Process intensified reactor, gas treatment system and method

Abstract

The application discloses a process intensification reactor, a gas treatment system and a method. The process intensification reactor comprises a reactor shell, an inner partition plate, a process intensification unit and a pressure energy recovery unit; the inner partition plate divides the reactor shell into two cavities in upper and lower parts; the process intensification unit is the upper part of the shell, and the pressure energy recovery unit is located in the lower part of the shell; the process intensification unit comprises a gas inlet, a gas outlet, a liquid inlet, a liquid outlet, a liquid distributor, a rotor assembly and a rotor driving shaft; the pressure energy recovery unit comprises a liquid inlet, a liquid outlet, a power impeller and a rotating shaft; the rotor driving shaft of the process intensification unit and the transmission shaft of the pressure energy recovery unit are coaxially connected through the inner partition plate. The application can fully utilize the pressure energy of the fluid under pressure, provide a strong centrifugal field for the process intensification reaction unit, greatly intensify the gas-liquid two-phase mass transfer process and promote the gas absorption effect.

Description

Technical Field

[0001] This invention belongs to the field of process intensification technology, and relates to an energy-saving process intensification reactor, particularly an energy-saving process intensification reactor and gas treatment method for gas-liquid mass transfer enhancement. Background Technology

[0002] In petrochemical production and natural gas processing, there are many gas treatment processes under medium and high pressure conditions. These include processes in refining plants to remove acidic components such as hydrogen sulfide and carbon dioxide from catalytic / coking dry gas, circulating hydrogen, and low-grade hydrogenation gas; and desulfurization and decarbonization in natural gas purification. Currently, these processes commonly employ the mature amine absorption process, namely the "amine liquid absorption-amine liquid regeneration" complete technology. The absorbent is mainly an alkaline aqueous solution such as DEA, MEA, MDEA, and DEPA. A typical absorption and regeneration process flow is as follows: the feed gas enters the absorption tower from the bottom, and in the packing layer, it comes into counter-current contact with the solution remaining from the top of the tower. The acidic gases in the gas phase are absorbed by the absorbent. The absorbed tail gas exits from the top of the tower to the separator and is then discharged. The rich solution after absorbing the acidic gases enters the regeneration tower, while the lean solution, after passing through a cooler, enters the absorption tower from the top. The rich solution undergoes thermal regeneration in the regeneration tower, releasing the acidic gases, which are then discharged from the top of the regeneration tower. After cooling by a cooler, the acidic gases are discharged from the system.

[0003] Currently, the amine absorption and regeneration process generally suffers from the following problems. First, the absorption process typically employs tower-type equipment, i.e., packed / plate towers. Factors affecting the absorption efficiency mainly include mass transfer efficiency, absorbent concentration, absorbent volume, absorbent temperature, and the degree of foaming in the absorbent. Traditional absorption towers suffer from poor mass transfer, uneven gas-liquid flow, high resistance, easy clogging of the packing, and unstable operation. Furthermore, due to impurities such as light hydrocarbon droplets and rust entrained in the gas, the absorbent exhibits severe foaming, seriously affecting the long-term, safe, and stable operation of the desulfurization unit. Simultaneously, the low desulfurization efficiency of the absorption tower results in acidic component content in the rich solution being far below the equilibrium value. Therefore, to ensure treatment effectiveness, a large amount of amine is often used, leading to a high regeneration load and high energy consumption. Therefore, developing efficient absorption equipment and treatment processes that reduce solvent consumption, lower regeneration load and circulating system energy consumption while ensuring absorption and purification effects, and improve the foaming phenomenon in the solvent absorption system, is of great significance for improving the treatment effect and saving energy for such gases.

[0004] Patent CN112159695A discloses an energy-saving natural gas MDEA decarbonization system and method. By pressurizing the desorbed gas output from the top of the regeneration tower, the heat grade is improved and used to heat the amine-rich liquid entering the regeneration tower, so that the low-grade heat can be reasonably recovered and utilized. At the same time, the desorbed gas is cooled and separated, and the liquid is returned to the regeneration tower. There is no need to set up an additional regeneration tower top cooler, thereby reducing the amount of refrigerant used and reducing energy consumption. However, this technology requires the addition of desorbed gas compressor equipment, which increases power consumption. In addition, the absorption-regeneration process uses tower equipment, which still has problems such as low mass transfer efficiency, low absorbent concentration, large absorbent volume, and easy foaming of absorbent.

