CN112295382B - Absorption tower for treating hydrogen sulfide gas by wet oxidation method - Google Patents
Absorption tower for treating hydrogen sulfide gas by wet oxidation method Download PDFInfo
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- CN112295382B CN112295382B CN201910712330.6A CN201910712330A CN112295382B CN 112295382 B CN112295382 B CN 112295382B CN 201910712330 A CN201910712330 A CN 201910712330A CN 112295382 B CN112295382 B CN 112295382B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—Hydrogen sulfide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/10—Particle separators, e.g. dust precipitators, using filter plates, sheets or pads having plane surfaces
- B01D46/12—Particle separators, e.g. dust precipitators, using filter plates, sheets or pads having plane surfaces in multiple arrangements
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
- C01B17/05—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by wet processes
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/103—Sulfur containing contaminants
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
- B01D2256/245—Methane
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/541—Absorption of impurities during preparation or upgrading of a fuel
Abstract
The invention belongs to the technical field of sulfur recovery, and particularly relates to an absorption tower for treating hydrogen sulfide gas by using a wet oxidation method. The device is characterized in that a mechanical stirring device is arranged in an absorption tower cylinder body, and comprises a transmission part, a sealing part, a stirring shaft and blades; the transmission component is arranged at the axis of the top end of the cylinder body, is isolated from the inner cavity of the cylinder body through a sealing element and drives the stirring shaft to rotate in the inner cavity of the cylinder body; the stirring shaft is fixedly connected with a plurality of layers of blades from top to bottom, and the blades rotate around the axis of the cylinder body to stir the filler. According to the absorption tower provided by the invention, when the pressure of an instrument in the tower is increased, the blades on the stirring shaft are rotated left and right, steam is sprayed from the steam coil pipe for spray cleaning, sulfur particles can be cleaned, the filler layer is loosened, two wire mesh filters are additionally arranged outside the air outlet of the absorption tower, one is opened and the other is reserved, and the cleaning is convenient.
Description
Technical Field
The invention belongs to the technical field of sulfur recovery, relates to sulfur recovery in petroleum refining, coal chemical industry and natural gas purification industry, and particularly relates to an absorption tower for treating hydrogen sulfide gas by using a wet oxidation method.
Background
Both natural gas and refinery tail gas contain a large amount of hydrogen sulfide, and methods for removing hydrogen sulfide and other sulfur-containing gases are more, but wet desulphurization is more mature.
The wet desulphurization is mainly based on the traditional amine-Claus sulfur recovery and tail gas treatment process, the process flow of the method is long, the equipment investment is large, the main treatment gas flow is large, and the gas source with high sulfur content is the leading process of the current sulfur recovery, and has better economy. Since natural gas or refinery sulfur-containing gas sources are very different, amine desulfurization is not suitable when the gas with small gas source amount and low gas sulfur content (less than 1%) is treated. For example, small-scale petrochemical plants or remote single oil and gas wells have low sulfur content and are located in geographical places, and the cost of pipeline transportation makes the traditional amine method centralized desulfurization treatment process difficult to apply. In order to meet the requirements of different gas desulfurization and purification processes, the liquid-phase direct conversion desulfurization technology is gradually mature.
Liquid phase direct conversion desulfurization, also known as wet oxidation desulfurization, refers to a gas desulfurization process in which hydrogen sulfide in industrial gas is oxidized to elemental sulfur using a solution containing an oxygen carrier, and the reduced oxidant is regenerated by air to restore its oxidizing ability. It has the characteristics of less investment, short flow, low energy consumption, The sulfur content of the effluent gas is classified by the oxygen carrier used; mainly comprises an iron method and a vanadium method. Currently, the iron method is the most widely applied at home and abroad. The basic principle is as follows: iron is a polyvalent metal element, and in the direct conversion process, ferric iron is often used as H 2 S in the presence of an oxidizing agent such as 2 S is oxidized into elemental sulfur and is converted into ferrous iron, and air regeneration is used for oxidizing into ferric iron.
