A gas purification apparatus, gas purification system and method

Abstract

The application discloses a kind of gas purification equipment, gas purification processing system and method.The gas purification equipment includes: process intensification reactor, auxiliary motor, clutch, pressure energy recovery device;The process intensification reactor includes shell, gas inlet, exhaust port, liquid inlet, liquid outlet, liquid distributor, rotor assembly and driving shaft;The pressure energy recovery device includes shell, liquid inlet, liquid outlet, power impeller and rotating shaft;The driving shaft of the process intensification reactor, auxiliary motor, clutch and the transmission shaft of the pressure energy recovery device are sequentially coaxially connected;The liquid outlet of the process intensification reactor is connected with the liquid inlet of the pressure energy recovery device by pipeline.The process intensification equipment is used for the intensification of gas-liquid mass transfer process, improves the gas absorption purification effect, reduces the amount of absorption solvent, and reduces the regeneration load and the energy consumption of circulating system.

Description

TECHNICAL FIELD

[0001] The present application belongs to the technical field of process intensification, and relates to a process intensification reactor, in particular to a gas purification device and a gas purification treatment system and method for gas-liquid mass transfer intensification. BACKGROUND

[0002] In petrochemical chemical production and natural gas treatment processes, there are many gas treatments under medium-high pressure conditions, such as removing hydrogen sulfide, carbon dioxide and other acidic components from catalytic / coking dry gas, circulating hydrogen, hydrogenation low-pressure gas and other streams in refining enterprises, and desulfurization and decarbonization treatment in natural gas purification processes. At present, the above processes generally adopt mature alcohol amine absorption process, that is, “amine liquid absorption-amine liquid regeneration” complete technology, and the absorbent is mainly an alkaline aqueous solution such as DEA, MEA, MDEA and DEPA. The typical absorption and regeneration process flow is that the raw gas enters the absorption tower from the bottom of the absorption tower, is in countercurrent contact with the solution left from the top of the tower in the packing layer, the acidic gas in the gas phase is absorbed by the absorbent, the tail gas after absorption is discharged from the top of the tower to the separator, and the rich liquid after absorbing the acidic gas enters the regeneration tower, and the lean liquid enters the absorption tower from the top of the absorption tower after being cooled by the cooler. The rich liquid is regenerated in the regeneration tower, releases the acidic gas, and is discharged from the top of the regeneration tower, and the acidic gas is discharged from the system after being cooled by the cooler.

[0003] At present, the amine liquid absorption and regeneration process generally has the following problems. First, 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 amount, absorption liquid temperature and absorption liquid foaming degree. The traditional absorption tower has the disadvantages of poor mass transfer effect, uneven gas-liquid flow, high resistance, easy plugging of the packing and unstable operation. In addition, due to the entrainment of light hydrocarbon droplets and rust and other impurities in the gas, the absorption liquid will have a serious foaming phenomenon, which seriously affects the long-period, 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 much lower than the equilibrium value, so in order to ensure the treatment effect, the amount of amine liquid is large, the regeneration load is large, and the energy consumption is high. Therefore, it is of great significance to develop high-efficiency absorption equipment and treatment processes to reduce the amount of solvent, reduce the regeneration load and the energy consumption of the circulating system, and improve the foaming phenomenon of the solvent absorption system, for improving the treatment effect and saving energy and reducing consumption of such gas.

[0004] Patent CN112159695A discloses an energy-saving natural gas MDEA decarburization system and method, which increases the pressure of the resolved gas output from the top of the regeneration tower, improves the heat grade, heats the rich amine liquid entering the regeneration tower, and reasonably recycles the low-grade heat, but the technology needs to increase the resolved gas compressor equipment, thereby increasing the power consumption, and the absorption-regeneration process uses tower equipment, which still has problems of low mass transfer efficiency, low absorption liquid concentration, large absorption liquid consumption, and easy foaming of the absorption liquid.