[0005] As a highly efficient process intensification device, the centrifugal reactor enhances mass transfer through centrifugal force, achieving orders-of-magnitude improvements in efficiency compared to traditional methods. It boasts advantages such as high efficiency, small size, ease of operation, and convenient maintenance. Currently, centrifugal technology has been applied in engineering fields such as selective H2S removal, flue gas desulfurization and dust removal, nanoparticle preparation, extraction, and distillation. In amine absorption systems, this technology not only provides highly efficient purification but also eliminates amine foaming, increasing the concentration of amine solution and reducing the amine circulation volume. This significantly reduces the amine regeneration load and the energy consumption of the circulation system. However, the centrifugal reactor bed (rotor) requires a motor for power, increasing energy consumption.

[0006] Patent CN105385479A discloses a supergravity desulfurization and decarbonization device that integrates hydrate and membrane methods. It combines hydrate and membrane methods and introduces supergravity technology to desulfurize and deacidify gases from industrial flue gas and oilfield extraction gas processes. By combining hydrate and membrane separation methods and introducing supergravity technology, it performs deep desulfurization and deacidification of natural gas, significantly improving the removal rate of acidic gases such as H2S and CO2 in natural gas. The upper part of the device is a supergravity membrane separation unit, and the lower part is a stirred hydrate reaction vessel. The overall structure is complex, and the rotating parts of the supergravity steering mechanism and the magnetic stirring of the stirred hydrate reaction vessel both require electric motors to drive, increasing power consumption. Summary of the Invention

[0007] To address the shortcomings of existing technologies, this invention provides a process intensification reactor, a gas treatment system, and a method. By using a process intensification device to recover system energy for enhancing the gas-liquid process, the gas absorption and purification effect is improved while reducing the amount of absorption solvent used, lowering the regeneration load and energy consumption of the circulation system. This ensures long-term, safe, and stable operation of the device, achieving efficient and low-cost gas purification treatment.

[0008] To achieve the above objectives, the first aspect of the present invention provides an energy-saving process intensification reactor.

[0009] The energy-saving process enhancement reactor includes a reactor shell, an internal partition plate, a process enhancement unit, and a pressure energy recovery unit;

[0010] The internal partition plate is basically horizontally arranged inside the reactor shell, dividing the reactor shell into upper and lower cavities; the process enhancement unit is located in the upper part of the shell, and the pressure energy recovery unit is located in the lower part of the shell.

[0011] The process enhancement unit includes an air inlet, an exhaust outlet, a liquid inlet, a liquid outlet, a liquid distributor, a rotor assembly, and a rotor drive shaft;

[0012] The pressure energy recovery unit includes an inlet, an outlet, a power impeller, and a rotating shaft; the rotor drive shaft of the process enhancement unit and the transmission shaft of the pressure energy recovery unit are coaxially connected through an internal partition plate.

[0013] Furthermore, in the above-mentioned process intensification reactor, the rotor structure of the rotor assembly can be a packing type, a disc type, a spiral type, a baffle type, or a combination type, and the rotor assembly is mounted on the rotor drive shaft.

[0014] Furthermore, in the aforementioned process intensification reactor, the liquid distributor inlet is connected to the liquid inlet of the process intensification unit, and the liquid distributor is located at the center of the rotor.

[0015] Furthermore, in the aforementioned process enhancement reactor, the air inlet of the process enhancement unit is located in the middle of the outer shell, with the inlet center radially horizontal to the rotor assembly; the air outlet of the process enhancement unit is located in the upper part of the outer shell; the liquid inlet of the process enhancement unit is located in the upper part of the outer shell; and the liquid outlet of the process enhancement unit is located in the lower part of the process enhancement unit shell, specifically below the rotor assembly.

