Process enhanced reactor and gas treatment system and method

Abstract

The invention discloses a process enhanced reactor, a gas treatment system and a gas treatment method. The process strengthening reactor comprises a reactor shell, an inner partition plate, a process strengthening unit and a pressure energy recovery unit; the inner partition plate divides the reactor shell into an upper cavity and a lower cavity; the process strengthening unit is the upper part of the shell, and the pressure energy recovery unit is located at the lower part of the shell; the process strengthening 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; a rotor driving shaft of the process strengthening unit and a transmission shaft of the pressure energy recovery unit penetrate through the inner partition plate to be coaxially connected. According to the invention, the pressure energy of the pressurized fluid can be fully utilized, a strong centrifugal field is provided for the process strengthening reaction unit, the gas-liquid two-phase mass transfer process is greatly strengthened, and the gas absorption effect is promoted.

Description

Technical Field

[0001] The present invention belongs to the technical field of process intensification, and relates to an energy-saving process intensification reactor, in particular to an energy-saving process intensification reactor for gas-liquid mass transfer intensification and a gas treatment method. Background Art

[0002] In the process of petrochemical production and natural gas processing, there are many gas treatments under medium and high pressure conditions, such as the removal of acidic components such as hydrogen sulfide and carbon dioxide from catalytic / coking dry gas, circulating hydrogen, hydrogenation low-fraction gas and other logistics in refining enterprises, and the desulfurization and decarbonization treatment in natural gas purification. At present, the above processes generally adopt the mature alcohol amine absorption process, that is, the "amine liquid absorption-amine liquid regeneration" complete set of technology, and the absorbent is mainly alkaline aqueous solution such as DEA, MEA, MDEA, DEPA, etc. The typical absorption and regeneration process is that the raw gas enters the absorption tower from the bottom of the absorption tower, and contacts with the solution left from the top of the tower in the packing layer in reverse, the acid gas in the gas phase is absorbed by the absorbent, and the tail gas after absorption is discharged from the top of the tower to the separator, and the rich liquid after absorbing the acid gas enters the regeneration tower, and the lean liquid enters the absorption tower from the top of the absorption tower after passing through the cooler. The rich liquid is thermally regenerated in the regeneration tower, releasing the acid gas, and is discharged from the top of the regeneration tower. After cooling by the cooler, the acid gas is discharged from the system.

[0003] At present, the following problems are common in the amine liquid absorption and regeneration process. First of all, the above absorption process generally adopts tower equipment, that is, it is carried out in a packed tower / plate tower. The factors affecting the absorption effect mainly include: mass transfer efficiency, absorption liquid concentration, absorption liquid volume, absorption liquid temperature and absorption liquid foaming degree. Traditional absorption towers have disadvantages such as poor mass transfer effect, uneven gas-liquid flow, high resistance, easy plugging of fillers and unstable operation. In addition, due to impurities such as light hydrocarbon droplets and rust entrained in the gas, the absorption liquid will have serious foaming phenomena, which seriously affects the long-term, safe and stable operation of the desulfurization device. At the same time, due to the low desulfurization efficiency of the absorption tower, the content of acidic components in the rich liquid is far lower than the equilibrium value. Therefore, in order to ensure the treatment effect, the amount of amine liquid is often large, the regeneration load is large, and the energy consumption is high. Therefore, the development of high-efficiency absorption equipment and treatment processes, while ensuring the absorption and purification effect, reduces the amount of solvent, reduces the regeneration load and the energy consumption of the circulation system, and improves the foaming phenomenon of the solvent absorption system, is of great significance for improving the treatment effect of such gases and saving energy and reducing consumption.

[0004] Patent CN112159695A discloses an energy-saving natural gas MDEA decarbonization system and method, which improves the thermal grade of the analytical gas output from the top of the regeneration tower by pressurizing the analytical gas output from the top of the regeneration tower, and uses it to heat the rich amine liquid entering the regeneration tower, so that the low-grade heat is reasonably recycled and utilized. At the same time, the analytical gas is cooled and then separated into gases, and the liquid returns to the regeneration tower. There is no need to set up an additional regeneration tower top cooler, thereby reducing the amount of refrigerant and reducing energy consumption. However, this technology requires the addition of analytical gas compressor equipment, which increases power consumption. In addition, the absorption-regeneration process uses tower equipment, and there are still problems such as low mass transfer efficiency, low absorption liquid concentration, large absorption liquid consumption, and easy foaming of the absorption liquid.

