阅读说明：本技术 一种可循环再生的湿法络合铁新工艺及其专用设备 (Novel process capable of recycling and regenerating wet-process iron complex and special equipment thereof ) 是由 邹光武 曾翔鹏 曹玉虎 吕明方 王世生 邱雷 盖群 谷振国 张树梅 孙浩彬 贾明 于 2021-01-15 设计创作，主要内容包括：本发明公开了一种可循环再生的湿法络合铁新工艺,其包括：1)调配铁离子吸收剂,设备准备；2)将调配好的铁离子吸收剂装入吸收罐内；3)含有硫化氢气体的天然气先经气液分离罐后通过气体分布器均匀分散在吸收罐内；吸收罐内硫化氢气体被吸收后转变为单质硫磺,单质硫磺沉降在吸收罐底部；4)达到第一次溶液的氧化置换间隔时间后,通过连接软管连接车载络合铁氧化撬装装置,进行第一次的溶液的氧化置换；5)进行溶液的第二次的氧化置换,溶液的第二次的氧化置换完成后,进行溶液的第三次的氧化置换,以此类推。本发明便利,生成的硫磺流动性好,不易块结,吸收剂不需替换,无固废,溶液可一直循环再生利用,一次投入可长期使用。(The invention discloses a new process for recycling wet-process complex iron, which comprises the following steps: 1) preparing an iron ion absorbent, and preparing equipment; 2) filling the prepared iron ion absorbent into an absorption tank; 3) the natural gas containing hydrogen sulfide gas is uniformly dispersed in the absorption tank through the gas distributor after passing through the gas-liquid separation tank; the hydrogen sulfide gas in the absorption tank is absorbed and then converted into elemental sulfur, and the elemental sulfur is settled at the bottom of the absorption tank; 4) after the time interval of the first solution oxidation replacement is reached, connecting a vehicle-mounted complexing iron oxidation skid-mounted device through a connecting hose to carry out the first solution oxidation replacement; 5) and (4) carrying out second-time oxidative substitution on the solution, carrying out third-time oxidative substitution on the solution after the second-time oxidative substitution on the solution is finished, and the like. The invention is convenient, the generated sulfur has good fluidity, is not easy to block, the absorbent does not need to be replaced, no solid waste exists, the solution can be recycled all the time, and the sulfur can be used for a long time after being put into once.)

1. A new process for recycling and regenerating wet-process complex iron is characterized by comprising the following specific steps:

1) preparing an iron ion absorbent, and preparing equipment;

2) filling the prepared iron ion absorbent into an absorption tank, keeping the liquid level height to be 5.6-6.2 m, the reaction temperature range in the absorption tank to be 10-53 ℃, and the pressure to be 50 KPa-3.5 MPa;

3) natural gas containing hydrogen sulfide gas from a small gas field is firstly subjected to gas-liquid separation to remove entrained free water, heavy hydrocarbon and other impurities, then directly enters an absorption tank filled with an iron ion absorbent, is uniformly dispersed in the absorption tank containing the iron ion absorbent through a gas distributor, and is subjected to primary absorption treatment, hydrogen sulfide in the gas is oxidized into elemental sulfur by the absorbent, Fe3+ in the absorbent is reduced into Fe2+, hydrogen sulfide in source gas is absorbed to below 10ppmv, and water vapor and reagents carried away by the gas are captured by a purified gas separation liquid tank and then can enter a rear-end gathering and transportation pipe network; hydrogen sulfide gas in the absorption tank is absorbed and then converted into elemental sulfur, and the elemental sulfur is settled at the bottom of the absorption tank through a downcomer in the tower;

4) first oxidative displacement of the solution:

after reaching the oxidative replacement interval time of the first solution, connecting a vehicle-mounted complexing iron oxidation skid-mounted device through a connecting hose, and carrying out oxidative replacement on the first solution: pumping the pregnant solution containing 5-15% of sulfur particles from the absorption tank into a filter press through a sulfur slurry pump of a vehicle-mounted complexing iron oxidation device for pressure filtration, removing sulfur in the solution in a filter cake form, enabling the filtrate to automatically flow into an oxidation tank, introducing compressed air into the oxidation tank by using a Roots blower, uniformly dispersing the compressed air in the filtrate through a gas distributor, reacting with Fe2+ in the solution, restoring the activity of the solution again to generate Fe3+, then pumping the solution back into a field device through a barren liquor pump again to complete the oxidative replacement of the solution, removing the sulfur particles, oxidizing the reduced solution, ensuring the stability of the system solution, removing the connection between the absorption tank and the vehicle-mounted complexing iron oxidation skid device through a connecting hose after the oxidative replacement running time of the first solution is reached, and completing the first oxidative replacement of the solution;

