A hydrogen carbon dioxide recovery purification system for formic acid

Abstract

The utility model discloses a kind of formic acid hydrogen production carbon dioxide recovery purification systems, its technical scheme main points include sequentially connected: formic acid hydrogen production unit, for by formic acid raw material preparation hydrogen-rich gas;Carbon dioxide separation unit, for separating crude carbon dioxide in hydrogen-rich gas, purifying hydrogen;Carbon dioxide collection unit, for collecting crude carbon dioxide and pressurization;Carbon dioxide purification unit, for filtering impurity in crude carbon dioxide, purifying carbon dioxide;Carbon dioxide storage unit, for storing after carbon dioxide of depositing;The utility model innovation fusion carbon dioxide recycling, realize the clean production process of high formic acid conversion rate, carbon dioxide purity, hydrogen purity, applicable to distributed energy and chemical carbon resource scene.

Description

Technical Field

[0001] This utility model relates to the field of hydrogen production technology, and more specifically to a formic acid hydrogen production and carbon dioxide recovery and purification system. Background Technology

[0002] Formic acid hydrogen production technology has become a research hotspot in the field of hydrogen production and storage due to its advantages such as mild reaction conditions, high efficiency in hydrogen production, and controllable hydrogen release. However, if the carbon dioxide byproduct produced by this reaction is emitted directly without treatment, it will not only waste carbon resources but also increase the environmental burden. Therefore, how to achieve efficient recovery and resource utilization of carbon dioxide in the formic acid hydrogen production process has become a key link in promoting the carbon cycle in this technology. Utility Model Content

[0003] To solve the above problems, this utility model provides the following technical solution: A formic acid hydrogen production and carbon dioxide recovery and purification system includes, in sequence: a formic acid hydrogen production unit for producing hydrogen-rich gas from formic acid raw material; a carbon dioxide separation unit for separating crude carbon dioxide from the hydrogen-rich gas and purifying hydrogen; a carbon dioxide collection unit for collecting the crude carbon dioxide and pressurizing it; a carbon dioxide purification unit for filtering impurities from the crude carbon dioxide and purifying carbon dioxide; and a carbon dioxide storage unit for storing the carbon dioxide purified by the carbon dioxide purification unit.

[0004] The present invention is further configured such that: the formic acid hydrogen production unit includes a delivery pump, a catalytic cracking reaction device, a heating device, a heat exchange device, and a first gas-liquid separation device; the delivery pump delivers formic acid raw material through the heat exchange device and then into the catalytic cracking reaction device; the heating device can heat the catalytic cracking reaction device; the hydrogen-rich gas generated by the catalytic cracking reaction device passes through the heat exchange device, exchanges heat with the formic acid raw material in the heat exchange device, and then enters the first gas-liquid separation device; the first gas-liquid separation device separates the moisture in the hydrogen-rich gas, forming dry hydrogen-rich gas, which then enters the carbon dioxide separation unit, and the separated moisture can be returned to the catalytic cracking reaction device or discharged.

[0005] The present invention is further configured such that: a first flow meter and a first solenoid valve are provided between the delivery pump and the heat exchange device; a first temperature sensor, a first pressure sensor and a first level gauge are provided on the catalytic cracking reaction device; a liquid blocking device is provided between the catalytic cracking reaction device and the heat exchange device; a second solenoid valve is provided between the heat exchange device and the first gas-liquid separation device; and a third solenoid valve, an adsorption device, a dew point meter and a second flow meter are provided between the first gas-liquid separation device and the carbon dioxide separation unit. The adsorption device is used to adsorb impurities in hydrogen-rich gas.

[0006] The present invention is further configured such that: the carbon dioxide separation unit includes a first adsorption tower, a first buffer tank and a first vacuum pump; the first adsorption tower is provided with a first adsorbent, which adsorbs crude carbon dioxide from hydrogen-rich gas to separate hydrogen, and the separated hydrogen is stored in the first buffer tank; the first vacuum pump is used to evacuate the first adsorption tower to desorb the crude carbon dioxide in the first adsorbent, and the desorbed crude carbon dioxide is transported to the carbon dioxide collection unit.

