Clean production process of amine liquid desulfurization system

Abstract

The invention discloses a clean production process of an amine liquid desulfurization system, which comprises the following steps: sulfur-containing liquefied gas and lean amine liquid respectively enter from a liquid hydrocarbon inlet at the lower part of a desulfurization tower and a lean amine liquid inlet at the upper part of the desulfurization tower, and are in countercurrent contact in the desulfurization tower to absorb sulfur-containing gas in the liquefied gas; the lean amine liquid becomes rich amine liquid after absorbing the sulfur-containing gas, the rich amine liquid enters a rich amine liquid pre-dealkylation device to remove liquid hydrocarbon in a non-depressurization state and then enters a rich amine liquid flash evaporator to remove gaseous hydrocarbon through depressurization flash evaporation, and the rich amine liquid without the gaseous hydrocarbon enters a rich amine liquid regeneration tower to be regenerated, then enters a lean amine liquid purifier to be purified and then returns to the desulfurization tower; the liquefied gas absorbed by the lean amine liquid enters a liquefied gas pre-liquid-removal solid-removal device for primary amine liquid removal and then enters a liquefied gas deep liquid removal device for liquefied gas deep amine liquid removal, and purified liquid hydrocarbon is obtained. According to the clean production process of the amine liquid desulfurization system, the liquid hydrocarbon entrained in the amine liquid can be efficiently recycled, and high economic and environment-friendly values are achieved.

Description

TECHNICAL FIELD

[0001] The present application belongs to the technical field of refinery gas alkanolamine desulfurization purification, in particular to an amine liquid desulfurization system clean production process. BACKGROUND

[0002] With the process of oil quality upgrading accelerating, the soluble substances such as hydrogen sulfide, mercaptan and sulfide in oil and gas are usually treated by absorption using the alkanolamine method.

[0003] The process of traditional alkanolamine method for liquefied gas desulfurization is roughly as shown in the following figure: Figure 1 The liquefied gas is pumped from the upstream device to the liquefied gas desulfurization tower 1 by the feed pump. The lean amine liquid is pressurized by the lean amine liquid pump and cooled to 40℃ by the lean amine liquid cooler, and then enters the upper part of the desulfurization tower 1. The lean amine liquid and the liquefied gas are countercurrently contacted in the tower, the amine liquid absorbs H2S in the liquefied gas to form rich amine liquid which flows out from the bottom of the tower to the amine regeneration tower 2. The purified liquefied gas produced at the top of the desulfurization tower 1 is sent to the demulsifying tank, and after the trace amine liquid carried by the liquefied gas is separated by coalescence and sedimentation, the liquefied gas is sent to the liquefied gas desulfuration device.

[0004] The rich amine liquid usually carries small gas bubbles and liquid light hydrocarbons, which causes the pressure and liquid level of the regeneration flash tower and the regeneration tower to fluctuate, the amount of flare gas to increase, the risk of tail gas exceeding the standard in the downstream sulfur device to increase, and the energy consumption of the rich liquid regeneration process to increase. The rich amine liquid usually adopts a sedimentation buffer tank, but the removal efficiency of small gas bubbles and emulsified oil droplets by simple gravity sedimentation is low. Moreover, excessive pressure reduction causes a large amount of light hydrocarbons and acidic gas to be separated, and the amount of solvent carried increases, which aggravates solvent loss.

[0005] In addition, during the recycling process of the amine liquid, solid impurities generated due to pipeline and equipment corrosion, amine liquid degradation and the like aggravate the system corrosion, which affects the safe and stable operation of the amine desulfurization and amine regeneration system.

[0006] Due to reasons such as liquid level control, operation fluctuation and load change, the liquefied gas at the top of the desulfurization tower may carry amine liquid, which causes the caustic liquid in the desulfuration system to be contaminated by foaming.

[0007] Therefore, it is necessary to realize rich liquid dehydrocarbon and liquefied gas deamination by certain efficient and low-consumption means, reduce the fluctuation of the rich liquid process, inhibit the risk of environmental hazards, and improve the economic and clean operation level of the device. SUMMARY

[0008] In view of the above needs existing in the prior art, the present application proposes an amine liquid desulfurization system clean production process and equipment on the basis of the existing alkanolamine desulfurization system, so as to improve the clean production level of the amine desulfurization system.