the time between oxidative displacement of the first solution needs to be determined experimentally: sampling through a sampling port of the absorption tank after 3 days, detecting the numerical value of the ORP of the solution by using an ORP detector, if the reading of the detector is within-50 to-280, then sampling once a day for detection until the reading of the ORP detector is not within-50 to-280, recording the interval days, and setting the interval oxidative substitution time of the first solution to be 3 days + interval days;

determining the oxidation replacement running time of the first solution according to the OPR value, detecting the reading every 1 hour when the oxidation replacement of the solution is started for 3-4 hours, recording the interval time until the ORP of the solution reaches-50 to-280, and continuing the oxidation replacement for 15 min; the oxidation and replacement time of the first solution is 3-4 hours plus interval time plus 15 min;

5) and carrying out the second time of oxidative displacement of the solution according to the interval time of the oxidative displacement of the first solution and the oxidative displacement running time of the first solution, after the second time of oxidative displacement of the solution is finished, carrying out the third time of oxidative displacement of the solution according to the interval time of the oxidative displacement of the first solution and the oxidative displacement time of the first solution, and so on until the exploitation of the small gas field is finished by the new recyclable wet-process iron complexing process.

2. The new process of claim 1, wherein the iron ion absorbent comprises 20000-30000 ppm of iron ion catalyst, 25000-38000 ppm of iron ion chelating agent, 10-100000 ppm of chelating agent protecting agent, 1-1000 ppm of sulfur surfactant, 1-1000 ppm of bactericide, 0.1-1 mol/L of KOH/NaOH solution with alkali concentration and desalted water, wherein the pH of the solution is 8-10;

wherein, the iron ion catalyst needs to meet the regulation of the enterprise standard Q/0601YXR001-A-2020, the iron ion chelating agent needs to meet the regulation of the enterprise standard Q/0601YXR002-A-2020, the sulfur surfactant needs to meet the regulation of the enterprise standard Q/0601YXR003-A-2020, and the bactericide needs to meet the regulation of the enterprise standard Q/0601YXR 004-2017.

3. The new process of claim 1, wherein the apparatus is prepared to:

(1) selecting a gas-liquid separation tank which meets the source gas: the gas velocity of the source gas in the gas-liquid separation tank is selected to be 0.3-0.6 m/s, and the specific calculation is as follows:

Q=πD²/4*3600*u

wherein Q: the working condition gas amount of the source gas is m 3/h;

d: the diameter of the gas-liquid separation tank, unit m;

u: gas velocity of gas, unit m/s;

(2) selecting an absorption tank with the diameter of 3.0m and the height of 9.0 m;

(3) selecting a purification gas liquid separation tank which meets source gas: the gas velocity of the purified gas in the purified gas separating tank is selected to be 2.4-3.6 m/s, and the specific calculation is as follows:

Q=πD²/4*3600*u

wherein Q: the working condition gas amount of the source gas is m 3/h;

d: the diameter of the gas-liquid separation tank, unit m;

u: gas velocity of gas, unit m/s.

4. The special equipment for the new process of wet process complexing iron capable of recycling and regenerating as claimed in claim 1, characterized in that it comprises an absorption tank, the acid gas inlet of the absorption tank is connected with the acid gas outlet of the gas-liquid separation tank, the purified gas outlet of the absorption tank is connected with the purified gas liquid separation tank, and the absorption tank is internally provided with a gas distributor; the device also comprises a vehicle-mounted complexing iron oxidation skid-mounted device, wherein the vehicle-mounted complexing iron oxidation skid-mounted device comprises a sulfur slurry pump, a filter press, an oxidation tank, a barren solution pump, a Roots blower and a small generator which are arranged on a skid block; the sulfur slurry pump is connected with a liquid inlet of the filter press through a pipeline, a liquid outlet of the filter press is connected with a liquid inlet of the oxidation tank, a liquid outlet of the oxidation tank is connected with the barren pump, the oxidation tank is connected with the roots blower through a pipeline, and cables of the small generator are respectively connected with motors of the sulfur slurry pump, the filter press, the barren pump and the roots blower; the sulfur slurry pump is movably connected with a rich liquid outlet of the absorption tank on the gas field site through a hose, and the barren solution pump is movably connected with a barren solution inlet of the absorption tank on the gas field site through a hose.