[0007] The present invention is further configured such that: a fourth solenoid valve, a second temperature sensor and a second pressure sensor are connected to the first adsorption tower; a third flow meter and a first online analyzer are provided between the first adsorption tower and the first buffer tank; the first online analyzer is used to detect the purity of hydrogen and the amount of impurities remaining at the outlet of the first buffer tank; and a fourth flow meter is provided between the first vacuum pump and the carbon dioxide collection unit.

[0008] The present invention is further configured such that: the carbon dioxide collection unit includes a gas filtration device, a second buffer tank, a compressor, a cooling device, and a second gas-liquid separator; the crude carbon dioxide is filtered by the gas filtration device and then transported to the second buffer tank; the crude carbon dioxide in the second buffer tank is pressurized by the compressor and then transported to the cooling device; the crude carbon dioxide is cooled by the cooling device and then transported to the second gas-liquid separator; the crude carbon dioxide is dehydrated by the second gas-liquid separator and then transported to the carbon dioxide purification unit.

[0009] The present invention is further configured such that: the carbon dioxide purification unit includes a second adsorption tower, a third buffer tank and a second vacuum pump; a second adsorbent is provided in the second adsorption tower, the second adsorbent adsorbs impurities in the crude carbon dioxide, and the separated high-purity carbon dioxide is stored in the third buffer tank; the second vacuum pump is used to evacuate the second adsorption tower, so that the impurities in the second adsorbent are desorbed, and the desorbed impurities are discharged from the second adsorption tower.

[0010] The present invention is further configured such that: the high-purity carbon dioxide in the third buffer tank is transported to the carbon dioxide storage unit, the carbon dioxide storage unit includes a storage tank, a fifth solenoid valve is provided between the third buffer tank and the storage tank, and the storage tank is provided with a third temperature sensor, a third pressure sensor, a second level gauge, a cooler, a heater, a safety valve and an audible and visual alarm device.

[0011] The present invention is further configured to include an intelligent control unit, which is used to control other units, and the intelligent control unit includes a PLC controller and a touch screen.

[0012] Compared with the prior art, the present invention has at least the following advantages: 1. The formic acid hydrogen production unit is connected to the catalytic cracking reactor via a pump. The reactor generates hydrogen-rich gas, which is then transported to a gas-liquid separation unit. The dried hydrogen-rich gas is then transported to the next unit. The carbon dioxide separation unit uses an adsorbent to separate hydrogen for collection, and the separated crude carbon dioxide is then transported to the next unit. The carbon dioxide collection unit integrates a multi-stage compressor unit to provide a stable pressure and low-impurity crude carbon dioxide gas source for the subsequent purification unit. The carbon dioxide purification unit also uses an adsorbent to separate high-purity carbon dioxide from impurities for collection. The carbon dioxide storage unit is used for low-temperature storage of purified carbon dioxide. This system innovatively integrates carbon dioxide recovery and utilization, achieving a clean production process with high formic acid conversion rate, high carbon dioxide purity, and high hydrogen purity. It is suitable for distributed energy and chemical carbon resource utilization scenarios.

[0013] 2. By setting up a heat exchange device, the formic acid feedstock exchanges heat with the generated hydrogen-rich gas before entering the catalytic cracking reactor. The formic acid feedstock is preheated by preheating recovery, which reduces heating energy consumption. Attached Figure Description

[0014] Figure 1 This is an overall schematic diagram of this embodiment; Figure 2 This is a schematic diagram of a formic acid hydrogen production unit; Figure 3 This is a schematic diagram of a carbon dioxide separation unit; Figure 4 This is a schematic diagram of a carbon dioxide collection unit; Figure 5 This is a schematic diagram of a carbon dioxide purification unit; Figure 6 This is a schematic diagram of a carbon dioxide storage unit. Detailed Implementation

[0015] To make the objectives, technical solutions, and advantages of the embodiments of this utility model clearer, the technical solutions of the embodiments of this utility model will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of this utility model, not all embodiments. The components of the embodiments of this utility model described and shown in the accompanying drawings can typically be arranged and designed in various different configurations.

[0016] In the description of this utility model, it should also be noted that, unless otherwise explicitly specified and limited, the terms "set," "install," "connect," and "link" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this utility model based on the specific circumstances.