[0009] To achieve the above-mentioned purpose, the present application adopts the following technical solutions:

[0010] A clean production process of amine liquid desulfurization system is provided, comprising the following steps:

[0011] Sulfur-containing liquid gas and lean amine liquid enter the desulfurization tower from the liquid hydrocarbon inlet at the lower part and the lean amine liquid inlet at the upper part respectively, and are in countercurrent contact in the desulfurization tower, so that the lean amine liquid fully absorbs the sulfur-containing gas in the sulfur-containing liquid gas;

[0012] The lean amine liquid after absorbing the sulfur-containing gas becomes rich amine liquid, enters the rich amine liquid pre-hydrocarbon-removing device to remove liquid hydrocarbon under non-reduced pressure, then enters the rich amine liquid flash evaporator to remove gaseous hydrocarbon under reduced pressure, and the rich amine liquid after removing gaseous hydrocarbon enters the rich amine liquid regenerator to become lean amine liquid again, and the regenerated lean amine liquid enters the lean amine liquid purifier, and after separating the particulate impurities in the lean amine liquid, returns to the desulfurization tower;

[0013] The liquid gas after being absorbed by the lean amine liquid enters the liquid gas pre-liquid-removing device to remove the free amine liquid and the particulate matter above 10 microns, and then enters the liquid gas deep-liquid-removing device to remove the free amine liquid and the particulate matter above 10 microns, and the purified liquid hydrocarbon is obtained.

[0014] According to the preferred embodiment of the present application, after the rich amine liquid pre-hydrocarbon-removing device removes the liquid hydrocarbon entrained in the rich amine liquid, the separated liquid hydrocarbon is combined with the liquid gas flowing out of the top liquid hydrocarbon outlet of the desulfurization tower, and then enters the liquid gas pre-liquid-removing device together.

[0015] According to the present application, the step of removing gaseous hydrocarbon from the rich amine liquid in the rich amine liquid flash evaporator includes using a centrifugal flash module to separate gas and liquid under reduced pressure, using a fiber coalescence separation module to remove the residual liquid hydrocarbon in the rich amine liquid, and using a fiber coalescence liquid-removing module to remove the liquid entrained in the sour gas after removing the liquid in the acid gas.

[0016] According to the preferred embodiment of the present application, two lean amine liquid purifiers are used to purify the lean amine liquid in the mode of “one in operation and one in standby”, and the switching operation is performed between operation and standby according to the running state.

[0017] According to the present application, when the lean amine liquid purifier is switched, the switched-off amine liquid purifier is connected to steam to backwash the filter module, and after the end of the backwashing, the switched-off amine liquid purifier is in standby.

[0018] According to the present application, the purifying operation of the lean amine liquid purifier is to filter out the solid particulate matter and the thermally stable salt in the lean amine liquid by using the filter module.

[0019] According to the present application, the preliminary amine liquid removal of the liquid gas pre-liquid-removing device is to remove the free amine liquid and the particulate matter above 10 microns entrained in the liquid gas by using centrifugal separation.

[0020] According to the present application, the step of deep liquid removal of the liquefied gas is to use multi-interface mixed fibers and corrugated plates in sequence to remove the amine liquid entrained in the liquefied gas.

[0021] According to the preferred embodiment of the present application, the amine liquid removed by the liquefied gas pre-liquid removal solid remover and the amine liquid removed by the liquefied gas deep liquid removal are merged with the rich amine liquid from the rich amine liquid pre-olefin remover through a pipeline and then enter the rich amine liquid flash evaporator.

[0022] According to the preferred embodiment of the present application, the liquefied gas is further washed by using a water washer after deep liquid removal to remove impurities and H2S gas entrained in the liquefied gas.

[0023] The present application has the following beneficial effects:

[0024] 1. The clean production process of the amine liquid desulfurization system of the present application can efficiently recover the liquid hydrocarbons entrained in the amine liquid, having high economic and environmental protection values.

[0025] 2. The clean production process of the present application can efficiently purify the lean amine liquid, reduce the corrosion of the system, and thus improve the safety and stability of the operation of the desulfurization system.

[0026] 3. The clean production process of the present application can deeply purify the liquefied gas, ensuring the long-period stable operation of the downstream device. BRIEF DESCRIPTION OF DRAWINGS

[0027] Figure 1 It is a process flow diagram of the traditional amine liquid desulfurization system.

[0028] Figure 2 It is a clean production process flow diagram of the amine liquid desulfurization system of the present application.