Technical Field

The invention relates to a new process for recycling wet-process complex iron and special equipment thereof, belongs to the technical field of wet-process complex iron desulfurization processes, and is suitable for working conditions of source gas with gas flow of less than or equal to 21000m³And d, dry desulfurization of the small gas field with the daily sulfur yield less than or equal to 150 kg.

Background

At present, in the project of removing hydrogen sulfide in small gas fields in the natural gas industry and the daily sulfur yield of less than or equal to 150kg, particularly less than or equal to 70kg, the dry desulfurization mode of solid iron oxide filler is mostly adopted to remove hydrogen sulfide gas. The main reason for selecting dry desulphurization is that the small gas field has short service time, and the dry desulphurization has less investment and small occupied area compared with the traditional wet desulphurization process, and is suitable for small gas field desulphurization. However, the dry desulfurization of iron oxide also has certain problems, and the specific problems are as follows:

(1) the dry desulfurizing agent is a one-time desulfurizing agent, can not be regenerated, needs to be replaced by manpower regularly, has high replacement frequency and increases the labor intensity of the manpower;

(2) the new desulfurizer is replaced regularly, so that the investment cost of the reagent is increased, and the long-term economic investment in the gas field exploitation process is realized;

(3) the disposable desulfurizer can not be used for other purposes after being used, and can only be used as solid waste for additional treatment, otherwise, the environment pollution is easily caused, and a new environmental protection problem is possibly formed;

(4) the desulfurizer is easy to spontaneously combust in the replacement process, and certain safety risk exists.

Disclosure of Invention

The invention aims to overcome the defects of the prior art and provide a new process for recycling the wet-process complex iron and special equipment thereof.

The technical scheme provided by the invention is as follows: a new process for recycling and regenerating wet-process complex iron is characterized by comprising the following specific steps:

1) preparing an iron ion absorbent, and preparing equipment;

2) filling the prepared iron ion absorbent into an absorption tank, keeping the liquid level height to be 5.6-6.2 m, the reaction temperature range in the absorption tank to be 10-53 ℃, and the pressure to be 50 KPa-3.5 MPa;

3) natural gas containing hydrogen sulfide gas from a small gas field is firstly subjected to gas-liquid separation to remove entrained free water, heavy hydrocarbon and other impurities, then directly enters an absorption tank filled with an iron ion absorbent, is uniformly dispersed in the absorption tank containing the iron ion absorbent through a gas distributor, and is subjected to primary absorption treatment, hydrogen sulfide in the gas is oxidized into elemental sulfur by the absorbent, Fe3+ in the absorbent is reduced into Fe2+, hydrogen sulfide in source gas is absorbed to below 10ppmv, and water vapor and reagents carried away by the gas are captured by a purified gas separation liquid tank and then can enter a rear-end gathering and transportation pipe network; hydrogen sulfide gas in the absorption tank is absorbed and then converted into elemental sulfur, and the elemental sulfur is settled at the bottom of the absorption tank through a downcomer in the tower;

4) first oxidative displacement of the solution:

after reaching the oxidative replacement interval time of the first solution, connecting a vehicle-mounted complexing iron oxidation skid-mounted device through a connecting hose, and carrying out oxidative replacement on the first solution: pumping the pregnant solution containing 5-15% of sulfur particles from the absorption tank into a filter press through a sulfur slurry pump of a vehicle-mounted complexing iron oxidation device for pressure filtration, removing sulfur in the solution in a filter cake form, enabling the filtrate to automatically flow into an oxidation tank, introducing compressed air into the oxidation tank by using a Roots blower, uniformly dispersing the compressed air in the filtrate through a gas distributor, reacting with Fe2+ in the solution, restoring the activity of the solution again to generate Fe3+, then pumping the solution back into a field device through a barren liquor pump again to complete the oxidative replacement of the solution, removing the sulfur particles, oxidizing the reduced solution, ensuring the stability of the system solution, removing the connection between the absorption tank and the vehicle-mounted complexing iron oxidation skid device through a connecting hose after the oxidative replacement running time of the first solution is reached, and completing the first oxidative replacement of the solution;

the time between oxidative displacement of the first solution needs to be determined experimentally: sampling through a sampling port of the absorption tank after 3 days, detecting the numerical value of the ORP of the solution by using an ORP detector, if the reading of the detector is within-50 to-280, then sampling once a day for detection until the reading of the ORP detector is not within-50 to-280, recording the interval days, and setting the interval oxidative substitution time of the first solution to be 3 days + interval days;

determining the oxidation replacement running time of the first solution according to the OPR value, detecting the reading every 1 hour when the oxidation replacement of the solution is started for 3-4 hours, recording the interval time until the ORP of the solution reaches-50 to-280, and continuing the oxidation replacement for 15 min; the oxidation and replacement time of the first solution is 3-4 hours plus interval time plus 15 min;