[0005] As a highly efficient process intensification equipment, the ultra-gravity reactor can achieve mass transfer process intensification through centrifugal force. Compared with the traditional mass transfer method, the mass transfer efficiency can be improved by an order of magnitude. It has the advantages of high efficiency, small equipment size, easy operation and convenient equipment maintenance. At present, ultra-gravity technology has been applied in engineering in the fields of selective H2S removal, flue gas desulfurization and dust removal, nano-powder preparation, extraction, and distillation. In addition to its efficient purification effect, this technology can also eliminate the foaming of amine liquid when used in the amine liquid absorption system. It can increase the concentration of amine liquid to a certain extent, thereby reducing the circulation volume of amine liquid, greatly reducing the regeneration load of amine liquid and the energy consumption of the circulation system. However, the drive of the ultra-gravity reactor bed (rotor) of this technology requires a motor to provide power, which increases the energy consumption problem.

[0006] Patent CN105385479A discloses a supergravity desulfurization and decarbonization device that integrates the hydrate method and the membrane method. It is a device that combines the hydrate method with the membrane method and introduces supergravity technology to desulfurize and deacidify gases in industrial flue gas and oilfield production gas processes. By combining the hydrate method with the membrane separation method and introducing supergravity technology on this basis, natural gas is deeply desulfurized and deacidified, and the removal rate of acidic gases such as H2S and CO2 in natural gas is greatly improved. The upper part of the device is a supergravity membrane separation unit, and the lower part of the device is a stirred hydrate reactor. The overall structure is complex, and the rotating parts of the supergravity steering mechanism and the magnetic stirring of the stirred hydrate reactor both need to be driven by electric motors, which increases power consumption. Summary of the invention

[0007] In view of the shortcomings of the prior art, the present invention provides a process intensification reactor, a gas treatment system and a method. Through a process intensification device, the system energy is recovered for the intensification of the gas-liquid process, the gas absorption and purification effect is improved, the amount of absorption solvent is reduced, the regeneration load and the energy consumption of the circulation system are reduced, the long-term, safe and stable operation of the device is ensured, and the gas purification treatment is realized efficiently and at low cost.

[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 intensification reactor comprises a reactor shell, an internal partition plate, a process intensification unit and a pressure energy recovery unit; The internal partition plate is substantially horizontally arranged inside the reactor shell, dividing the reactor shell into two cavities, an upper cavity and an lower cavity; the process intensification unit is the upper cavity of the shell, and the pressure energy recovery unit is located in the lower cavity of the shell; The process intensification unit includes an air inlet, an exhaust port, a liquid inlet, a liquid outlet, a liquid distributor, a rotor assembly and a rotor drive 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 an internal partition plate.

[0010] Furthermore, in the above 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 composite type, and the rotor assembly is mounted on a rotor drive shaft.

[0011] Furthermore, in the above process intensification reactor, the inlet of the liquid distributor is connected to the liquid inlet of the process intensification unit, and the liquid distributor is arranged at the center of the rotor.

[0012] Furthermore, in the above-mentioned process intensification reactor, the air inlet of the process intensification unit is arranged in the middle of the outer shell, and the center of the inlet is radially horizontal to the rotor assembly; the air outlet of the process intensification unit is arranged in the upper part of the outer shell; the liquid inlet of the process intensification unit is arranged in the upper part of the outer shell; the liquid discharge port of the process intensification unit is arranged in the lower part of the shell of the process intensification unit, specifically, below the rotor assembly.

[0013] Furthermore, in the above process intensification reactor, the power impeller of the pressure energy recovery unit may be a single-stage or multi-stage impeller, and the power impellers are evenly arranged along the circumference and installed on the transmission shaft.

[0014] Furthermore, in the above process intensification reactor, the liquid inlet of the pressure energy recovery unit is arranged on the side of the outer shell, and the center of the inlet is radially horizontal to the power impeller assembly; the liquid discharge port of the pressure energy recovery unit is located at the lower part or bottom of the outer shell.