[0005] As a kind of efficient process intensification equipment, high gravity reactor realizes mass transfer process intensification through centrifugal force, and compared with traditional mass transfer mode, mass transfer efficiency can be improved by orders of magnitude, with advantages of high efficiency, small equipment size, easy operation and convenient equipment maintenance. At present, high gravity technology has been applied in engineering in the fields of selective H2S removal, flue gas desulfurization and dust removal, nano powder preparation, extraction, rectification and the like. In addition to high purification efficiency, the technology used in amine liquid absorption system can also eliminate amine liquid foaming, and can improve the amine liquid concentration to a certain extent, thereby reducing the circulation amount of amine liquid and greatly reducing the regeneration load of amine liquid and the energy consumption of circulation system. However, the driving of the bed layer (rotor) of the high gravity reactor needs to be powered by a motor, which increases the energy consumption problem.

[0006] Patent CN105385479A discloses a high gravity type desulfurization and decarburization device integrating hydrate method and membrane method, which combines hydrate method and membrane separation method, and introduces high gravity technology to deeply desulfurize and deacidify natural gas, thereby greatly improving the removal rate of H2S and CO2 and other acid gases in natural gas. The upper half of the device is a high gravity type membrane separation unit, and the lower half of the device is a stirring type hydrate reaction kettle. The overall structure is complex, and the rotating parts of the high gravity type steering mechanism and the magnetic stirring of the stirring type hydrate reaction kettle need to be driven by a motor, thereby increasing the power consumption. SUMMARY

[0007] In view of the deficiencies of the prior art, the present application provides a gas purification device, a gas purification system and a method. The system energy is recycled by a process intensification equipment for gas-liquid process intensification, which improves the gas absorption purification effect, reduces the absorption solvent consumption, reduces the regeneration load and the circulation system energy consumption, ensures the long-period, safe and stable operation of the device, and realizes the gas purification treatment with high efficiency and low cost.

[0008] To achieve the above object, the first aspect of the present application provides a gas purification device.

[0009] The gas purification device provided by the present application comprises a process intensification reactor, an auxiliary motor, a clutch, and a pressure energy recycler.

[0010] The process intensification reactor comprises a shell, an air inlet, an air outlet, a liquid inlet, a liquid outlet, a liquid distributor, a rotor assembly and a driving shaft;

[0011] The pressure energy recovery device comprises a shell, a liquid inlet, a liquid outlet, a power impeller and a rotating shaft; the driving shaft of the process intensification reactor, the auxiliary motor, the clutch and the transmission shaft of the pressure energy recovery device are coaxially connected in sequence;

[0012] The liquid outlet of the process intensification reactor is connected to the liquid inlet of the pressure energy recovery device through a pipeline.

[0013] Further, in the gas purification device, the rotor structure of the rotor assembly can be a filler type, a disc type, a spiral type, a baffle type or a composite type, and the rotor assembly is installed on the driving shaft.

[0014] Further, in the gas purification device, the liquid inlet of the liquid distributor is connected to the liquid inlet of the process intensification reactor, and the liquid distributor is arranged at the center of the rotor.

[0015] Further, in the gas purification device, the air inlet of the process intensification reactor is arranged at the middle part of the shell, the center of the inlet is horizontally radially arranged with the rotor assembly; the air outlet of the process intensification reactor is arranged at the upper part of the shell; the liquid inlet of the process intensification reactor is arranged at the upper part of the shell; the liquid outlet of the process intensification reactor is arranged at the lower part of the shell, specifically at the lower part of the rotor assembly.

[0016] Further, in the gas purification device, the power impeller can be a single-stage or multi-stage impeller, and the power impeller is uniformly arranged and installed on the transmission shaft along the circumference.

[0017] Further, in the gas purification device, the liquid inlet of the pressure energy recovery device is arranged at the side of the shell, the center of the inlet is horizontally radially arranged with the power impeller assembly; the liquid outlet of the pressure energy recovery device is arranged at the lower part or the bottom of the shell.