[0017] A formic acid to hydrogen production and carbon dioxide recovery and purification system, such as Figure 1 As shown, it includes: a formic acid hydrogen production unit 1000, used to produce hydrogen-rich gas from formic acid raw material; a carbon dioxide separation unit 2000, used to separate crude carbon dioxide from the hydrogen-rich gas and purify hydrogen; a carbon dioxide collection unit 3000, used to collect the crude carbon dioxide and pressurize it; a carbon dioxide purification unit 4000, used to filter impurities from the crude carbon dioxide and purify carbon dioxide; and a carbon dioxide storage unit 5000, used to store the carbon dioxide purified by the carbon dioxide purification unit.

[0018] like Figure 2 As shown, the formic acid hydrogen production unit includes a transfer pump 1010, a catalytic cracking reactor 1050, a heating device 1100, a heat exchange device 1040, and a gas-liquid separator 1140. The transfer pump 1010 transports formic acid feedstock through the heat exchange device 1040 and then into the catalytic cracking reactor 1050. The heating device 1100 heats the catalytic cracking reactor 1050. The hydrogen-rich gas generated by the catalytic cracking reactor 1050 passes through the heat exchange device 1040, exchanges heat with the formic acid feedstock in the heat exchange device 1040, and then enters the gas-liquid separator 1140. The gas-liquid separator 1140 separates the moisture from the hydrogen-rich gas, forming dry hydrogen-rich gas, which then enters the carbon dioxide separation unit 2000. The separated moisture can be returned to the catalytic cracking reactor 1050 or discharged.

[0019] A flow meter 1020 and a solenoid valve 1030 are installed between the transfer pump 1010 and the heat exchange device 1040. A temperature sensor 1060, a pressure sensor 1090, and a level gauge 1080 are installed on the catalytic cracking reactor 1050. A liquid blocking device 1070 is installed between the catalytic cracking reactor 1050 and the heat exchange device 1040. A solenoid valve 1110 is installed between the heat exchange device 1040 and the gas-liquid separation device 1140. A solenoid valve 1160, an adsorption device 1170, a dew point meter 1180, and a flow meter 1190 are installed between the gas-liquid separation device 1140 and the carbon dioxide separation unit 2000. The adsorption device 1170 is used to adsorb impurities in hydrogen-rich gas.

[0020] Specifically, formic acid raw material is stored in a specific container. After the transfer pump 1010 is turned on, it will transport formic acid to the heat exchange device 1040 according to the set flow rate. During the transportation process, the flow meter 1020 will monitor the formic acid transportation flow rate in real time to ensure that the transportation volume is stable and meets the reaction requirements. At the same time, the solenoid valve 1030 can adjust or cut off the transportation of formic acid according to the control command to ensure system safety.

[0021] After formic acid is transported to heat exchanger 1040 and cooled by gas-liquid heat exchange with the gas from catalytic cracking reactor 1050, it enters catalytic cracking reactor 1050. The catalyst in the reactor accelerates the cracking reaction of formic acid; in this embodiment, a ruthenium-based catalyst is used. Temperature sensor 1060 and pressure sensor 1090 monitor the temperature and pressure inside the reactor in real time to ensure the reaction proceeds under suitable conditions. If the temperature, pressure, or liquid level exceeds the set range, an audible and visual alarm will sound, and the reaction conditions can be adjusted by controlling the flow rate of heating device 1100 and transfer pump 1010. After catalytic cracking, formic acid decomposes to produce a hydrogen-rich gas including hydrogen, carbon dioxide, and possibly a small amount of water vapor. The high-temperature hydrogen-rich gas from catalytic cracking reactor 1050 enters heat exchanger 1040 after passing through liquid-blocking device 1070. The function of heat exchanger 1040 is to lower the temperature of the mixed gas, making it easier for subsequent processing. Through heat exchange with the formic acid feedstock, the temperature of the hydrogen-rich gas will drop to a suitable range.