[0015] Furthermore, in the above process intensification reactor, the rotor assembly rotates following the rotor drive shaft, the rotor drive shaft rotates following the rotating shaft, the rotating shaft is driven by a power impeller, and the strong centrifugal force field generated by the rotation of the rotor is used to achieve gas-liquid process intensification.

[0016] Furthermore, in the above process intensification reactor, sealing components are arranged 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 between the mutual areas.

[0017] Furthermore, in the above process intensification reactor, the liquid discharge port of the process intensification unit is connected to the liquid inlet of the pressure energy recovery unit.

[0018] The process intensification reactor of the present invention is suitable for gas purification treatments such as gas desulfurization, gas decarbonization, natural gas absorption dehydration, circulating hydrogen desulfurization and selective dehydrogen sulfide under certain pressure conditions. It can also be used for gas-liquid process intensification treatment under other pressurized conditions, and is particularly suitable for the gas treatment field of absorption-regeneration process with certain pressure drop conditions.

[0019] According to a second aspect of the present invention, a gas processing system is provided, wherein the process intensification reactor described above is applied.

[0020] A gas processing system, the system comprising a 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 external gas pipeline, the liquid inlet of the process intensification reactor is connected to the filter outlet, 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 lean liquid cooler inlet after passing through the lean liquid pump and the lean-rich liquid heat exchanger in turn; the lean liquid cooler outlet is connected to the filtration system inlet.

[0021] Furthermore, the lean-rich liquid heat exchanger is a liquid-liquid heat exchanger, and the form of the heat exchanger is not limited.

[0022] Furthermore, a condenser is provided at the top of the regeneration tower, and a reboiler is provided at the bottom of the tower.

[0023] Furthermore, the process intensification reactor has the structure described above.

[0024] Furthermore, the liquid discharge port 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.

[0025] According to a third aspect of the present invention, a gas processing method is provided, wherein the above-mentioned system is applied.

[0026] A gas processing method comprises the following steps: (1) The gas to be treated first enters the process intensification unit of the process intensification reactor through the gas 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, undergoes an intensified process of gas-liquid two-phase mass transfer and undergoes gas absorption, and the treated gas is discharged from the reactor, and the lean absorption liquid that absorbs the components to be treated becomes rich absorption liquid and is discharged from the liquid discharge port of the process intensification unit; (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, and the pressure energy of the rich absorbent is converted into kinetic energy. The pressurized liquid impacts the power impeller and drives the impeller to rotate, thereby driving the coaxially mounted rotor assembly to rotate, and the depressurized fluid enters the flash tank from the discharge port of the pressure energy recovery unit; the second path of rich absorbent directly enters the flash tank; (3) The rich absorbent entering the flash tank in step (2) flashes off the dissolved hydrocarbons and then passes through the lean-rich liquid heat exchanger to be heated and enter the regeneration tower. In the regeneration tower, the rich absorbent is heated and decomposed to release the absorbed components to become lean absorbent, completing the regeneration of the absorbent. The high-concentration component gas released by the regeneration is subsequently treated. The regenerated lean absorbent is pressurized by a lean liquid pump, cooled by a lean-rich liquid heat exchanger, cooled by a lean liquid cooler, and filtered by a filtration system before being returned to the process intensification reactor for recycling.

[0027] Furthermore, the gas to be treated in step (1) may be natural gas, liquefied gas, dry gas, low-fraction gas or circulating hydrogen for the purpose of removing acidic components such as H2S and CO2, or may be natural gas or other gas for the purpose of removing moisture, and the components to be treated are H2S, CO2 and H2O respectively.

[0028] Furthermore, the operating pressure of the process intensification reactor in step (1) is 0.5-20 MPa, and the operating temperature can be determined according to the specific treatment system.

[0029] Furthermore, the rotation speed of the rotor assembly in step (1) is 50 to 5000 rpm, preferably 200 to 2000 rpm.

[0030] Furthermore, the rich absorbent discharged in step (2) is divided into two paths, the first path accounts for 20% to 100% of the total amount of the rich absorbent, and the second path accounts for 0% to 80% of the total amount of the rich absorbent. The rotation speed of the rotor assembly can be controlled by adjusting the flow rates of the two paths.

[0031] Furthermore, the operating pressure of the regeneration tower in step (3) is 0.1-15 MPa, which is lower than the operating pressure of the process intensification reactor, and the operating pressure difference is 0.4 MPa-20 MPa. The operating temperature can be determined and adjusted according to the specific treatment system.