[0018] Further, in the gas purification device, when the driving shaft of the process intensification reactor, the auxiliary motor, the clutch and the transmission shaft of the pressure energy recovery device are connected, a shaft coupling can be selected to be coaxially connected between the devices.

[0019] Further, in the gas purification device, a speed changer can be selected to be arranged between the driving shaft of the process intensification reactor and the auxiliary motor.

[0020] Further, in the gas purification device, the auxiliary motor is used as the first drive of the process intensification reactor rotor assembly, and the pressure energy recovery device is used as the second drive of the rotor assembly.

[0021] Further, in the gas purification device, the sealing member is arranged between the rotating member and the shell to ensure that the relevant area is free of leakage.

[0022] Further, the gas purification device can be used for gas purification treatment such as gas desulfurization, gas decarburization, natural gas absorption dehydration, circulating hydrogen desulfurization, and selective hydrogen sulfide removal under certain pressure conditions, and can also be used for gas-liquid process intensification treatment under other pressure conditions, and is particularly suitable for gas treatment in the field of absorption-regeneration process under certain pressure drop conditions.

[0023] According to a second aspect of the present application, the present application provides a gas purification system in which the above-mentioned gas purification device is applied.

[0024] The gas purification system comprises a gas purification device, a flash tank, a lean-rich liquid heat exchanger, a regeneration tower, a lean liquid pump, a lean liquid cooler, and a filtration system.

[0025] The gas inlet of the gas purification device is connected with a raw gas pipeline, the gas outlet of the gas purification device is connected with an exhaust gas pipeline, the liquid inlet of the gas purification device is connected with the outlet of the filter, and the liquid outlet of the gas purification device is connected with the liquid inlet of the flash tank.

[0026] The liquid outlet of the flash tank is connected with the liquid inlet of the regeneration tower through the lean-rich liquid heat exchanger.

[0027] The gas phase outlet of the regeneration tower is connected with a regeneration gas pipeline, and the liquid phase outlet of the regeneration tower is connected with the inlet of the lean liquid cooler through the lean liquid pump and the lean-rich liquid heat exchanger.

[0028] The outlet of the lean liquid cooler is connected with the inlet of the filtration system.

[0029] Further, the lean-rich liquid heat exchanger is a liquid-liquid heat exchanger, and the form of the heat exchanger is not limited.

[0030] Further, the regeneration tower is provided with a condenser at the top and a reboiler at the bottom.

[0031] Further, the liquid outlet of the process intensification reactor of the gas purification device is connected with the liquid inlet of the pressure energy recovery device.

[0032] According to a third aspect of the present application, the present application provides a gas purification method, wherein the above-mentioned gas purification system is applied.

[0033] A gas purification method, comprising the following steps:

[0034] (1) The gas to be treated firstly enters the process intensification reactor of the gas purification equipment through the gas inlet, and the gas contacts with 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 which has absorbed the components to be treated becomes the rich absorption liquid and is discharged from the liquid outlet of the process intensification reactor.

[0035] (2) The rich absorption liquid discharged in step (1) enters the pressure energy recovery device of the gas purification equipment. In the pressure energy recovery device, the pressure energy of the rich absorption liquid is converted into kinetic energy, which drives the impeller to rotate by impacting the power impeller, thereby driving the transmission shaft to rotate. When the number of revolutions of the power impeller reaches or exceeds the number of revolutions of the motor, the transmission shaft engages with the clutch, and the pressure energy recovery device starts to work on the motor. At the same time, the motor drives the rotor assembly to rotate. The fluid after pressure relief enters the flash tank through the liquid outlet of the pressure energy recovery device.

[0036] (3) The rich absorption liquid entering the flash tank in step (2) is flashed to release the dissolved hydrocarbon, and then enters the regeneration tower after being heated by the lean-rich liquid heat exchanger. In the regeneration tower, the rich absorption liquid is heated and decomposed to release the absorbed components to become the lean absorption liquid. The regeneration of the absorption liquid is completed, and the high-concentration component gas released by the regeneration is subjected to subsequent treatment. The lean absorption liquid after regeneration is subjected to treatment such as pressurization by a lean liquid pump, temperature reduction by a lean-rich liquid heat exchanger, cooling by a lean liquid cooler, and filtration by a filtration system, and then returns to the process intensification reactor for recycling.