The reactions that occur: 2Fe 3+ +HS - ＝2Fe 2+ +S+H + ，
Fe 2+ The regeneration reaction of (1) is 2Fe 2+ +1/2O 2 +2H + ＝2Fe 3+ +H 2 O；
The technological process is as shown in fig. 1 and fig. 2, natural gas or refinery gas is pressurized by a fan and then fed into a Venturi mixer, the natural gas or refinery gas is mixed with part of ironic agent barren liquor from a circulating pump and then fed into an absorption tower, cylindrical metal pall ring packing is arranged in the absorption tower, ironic agent barren liquor spraying is arranged at the upper part of the absorption tower, H is removed by gas-liquid contact 2 S, the desulfurized gas escapes from the upper part of the absorption tower and enters the next treatment procedure, and H in the gas is removed 2 The S content is less than 10 ppm. The solution after absorbing the hydrogen sulfide contains particle sulfur simple substance, and is sent into an oxidation regeneration tank by a circulating pump for aeration regeneration, and part of the solution returns to the absorption tower. Wherein the iron agent solution returned to the oxidation regeneration tank contains a large amount of granular sulfur, and the sulfur in the iron agent slurry is sent to a sulfur slurry processor after reaching a certain concentration.
One of the main devices in the process is a hydrogen sulfide absorption tower. Solid sulfur particles are generated in the absorption tower, and the adhesion to the filler and the wall of the container is strong. Under the conditions that the fluctuation of sulfur content from a gas phase source is large, the process parameters are unstable and the like, the growth speed of sulfur monomer crystal grains in the tower is high, the blockage of internal parts of the absorption tower such as a filler, a wire mesh demister at the top, a discharge pipe at the bottom and the like is easily caused, once the internal parts of the tower are blocked, the pressure drop is increased rapidly, the device must be stopped, the filler is disassembled to clean the internal parts of the tower, and a pipeline is dredged, and the sulfur blockage is the biggest defect of a wet oxidation reduction desulfurization method and is also an important reason for limiting the large-scale popularization of the wet oxidation reduction desulfurization method.
Disclosure of Invention
Aiming at the problems in the prior art, the invention aims to provide the absorption tower for treating the hydrogen sulfide gas by using the wet oxidation method, change the internal structure of the absorption tower, reduce the blocking frequency and ensure the long-period stable operation of the device.
In order to achieve the purpose, the invention is realized by adopting the following technical scheme:
the invention provides an absorption tower for treating hydrogen sulfide gas by using a wet oxidation method, which comprises a cylindrical barrel, wherein the top of the barrel is provided with a gas outlet, one or more than two iron agent solution inlets are arranged above the inside of the barrel, a plurality of support grid plates are arranged below the iron agent solution inlets, fillers are placed on the support grid plates, a gas-liquid inlet pipe is arranged at the lower part of the barrel, a discharging pipe is arranged at the bottom of the barrel, a mechanical stirring device is arranged inside the barrel, and the mechanical stirring device comprises a transmission part, a sealing part, a stirring shaft and blades; the transmission component is arranged at the top end of the cylinder body, is isolated from the inner cavity of the cylinder body through a sealing element and drives the stirring shaft to rotate in the inner cavity of the cylinder body; the stirring shaft is fixedly connected with a plurality of layers of blades from top to bottom, and the blades rotate around the axis of the cylinder body to stir the filler.
Furthermore, a plurality of stirring shaft support frames are fixed in the inner cavity of the cylinder body, and the stirring shaft support frames are connected with the stirring shaft in a sliding mode through sliding bearings.
Furthermore, the paddles in each section of the packing are three layers, each layer of the paddles comprises three paddle tubes which are radially distributed, the included angle between every two layers of the paddle tubes is 120 degrees, and the included angle between every two nine paddle tubes of the three layers of the paddles is 30 degrees.