5) and carrying out the second time of oxidative displacement of the solution according to the interval time of the oxidative displacement of the first solution and the oxidative displacement running time of the first solution, after the second time of oxidative displacement of the solution is finished, carrying out the third time of oxidative displacement of the solution according to the interval time of the oxidative displacement of the first solution and the oxidative displacement time of the first solution, and so on until the exploitation of the small gas field is finished by the new recyclable wet-process iron complexing process.

Further, the iron ion absorbent consists of 20000-30000 ppm of iron ion catalyst, 25000-38000 ppm of iron ion chelating agent, 10-100000 ppm of chelating agent protective agent, 1-1000 ppm of sulfur surfactant, 1-1000 ppm of bactericide, 0.1-1 mol/L of KOH/NaOH solution with alkali concentration and desalted water, wherein the pH of the solution is 8-10;

wherein, the iron ion catalyst needs to meet the regulation of the enterprise standard Q/0601YXR001-A-2020, the iron ion chelating agent needs to meet the regulation of the enterprise standard Q/0601YXR002-A-2020, the sulfur surfactant needs to meet the regulation of the enterprise standard Q/0601YXR003-A-2020, and the bactericide needs to meet the regulation of the enterprise standard Q/0601YXR 004-2017.

Further, the apparatus prepares:

(1) selecting a gas-liquid separation tank which meets the source gas: the gas velocity of the source gas in the gas-liquid separation tank is selected to be 0.3-0.6 m/s, and the specific calculation is as follows:

Q=πD²/4*3600*u

wherein Q: the working condition gas amount of the source gas is m 3/h;

d: the diameter of the gas-liquid separation tank, unit m;

u: gas velocity of gas, unit m/s;

(2) selecting an absorption tank with the diameter of 3.0m and the height of 9.0 m;

(3) selecting a purification gas liquid separation tank which meets source gas: the gas velocity of the purified gas in the purified gas separating tank is selected to be 2.4-3.6 m/s, and the specific calculation is as follows:

Q=πD²/4*3600*u

wherein Q: the working condition gas amount of the source gas is m 3/h;

d: the diameter of the gas-liquid separation tank, unit m;

u: gas velocity of gas, unit m/s.

Furthermore, the special equipment for the new process of the circularly regenerated wet-process iron complex is characterized by comprising an absorption tank, wherein an acid gas inlet of the absorption tank is connected with an acid gas outlet of a gas-liquid separation tank, a purified gas outlet of the absorption tank is connected with a purified gas liquid separation tank, and a gas distributor is arranged in the absorption tank; the device also comprises a vehicle-mounted complexing iron oxidation skid-mounted device, wherein the vehicle-mounted complexing iron oxidation skid-mounted device comprises a sulfur slurry pump, a filter press, an oxidation tank, a barren solution pump, a Roots blower and a small generator which are arranged on a skid block; the sulfur slurry pump is connected with a liquid inlet of the filter press through a pipeline, a liquid outlet of the filter press is connected with a liquid inlet of the oxidation tank, a liquid outlet of the oxidation tank is connected with the barren pump, the oxidation tank is connected with the roots blower through a pipeline, and cables of the small generator are respectively connected with motors of the sulfur slurry pump, the filter press, the barren pump and the roots blower; the sulfur slurry pump is movably connected with a rich liquid outlet of the absorption tank on the gas field site through a hose, and the barren solution pump is movably connected with a barren solution inlet of the absorption tank on the gas field site through a hose.