[0016] Furthermore, in the above-mentioned process-enhanced reactor, the power impeller of the pressure energy recovery unit can be a single-stage or multi-stage impeller, and the power impellers are evenly arranged and mounted on the drive shaft along the circumference.

[0017] Furthermore, in the above-mentioned process intensification reactor, the inlet of the pressure energy recovery unit is located on the side of the outer shell, and the center of the inlet is radially horizontal with the power impeller assembly; the outlet of the pressure energy recovery unit is located at the lower part or bottom of the outer shell.

[0018] Furthermore, in the above-mentioned process intensification reactor, the rotor assembly rotates following the rotor drive shaft, which in turn rotates following the rotating shaft, which is driven by a power impeller. The gas-liquid process is intensified by utilizing the strong centrifugal force field generated by the rotor rotation.

[0019] Furthermore, in the process-enhanced reactor described above, sealing components are installed between the rotor assembly and the reactor shell, and between the rotating shaft and the internal partition plate, to ensure that there is no leakage in the respective areas.

[0020] Furthermore, in the above-mentioned process intensification reactor, the discharge port of the process intensification unit is connected to the inlet of the pressure energy recovery unit.

[0021] The process enhancement reactor of this invention is suitable for gas purification treatment such as gas desulfurization, gas decarbonization, natural gas absorption and dehydration, circulating hydrogen desulfurization, and selective hydrogen sulfide removal under certain pressure conditions. It can also be used for gas-liquid process enhancement treatment under other pressurized conditions, and is especially suitable for gas treatment fields with absorption-regeneration processes under certain pressure drop conditions.

[0022] A second aspect of the invention provides a gas processing system in which the aforementioned process enhancement reactor is used.

[0023] A gas processing system comprising a process intensification reactor, a flash tank, a lean and rich liquor heat exchanger, a regeneration tower, a lean liquor pump, a lean liquor cooler, and a filtration system;

[0024] The gas inlet of the process enhancement reactor is connected to the feed gas pipeline, the gas outlet of the process enhancement reactor is connected to the exhaust gas pipeline, the liquid inlet of the process enhancement reactor is connected to the filter outlet, and the liquid outlet of the process enhancement reactor is connected to the liquid inlet of the flash tank; the liquid outlet of the flash tank is connected to the liquid inlet of the regeneration tower via a lean-rich liquid heat exchanger; the gas phase outlet of the regeneration tower is connected to the regeneration gas pipeline, and the liquid phase outlet of the regeneration tower is connected to the lean liquid cooler inlet after passing through a lean liquid pump and a lean-rich liquid heat exchanger; the outlet of the lean liquid cooler is connected to the filtration system inlet.

[0025] Furthermore, the liquid-liquid heat exchanger is a liquid-liquid heat exchanger, and the type of heat exchanger is not limited.

[0026] Furthermore, the regeneration tower is equipped with a condenser at the top and a reboiler at the bottom.

[0027] Furthermore, the process intensification reactor has the structure described above.

[0028] Furthermore, the drain outlet of the process enhancement unit is divided into two paths: the first path is connected to the liquid inlet of the pressure energy recovery unit, and the second path is connected to the liquid inlet of the flash tank.

[0029] A third aspect of the invention provides a gas processing method in which the system described above is applied.

[0030] A gas treatment method includes the following steps:

[0031] (1) The gas to be treated first enters the process enhancement unit of the process enhancement reactor through the gas inlet, and the lean absorbent enters the process enhancement unit through the liquid inlet; the gas contacts the lean absorbent from the liquid distributor in the rotor assembly area, and the gas-liquid two-phase mass transfer enhancement process is carried out and the gas is absorbed. The treated gas is discharged from the reactor, and the lean absorbent that has absorbed the components to be treated becomes the rich absorbent and is discharged from the liquid outlet of the process enhancement unit.