[0032] The gas treatment method of the present invention can be used in absorption-regeneration gas treatment fields with certain pressure drop conditions such as gas desulfurization, gas decarbonization, natural gas absorption dehydration, circulating hydrogen desulfurization and selective dehydrogen sulfide, such as amine liquid desulfurization, amine liquid decarbonization, MDEA selective dehydrogen sulfide, natural gas glycol dehydration and other processes.

[0033] Compared with the prior art, the present invention has the following beneficial effects: 1. Compared with the existing supergravity equipment, the present invention can make full use of the pressure energy of the pressurized fluid. The pressurized liquid impacts the power impeller and drives the impeller to rotate, thereby driving the coaxially installed rotor assembly to rotate, providing a powerful centrifugal field for the process intensification reaction unit, greatly enhancing the gas-liquid two-phase mass transfer process and promoting the gas absorption effect.

[0034] 2. Compared with the existing tower equipment, the reactor of the present invention greatly strengthens the mass transfer process, the equipment volume and floor space are greatly reduced, saving infrastructure and equipment investment, and has the advantages of convenient inspection and maintenance, easy start and stop. The process intensification reactor of the present invention can not only ensure the efficient treatment effect of gas, but also eliminate foaming in the absorption liquid treatment system, and can increase the concentration of absorption liquid to a certain extent. For example, the concentration of amine liquid used in amine desulfurization can be increased from the conventional 30% to 50%, thereby reducing the circulation amount of amine liquid, greatly reducing the amine liquid regeneration load and the energy consumption of the circulation system.

[0035] 3. The present invention fully recovers the pressure energy of the pressurized rich absorption liquid before reducing the pressure for regeneration and uses it as energy to drive the rotor assembly, thereby strengthening the absorption process. It not only utilizes the advantages of ultra-gravity equipment to solve the problems of traditional tower equipment, but also utilizes the system pressure energy to solve the motor energy consumption problem of the ultra-gravity reactor, thereby realizing gas treatment with high efficiency and low cost. BRIEF DESCRIPTION OF THE DRAWINGS

[0036] Figure 1 This is a schematic diagram of an energy-saving process intensification reactor described in the present invention.

[0037] In the figure, 1-reactor shell, 2-internal partition plate, 3-process intensification unit, 4-pressure energy recovery unit, 5-air inlet, 6-exhaust port, 7-liquid inlet of process intensification unit, 8-liquid discharge port of process intensification unit, 9-liquid distributor, 10-rotor assembly, 11-rotor drive shaft, 12-liquid inlet of pressure energy recovery unit, 13-liquid discharge port of pressure energy recovery unit, 14-power impeller, 15-rotating shaft, 16-sealing component.

[0038] Figure 2 This is a schematic diagram of a gas processing system according to the present invention.

[0039] In the figure, 51-raw gas pipeline, 52-process intensification reactor, 53-exhaust gas pipeline, 54-filter, 55-flash tank, 56-rich absorption liquid pipeline, 57-lean and rich liquid heat exchanger, 58-regeneration tower, 59-regeneration gas pipeline, 60-lean liquid pump, 61-lean absorption liquid pipeline, 62-lean liquid cooler, 63-the first drainage pipeline of the process intensification unit, 64-the second drainage pipeline of the process intensification unit, 65-flash gas pipeline. Implementation

[0040] A process intensification reactor, a gas treatment system and a method of the present invention are described in detail below in conjunction with the accompanying drawings and embodiments, but the present invention is not limited thereby. Example 1