The invention has the beneficial effects that: the novel process meets the requirement of convenience for small gas field exploitation, and meets the requirement of absorption of hydrogen sulfide gas in source gas by increasing the concentration of the traditional complex iron absorbent; meanwhile, the absorbent does not need to continuously blow oxidizing air, hydrogen sulfide in the gas can be continuously converted into sulfur under the condition that the solution is not circulated, and the generated sulfur has good fluidity and is not easy to block. According to the time designed by different projects, the solution is oxidized and sulfur is filtered regularly without replacing an absorbent, no solid waste is generated, the solution can be recycled all the time, the whole reaction process can be operated under the conditions of low temperature and low pressure, and the solution can be used for a long time after being put into use once. The invention can use the regenerated wet process complex iron process equipment circularly, avoid the defects of large equipment investment, large occupied area and overlarge investment on small gas fields of the traditional wet process complex iron project; overcomes the defects that the desulfurizer needs to be continuously updated and replaced in the dry desulfurization, solid waste is generated to cause secondary pollution, the labor intensity is high, the investment is continuous, and the like; meanwhile, the equipment is movable, the convenience that a plurality of gas fields can share one piece of equipment is met, the equipment can be used for a long time, the equipment investment in the early stage is reduced, the occupied area is reduced, the absorbent does not need to be frequently replaced in the later stage, the absorbent is put into recycling and recycling once, the gas fields can be conveniently moved to other new wells for reuse after being exploited, and the convenience and the flexibility of the equipment are improved; the small generator of the equipment saves high consumption of public works and solves the problems of inconvenient power supply in partial areas and the like. The recyclable wet process complexing iron process equipment is designed in a skid-mounted manner, can be moved on site through a vehicle, can be transported by one person on site, is simple in recycling operation of the solution due to oxidation and regeneration of the solution, can be operated by one person, greatly reduces the manual strength, and replaces the reagent replacement frequency and cost of a dry method with recycling property of the solution. The replacement interval time required by replacing the solution in each small gas field is respectively designed according to the daily sulfur yield of the small gas field, and only one person needs to drive the vehicle regularly for replacement, so that the method is very favorable for the exploitation of the small gas field.

Drawings

FIG. 1 is a schematic structural diagram of a recyclable wet complex iron process apparatus according to the present invention.

Detailed Description

The following detailed description of embodiments of the invention refers to the accompanying drawings in which:

a new process for recycling and regenerating wet-process complexing iron specifically comprises the following specific steps:

1) preparing an iron ion absorbent:

20000-30000 ppm of iron ion catalyst, 25000-38000 ppm of iron ion chelating agent, 10-100000 ppm of chelating agent protective agent, 1-1000 ppm of sulfur surfactant, 1-1000 ppm of bactericide, 0.1-1 mol/L of KOH/NaOH solution with alkali concentration and desalted water, wherein the pH of the solution is 8-10.

Wherein, the iron ion catalyst needs to meet the regulation of the enterprise standard Q/0601YXR001-A-2020, the iron ion chelating agent needs to meet the regulation of the enterprise standard Q/0601YXR002-A-2020, the sulfur surfactant needs to meet the regulation of the enterprise standard Q/0601YXR003-A-2020, and the bactericide needs to meet the regulation of the enterprise standard Q/0601YXR 004-2017.

Preparing equipment:

(1) selecting a gas-liquid separation tank which meets the source gas: the gas velocity of the source gas in the gas-liquid separation tank is selected to be 0.3-0.6 m/s, and the specific calculation is as follows:

Q=πD²/4*3600*u

wherein Q: the working condition gas amount of the source gas is m 3/h;

d: the diameter of the gas-liquid separation tank, unit m;

u: gas velocity of gas, unit m/s;

(2) selecting an absorption tank with the diameter of 3.0m and the height of 9.0 m;

(3) selecting a purification gas liquid separation tank which meets source gas: the gas velocity of the purified gas in the purified gas separating tank is selected to be 2.4-3.6 m/s, and the specific calculation is as follows:

Q=πD²/4*3600*u

wherein Q: the working condition gas amount of the source gas is m 3/h;

d: the diameter of the gas-liquid separation tank, unit m;

u: gas velocity of gas, unit m/s;

2) filling the prepared iron ion absorbent into an absorption tank, keeping the liquid level height to be 5.6-6.2 m, the reaction temperature range in the absorption tank to be 10-53 ℃, and the pressure to be 50 KPa-3.5 MPa;

3) natural gas containing hydrogen sulfide gas from a small gas field is firstly subjected to gas-liquid separation to remove entrained free water, heavy hydrocarbon and other impurities, then directly enters an absorption tank filled with an iron ion absorbent, is uniformly dispersed in the absorption tank containing the iron ion absorbent through a gas distributor, and is subjected to primary absorption treatment, hydrogen sulfide in the gas is oxidized into elemental sulfur by the absorbent, Fe3+ in the absorbent is reduced into Fe2+, hydrogen sulfide in source gas is absorbed to below 10ppmv, and water vapor and reagents carried away by the gas are captured by a purified gas separation liquid tank and then can enter a rear-end gathering and transportation pipe network; the hydrogen sulfide gas in the absorption tank is absorbed and then converted into elemental sulfur, and the elemental sulfur is settled at the bottom of the absorption tank through a downcomer in the tower.

