power, characterized in that, include: Platform 1 (1) is equipped with an emergency generator room (3), a high-voltage switchboard room (4), a central control room (5), a low-voltage switchboard room (6), a hydrogen compressor unit (7), an air compressor unit (8), a PSA tank group unit (9), a TSA tank group unit (10), a cooler (11), a start-up boiler (12), a circulating cooling equipment (13), a steam turbine generator set (14), a seawater desalination unit (15), an energy storage battery room (16), and a transformer room (17). Platform 2 (2) is equipped with an electrolysis water hydrogen production module (18), an ammonia synthesis section module (19), an ammonia freezing section module (20), a liquid cargo processing equipment (21), a flare tower (22), a liquid ammonia storage tank 1 (23), a liquid ammonia storage tank 2 (24), a nitrogen purification equipment (25), and a synthesis section module (26).

2. The offshore green ammonia production platform based on offshore new energy power as described in claim 1, characterized in that, The synthesis section module (26) also includes: Waste heat boiler (261), said waste heat boiler (261) is installed on platform one (1); An air chamber (262) is mounted on a waste heat boiler (261); A traction component (263) is disposed inside the waste heat boiler (261); A spraying component (264), comprising a main frame (2641), a nozzle device (2642), and a base (2643), wherein the nozzle device (2642) is mounted on the main frame (2641) via the base (2643), and the main frame (2641) is disposed inside the waste heat boiler (261) and connected to the traction component (263); and A drive unit (265) is installed between the waste heat boiler (261) and the nozzle device (2642) to adjust the flow rate of the nozzle device (2642) when the nozzle device (2642) moves vertically.

3. The offshore green ammonia production platform based on offshore new energy power as described in claim 2, characterized in that, The waste heat boiler (261) includes an air inlet pipe (2611) fixedly connected to one end of the waste heat boiler (261) and an exhaust pipe (2612) fixedly connected to the other end of the waste heat boiler (261). The waste heat boiler (261) has a downcomer pipe (2613) and a heat exchange pipe (2614) vertically arranged inside. The nozzle device (2642) is arranged on one side of the heat exchange pipe (2614) to spray cleaning liquid on its surface.

4. The offshore green ammonia production platform based on offshore new energy power according to claim 3, characterized in that, The downcomer (2613) and its top end are connected to the inside of the gas chamber (262). The gas chamber (262) includes a water inlet pipe (2621) fixedly connected to one end of the gas chamber (262) and a steam outlet pipe (2622) fixedly connected to the top of the gas chamber (262). A steam-water separator (2623) is installed inside the gas chamber (262). The top end of the heat exchange tube (2614) is connected to the input end of the steam-water separator (2623).

5. A marine green ammonia production platform based on offshore new energy power as described in claim 2, characterized in that, The traction component (263) includes a motor (2631) fixedly installed on the outer wall of the waste heat boiler (261) and a main shaft (2632) connected to the output shaft of the motor (2631). The main frame (2641) is vertically slidably connected to the inner wall of the waste heat boiler (261). A sliding groove (2635) is provided on the main frame (2641). A swing arm (2633) is fixedly connected to one end of the main shaft (2632). A traction rod (2634) is fixedly connected to one end of the swing arm (2633). One end of the traction rod (2634) is slidably connected inside the sliding groove (2635).

6. A marine green ammonia production platform based on offshore renewable energy power as described in claim 2, characterized in that, The nozzle device (2642) includes a housing (26421), a drug inlet (26422), and a push rod (26423). The push rod (26423) is axially slidably connected inside the housing (26421). The drug inlet (26422) is fixedly connected to the top of the housing (26421). The inner wall of one end of the housing (26421) is configured as a second conical surface (26425), and the outer wall of one end of the push rod (26423) is configured as a first conical surface (26424).

7. A marine green ammonia production platform based on offshore new energy power as described in claim 6, characterized in that, The drive unit (265) includes a traction plate (2654) connected to a plurality of push rods (26423), the traction plate (2654) being horizontally slidably connected to the main frame (2641).