[0022] After being cooled by heat exchange, the hydrogen-rich gas enters the gas-liquid separator 1140. In the gas-liquid separator 1140, water vapor in the hydrogen-rich gas is separated into liquid water and stored in a tank. The level gauge 1180 monitors the liquid level of the reaction device in real time. When the liquid level in the reaction device is low, the liquid can be returned to the reaction device through the solenoid valve 1150. When the liquid level in the reaction device meets the requirements and the liquid level in the tank reaches a certain height, the liquid can be discharged through the solenoid valve 1150. After gas-liquid separation, relatively dry hydrogen-rich gas is obtained. The hydrogen-rich gas after gas-liquid separation then enters the adsorption device 1170. The adsorption device 1170 is filled with adsorbent, which is used to adsorb impurities in the hydrogen-rich gas, such as trace amounts of formic acid that may remain, and other impurity gases, thereby further improving the purity of the hydrogen. The gas treated by the adsorption device 1170 is then tested by the dew point meter 1180. The 1180 dew point meter can detect the moisture content in a gas to determine its dryness and purity, ensuring that the final hydrogen-rich gas produced meets the expected quality standards.

[0023] like Figure 3As shown, the carbon dioxide separation unit 2000 includes a first adsorption tower 2100, a first buffer tank 2060, and a first vacuum pump 2080. The first adsorption tower 2100 is provided with an adsorbent 2040, which adsorbs crude carbon dioxide from hydrogen-rich gas to separate hydrogen. The separated hydrogen is stored in the first buffer tank 2060. The first vacuum pump 2080 is used to evacuate the first adsorption tower 2100 to desorb the crude carbon dioxide in the adsorbent 2040. The desorbed crude carbon dioxide is then transported to the carbon dioxide collection unit 3000.

[0024] A solenoid valve 2010, a temperature sensor 2030, and a pressure sensor 2020 are connected to the first adsorption tower 2100. A flow meter 2050 and an online analyzer 2070 are installed between the first adsorption tower 2100 and the first buffer tank 2060. The online analyzer 2070 is used to detect the purity of hydrogen and the amount of impurities at the outlet of the first buffer tank 2060. A flow meter 2090 is installed between the first vacuum pump 2080 and the carbon dioxide collection unit 3000.

[0025] Specifically, during the adsorption preparation stage, the first adsorption tower 2100 is pre-filled with adsorbent 2040 (modified activated carbon). The entire system is checked to ensure normal operation. During the adsorption stage, hydrogen-rich gas from the formic acid hydrogen production unit 1000 enters the first adsorption tower 2100 through pipelines via solenoid valves 2010. During this process, pressure sensor 2020 monitors the pressure inside the tower in real time to ensure it is maintained within the adsorption pressure range; temperature sensor 2030 monitors the temperature inside the tower to avoid high temperatures affecting the performance of the adsorbent, typically requiring the temperature to be controlled at ≤50℃; flow meter 1190 measures the inlet flow rate to ensure a stable inlet flow rate; under high pressure, adsorbent 2040 preferentially adsorbs impurities such as carbon dioxide, carbon monoxide, and water vapor, while high-purity hydrogen flows out from the bottom of the tower, is metered by flow meter 2050, and then enters the first buffer tank 2060 for temporary storage; simultaneously, online analyzer 2070 detects the purity of the outlet hydrogen and the amount of residual impurities in real time. This online analyzer 2070 is a hydrogen concentration analyzer. Then, the first vacuum pump 2080 is started to reduce the pressure inside the first adsorption tower 2100 to near vacuum, so that the carbon dioxide and other impurities on the adsorbent 2040 are completely desorbed, and the desorbed crude carbon dioxide is transported to the carbon dioxide collection unit 3000.

[0026] In other embodiments, the first adsorption tower 2100 may consist of multiple adsorption towers. During the pressure equalization and reduction stage, when the adsorbent 2040 is close to saturation, the pressure equalization step is initiated. Under the real-time monitoring of the pressure sensor 2020, the high-pressure gas in the first adsorption tower 2100 is slowly released to other low-pressure adsorption towers via the control of the solenoid valve 2010 to recover hydrogen and balance the pressure. After pressure equalization is completed, the pressure inside the tower continues to decrease, causing the carbon dioxide and other impurities adsorbed on the adsorbent 2040 to begin desorption. During the desorption stage, the first vacuum pump 2080 is started. Under the real-time monitoring of the pressure sensor 2020, the pressure inside the first adsorption tower 2100 is further reduced to a set desorption pressure close to vacuum, allowing for more thorough desorption of carbon dioxide and other impurities on the adsorbent 2040. The desorbed gas is discharged from the first adsorption tower 2100. During this process, the flow meter 2050 monitors the discharge flow rate, and the solenoid valve 2010 ensures smooth impurity discharge according to control commands. During the pressure equalization and pressurization stage, after desorption is completed, under the monitoring of pressure sensor 2020 and controlled by solenoid valve 2010, gas from other high-pressure adsorption towers is first introduced into the current low-pressure adsorption tower for pressure equalization, so that the pressure of each tower is balanced and energy is recovered. Then, the gas is replenished to raise the pressure of the first adsorption tower 2100 to the set adsorption pressure, preparing for the next round of adsorption operation. Each adsorption tower performs adsorption, pressure equalization and depressurization, desorption, and pressure equalization and pressurization in a certain order, forming a continuous cycle process, thereby realizing the continuous purification of hydrogen and the separation of carbon dioxide and other impurities.