[0041] This embodiment describes in detail a process intensification reactor of the present invention. Figure 1 As shown, a process intensification reactor structure of the present invention is as follows: The energy-saving process intensification reactor comprises a reactor shell 1, an internal partition plate 2, a process intensification unit 3 and a pressure energy recovery unit 4; the internal partition plate 2 is arranged inside the reactor shell 1, dividing the reactor shell 1 into two upper and lower cavities of the process intensification unit 3 and the pressure energy recovery unit 4; the process intensification unit 3 comprises an air inlet 5, an exhaust port 6, a liquid inlet 7, a liquid discharge port 8, a liquid distributor 9, a rotor assembly 10 and a rotor drive shaft 11; the pressure energy recovery unit 4 comprises a liquid inlet 12, a liquid discharge port 13, a power impeller 14 and a rotating shaft 15; the rotor drive shaft 11 of the process intensification unit 3 is coaxially connected with the transmission shaft 15 of the pressure energy recovery unit 4 through the internal partition plate 2; the rotor assembly 10 is installed on the rotor drive shaft 11; the inlet of the liquid distributor 9 is connected to the liquid inlet 7 of the process intensification unit, and the liquid distributor 9 is arranged at the center of the rotor 10; The air inlet 5 of the process intensification unit 3 is arranged in the middle of the outer shell, and the center of the inlet is radially horizontal with the rotor assembly 10; the air outlet 6 of the process intensification unit 3 is arranged at the upper part of the outer shell; the liquid inlet 7 of the process intensification unit 3 is arranged at the upper part of the outer shell, and the discharge port 8 of the process intensification unit 3 is arranged at the lower part of the shell of the process intensification unit; the power impeller 14 is evenly arranged and installed on the transmission shaft 15 along the circumference; the liquid inlet 12 of the pressure energy recovery unit 4 is arranged on the side of the outer shell, and the center of the inlet is radially horizontal with the power impeller assembly 14; the discharge port 13 of the pressure energy recovery unit 4 is located at the lower part or bottom of the outer shell; in the above-mentioned process intensification reactor, sealing components are arranged between the rotor assembly 10 and the reactor shell 1, and between the rotating shaft 15 and the internal partition plate 2 to ensure that there is no leakage in the mutual area; the discharge port 8 of the process intensification unit 3 is connected with the liquid inlet 12 of the pressure energy recovery unit 4. When the process intensification reactor is working, the rotor assembly 10 rotates following the rotor drive shaft 11, and the rotor drive shaft 11 rotates following the rotating shaft 15. The rotating shaft 15 is driven by the power impeller 14, and the strong centrifugal force field generated by the rotation of the rotor is used to achieve gas-liquid process intensification. Example 2

[0042] This embodiment describes a gas processing system of the present invention in detail.

[0043] like Figure 2As shown, the present invention provides a gas processing system, which includes the process intensification reactor described above. The system includes a process intensification reactor 52, a flash tank 55, a lean-rich liquid heat exchanger 57, a regeneration tower 58, a lean liquid pump 60, a lean liquid cooler 62 and a filtration system 54; the gas inlet of the process intensification reactor 52 is connected to the raw gas pipeline 51, the gas outlet of the process intensification reactor 52 is connected to the external 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 liquid in the flash tank 55 is connected to the liquid inlet of the flash tank 55. The gas phase outlet is connected to the liquid inlet of the regeneration tower 58 through the lean-rich liquid heat exchanger 57; the gas phase outlet of the regeneration tower 58 is connected to the regeneration gas pipeline 59, and 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 intensification unit 3 is divided into two routes, the first route 63 is connected to the liquid inlet of the pressure energy recovery unit 4, and the second route 64 is connected to the liquid inlet of the flash tank 55. Example 3

[0044] This embodiment describes the gas treatment method of the present invention in detail. Figure 1-2 The working process of a gas treatment system and method provided by the present invention is as follows: The gas to be treated first enters the process intensification unit 3 of the process intensification reactor 52 through the gas inlet 51, and the lean absorption liquid enters the process intensification unit 3 through the liquid inlet 7; the gas contacts the lean absorption liquid from the liquid distributor 9 in the rotor assembly 10 area, performs the gas-liquid two-phase mass transfer intensification process and performs gas absorption, and the treated gas is discharged from the reactor 52, and the lean absorption liquid that absorbs the components to be treated becomes rich absorption liquid and is discharged from the liquid discharge port 8 of the process intensification unit 3; the discharged rich absorption liquid is divided into two paths: the first path 63 enters the pressure energy recovery unit 4 of the reactor, and the pressure energy of the rich absorption liquid is converted into kinetic energy, which impacts the power impeller 14 through the pressurized liquid and drives the impeller to rotate, thereby driving The coaxially mounted rotor assembly 10 rotates, and the depressurized fluid enters the flash tank 55 from the discharge port 13 of the pressure energy recovery unit 4, and the second rich absorption liquid 64 directly enters the flash tank 55; the rich absorption liquid entering the flash tank 55 flashes to evaporate the dissolved hydrocarbons, and then passes through the lean-rich liquid heat exchanger 57 to be heated and enter the regeneration tower 58, 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, and the high-concentration component gas 59 released by the regeneration is subsequently treated, and the regenerated lean absorption liquid 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, and then returned to the process intensification reactor 52 for recycling. Example 4

[0045] This embodiment provides a specific application example of a gas processing system of the present invention.