[0037] Further, the gas to be treated in step (1) can be natural gas, liquefied gas, dry gas, low-pressure gas or recycled hydrogen for the purpose of removing acidic components such as H2S and CO2, or natural gas or other gas for the purpose of removing water, and the components to be treated correspondingly are H2S, CO2 and H2O.

[0038] Further, the operating pressure of the gas purification equipment in step (1) is 0.5-20 MPa, and the operating temperature can be determined according to the specific treatment system.

[0039] Further, the rotational speed of the rotor assembly in step (1) is 50-5000 revolutions per minute (rpm), preferably 200-2000 revolutions per minute (rpm).

[0040] Further, the rotational speed of the motor in step (2) is 50-3000 revolutions per minute (rpm), preferably 200-1000 revolutions per minute (rpm).

[0041] Further, the operating pressure of the regeneration tower in step (3) is 0.1-15 MPa, the operating pressure is lower than the operating pressure of the process intensification reactor, and the operating pressure difference is 0.4-20 MPa, and the operating temperature can be determined and adjusted according to the specific treatment system.

[0042] The gas purification method can be used in the absorption-regeneration gas treatment field with certain pressure drop conditions, such as amine liquid desulfurization, amine liquid decarburization, MDEA selective desulfurization, natural gas glycol dehydration and the like.

[0043] Compared with the prior art, the present application has the following advantages:

[0044] 1. Compared with the existing supergravity rotating bed equipment, the pressure energy of the fluid under pressure is fully utilized to assist the motor as the first drive of the rotor assembly, and the pressure energy recovery device is the second drive of the rotor assembly. When the number of revolutions of the power impeller reaches or exceeds the number of revolutions of the motor, the clutch is engaged, and the pressure energy recovery device starts to work on the motor, and the motor simultaneously drives the rotor assembly to rotate, providing a strong centrifugal field for the process intensification reaction unit, greatly strengthening the gas-liquid two-phase mass transfer process, promoting the gas absorption effect, and reducing the power consumption of the motor, thereby achieving energy saving effect.

[0045] 2. Compared with the existing tower equipment, the mass transfer process of the reactor is greatly intensified, the equipment volume and land area are greatly reduced, the capital construction and equipment investment are saved, and the invention has the advantages of convenient maintenance, easy start-up and shutdown. The process intensification reactor of the present application can not only ensure the efficient treatment effect of the gas, but also eliminate the foaming of the absorption liquid treatment system, and can improve the use concentration of the absorption liquid to a certain extent. For example, the use concentration of amine liquid in amine desulfurization can be increased from 30% to 50%, thereby reducing the circulation amount of amine liquid and greatly reducing the regeneration load of amine liquid and the energy consumption of the circulation system.

[0046] 3. The present application fully recovers the pressure energy of the pressurized rich absorption liquid before depressurization and regeneration, and uses it as the driving energy of the rotor assembly, thereby intensifying the absorption process. The advantages of the supergravity equipment solve the problems of traditional tower equipment, and the system pressure energy solves the motor energy consumption problem of the supergravity reactor, thereby achieving efficient and low-cost gas treatment. BRIEF DESCRIPTION OF DRAWINGS

[0047] Figure 1 The present application is a schematic diagram of a gas purification device.

[0048] In the figure, 1 - process intensifying reactor, 2 - auxiliary motor, 3 - clutch, 4 - pressure energy recovery device, 5 - reactor shell, 6 - gas inlet, 7 - gas outlet, 8 - process intensifying reactor liquid inlet, 9 - process intensifying reactor liquid outlet, 10 - liquid distributor, 11 - rotor assembly, 12 - rotor drive shaft, 13 - pressure energy recovery device liquid inlet, 14 - pressure energy recovery device liquid outlet, 15 - power impeller, 16 - rotating shaft, 17 - coupling, 18 - sealing member.