[0027] like Figure 4 As shown, the carbon dioxide collection unit 3000 includes a gas filtration device 3010, a second buffer tank 3020, a compressor 3060, a cooling device 3090, and a gas-liquid separator 3110. Crude carbon dioxide is filtered by the gas filtration device 3110 and then transported to the second buffer tank 3020. The crude carbon dioxide in the second buffer tank 3020 is pressurized by the compressor 3060 and then transported to the cooling device 3090. The crude carbon dioxide is cooled by the cooling device 3090 and then transported to the gas-liquid separator 3110. After the crude carbon dioxide is dehydrated by the gas-liquid separator 3110, it is transported to the carbon dioxide purification unit 4000.

[0028] Specifically, the carbon dioxide collection unit 3000 achieves efficient collection and pressurization through the coordinated operation of various devices: the crude carbon dioxide first passes through the gas filtration device 3010 to remove solid particles and liquid impurities, and then enters the second buffer tank 3020. The pressure is monitored and stabilized in real time by the pressure sensor 3050. When the pressure inside the tank is lower than the set lower limit, the system controls the compressor 3060 to accelerate, and when the pressure is higher than the upper limit, it decelerates, thus realizing automatic flow regulation. The second buffer tank 3020 is equipped with a solenoid valve 3030 at the top. When the pressure is over-pressurized, the system controls the pressure relief to the high-altitude vent pipe. The bottom is equipped with a drain solenoid valve 3040 to periodically discharge settled impurities. The gas from the outlet of the second buffer tank 3020 is pressurized to 1.5 MPa by the compressor 3060 after passing through a one-way valve. The pressure sensor 3080 and temperature sensor 3070 at the outlet synchronously monitor the pressure and temperature (controlled between 80-100℃). The pressurized gas is cooled to below 40℃ by the cooling device 3090, and the cooling intensity is adjusted by the temperature sensor 3100. After cooling, the gas enters the gas-liquid separator 3110 tangentially. Centrifugal force separates the liquid droplets from the gas, and the liquid water settles to the bottom of the device. The liquid level is monitored by the level gauge 3130. When the liquid level reaches 30%, the system controls the solenoid valve 3120 to open and drain the water into the sewage tank. The separated dry gas enters the carbon dioxide purification unit 4000 through the top outlet. The flow meter 3140 on the pipeline monitors the flow rate. Finally, the clean gas is metered by the flow meter 3140 and output, providing a stable pressure and low impurity gas source for the subsequent carbon dioxide purification unit 4000. The entire process is controlled by the system to achieve efficient and safe operation.

[0029] like Figure 5 As shown, the carbon dioxide purification unit 4000 includes a second adsorption tower 4010, a third buffer tank 4070, and a second vacuum pump 4090. The second adsorption tower 4010 is equipped with an adsorbent 4050, which adsorbs impurities in the crude carbon dioxide. The separated high-purity carbon dioxide is stored in the third buffer tank 4070. The second vacuum pump 4090 is used to evacuate the second adsorption tower 4010, so that the impurities in the adsorbent 4050 are desorbed, and the desorbed impurities are discharged from the second adsorption tower 4010.