[0032] (2) The rich absorbent discharged in step (1) is divided into two paths: the first path enters the pressure energy recovery unit of the reactor, where the pressure energy of the rich absorbent is converted into kinetic energy, which is used to drive the impeller to rotate through the pressurized liquid impact, thereby driving the coaxially mounted rotor assembly to rotate. The depressurized fluid enters the flash tank through the discharge port of the pressure energy recovery unit; the second path of rich absorbent directly enters the flash tank.

[0033] (3) After the dissolved hydrocarbons in the rich absorbent entering the flash tank in step (2) are flashed, the rich absorbent is heated by the rich-lean heat exchanger and enters the regeneration tower. In the regeneration tower, the rich absorbent is heated and decomposed to release the absorbed components and become the lean absorbent, thus completing the regeneration of the absorbent. The high-concentration component gas released by the regeneration is then processed. The regenerated lean absorbent is pressurized by the lean pump, cooled by the rich-lean heat exchanger, cooled by the lean cooler, and filtered by the filtration system before being returned to the process enhancement reactor for recycling.

[0034] Furthermore, the gas to be treated in step (1) can be natural gas, liquefied gas, dry gas, low-fraction gas or recycled hydrogen for the purpose of removing acidic components such as H2S and CO2, or natural gas or other gases for the purpose of removing moisture. The components to be treated are H2S, CO2 and H2O respectively.

[0035] Furthermore, the operating pressure of the process enhancement reactor in step (1) is 0.5~20MPa, and the operating temperature can be determined according to the specific treatment system.

[0036] Furthermore, the rotational speed of the rotor assembly in step (1) is 50 to 5000 rpm, preferably 200 to 2000 rpm.

[0037] Furthermore, the discharged rich absorbent in step (2) is divided into two streams. The first stream accounts for 20% to 100% of the total rich absorbent, and the second stream accounts for 0% to 80% of the total rich absorbent. The rotational speed of the rotor assembly can be controlled by adjusting the flow rates of the two streams.

[0038] Furthermore, the operating pressure of the regeneration tower in step (3) is 0.1~15MPa, which is lower than the operating pressure of the process enhancement reactor, and the operating pressure difference is 0.4MPa~20MPa. The operating temperature can be determined and adjusted according to the specific treatment system.

[0039] The gas treatment method of the present invention can be used in the field of absorption-regeneration gas treatment under certain pressure drop conditions, such as gas desulfurization, gas decarbonization, natural gas absorption dehydration, circulating hydrogen desulfurization, and selective hydrogen sulfide desulfurization, for example, amine desulfurization, amine decarbonization, MDEA selective hydrogen sulfide desulfurization, and natural gas glycol dehydration.

[0040] Compared with the prior art, the present invention has the following beneficial effects:

[0041] 1. Compared with existing hypergravity devices, this invention can make full use of the pressure energy of pressurized fluids. By impacting the power impeller with pressurized liquid and driving the impeller to rotate, the coaxially mounted rotor assembly is driven to rotate, providing a strong centrifugal field for the process intensification reaction unit, greatly enhancing the gas-liquid two-phase mass transfer process and promoting the gas absorption effect.

[0042] 2. Compared with existing tower equipment, the reactor of this invention greatly enhances the mass transfer process, significantly reducing equipment size and floor space, saving on infrastructure and equipment investment. It also offers advantages such as convenient maintenance and easy start-up and shutdown. While ensuring efficient gas treatment, the process-enhanced reactor of this invention also eliminates foaming in the absorbent treatment system, increasing the absorbent concentration to a certain extent. For example, the amine concentration used in amine desulfurization can be increased from the conventional 30% to 50%, thereby reducing the amine circulation volume and significantly lowering the amine regeneration load and energy consumption of the circulation system.

[0043] 3. Before depressurizing and regenerating the pressurized rich absorbent, the present invention fully recovers its pressure energy and uses it as the energy to drive the rotor assembly, thereby enhancing the absorption process. It not only utilizes the advantages of the hypergravity equipment to solve the problems of traditional tower equipment, but also uses the system pressure energy to solve the motor energy consumption problem of the hypergravity reactor, thus achieving gas treatment efficiently and at low cost. Attached Figure Description

[0044] Figure 1 This is a schematic diagram of an energy-saving process enhancement reactor according to the present invention.