[0029] Figure 3 It is a structure schematic diagram of the rich amine liquid pre-olefin remover.

[0030] Figure 4 It is a structure schematic diagram of the rich amine liquid flash evaporator.

[0031] Figure 5 It is a structure schematic diagram of the amine liquid purifier.

[0032] Figure 6 It is a structure schematic diagram of the liquefied gas pre-liquid removal solid remover.

[0033] Figure 7 It is a structure schematic diagram of the liquefied gas deep liquid removal. DETAILED DESCRIPTION

[0034] The technical solutions of the present application will be described in detail below with specific embodiments in conjunction with the drawings. It should be understood that the following embodiments are only used to illustrate the present application but not to limit the scope of the present application.

[0035] Unless otherwise specified, the various devices used in the following embodiments, such as desulfurization towers, pre-hydrocarbon removers, and flash evaporators, can be selected from similar devices known in the prior art according to their respective functions. The innovation of this invention lies not in these devices themselves, but in the overall process system composed of these devices and the corresponding production process.

[0036] Example 1: Clean production process and equipment for amine liquid desulfurization system

[0037] like Figure 2 The diagram shows a flowchart of the clean production process of the amine liquid desulfurization system of the present invention. The equipment for this production process includes a desulfurization tower 10 for countercurrent contact desulfurization of sulfur-containing liquefied petroleum gas (LPG) and lean amine liquid. A rich amine liquid pre-hydrocarbon remover 20, a rich amine liquid flash evaporator 30, a rich amine liquid regeneration device 40, and an amine liquid purifier 50 are sequentially connected to the rear end of the rich amine liquid outlet 14 of the desulfurization tower 10. A liquefied gas pre-liquid and solid desulfurization device 60 and a liquefied gas deep deliquidation device 70 are sequentially connected to the rear end of the liquid hydrocarbon outlet 13 of the desulfurization tower 10. The lean amine liquid outlet of the amine liquid purifier 50 is connected to the desulfurization tower via a pipeline, so that the regenerated lean amine liquid can be reused for the desulfurization of sulfur-containing LPG.

[0038] The upper and lower parts of the desulfurization tower 10 are respectively provided with a lean amine liquid inlet 11 and a liquid hydrocarbon inlet 12, which are used for lean amine liquid and sulfur-containing liquefied gas to enter the desulfurization tower 10 for countercurrent absorption process. The top and bottom of the desulfurization tower 10 are respectively the liquid hydrocarbon outlet 13 and the rich amine liquid outlet 14.

[0039] The amine-rich liquid pre-dehydrocarbonizer 20 is a vertical or horizontal container, such as... Figure 3 As shown, the preferred container is a vertical container, with a rich amine liquid inlet 21 in the middle, which is connected to the rich amine liquid outlet 14 of the desulfurization tower 10 through a pipeline; the top and bottom of the container are respectively provided with a liquefied gas outlet 22 and a rich amine liquid outlet 23, and the interior is provided with a fiber coalescence rapid separation module 24 for removing liquid hydrocarbons entrained in the rich amine liquid.

[0040] The rich amine liquid flash evaporator 30 is a vertical or horizontal container, such as... Figure 4 As shown, the preferred container is a horizontal container with an amine-rich liquid inlet 31 on the left side, an amine-rich liquid outlet 32 ​​at the bottom and an acid gas outlet 39 at the top on the right side, and a centrifugal flash evaporation module 33, a fiber coalescing separation module 34, a U-shaped oil collection tank 35, and a baffle 36 arranged sequentially from left to right inside the container. A liquid hydrocarbon outlet 37 is provided above the U-shaped oil collection tank 35, and a fiber coalescing deliquencing module 38 is provided below the acid gas outlet 39 to remove the liquid entrained in the acid gas.

[0041] The top and bottom of the rich amine liquid regeneration tower 40 are respectively provided with an acid gas outlet and a lean amine liquid outlet, and the bottom of the rich amine liquid regeneration tower is provided with a tower bottom reboiler for removing H2S gas in the rich amine liquid by heating to regenerate the amine liquid into lean amine liquid.