[0030] Specifically, adsorbent 4050 is a zeolite molecular sieve. During the adsorption stage, crude carbon dioxide gas enters the second adsorption tower 4010 via a pipeline through solenoid valve group 4020. During this process, pressure sensor 4030 monitors the pressure inside the tower in real time to ensure it is maintained within the adsorption pressure range; temperature sensor 4040 monitors the temperature inside the tower to avoid high temperatures affecting the performance of adsorbent 4050, and the temperature usually needs to be controlled at ≤50℃; flow meter 3140 measures the inlet flow rate to ensure a stable inlet volume; under high pressure, adsorbent 4050 preferentially adsorbs impurities such as hydrogen, carbon monoxide, and water vapor. High-purity carbon dioxide flows out from the bottom of the tower, is metered by flow meter 4060, and then enters the third buffer tank 4070 for temporary storage; at the same time, online analyzer 4080 detects the purity of outlet carbon dioxide and the amount of impurities in real time. This online analyzer 4080 is a carbon dioxide concentration analyzer. Then, the second vacuum pump 4090 is started to reduce the pressure inside the second adsorption tower 4010 to near vacuum, so that the hydrogen and other impurities on the adsorbent 4050 are completely desorbed, and the desorbed gas is discharged through the pipeline.

[0031] In other embodiments, the second adsorption tower 4010 may consist of multiple adsorption towers. During the pressure equalization and reduction stage, when the adsorbent is close to saturation, the pressure equalization step is initiated. Under the real-time monitoring of the pressure sensor 4030, the high-pressure gas in the second adsorption tower 4010 is slowly released to other low-pressure adsorption towers through the control of the solenoid valve group 4020 to recover energy and balance the pressure. After the pressure equalization is completed, the pressure inside the tower continues to decrease, causing the hydrogen and other impurities adsorbed on the adsorbent 4050 to begin desorption. During the desorption stage, the second vacuum pump 4090 is started. Under the real-time monitoring of the pressure sensor 4030, the pressure inside the second adsorption tower 4010 is further reduced to a set desorption pressure close to vacuum, so that the hydrogen and other impurities on the adsorbent 4050 are more thoroughly desorbed. The desorbed impurity gas is discharged through a pipeline. During this period, the flow meter 4100 monitors the discharge flow rate, and the solenoid valve group 4020 ensures smooth impurity discharge according to control commands. During the pressure equalization and pressurization stage, after desorption, under the monitoring of pressure sensor 4030 and controlled by solenoid valve group 4020, gas from other high-pressure adsorption towers is first introduced into the current low-pressure adsorption tower for pressure equalization, so that the pressure of each tower is balanced and energy is recovered. Then, the gas is added to raise the pressure of the second adsorption tower 4010 to the set adsorption pressure, preparing for the next round of adsorption operation. Each adsorption tower performs adsorption, pressure equalization and depressurization, desorption, and pressure equalization and pressurization in a certain order, forming a continuous cycle process, thereby realizing the continuous purification of carbon dioxide and the separation of hydrogen and other impurities.

[0032] like Figure 6As shown, the high-purity carbon dioxide in the third buffer tank 4070 is transported to the carbon dioxide storage unit 5000. The carbon dioxide storage unit 5000 includes a storage tank 5020. A solenoid valve 5010 is installed between the third buffer tank 4070 and the storage tank 5020. The storage tank 5020 is equipped with a temperature sensor 5060, a pressure sensor 5070, a level gauge 5080, a cooler 5030, a heater 5040, a safety valve 5090, and an audible and visual alarm device 5050.

[0033] Specifically, the purified carbon dioxide enters the storage tank 5020 in the carbon dioxide storage unit 5000. The cooler 5030 continuously cools the storage unit to lower the internal temperature and keep the carbon dioxide in a low-temperature liquid state (usually maintained at -23°C to -30°C) to meet the temperature requirements for liquid carbon dioxide storage. The temperature sensor 5060 monitors the temperature inside the storage unit in real time and feeds the data back to the control system. If the temperature rises, the cooler intensifies the cooling. If the temperature is too low, the heater 5040 (electric heating belt) is activated to maintain the temperature within a reasonable range by heating, preventing the equipment from being damaged due to overcooling or abnormal internal material conditions.

[0034] Pressure sensor 5070 monitors the internal pressure of storage tank 5020 in real time to ensure it remains within a safe range. When the pressure rises abnormally, safety valve 5090 opens to release pressure and prevent overpressure hazards. Simultaneously, solenoid valve 5010 adjusts gas inlet and outlet and the opening and closing of related pipelines based on pressure and other control signals, assisting in pressure control and media delivery. Level gauge 5080 displays the carbon dioxide storage level in real time, preventing overfilling or underfilling and ensuring stable operation of the storage unit. If parameters such as temperature or pressure exceed set thresholds, audible and visual alarm device 5050 immediately sounds an alarm, alerting operators to handle the anomaly promptly and ensuring safe storage. The output flow of storage tank 5020 via solenoid valve 5100 is monitored in real time by flow meter 5110. Through the close cooperation of these devices, carbon dioxide storage unit 5000 can safely and stably store carbon dioxide under low-temperature conditions, meeting the storage requirements for liquid carbon dioxide.