8. A marine green ammonia production platform based on offshore new energy power as described in claim 7, characterized in that, A drive shaft (2653) is rotatably connected to the main frame (2641). A spiral adjustment groove (2655) is provided on the drive shaft (2653). A protrusion (2656) is fixedly provided on the traction plate (2654). The traction plate (2654) is axially slidably connected to the drive shaft (2653), and the protrusion (2656) is slidably connected in the adjustment groove (2655).

9. A marine green ammonia production platform based on offshore new energy power as described in claim 8, characterized in that, The waste heat boiler (261) is internally fixedly equipped with a linear guide rail (2636) and a rack (2651). One end of the drive shaft (2653) is coaxially fixedly connected to a gear (2652). The drive shaft (2653) meshes with the rack (2651). The slider of the linear guide rail (2636) is fixedly connected to the main frame (2641).

10. A production system, characterized in that, Including a marine green ammonia production platform based on offshore renewable energy power as described in any one of claims 1-9, and: The water electrolysis hydrogen production module (18) includes a hydrogen purification device (1801) and a hydrogen buffer tank (1802), which are connected together. PSA tank assembly equipment (9), the PSA tank assembly equipment (9) includes a nitrogen compressor unit (901), a nitrogen purification device (902) and a nitrogen buffer tank (903), the nitrogen buffer tank (903) is connected to the nitrogen compressor unit (901), and the nitrogen compressor unit (901) is connected to the nitrogen purification device (902); The ammonia synthesis section module (19) includes a synthesis gas compressor unit (1901), a circulating gas compressor unit (1902), an oil-water separator (1903), a first ammonia synthesis tower (1904), a second ammonia synthesis tower (1905), a first waste heat boiler (1906), a second waste heat boiler (1907), a water cooler (1908), a cold exchanger (1909), a primary ammonia cooler (1910), a secondary ammonia cooler (1911), a non-condensable gas ammonia cooler (1912), a primary ammonia separator (1913), and a secondary ammonia separator. The system includes a flash evaporator (1914), a low-pressure flash evaporator (1915), an atmospheric-pressure flash evaporator (1916), an ammonia washing tower (1917), a hydrogen recovery unit (1918), a heat exchanger (1919), and a non-condensable gas separator (1920). The syngas compressor unit (1901) is connected to a nitrogen purification unit (902), an oil-water separator (1903), and a hydrogen recovery unit (1918). The hydrogen recovery unit (1918) is connected to the ammonia washing tower (1917) and a cold exchanger (1909). The cold exchanger (1909) is connected to the primary ammonia separator (1913) and... A secondary ammonia separator (1914) is connected, and a primary ammonia cooler (1910) and a secondary ammonia cooler (1911) are sequentially connected between the primary ammonia separator (1913) and the secondary ammonia separator (1914). Both the primary ammonia separator (1913) and the secondary ammonia separator (1914) are connected to a low-pressure flash tank (1915), which is connected to an atmospheric pressure flash tank (1916). The atmospheric pressure flash tank (1916) is connected to a non-condensable gas separator (1920), and the circulating gas compressor unit (1902) is connected to the cold exchanger. Between the apparatus (1909) and the oil-water separator (1903), the oil-water separator (1903) is simultaneously connected to the first ammonia synthesis tower (1904) and the second ammonia synthesis tower (1905). The first ammonia synthesis tower (1904) is connected to the first waste heat boiler (1906), and the second ammonia synthesis tower (1905) is connected to the second waste heat boiler (1907). Both the first waste heat boiler (1906) and the second waste heat boiler (1907) are connected to a heat exchanger (1919), which is connected to a water cooler (1908). The ammonia refrigeration section module (20) is connected to the non-condensable gas separator (1920) via a non-condensable gas ammonia cooler (2001), and is also connected to the primary ammonia cooler (1910), the secondary ammonia cooler (1911), and the atmospheric flash evaporator (1916).

Images