[0042] In combination Figure 5 As shown, the lean amine liquid purifier 50 is a vertical container, which is provided with a filter module 51, and the container is respectively provided with a lean amine liquid inlet 52 and a steam inlet 53 at the upper part and lower part of the filter module 51, and the top and bottom of the container are respectively provided with an acid gas outlet 54 and a lean amine liquid outlet 55; the inside of the filter module 51 is filled with filter material particles with a particle size of 100-5000 microns, and the material of the filter material particles is preferably ceramic, resin, stainless steel, polysilicon or PTFE, for removing solid particles above 25 microns and heat stable salts in the lean liquid. Preferably, the amine liquid purifier 50 is configured with two, in a “one in operation and one in standby” mode, for separating the particulate impurities existing in the lean amine liquid, and can be switched between operation and standby according to the operating state. When the filter module 51 of one amine liquid purifier is switched due to the pressure drop exceeding the set value, the switched amine liquid purifier 50 blows steam into the filter module 51 through the steam inlet 53 for backwashing, and the acid gas containing hydrogen sulfide blown out is discharged from the acid gas outlet 54 at the top; the amine liquid purifier after backwashing is standby.

[0043] In combination Figure 6 As shown, the liquefied gas pre-liquid removal and solid removal device 60 is a vertical container, the middle part of the container is provided with a liquefied gas inlet 61, the top and bottom are respectively provided with a liquefied gas outlet 62 and a lean amine liquid outlet 63, and a centrifugal separation module 64 such as a cyclone separator or similar equipment is installed inside, for removing free amine liquid and particles above 10 microns entrained in the liquefied gas.

[0044] The liquefied gas deep liquid removal device 70 is a vertical or horizontal container, such as Figure 7 As shown, it is preferably a horizontal container, the left side of the container is provided with a liquefied gas inlet 71, the top and bottom of the right side are respectively provided with a liquefied gas outlet 72 and a lean amine liquid outlet 73, and the inside of the container is sequentially provided with a multi-interface mixed fiber module 74 and a rapid separation module 75 from the left side to the right side, for removing amine liquid entrained in the liquefied gas. The multi-interface mixed fiber module 74 is preferably composed of the coalescence guide module disclosed in CN117509815A and filled with fibers between the coalescence plates, and the rapid separation module 75 is preferably a corrugated plate.

[0045] Back to Figure 1Preferably, the liquid hydrocarbon outlet of the rich amine liquid pre-hydrocarbon-removing device 20 is also connected to the liquid hydrocarbon outlet 13 of the top of the desulfurization tower 10 through a pipeline, so that the separated liquid hydrocarbon and the liquefied gas flowing out of the top of the desulfurization tower 10 are merged and then enter the liquefied gas pre-liquid-removing device 60.

[0046] The lean amine liquid outlet of the liquefied gas pre-liquid-removing device 60 is also connected to the rich amine liquid inlet of the rich amine liquid flash evaporator 30 through a pipeline, and the lean amine liquid outlet of the liquefied gas deep-liquid-removing device 70 is also connected to the rich amine liquid inlet of the rich amine liquid flash evaporator 30 through a pipeline, so that the amine liquid removed by the liquefied gas pre-liquid-removing device 60 and the liquefied gas deep-liquid-removing device 70 is merged with the rich amine liquid from the rich amine liquid pre-hydrocarbon-removing device 20 and then enters the rich amine liquid flash evaporator 30.

[0047] Preferably, a liquefied gas water washing device 80 is further connected to the rear end of the liquefied gas deep-liquid-removing device 70, which is used to further absorb a small amount of impurities and H2S in the liquefied gas by, for example, spraying, so as to further improve the cleanliness of the liquefied gas.

[0048] The clean production process of the amine liquid desulfurization system of the present application is as follows:

[0049] The sulfur-containing liquefied gas and the lean amine liquid enter the desulfurization tower 10 from the liquid hydrocarbon inlet 12 and the lean amine liquid inlet 11, respectively, and are in countercurrent contact in the desulfurization tower 10, so that the lean amine liquid fully absorbs the sulfur-containing gas in the sulfur-containing liquefied gas;

[0050] The lean amine liquid after absorbing the sulfur-containing gas becomes rich amine liquid, enters the rich amine liquid pre-hydrocarbon-removing device 20 to remove the liquid hydrocarbon in a non-pressure-reducing state, and then enters the rich amine liquid flash evaporator 30 to remove the gaseous hydrocarbon in a pressure-reducing flash evaporation state. The rich amine liquid after removing the gaseous hydrocarbon enters the rich amine liquid regenerator 40 to be regenerated into lean amine liquid. The regenerated lean amine liquid enters the lean amine liquid purifier 50 and then returns to the desulfurization tower 10 after being purified.