[0049] Figure 2 A schematic diagram of a gas purification system according to the present application is shown in the figure.

[0050] In the figure, 51 - raw gas pipeline, 52 - gas purification device, 53 - exhaust gas pipeline, 54 - filter, 55 - flash tank, 56 - rich absorbent liquid pipeline, 57 - lean and rich liquid heat exchanger, 58 - regeneration tower, 59 - regeneration gas pipeline, 60 - lean liquid pump, 61 - lean absorbent liquid pipeline, 62 - lean liquid cooler, 63 - process intensifying reactor liquid outlet pipeline, 64 - flash gas pipeline. DETAILED DESCRIPTION

[0051] The gas purification device, gas purification system and method of the present application are described in detail below in conjunction with the accompanying drawings and examples, but the present application is not limited thereto. Example 1

[0052] This embodiment describes a gas purification device according to the present application in detail. As shown in the figure, the structure of a gas purification device according to the present application is as follows: Figure 1

[0053] ​The gas purification device comprises a process intensification reactor 1, an auxiliary motor 2, a clutch 3, and a pressure energy recovery device 4; the process intensification reactor 1 comprises a shell 5, an air inlet 6, an air outlet 7, a liquid inlet 8, a liquid outlet 9, a liquid distributor 10, a rotor assembly 11, and a driving shaft 12; the pressure energy recovery device 4 comprises a liquid inlet 13, a liquid outlet 14, a power impeller 15, and a rotating shaft 16; the driving shaft 16 of the process intensification reactor 1, the auxiliary motor 2, the clutch 3, and the rotating shaft 16 of the pressure energy recovery device 4 are coaxially connected in sequence; the liquid outlet 7 of the process intensification reactor 1 is connected in communication with the liquid inlet 13 of the pressure energy recovery device 4 through a pipeline; the rotor assembly 11 is installed on the driving shaft 12; the liquid inlet of the liquid distributor 10 is connected with the liquid inlet 8 of the process intensification reactor 1, and the liquid distributor 10 is arranged at the central position of the rotor assembly 11; the air inlet 6 of the process intensification reactor 1 is arranged at the middle position of the shell, the inlet center is horizontally radially arranged with the rotor assembly 11, the air outlet 7 is arranged at the upper portion of the shell, the liquid inlet 8 is arranged at the upper portion of the shell, and the liquid outlet 9 is arranged at the lower portion of the shell, specifically, the lower portion of the rotor assembly 11; the power impeller 15 is uniformly arranged and installed on the rotating shaft 16 along the circumference; the liquid inlet 13 of the pressure energy recovery device 4 is arranged at the side portion of the shell, and the inlet center is horizontally radially arranged with the power impeller assembly 15; the liquid outlet 14 of the pressure energy recovery device 4 is arranged at the lower portion or the bottom of the shell; when the driving shaft 16 of the process intensification reactor 1, the auxiliary motor 2, the clutch 3, and the rotating shaft 16 of the pressure energy recovery device 4 are coaxially connected in sequence, a shaft coupling 17 can be selectively arranged and coaxially connected between the devices; a speed changer 3 can be selectively arranged between the driving shaft 16 of the process intensification reactor 1 and the auxiliary motor 2; when the auxiliary motor 2 is used as the first driving of the rotor assembly 11 of the process intensification reactor, the pressure energy recovery device 4 is used as the second driving of the rotor assembly, when the rotation number of the power impeller reaches or exceeds the rotation number of the motor, the clutch 3 is engaged, the pressure energy recovery device 4 starts to work on the motor 2, and the rotor assembly 11 is driven to rotate by the motor 2 at the same time, and the strong centrifugal field generated by the rotation of the rotor is used to realize the intensification of the gas-liquid mass transfer process. Example 2

[0054] The embodiment describes a gas purification system of the application in detail.