[0045] In the figure, 1-reactor shell, 2-internal partition plate, 3-process enhancement unit, 4-pressure energy recovery unit, 5-air inlet, 6-exhaust port, 7-process enhancement unit liquid inlet, 8-process enhancement unit liquid outlet, 9-liquid distributor, 10-rotor assembly, 11-rotor drive shaft, 12-pressure energy recovery unit liquid inlet, 13-pressure energy recovery unit liquid outlet, 14-power impeller, 15-rotating shaft, 16-sealing component.

[0046] Figure 2 This is a schematic diagram of a gas processing system according to the present invention.

[0047] In the diagram, 51-raw material gas pipeline, 52-process enhancement reactor, 53-exhaust gas pipeline, 54-filter, 55-flash tank, 56-rich absorbent pipeline, 57-lean and rich liquid heat exchanger, 58-regeneration tower, 59-regeneration gas pipeline, 60-lean liquid pump, 61-lean absorbent pipeline, 62-lean liquid cooler, 63-first drain pipeline of process enhancement unit, 64-second drain pipeline of process enhancement unit, 65-flash vapor pipeline. Implementation

[0048] The following detailed description of a process enhancement reactor, gas treatment system, and method according to the present invention, in conjunction with the accompanying drawings and embodiments, does not limit the scope of the invention. Example 1

[0049] This embodiment provides a detailed description of a process intensification reactor according to the present invention. For example... Figure 1 As shown, the structure of a process enhancement reactor according to the present invention is as follows:

[0050] The energy-saving process enhancement reactor includes a reactor shell 1, an internal partition plate 2, a process enhancement unit 3, and a pressure energy recovery unit 4. The internal partition plate 2 is disposed inside the reactor shell 1, dividing the reactor shell 1 into upper and lower cavities for the process enhancement unit 3 and the pressure energy recovery unit 4. The process enhancement unit 3 includes an air inlet 5, an exhaust outlet 6, a liquid inlet 7, a liquid outlet 8, a liquid distributor 9, a rotor assembly 10, and a rotor drive shaft 11. The pressure energy recovery unit 4 includes a liquid inlet 12, a liquid outlet 13, a power impeller 14, and a rotating shaft 15. The rotor drive shaft 11 of the process enhancement unit 3 and the drive shaft 15 of the pressure energy recovery unit 4 are coaxially connected through the internal partition plate 2. The rotor assembly 10 is mounted on the rotor drive shaft 11. The inlet of the liquid distributor 9 is connected to the liquid inlet 7 of the process enhancement unit, and the liquid distributor 9 is located at the center of the rotor 10. The air inlet 5 of the process enhancement unit 3 is located in the middle of the outer shell, with the inlet center radially horizontal to the rotor assembly 10; the air outlet 6 of the process enhancement unit 3 is located on the upper part of the outer shell; the liquid inlet 7 of the process enhancement unit 3 is located on the upper part of the outer shell, and the liquid outlet 8 of the process enhancement unit 3 is located on the lower part of the process enhancement unit shell; the power impeller 14 is evenly arranged and mounted on the drive shaft 15 along the circumference; the liquid inlet 12 of the pressure energy recovery unit 4 is located on the side of the outer shell, with the inlet center radially horizontal to the power impeller assembly 14; the liquid outlet 13 of the pressure energy recovery unit 4 is located on the lower part or bottom of the outer shell; in the above process enhancement reactor, sealing components are provided between the rotor assembly 10 and the reactor shell 1, and between the rotating shaft 15 and the internal partition plate 2 to ensure no leakage in the respective areas; the liquid outlet 8 of the process enhancement unit 3 is connected to the liquid inlet 12 of the pressure energy recovery unit 4. When the above-mentioned process enhancement reactor is working, the rotor assembly 10 rotates with the rotor drive shaft 11, the rotor drive shaft 11 rotates with the rotating shaft 15, and the rotating shaft 15 is driven by the power impeller 14. The gas-liquid process is enhanced by the strong centrifugal force field generated by the rotor rotation. Example 2

[0051] This embodiment describes in detail a gas processing system of the present invention.