[0035] like Figure 1 As shown, this embodiment also includes an intelligent control unit, which is used to control other units. The intelligent control unit includes a PLC controller and a touch screen, and human-machine interaction is realized through the touch screen.

[0036] Specifically, the PLC controller serves as the core control hub, collecting data, automatically controlling, and providing early warnings of anomalies for all electrical equipment in the system. In the formic acid hydrogen production unit 1000, the PLC controller collects data in real time from temperature and pressure sensors, adjusts the power of the electric heater and the speed of the circulating pump, and triggers audible and visual alarms and implements corresponding control measures when the temperature, pressure, or liquid level exceeds the threshold, ensuring the stable operation of hydrogen production.

[0037] In the carbon dioxide separation unit 2000, the PLC controller collects data in real time through pressure sensors, temperature sensors and online analyzers, and displays the adsorption tower status in real time on the touch screen. The PLC controller switches the adsorption tower status through the solenoid valve group according to the preset cycle. The vacuum pump automatically starts and stops during the desorption stage, and an alarm is triggered when the amount of impurities remaining exceeds the set value.

[0038] The carbon dioxide collection unit has a capacity of 3000. The PLC controller monitors the buffer tank pressure, compressor outlet temperature, and gas-liquid separator level in real time. The touch screen monitors and displays the real-time flow curve. The PLC controller adjusts the compressor speed according to the buffer tank pressure and controls the cooling water flow of the cooling device through the temperature sensor. When the buffer tank pressure exceeds the set safety value, the safety valve is activated to release air and flashes an alarm.

[0039] In the carbon dioxide purification unit, the PLC controller collects data in real time through pressure sensors, temperature sensors, and an online analyzer. The status of the adsorption tower is displayed on the touch screen in real time. Based on the pressure sensor signal of the adsorption tower, the PLC controller can automatically switch the solenoid valve group in the cycle of "adsorption → equalization and pressure reduction → desorption → equalization and pressure increase". The vacuum pump starts synchronously during the desorption stage. When the purity of carbon dioxide after purification is less than the target value or the pressure difference of the adsorption tower is greater than the set value, the touch screen will highlight the corresponding alarm prompt in red.

[0040] In the 5000 carbon dioxide storage unit, a PLC controller monitors temperature, pressure, and liquid level in real time. Based on the set temperature value, the program determines whether to activate the cooler and electric heating element. When the pressure exceeds the set value, the safety valve releases pressure and records the fault. The touchscreen integrates real-time data monitoring, parameter setting, alarm management, and safety interlock functions, supporting remote operation and fault early warning to ensure the safe and efficient operation of each unit. Through the collaboration of the PLC controller and the touchscreen, the intelligent control unit achieves closed-loop management of the entire process from data acquisition and automatic control to anomaly handling, ensuring the safe and efficient operation of each unit.

[0041] The above description is only a preferred embodiment of the present utility model and is not intended to limit the present utility model. Any modifications, equivalent substitutions, improvements, etc., made within the design concept of the present utility model should be included within the protection scope of the present utility model.

Claims

1. A formic acid-to-hydrogen carbon dioxide recovery and purification system, characterized in that, Including those connected in sequence: Formic acid hydrogen production unit, used to produce hydrogen-rich gas from formic acid feedstock; A carbon dioxide separation unit is used to separate crude carbon dioxide from the hydrogen-rich gas and purify the hydrogen. A carbon dioxide collection unit for collecting and pressurizing the crude carbon dioxide; A carbon dioxide purification unit is used to filter impurities from the crude carbon dioxide and purify the carbon dioxide. A carbon dioxide storage unit is used to store the carbon dioxide purified by the carbon dioxide purification unit.