[0055] As Figure 2As shown, the present application provides a gas purification system in which the gas purification device described above is applied. The gas purification system comprises a gas purification device 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 filter system 54; the gas inlet of the gas purification device 52 is connected with a raw gas pipeline 51, the gas outlet of the gas purification device 52 is connected with an exhaust gas pipeline 53, the liquid inlet of the gas purification device 52 is connected with the outlet of the filter 54, and the liquid outlet of the gas purification device 52 is connected with the liquid inlet of the flash tank 55; the liquid outlet of the flash tank 55 is connected with 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 with a regeneration gas pipeline 59, and the liquid phase outlet of the regeneration tower 58 is connected with the inlet of the lean liquid cooler 62 after passing through the lean liquid pump 60 and the lean-rich liquid heat exchanger 57 in sequence; the outlet of the lean liquid cooler 62 is connected with the inlet of the filter system 54; and the liquid discharge port 9 of the process intensification reactor 1 of the gas purification device 52 is connected with the liquid inlet 13 of the pressure energy recovery device 4. Example 3

[0056] The present embodiment describes the gas purification method of the present application in detail. In combination with Figures 1-2 , the working process of the gas purification system and method provided by the present application is as follows:

[0057] The gas to be treated first enters the process intensification reactor 1 of the gas purification device 52 through the gas inlet 51, and the gas contacts with the lean absorption liquid from the liquid distributor 10 in the area of the rotor assembly 11 to perform the intensification process of gas-liquid two-phase mass transfer and gas absorption. The treated gas is discharged from the reactor, and the lean absorption liquid that has absorbed the components to be treated becomes the rich absorption liquid which is discharged from the liquid discharge port 9 of the process intensification reactor 1. The discharged rich absorption liquid enters the pressure energy recovery device 4 of the gas purification device 52. In the pressure energy recovery device 4, the pressure energy possessed by the rich absorption liquid is converted into kinetic energy, which drives the impeller to rotate by impacting the power impeller 15, thereby driving the transmission shaft 16 to rotate. When the number of revolutions of the power impeller 15 reaches or exceeds the number of revolutions of the motor, the transmission shaft 16 engages with the clutch 3, and the pressure energy recovery device 4 starts to work on the motor 2. At the same time, the motor 2 drives the rotor assembly 11 to rotate, and the fluid after pressure relief enters the flash tank 55 through the liquid discharge port 14 of the pressure energy recovery device 4. The rich absorption liquid entering the flash tank 55 is flashed to dissolve hydrocarbons, and then is heated by the lean-rich liquid heat exchanger 57 to enter the regeneration tower 58. In the regeneration tower 58, the rich absorption liquid is heated and decomposed to release the absorbed components to become the lean absorption liquid, and the regeneration is completed. The high-concentration component gas 59 released by the regeneration is subjected to subsequent treatment, and the regenerated lean absorption liquid is subjected to pressure boosting by the lean liquid pump 60, temperature reduction by the lean-rich liquid heat exchanger 57, cooling by the lean liquid cooler 62 and filtration by the filter system 54, and then is returned to the process intensification reactor 1 for recycling. Example 4

[0058] The embodiment gives a specific application case of the gas purification system of the application.