[0052] like Figure 2As shown, the present invention provides a gas processing system comprising the aforementioned process intensification reactor. The system includes a process intensification reactor 52, a flash tank 55, a lean-rich liquor heat exchanger 57, a regeneration tower 58, a lean liquor pump 60, a lean liquor cooler 62, and a filtration system 54. The gas inlet of the process intensification reactor 52 is connected to the feed gas pipeline 51, the gas outlet of the process intensification reactor 52 is connected to the exhaust gas pipeline 53, the liquid inlet of the process intensification reactor 52 is connected to the outlet of the filter 54, and the liquid outlet of the process intensification reactor 52 is connected to the liquid inlet of the flash tank 55. The outlet of the liquid phase is connected to the liquid inlet of the regeneration tower 58 via the lean-rich liquid heat exchanger 57; the gas phase outlet of the regeneration tower 58 is connected to the regeneration gas pipeline 59; the liquid phase outlet of the regeneration tower 58 is connected to the inlet of the lean liquid cooler 62 after passing through the lean liquid pump 60 and the lean-rich liquid heat exchanger 57; the outlet of the lean liquid cooler 62 is connected to the inlet of the filtration system 54; the discharge port of the process enhancement unit 3 is divided into two paths, the first path 63 is connected to the liquid inlet of the pressure energy recovery unit 4, and the second path 64 is connected to the liquid inlet of the flash tank 55. Example 3

[0053] This embodiment provides a detailed description of the gas treatment method of the present invention. (In conjunction with...) Figure 1-2 The working process of the gas treatment system and method provided by the present invention is as follows:

[0054] The gas to be treated first enters the process enhancement unit 3 of the process enhancement reactor 52 through the air inlet 51, and the lean absorbent enters the process enhancement unit 3 through the liquid inlet 7. The gas contacts the lean absorbent from the liquid distributor 9 in the rotor assembly 10 area, and a gas-liquid two-phase mass transfer enhancement process is carried out and gas absorption is performed. The treated gas is discharged from the reactor 52, and the lean absorbent that has absorbed the components to be treated becomes a rich absorbent and is discharged from the liquid outlet 8 of the process enhancement unit 3. The discharged rich absorbent is divided into two paths: the first path 63 enters the pressure energy recovery unit 4 of the reactor, where the pressure energy of the rich absorbent is converted into kinetic energy, which impacts the power impeller 14 through the pressurized liquid and drives the impeller to rotate, thereby driving the process. The coaxially mounted rotor assembly 10 rotates, and the depressurized fluid enters the flash tank 55 through the drain port 13 of the pressure energy recovery unit 4. The second rich absorbent 64 directly enters the flash tank 55. After the rich absorbent enters the flash tank 55 and dissolves hydrocarbons, it is heated by the lean-rich liquid heat exchanger 57 and enters the regeneration tower 58. In the regeneration tower, the rich absorbent is heated and decomposed to release the absorbed components, becoming lean absorbent, thus completing the absorbent regeneration. The high-concentration component gas 59 released during regeneration is further processed. The regenerated lean absorbent is pressurized by the lean liquid pump 60, cooled by the lean-rich liquid heat exchanger 57, cooled by the lean liquid cooler 62, and filtered by the filtration system 54 before being returned to the process enhancement reactor 52 for recycling. Example 4

[0055] This embodiment provides a specific application example of a gas processing system according to the present invention.