[0051] The liquefied gas after being absorbed by the lean amine liquid enters the liquefied gas pre-liquid-removing device 60 to be preliminarily removed of the amine liquid, and then enters the liquefied gas deep-liquid-removing device 70 to be deeply removed of the amine liquid, so as to obtain the purified liquefied gas. The liquefied gas from the liquefied gas deep-liquid-removing device 70 can further enter the liquefied gas water washing device 80 to be washed, so as to further improve the cleanliness of the obtained liquefied gas.

[0052] Further, the coalescence rapid separation module 24 installed in the rich amine liquid pre-hydrocarbon-removing device 20 is used to remove the liquid hydrocarbon entrained in the rich amine liquid. The separated liquid hydrocarbon and the liquefied gas flowing out of the top of the desulfurization tower 10 are merged and then enter the liquefied gas pre-liquid-removing device 60. The content of the liquid hydrocarbon entrained in the rich amine liquid after being treated by the coalescence rapid separation module 24 is less than 50 mg / L.

[0053] The centrifugal flash module 33 installed inside the rich liquid flasher 30 is used to remove the fine bubble state and dissolved state light hydrocarbon and H2S gas entrained in the rich amine solution under the condition of pressure drop less than 0.01 MPa, which is sent to the low pressure gas system for treatment; the fiber coalescence separation module 34 is used to coalesce the residual liquid hydrocarbon droplets in the rich amine solution, the U-shaped oil collection tank 35 is used to collect the liquid hydrocarbon floating on the surface of the rich amine solution after coalescence, and the baffle 36 is used to control the liquid level of the rich amine solution not lower than the bottom of the U-shaped oil collection tank; after treatment of the rich amine solution, the content of dissolved light hydrocarbon is less than 5 mg / L.

[0054] The filter module 51 provided in the lean amine solution purifier 50 is filled with filter material particles with particle size of 100-5000 microns, and the material of the filter material particles is preferably ceramic, resin, stainless steel, polysilicon, PTFE, which is used to remove solid particles and heat stable salts in the lean liquid with size more than 25 microns, and the solid particles and heat stable salts with size more than 25 microns in the lean amine solution can be completely removed after treatment by the purifier 50.

[0055] The centrifugal separation module 64 installed inside the liquefied gas pre-liquid removal and solid removal device 60 is used to remove the free amine solution and particles with size more than 10 microns entrained in the liquefied gas, and the removal rate of the free amine solution and particles with size more than 10 microns can be more than 99% after treatment by the centrifugal separation module 64.

[0056] The multi-interface mixed fiber module 74 and the rapid separation module 75 installed inside the liquefied gas deep liquid removal device 70 are used to remove the amine solution entrained in the liquefied gas, and the content of the amine solution in the liquefied gas is less than 5 mg / m 3 .

[0057] Example 2, application example

[0058] In this example, the amine solution desulfurization system clean production process and equipment of Example 1 are used, which are as follows:

[0059] As Figure 1The lean amine solution, weak alkaline N-methyl diethanolamine aqueous solution (MDEA) is used as the absorbent to remove H2S in the liquefied gas from a catalytic device of a refinery. The H2S in the liquefied gas is absorbed in the liquefied gas desulfurization tower 10. The rich amine solution absorbing H2S is treated in the rich amine solution pre-dehydrocarbon device 20 and the rich amine solution flash evaporator 30 in turn, and then enters the regeneration tower 40 after being heated to regenerate the solvent. The regenerated lean amine solution is cooled and then enters the lean liquid purifier 50 for treatment. The treated lean liquid is sent to the absorption tower 10 for recycling. The acid gas discharged from the regeneration tower 10 is condensed and separated, and then sent to a sulfur recovery device for further treatment. The liquefied gas from the top of the desulfurization tower 10 is treated in the liquefied gas pre-dehydrocarbon device 60 and the liquefied gas deep dehydrocarbon device 70 in turn, and then treated in the liquefied gas water washer 80. The treated liquefied gas is sent to a downstream device.

[0060] Effect: The hydrocarbon content in the rich amine solution is reduced from more than 200 mg / L in the original system to less than 5 mg / L, the amine solution entrained in the liquefied gas is reduced from 80 mg / m 3 to 5 mg / m 3 The amount of acid waste gas is reduced by more than 90%, and the corrosion rate of the amine desulfurization system is reduced from 3 mm / a to about 1 mm / a, which greatly improves the clean production level of the desulfurization system.