Furthermore, the filler is spherical, the diameter of the hollow part inside the filler is 35-40 mm, the filler is made of stainless steel or 150 ℃ resistant plastic, and the thickness of each layer of the filler is not more than 2000 mm.
Furthermore, the paddle tube is made of a corrosion-resistant hard material DN 14-DN 20.
Furthermore, the discharging pipe is a cross straight pipe, two ends of the straight pipe are sealed by flanges, and a steam sleeve is arranged on the outer side of the discharging pipe.
Furthermore, a steam coil is further arranged at the top of each support grid plate, the diameter of a pipeline of the steam coil is DN 50-DN 100, 12-20 spray heads are installed on the steam coil, and the installation angle of each spray head faces to the intersection of the filler and the inner wall of the cylinder.
Further, the air outlet is movably connected with one or more than two wire mesh filters.
Furthermore, a cylindrical framework which is opened towards the air inlet direction is arranged in the wire mesh filter, and the framework is provided with an opening 
Two layers of stainless steel wire meshes are laid on the outer side of the framework, the inner layer is 40 meshes, the outer layer is 20 meshes, and the framework and the stainless steel wire meshes are of an integral structure.
Further, a gas-liquid mixture distributor is arranged at the gas-liquid inlet pipe and is in a disc shape, the axis of the gas-liquid mixture distributor coincides with that of the cylinder, the diameter of the gas-liquid mixture distributor is one third of that of the cylinder, and round holes are uniformly formed in the bottom and the side face of the gas-liquid mixture distributor.
By adopting the technical scheme, the invention has the beneficial effects that:
after the absorption tower provided by the invention is improved, the device is stopped due to sulfur particle blockage, the maintenance frequency of the absorption tower is obviously reduced, and the previous set of absorption tower with the length of 1200m 3 The device of the sulfur-containing gas treatment capacity is shut down due to the fact that sulfur blocks the device for 2-3 months, the absorption tower filler is cleaned, the wire mesh demister is replaced, and the problem of sulfur accumulation in a pipeline is solved. According to the absorption tower provided by the invention, when the pressure of an instrument in the tower is increased, the blades on the stirring shaft are rotated left and right, steam is sprayed from the steam coil pipe for spray cleaning, sulfur particles can be cleaned, the filler layer is loosened, two wire mesh filters are additionally arranged outside the air outlet of the absorption tower, one is opened and the other is reserved, and the cleaning is convenient. The absorption tower is maintained once in 1 year under normal conditions, and long-period stable operation of the device is realized.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention.
In the drawings:
FIG. 1 is a flow diagram of a conventional wet oxidation desulfurization process for hydrogen sulfide gas;
FIG. 2 is a schematic view of the structure of the conventional absorption column of FIG. 1;
FIG. 3 is a schematic structural diagram of an absorption tower for treating hydrogen sulfide gas by wet oxidation according to the present invention;
FIG. 4 is a schematic structural view of a wire mesh filter according to the present invention;
FIG. 5 is an enlarged view of a portion of the structure of FIG. 4;
FIG. 6 is a top view of an upper paddle of each section of packing layer of the present invention;
FIG. 7 is a top view of each section of a lower paddle of the packing layer of the present invention;
FIG. 8 is a top view of a layer paddle in each section of packing layer of the present invention;
FIG. 9 is a top view of the agitator shaft support bracket of the present invention;
FIG. 10 is a top view of the gas-liquid mixture distributor of the present invention;
the labels in the figure are as follows: the device comprises a skirt support 1, a discharge pipe 2, a steam sleeve 201, a cylinder 3, a gas-liquid mixture distributor 4, a stirring shaft support 5, a stirring shaft 6, a blade 7, a blade pipe 701, a supporting grid plate 8, an iron agent solution inlet 9, a filler 10, a sealing element 11, a transmission part 12, a pressure display meter 13, a gas-liquid inlet pipe 14, a wire mesh demister 15, a steam coil 16, a gas outlet 17, a wire mesh filter 18, a framework 1801 and a stainless steel wire mesh 1802.