[0056] use Figure 1 The process intensification reactor shown is selected. Figure 2 The gas treatment system shown desulfurizes circulating hydrogen from a hydrocracking unit in a petrochemical enterprise. The H2S concentration in the circulating hydrogen is approximately 0.2% (V). The desulfurizing agent selected is N-methyldiethanolamine (MDEA) with a mass concentration of 50% (w). The absorption pressure is 13 MPa, the absorption temperature is 45℃, the regeneration pressure is 2 MPa, and the regeneration temperature is 130℃. The sulfur-containing circulating hydrogen first enters the process enhancement unit 3 of the process enhancement reactor 52, where it contacts the lean methyldiethanolamine in the rotor assembly 10 area to enhance the gas-liquid two-phase mass transfer process and absorb H2S gas. The purified gas is discharged from the reactor 52, and the lean absorbent liquid that has absorbed the H2S component becomes a rich absorbent liquid. It then enters the pressure energy recovery unit 4 of the reactor from the process enhancement unit 3. The pressure of the rich absorbent liquid is reduced from 13 MPa to approximately 2.5 MPa, and the pressure energy is converted into kinetic energy. This kinetic energy is then used to drive the pressurized liquid impeller 14. The rotor assembly 10 mounted on the shaft rotates, adjusting the flow rate of the high-pressure rich absorbent into the pressure energy recovery unit, and controlling the rotor assembly speed to be around 600 rpm. This ensures that the H2S concentration in the recycled hydrogen after treatment is less than 10 mg / m3. After being depressurized to 2.5 MPa, the rich absorbent enters the flash tank 55, where dissolved hydrocarbons are flashed out. After passing through the lean-rich liquid heat exchanger 57, it is heated and enters the regeneration tower 58. In the regeneration tower, the rich absorbent is heated and decomposed to release the absorbed H2S gas, becoming a lean absorbent. This completes the regeneration of the absorbent and allows it to be recycled.

[0057] Comparative Example 1

[0058] Similar to Example 1, the difference is that the circulating hydrogen desulfurization equipment uses a traditional tower-type equipment. The entire gas-liquid contact process of the traditional tower is carried out under constant gravity. Due to the limitation of gravity, the gas-liquid contact flow is slow and the mass transfer coefficient is not high, resulting in a low mass transfer rate. The content of acidic components in the rich liquid is far lower than the equilibrium value. Therefore, it is necessary to increase the amount of absorbent. In order to avoid severe foaming of the absorbent, the amine concentration is generally controlled at about 30%. Compared with Example 1, when achieving the same treatment effect, the amount of amine used and the regeneration energy consumption of this comparative example increase by more than 45%.

[0059] Comparative Example 2

[0060] Similar to Example 1, the difference is that the circulating hydrogen desulfurization equipment uses conventional hypergravity equipment. The drive of the conventional hypergravity reactor bed (rotor) requires a motor to provide power. Under the same operating conditions as Example 1, the hypergravity equipment needs to be equipped with at least a 20 KW motor, which increases the operating energy consumption of the system. In Example 1, the motor energy consumption problem of the hypergravity reactor was solved by utilizing the system pressure energy, and gas treatment was achieved efficiently and at low cost.

Claims

1. An energy efficient process intensified reactor characterized in that, The reactor shell, the internal partition plate, the process intensification unit and the pressure energy recovery unit are included. The internal partition plate is horizontally arranged in the reactor shell to divide the reactor shell into two parts, the process intensification unit is the upper part of the shell, and the pressure energy recovery unit is located in the lower part of the shell. The process intensification unit includes an air inlet, an air outlet, a liquid inlet, a liquid outlet, a liquid distributor, a rotor assembly and a rotor drive shaft. The pressure energy recovery unit includes a liquid inlet, a liquid outlet, a power impeller and a rotating shaft. The rotor drive shaft of the process intensification unit and the transmission shaft of the pressure energy recovery unit are coaxially connected through the internal partition plate. The liquid inlet of the pressure energy recovery unit is arranged on the side of the outer shell, and the inlet center is radially horizontal to the power impeller assembly.

2. The reactor of claim 1, wherein, The liquid outlet of the process intensification unit is connected to the liquid inlet of the pressure energy recovery unit.

3. The reactor of claim 1, wherein, The rotor structure of the rotor assembly is a filler type, a disc type, a spiral type, a baffle type or a composite type, and the rotor assembly is installed on the rotor drive shaft.

4. The reactor of claim 1, wherein, The air inlet of the process intensification unit is arranged at the middle position of the outer shell, and the inlet center is radially horizontal to the rotor assembly.