[0061] The amine desulfurization system clean production process of the present application is described in detail through the preferred embodiments. However, it should be understood that the described embodiments are only part of the embodiments of the present application, not all. Based on the embodiments of the present application, all other embodiments obtained by those of ordinary skill in the art without creative labor fall within the scope of the present application.

Claims

1. A clean production process for an amine liquid desulfurization system, characterized in that... Includes the following steps: Sulfur-containing liquefied gas and lean amine liquid enter from the liquid hydrocarbon inlet at the bottom of the desulfurization tower and the lean amine liquid inlet at the top, respectively, and are in countercurrent contact inside the desulfurization tower so that the lean amine liquid can fully absorb the sulfur-containing gas in the sulfur-containing liquefied gas. After absorbing sulfur-containing gas, the lean amine liquid becomes a rich amine liquid. It then enters the rich amine liquid pre-dehydrocarbonizer to remove liquid hydrocarbons under non-pressure reduction conditions. Next, it enters the rich amine liquid flash evaporator to remove gaseous hydrocarbons by pressure reduction flash evaporation. The rich amine liquid after removing gaseous hydrocarbons enters the rich amine liquid regeneration tower to be regenerated into lean amine liquid. The regenerated lean amine liquid enters the lean amine liquid purifier, and after separating particulate impurities from the lean amine liquid, it is returned to the desulfurization tower. After being absorbed by the lean amine solution, the liquefied gas enters the liquefied gas pre-dehydration and desolidification unit for preliminary amine removal, and then enters the liquefied gas deep dehydration unit for deep amine removal, resulting in purified liquid hydrocarbons.

2. The clean production process of the amine liquid desulfurization system according to claim 1, characterized in that, After the rich amine liquid pre-dehydrocarbonizer removes the liquid hydrocarbons entrained in the rich amine liquid, the separated liquid hydrocarbons merge with the liquefied gas flowing out of the liquid hydrocarbon outlet at the top of the desulfurization tower, and then enter the liquefied gas pre-dehydrocarbonizer together.

3. The clean production process of the amine liquid desulfurization system according to claim 1, characterized in that, The step of depressurizing and flashing to remove gaseous hydrocarbons from the rich amine liquid in the rich amine liquid flash evaporator includes using a centrifugal flash evaporation module to depressurize and flash for gas-liquid separation, using a fiber coalescing separation module to remove residual liquid hydrocarbons in the rich amine liquid, and using a fiber coalescing deliquencing module to remove liquid entrained in the acidic gas before discharging the acidic gas.

4. The clean production process of the amine liquid desulfurization system according to claim 1, characterized in that, Two amine-poor solution purifiers are used in a "one on, one on standby" mode to purify the amine-poor solution, and the operation is switched between running and standby according to the operating status.

5. The clean production process of the amine liquid desulfurization system according to claim 4, characterized in that, After the amine liquid purifier is switched, the amine liquid purifier that was switched off is backwashed with steam through the filter module, and then put into standby mode.

6. The clean production process of the amine liquid desulfurization system according to claim 4, characterized in that, The purification operation of the lean amine solution purifier involves using a filtration module to remove solid particles and thermally stable salts from the lean amine solution.

7. The clean production process of the amine liquid desulfurization system according to claim 1, characterized in that, The initial deamine removal liquid of the liquefied gas pre-dehydration and desolidification device is obtained by centrifugal separation to remove free amine liquid and particulate matter larger than 10 micrometers entrained in the liquefied gas.

8. The clean production process of the amine liquid desulfurization system according to claim 1, characterized in that, The deep deliquor removal step of the liquefied gas involves sequentially using multi-interface hybrid fibers and corrugated plates to deeply remove the amine liquid entrained in the liquefied gas.

9. The clean production process of the amine liquid desulfurization system according to claim 1, characterized in that, The amine solution removed by the liquefied gas pre-dehydration and desolidification unit and the amine solution removed by the deep dehydration of liquefied gas are combined with the rich amine solution from the rich amine solution pre-dehydrocarbonization unit through pipelines and then enter the rich amine solution flash evaporator.

10. The clean production process of the amine liquid desulfurization system according to claim 1, characterized in that, After undergoing deep dehydration, the liquefied gas is further washed with a water scrubber to remove impurities and H2S gas entrained in the liquefied gas.

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