[0046] use Figure 1 The process intensification reactor shown in the figure is selected Figure 2 A gas treatment system shown in the figure desulfurizes the circulating hydrogen of a hydrocracking unit of a petrochemical enterprise. The H2S concentration in the circulating hydrogen is about 0.2% (V). The desulfurizer is N-methyldiethanolamine (MDEA), with a mass concentration of 50% (w), an absorption pressure of 13Mpa, an absorption temperature of 45°C, a regeneration pressure of 2Mpa, and a regeneration temperature of 130°C. The sulfur-containing circulating hydrogen first enters the process intensification unit 3 of the process intensification reactor 52, contacts with lean methyldiethanolamine in the rotor assembly 10 area, performs an intensified process of gas-liquid two-phase mass transfer and absorbs H2S gas. The purified gas is discharged from the reactor 52, and the lean absorption liquid that absorbs the H2S component becomes a rich absorption liquid, and enters the pressure energy recovery unit 4 of the reactor from the process intensification unit 3. The rich absorption liquid is depressurized from 13Mpa to about 2.5Mpa, and the pressure energy it has is converted into kinetic energy. The pressurized liquid impacts the power impeller 14 to drive the same The shaft-mounted rotor assembly 10 rotates to adjust the flow rate of the high-pressure rich liquid absorption liquid entering the pressure energy recovery unit, and the rotation speed of the rotor assembly is controlled at about 600 revolutions per minute (rpm), so that the H2S concentration in the treated circulating hydrogen can be less than 10 mg / m3. The rich absorption liquid after decompression to 2.5 MPa enters the flash tank 55, flashes out the dissolved hydrocarbons, and then passes through the lean-rich liquid heat exchanger 57 to be heated and enter the regeneration tower 58. In the regeneration tower, the rich absorption liquid is heated and decomposed to release the absorbed H2S gas to become lean absorption liquid, completing the regeneration of the absorption liquid and recycling it.

[0047] Comparative Example 1 The same as Example 1, except that the circulating hydrogen desulfurization equipment adopts traditional tower equipment, and the entire process of gas-liquid contact in the traditional tower is carried out under normal gravity field. Due to the limitation of the gravity field, 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, so it is necessary to increase the amount of absorption liquid. In order to avoid serious foaming of the absorption liquid, the concentration of amine liquid is generally controlled at about 30%. Compared with Example 1, when the same treatment effect is achieved, the amount of amine liquid used and the regeneration energy consumption of this comparative example increase by more than 45%.

[0048] Comparative Example 2 The same as Example 1, except that the circulating hydrogen desulfurization equipment adopts conventional supergravity equipment. The drive of the bed (rotor) of the conventional supergravity reactor requires power from a motor. Under the same operating conditions as in Example 1, the supergravity equipment needs to be equipped with at least a 20 KW motor, which increases the operating energy consumption of the system processing. In Example 1, the system pressure energy is used to solve the motor energy consumption problem of the supergravity reactor, thereby realizing gas processing with high efficiency and low cost.

Claims

1. An energy-saving process intensification reactor, characterized in that: including a reactor shell, an internal partition plate, a process intensification unit and a pressure energy recovery unit; The internal partition plate is substantially horizontally arranged inside the reactor shell, dividing the reactor shell into two cavities, an upper cavity and an lower cavity; the process intensification unit is the upper cavity of the shell, and the pressure energy recovery unit is located in the lower cavity of the shell; The process intensification unit includes an air inlet, an exhaust port, a liquid inlet, a liquid outlet, a liquid distributor, a rotor assembly and a rotor drive 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 an internal partition plate.

2. The reactor according to claim 1, characterized in that The rotor structure of the rotor assembly is a packing type, a disc type, a spiral type, a baffle type or a composite type, and the rotor assembly is installed on a rotor driving shaft.