4) First oxidative displacement of the solution:

after reaching the oxidative replacement interval time of the first solution, connecting a vehicle-mounted complexing iron oxidation skid-mounted device through a connecting hose, and carrying out oxidative replacement on the first solution: pumping the pregnant solution containing 5-15% of sulfur particles from the absorption tank into a filter press through a sulfur slurry pump of a vehicle-mounted complexing iron oxidation device for pressure filtration, removing sulfur in the solution in a filter cake form, enabling the filtrate to automatically flow into an oxidation tank, introducing compressed air into the oxidation tank by using a Roots blower, uniformly dispersing the compressed air in the filtrate through a gas distributor, reacting with Fe2+ in the solution, restoring the activity of the solution to generate Fe3+, then pumping the solution back into a field device through a barren liquor pump again, completing the oxidation replacement of the solution, removing sulfur particles, oxidizing the reduced solution, ensuring the stability of the system solution, removing the connection of the absorption tank and the vehicle-mounted complexing iron oxidation skid device through a connecting hose after the oxidation replacement running time of the first solution is reached, and completing the first oxidation replacement of the solution;

the time between oxidative displacement of the first solution needs to be determined experimentally: sampling through a sampling port of the absorption tank after 3 days, detecting the numerical value of the ORP of the solution by using an ORP detector, if the reading of the detector is within-50 to-280, then sampling once a day for detection until the reading of the ORP detector is not within-50 to-280, recording the interval days, and setting the interval time of the first solution as 3 days + interval days;

determining the oxidation replacement running time of the first solution according to the OPR value, detecting the reading every 1 hour when the oxidation replacement of the solution is started for 3-4 hours, recording the interval time until the ORP of the solution reaches-50 to-280, and continuing the oxidation replacement for 15 min; the running time of the oxidation and replacement of the first solution is 3-4 hours plus the interval time plus 15 min.

5) And carrying out the second time of oxidative displacement of the solution according to the interval time of the oxidative displacement of the first solution and the oxidative displacement running time of the first solution, after the second time of oxidative displacement of the solution is finished, carrying out the third time of oxidative displacement of the solution according to the interval time of the oxidative displacement of the first solution and the oxidative displacement time of the first solution, and so on until the exploitation of the small gas field is finished by the new recyclable wet-process iron complexing process.

As shown in figure 1, the recyclable wet process complex iron process equipment comprises a vehicle-mounted complex iron oxidation skid-mounted device, wherein the vehicle-mounted complex iron oxidation skid-mounted device comprises a sulfur slurry pump 5, a filter press 6, an oxidation tank 7, a lean liquid pump 8, a Roots blower 9 and a small-sized generator 10 which are arranged on a skid block. The sulfur slurry pump 5 is connected with a liquid inlet of the filter press 6 through a pipeline, a liquid outlet of the filter press 6 is connected with a liquid inlet of the oxidation tank 7, a liquid outlet of the oxidation tank 7 is connected with the barren liquor pump 8, the oxidation tank 7 is connected with the roots fan 9 through a pipeline, and a cable of the small generator 10 is respectively connected with motors of the sulfur slurry pump 5, the filter press 6, the barren liquor pump 8 and the roots fan 9. The sulfur slurry pump 5 is movably connected with a rich liquid outlet of the absorption tank 2 on the gas field site through a hose 4, the barren liquid pump 8 is movably connected with a barren liquid inlet of the absorption tank 2 on the gas field site through the hose 4, an acid gas inlet of the absorption tank 2 is connected with an acid gas outlet of the gas-liquid separation tank 1, and a purified gas outlet of the absorption tank 2 is connected with the purified gas liquid separation tank 3. The absorption tank 2 is internally provided with a gas distributor 11.

The absorbent in the absorption tank 2 is periodically connected with a movable complexing iron oxidation device through a hose 4 to circulate the solution, and the solution is oxidized while sulfur particles produced in the filtered solution are oxidized to restore the activity of the solution.

The absorbent in the above embodiments can also be other existing absorbent containing chelated iron ions, and the above embodiments are only used for describing the preferred embodiments of the present invention, and are not intended to limit the scope of the present invention, and various modifications and improvements made to the technical solution of the present invention by those skilled in the art without departing from the spirit of the present invention are intended to fall within the protection scope defined by the claims of the present invention.