2. The formic acid to hydrogen production and carbon dioxide recovery and purification system according to claim 1, characterized in that: The formic acid hydrogen production unit includes a delivery pump, a catalytic cracking reaction device, a heating device, a heat exchange device, and a first gas-liquid separation device. The delivery pump transports formic acid raw material through a heat exchange device and then into the catalytic cracking reaction device. The heating device is capable of heating the catalytic cracking reaction device; The hydrogen-rich gas generated by the catalytic cracking reactor passes through a heat exchanger and exchanges heat with the formic acid feedstock in the heat exchanger before entering the first gas-liquid separation device. The first gas-liquid separation device separates the moisture in the hydrogen-rich gas, forming a dry hydrogen-rich gas that then enters the carbon dioxide separation unit. The separated moisture can be returned to the catalytic cracking reactor or discharged.

3. The formic acid to hydrogen production and carbon dioxide recovery and purification system according to claim 2, characterized in that: A first flow meter and a first solenoid valve are provided between the delivery pump and the heat exchange device. A first temperature sensor, a first pressure sensor, and a first level gauge are provided on the catalytic cracking reaction device. A liquid blocking device is provided between the catalytic cracking reaction device and the heat exchange device. A second solenoid valve is provided between the heat exchange device and the first gas-liquid separation device. A third solenoid valve, an adsorption device, a dew point meter, and a second flow meter are provided between the first gas-liquid separation device and the carbon dioxide separation unit. The adsorption device is used to adsorb impurities in hydrogen-rich gas.

4. The formic acid to hydrogen production and carbon dioxide recovery and purification system according to claim 2, characterized in that: The carbon dioxide separation unit includes a first adsorption tower, a first buffer tank, and a first vacuum pump; The first adsorption tower is equipped with a first adsorbent, which adsorbs crude carbon dioxide in hydrogen-rich gas to separate hydrogen. The separated hydrogen is stored in the first buffer tank. The first vacuum pump is used to evacuate the first adsorption tower, so as to desorb the crude carbon dioxide in the first adsorbent, and the desorbed crude carbon dioxide is transported to the carbon dioxide collection unit.

5. The formic acid to hydrogen production and carbon dioxide recovery and purification system according to claim 4, characterized in that: The first adsorption tower is connected to a fourth solenoid valve, a second temperature sensor, and a second pressure sensor. A third flow meter and a first online analyzer are installed between the first adsorption tower and the first buffer tank. The first online analyzer is used to detect the purity of hydrogen and the amount of impurities at the outlet of the first buffer tank. A fourth flow meter is installed between the first vacuum pump and the carbon dioxide collection unit.

6. The formic acid to hydrogen production and carbon dioxide recovery and purification system according to claim 4, characterized in that: The carbon dioxide collection unit includes a gas filtration device, a second buffer tank, a compressor, a cooling device, and a second gas-liquid separator. The crude carbon dioxide is filtered by the gas filtration device and then transported to the second buffer tank. The crude carbon dioxide in the second buffer tank is pressurized by the compressor and then transported to the cooling device. The crude carbon dioxide is cooled by the cooling device and then transported to the second gas-liquid separator. The crude carbon dioxide is dehydrated by the second gas-liquid separator and then transported to the carbon dioxide purification unit.

7. The formic acid to hydrogen production and carbon dioxide recovery and purification system according to claim 6, characterized in that: The carbon dioxide purification unit includes a second adsorption tower, a third buffer tank, and a second vacuum pump. The second adsorption tower is equipped with a second adsorbent, which adsorbs impurities in the crude carbon dioxide, and the separated high-purity carbon dioxide is stored in the third buffer tank. The second vacuum pump is used to evacuate the second adsorption tower, so that the impurities in the second adsorbent are desorbed and the desorbed impurities are discharged from the second adsorption tower.

8. The formic acid to hydrogen production and carbon dioxide recovery and purification system according to claim 7, characterized in that: The high-purity carbon dioxide in the third buffer tank is transported to the carbon dioxide storage unit, which includes a storage tank. A fifth solenoid valve is provided between the third buffer tank and the storage tank. The storage tank is equipped with a third temperature sensor, a third pressure sensor, a second level gauge, a cooler, a heater, a safety valve, and an audible and visual alarm device.

9. The formic acid to hydrogen production and carbon dioxide recovery and purification system according to claim 1, characterized in that: It also includes an intelligent control unit, which is used to control the other units. The intelligent control unit includes a PLC controller and a touch screen.

Images