3. The reactor according to claim 1, characterized in that The air inlet of the process intensification unit is arranged in the middle of the outer shell, and the center of the inlet is horizontal to the radial direction of the rotor assembly; the air outlet of the process intensification unit is arranged at the upper part of the outer shell; the liquid inlet of the process intensification unit is arranged at the upper part of the outer shell; and the liquid discharge port of the process intensification unit is arranged at the lower part of the rotor assembly.

4. The reactor according to claim 1, characterized in that The power impellers are evenly arranged along the circumference and installed on the transmission shaft.

5. The reactor according to claim 1, characterized in that The liquid inlet of the pressure energy recovery unit is arranged on the side of the outer shell, and the center of the inlet is parallel to the radial direction of the power impeller assembly; the liquid discharge port of the pressure energy recovery unit is located at the lower part or bottom of the outer shell.

6. The reactor according to claim 1 or 5, characterized in that The liquid discharge port of the process intensification unit is communicated with the liquid inlet of the pressure energy recovery unit.

7. A gas processing system, characterized in that: The system comprises the process intensification reactor according to any one of claims 1 to 6, a flash tank, a lean and 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 external gas pipeline, the liquid inlet of the process intensification reactor is connected to the filter outlet, 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 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 inlet of the lean liquid cooler after passing through the lean liquid pump and the lean-rich liquid heat exchanger in sequence; The lean liquid cooler outlet is connected to the filter system inlet.

8. The gas processing system according to claim 7, characterized in that: The lean-rich liquid heat exchanger is a liquid-liquid heat exchanger.

9. The gas processing system according to claim 7, characterized in that: The regeneration tower has a condenser at the top and a reboiler at the bottom.

10. The gas processing system according to claim 7, characterized in that: The liquid discharge port 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.

11. A gas processing method, wherein the gas processing system according to any one of claims 8 to 10 is used.

12. The gas processing method according to claim 11, characterized in that: The steps include: (1) The gas to be treated first enters the process intensification unit of the process intensification reactor through the gas 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, undergoes an intensified process of gas-liquid two-phase mass transfer and undergoes gas absorption, and the treated gas is discharged from the reactor, and the lean absorption liquid that absorbs the components to be treated becomes rich absorption liquid and is discharged from the liquid discharge port of the process intensification unit; (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, and the pressure energy of the rich absorbent is converted into kinetic energy. The pressurized liquid impacts the power impeller and drives the impeller to rotate, thereby driving the coaxially mounted rotor assembly to rotate, and the depressurized fluid enters the flash tank from the discharge port of the pressure energy recovery unit; the second path of rich absorbent directly enters the flash tank; (3) The rich absorbent entering the flash tank in step (2) flashes off the dissolved hydrocarbons and then passes through the lean-rich liquid heat exchanger to be heated and enter the regeneration tower. In the regeneration tower, the rich absorbent is heated and decomposed to release the absorbed components to become lean absorbent, completing the regeneration of the absorbent. The high-concentration component gas released by the regeneration is subsequently treated. The regenerated lean absorbent is pressurized by a lean liquid pump, cooled by a lean-rich liquid heat exchanger, cooled by a lean liquid cooler, and filtered by a filtration system before being returned to the process intensification reactor for recycling.

13. The gas processing method according to claim 12, characterized in that: The gas to be treated is natural gas, liquefied gas, dry gas, low-fraction gas or circulating hydrogen for the purpose of removing H2S and CO2, or natural gas for the purpose of removing moisture, and the components to be treated are H2S, CO2 or H2O respectively.

14. The gas processing method according to claim 12, characterized in that: The operating pressure of the process intensification reactor in step (1) is 0.5~20MPa.

15. The gas processing method according to claim 12, characterized in that: In step (2), the first path of rich absorption liquid accounts for 20% to 100% of the total amount of the rich absorption liquid, and the second path of rich absorption liquid accounts for 0% to 80% of the total amount of the rich absorption liquid.

16. The gas processing method according to claim 12, characterized in that: The operating pressure of the regeneration tower in step (3) is 0.4 MPa to 20 MPa lower than the operating pressure of the process intensification reactor.

17. The gas processing method according to claim 12, characterized in that: The operating pressure of the regeneration tower is 0.1~15MPa.

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