[0059] The gas purification system shown in the application is adopted. Figure 1 The gas purification system shown in the application is adopted. Figure 2 The gas purification system shown in the application is adopted. The H2S concentration in the dry gas is about 0.4% (V), the desulfurizing agent is N-methyldiethanolamine (MDEA) with a mass concentration of 45% (w), the absorption pressure is 1.5 MPa, the absorption temperature is 40°C, the regeneration pressure is 0.6 MPa, and the regeneration temperature is 120°C. The sulfur-containing dry gas first enters the process intensification reactor 1 of the gas purification equipment 52, contacts with the lean methyldiethanolamine in the rotor assembly 11 area, and carries out the intensification process of gas-liquid two-phase mass transfer and the absorption of H2S gas. The purified gas is discharged from the reactor 52, the lean absorption liquid that has absorbed the H2S component becomes the rich absorption liquid, and enters the pressure energy recovery device 4 of the gas purification equipment 52. In the pressure energy recovery device 4, the rich absorption liquid is reduced in pressure from 1.5 MPa to about 0.8 MPa, the pressure energy of the rich absorption liquid is converted into kinetic energy, passes through the impact power impeller 15, and drives the impeller to rotate, thereby driving the transmission shaft 16 to rotate, and controlling the rotating speed of the rotor assembly to be about 800 revolutions per minute (rpm). The H2S concentration in the treated circulating hydrogen is less than 10 mg / m3. After being reduced in pressure to 0.8 MPa, the fluid enters the flash tank 55 from the liquid outlet 14 of the pressure energy recovery device 4, flashes out the dissolved hydrocarbon, is warmed by the lean-rich liquid heat exchanger 57, enters the regeneration tower 58, and is heated and decomposed in the regeneration tower to release the absorbed H2S gas to become the lean absorption liquid, thereby completing the regeneration and recycling of the absorption liquid.

[0060] Comparative Example 1

[0061] The same as Example 1, except that the circulating hydrogen desulfurization equipment adopts a traditional tower type equipment. The gas-liquid contact process of the traditional tower type equipment is carried out in a normal gravity field. Due to the limitation of the gravity field, the gas-liquid contact flow is slow, the mass transfer coefficient is not high, the mass transfer rate is low, and the acid component content in the rich liquid is far lower than the equilibrium value. Therefore, it is necessary to increase the amount of absorption liquid, and in order to avoid the serious foaming phenomenon of the absorption liquid, the amine liquid concentration is generally controlled at about 30%. Compared with Example 1, when the same treatment effect is achieved, the amine liquid usage and the regeneration energy consumption of the present comparative example are increased by about 40%.

[0062] Comparative Example 2

[0063] The same as example 1, except that the circulating hydrogen desulfurization equipment adopts a conventional supergravity equipment. Since the driving of the conventional supergravity reactor bed (rotor) completely relies on the power provided by the motor, and in example 1, the auxiliary motor is used as the first driving of the rotor assembly, and the pressure energy recovery device is used as the second driving of the rotor assembly, so that the pressure energy of the fluid can be fully utilized. Therefore, under the same operating conditions as example 1, the energy consumption of the conventional supergravity equipment is increased by at least 50% or more.

Claims

1. A gas purification apparatus, characterized by comprising: The process intensification reactor, the auxiliary motor, the clutch, and the pressure energy recovery device are coaxially connected in sequence. The process intensification reactor comprises a shell, a gas inlet, a gas outlet, a liquid inlet, a liquid outlet, a liquid distributor, a rotor assembly, and a driving shaft. The pressure energy recovery device comprises a shell, a liquid inlet, a liquid outlet, a power impeller, and a rotating shaft. The driving shaft of the process intensification reactor, the auxiliary motor, the clutch, and the transmission shaft of the pressure energy recovery device are coaxially connected in sequence. The liquid outlet of the process intensification reactor is connected to the liquid inlet of the pressure energy recovery device through a pipeline. The power impeller is uniformly arranged and installed on the transmission shaft along the circumference. The liquid inlet of the pressure energy recovery device is arranged on the side of the shell, and the inlet center is radially horizontal to the power impeller assembly.

2. The gas purification apparatus according to claim 1, characterized by The liquid outlet of the pressure energy recovery device is located at the lower part or the bottom of the shell.

3. The gas cleaning apparatus according to claim 1, characterized in that The auxiliary motor is used as the first driving of the rotor assembly of the process intensification reactor, and the pressure energy recovery device is used as the second driving of the rotor assembly.

4. The gas cleaning apparatus according to claim 1, characterized in that When the number of revolutions of the power impeller reaches or exceeds the number of revolutions of the motor, the clutch is engaged, the pressure energy recovery device starts to work on the motor, and the rotor assembly is driven to rotate simultaneously with the motor.