5. A gas treatment system characterized by, The power impeller is uniformly arranged and installed on the transmission shaft along the circumference. The system includes the process intensification reactor, a flash tank, a lean- rich liquid heat exchanger, a regeneration tower, a lean liquid pump, a lean liquid cooler and a filtration system. The gas inlet of the process intensification reactor is connected to the raw gas pipeline, the gas outlet of the process intensification reactor is connected to the exhaust gas pipeline, the liquid inlet of the process intensification reactor is connected to the outlet of the filter, and the liquid outlet of the process intensification reactor is connected to the liquid inlet of the flash tank. The liquid outlet of the flash tank is connected to the liquid inlet of the regeneration tower through the lean- rich liquid heat exchanger. The gas phase outlet of the regeneration tower is connected to the regeneration gas pipeline, and the liquid phase outlet of the regeneration tower is connected to the inlet of the lean liquid cooler after passing through the lean liquid pump and the lean- rich liquid heat exchanger.

6. The gas treatment system of claim 5, wherein, The outlet of the lean liquid cooler is connected to the inlet of the filtration system.

7. The gas treatment system of claim 5, wherein, The lean- rich liquid heat exchanger is a liquid- liquid heat exchanger.

8. The gas treatment system of claim 5, wherein, The regeneration tower is provided with a condenser at the top and a reboiler at the bottom.

9. A method of gas treatment, characterized by The liquid outlet of the process intensification unit is divided into two paths, the first path is connected to the liquid inlet of the pressure energy recovery unit, and the second path is connected to the liquid inlet of the flash tank.

10. The gas treatment method according to claim 9, wherein The gas treatment system is applied. The steps include: (1) The gas to be treated first enters the process intensification unit of the process intensification reactor through the air inlet, and the lean absorption liquid enters the process intensification unit through the liquid inlet; the gas contacts the lean absorption liquid from the liquid distributor in the rotor assembly area to perform the gas- liquid two-phase mass transfer intensification process and gas absorption, the treated gas is discharged from the reactor, and the lean absorption liquid containing the treated components becomes the rich absorption liquid which is discharged from the liquid outlet of the process intensification unit. (2) The rich absorption liquid discharged in step (1) is divided into two routes: the first route enters the pressure energy recovery unit of the reactor, and the pressure energy possessed by the rich absorption liquid is converted into kinetic energy, which drives the power impeller to rotate by impacting the impeller with the liquid under pressure, thereby driving the rotor assembly installed coaxially to rotate, and the fluid after pressure relief enters the flash tank through the discharge port of the pressure energy recovery unit; the second route of the rich absorption liquid directly enters the flash tank; (3) The rich absorption liquid entering the flash tank in step (2) is flashed to dissolve hydrocarbons, then is heated by the lean-rich liquid heat exchanger to enter the regeneration tower, in which the rich absorption liquid is heated and decomposed to release the absorbed components to become lean absorption liquid, completing the regeneration of the absorption liquid, the high-concentration component gas released by the regeneration is treated subsequently, and the lean absorption liquid after regeneration is pressurized by a lean liquid pump, cooled by a lean liquid cooler, filtered by a filtering system, and then returned to the process intensification reactor for recycling.

11. The gas treatment method according to claim 10, wherein The gas to be treated is natural gas, liquefied gas, dry gas, low-pressure gas, or recycled hydrogen for the purpose of removing H2S and CO2, or natural gas for the purpose of removing water, and the component to be treated is H2S, CO2, or H2O.

12. The gas treatment method according to claim 10, wherein The operating pressure of the process intensification reactor in step (1) is 0.5-20 MPa.

13. The gas treatment method according to claim 10, wherein The first route of the rich absorption liquid in step (2) accounts for 20%-100% of the total amount of the rich absorption liquid, and the second route of the rich absorption liquid accounts for 0%-80% of the total amount of the rich absorption liquid.

14. The gas treatment method according to claim 10, wherein The operating pressure of the regeneration tower in step (3) is 0.1-15 MPa.

15. The gas treatment method according to claim 10, wherein The operating pressure of the regeneration tower is 0.1-15 MPa.

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