5. The gas purification apparatus according to claim 1, characterized by The rotor structure of the rotor assembly is a filler type, a disc type, a spiral type, a baffle type, or a composite type.

6. The gas cleaning apparatus according to claim 1, characterized in that The liquid inlet of the process intensification reactor is connected to the liquid distributor, which is arranged at the center of the rotor.

7. The gas cleaning apparatus according to claim 1, characterized in that The gas inlet of the process intensification reactor is arranged at the middle part of the shell, and the inlet center is radially horizontal to the rotor assembly.

8. A gas purification system, characterized by, The gas outlet of the process intensification reactor is arranged at the upper part of the shell.

9. The gas purification system of claim 8, wherein The liquid outlet of the process intensification reactor is arranged at the lower part of the shell. When the driving shaft of the process intensification reactor, the auxiliary motor, the clutch, and the transmission shaft of the pressure energy recovery device are connected, a shaft coupling is selected to be arranged between the devices for coaxial connection. A speed changer is arranged between the driving shaft of the process intensification reactor and the auxiliary motor. A sealing member is arranged between the rotating member and the shell to ensure that there is no leakage in the relevant area. The gas purification device of any one of claims 1-7 is contained therein.

10. The gas purification system of claim 9, wherein The gas purification system comprises a gas purification device, a flash tank, a lean- rich liquid heat exchanger, a regeneration tower, a lean liquid pump, a lean liquid cooler, and a filtration system.

11. A method of purifying a gas, characterized by, The gas inlet of the gas purification device is connected to a raw gas pipeline, the gas outlet of the gas purification device is connected to an exhaust gas pipeline, the liquid inlet of the gas purification device is connected to the outlet of a filter, and the liquid outlet of the gas purification device is connected to the liquid inlet of a 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 a regeneration gas pipeline, and the liquid phase outlet of the regeneration tower is connected to the inlet of a lean liquid cooler through the lean liquid pump and the lean- rich liquid heat exchanger in sequence. The outlet of the lean liquid cooler is connected to the inlet of the filtration system. A condenser is arranged at the top of the regeneration tower, and a reboiler is arranged at the bottom of the regeneration tower. The gas purification system of any one of claims 8-10 is applied, and the purification method comprises the following steps: (1) The gas to be treated first enters the process intensification reactor of the gas purification device through the gas inlet, and 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 that has absorbed the components to be treated becomes rich absorption liquid and is discharged from the liquid outlet of the process intensification reactor; (2) The rich absorption liquid discharged in step (1) enters the pressure energy recovery device of the gas purification device. In the pressure energy recovery device, the pressure energy of the rich absorption liquid is converted into kinetic energy, which drives the impeller to rotate by impacting the power impeller, thereby driving the transmission shaft to rotate. When the number of revolutions of the power impeller reaches or exceeds the number of revolutions of the motor, the transmission shaft engages with the clutch, and the pressure energy recovery device starts to work on the motor. At the same time, the motor drives the rotor assembly to rotate, and the fluid after pressure relief enters the flash tank through the liquid outlet of the pressure energy recovery device; (3) The rich absorption liquid entering the flash tank in step (2) is flashed to dissolve hydrocarbons, then heated by the lean-rich liquid heat exchanger and enters the regeneration tower. In the regeneration tower, 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 processed subsequently. The lean absorption liquid after regeneration is pressurized by the lean liquid pump, cooled by the lean liquid cooler, and filtered by the filtration system, and then returns to the process intensification reactor for recycling.

12. The gas purification method according to claim 11, characterized by, The gas to be treated is natural gas, liquefied gas, dry gas, low-pressure gas, or recycled hydrogen containing one or more of H2S, CO2, or water.

13. The gas purification method according to claim 11, characterized by, The operating pressure of the regeneration tower is 0.4-20 MPa lower than the operating pressure of the process intensification reactor.

14. The gas purification method according to claim 11, characterized by, The operating pressure of the gas purification device is 0.5-20 MPa, and the operating pressure of the regeneration tower is 0.1-15 MPa.

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