Detailed Description
In the description of the present invention, it should be noted that the terms "vertical", "upper", "lower", "horizontal", and the like indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of describing the present invention and simplifying the description, but do not indicate or imply that the referred device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention.
The invention will be further explained with reference to the drawings.
As shown in figures 3-10, the absorption tower for treating hydrogen sulfide gas by wet oxidation provided by the invention comprises a cylindrical barrel 3, wherein the top of the barrel is provided with an air outlet 17, one or more than two ironic solution inlets 9 are arranged above the inside of the barrel, a plurality of supporting grid plates 8 are arranged below the ironic solution inlets, packing 10 are placed on the supporting grid plates, the lower part of the barrel is provided with a gas-liquid inlet pipe 14, and the bottom of the barrel is provided with a discharging pipe 2. A skirt 1 is arranged below the cylinder body.
A mechanical stirring device is arranged in the cylinder body and comprises a transmission part 12, a sealing part 11, a stirring shaft 6 and blades 7; the transmission component is arranged at the axis of the top end of the cylinder body, is isolated from the inner cavity of the cylinder body through a sealing element and drives the stirring shaft to rotate in the inner cavity of the cylinder body; the stirring shaft is fixedly connected with a plurality of layers of blades from top to bottom, and the blades rotate around the axis of the cylinder body to stir the filler.
The transmission part comprises a motor and a transmission, and the motor and the transmission are controlled by the DCS controller by common means in the prior art. Pressure sensors are arranged between the tower top and each section of packing, and a pressure display meter 13 is arranged on the outer side of the cylinder body and used for displaying the air pressure in the tower body.
A plurality of stirring shaft support frames 5 are fixed in the inner cavity of the cylinder body and are in sliding connection with the stirring shaft through sliding bearings.
The paddle in each section of packing is three layers, each layer of paddle comprises three paddle tubes 701 distributed in a radial mode, the included angle between every two layers of paddle tubes is 120 degrees, and the included angle between every two nine paddle tubes of the three layers of paddles is 30 degrees.
The paddle tube is made of a corrosion-resistant hard material DN 14-DN 20.
The filler is spherical, the diameter of the hollow part inside the filler is 35 mm-40 mm, the filler is made of stainless steel or 150 ℃ resistant plastic, and the thickness of each layer of the filler is not more than 2000 mm.
When the DCS controller detects that the air pressure in the tower is higher than a set value through the pressure sensor, the motor and the transmission are controlled to work, the motor drives the stirring shaft to rotate in a clockwise and anticlockwise direction in a circulating mode, the blades are in a swinging state when viewed from the axial direction, each blade pipe swings left and right at a low speed in the respective direction, the swinging angle is smaller than 120 degrees, and the swinging times per minute are not more than 6 times. The sulfur particles between the fillers are loosened and fall off by the left and right circular rotation of the paddle pipe.
The discharging pipe is a cross straight pipe, both ends of the straight pipe are sealed by flanges, and when the discharging pipe section is blocked by sulfur particles, the flanges can be detached to remove impurities in the pipe by using a cleaner, so that the problem that the traditional bent pipe is difficult to clean after being blocked is solved. The outer side of the discharging pipe is provided with a welding steam sleeve 201, and steam is introduced into the steam sleeve, so that the temperature of the pipe wall of the discharging pipe exceeds 120 ℃ and exceeds the melting point of sulfur, and the blocking of the discharging pipe is prevented.
The top of each support grid plate is also provided with a steam coil 16, the diameter of a pipeline of the steam coil is DN 50-DN 100, 12-20 spray heads are arranged on the steam coil, and the installation angle of the spray heads faces to the intersection of the filler and the inner wall of the cylinder body. When the filler and the tower wall of the absorption tower are gathered with a lot of micro-sulfur particles, the absorption tower cannot normally operate, the monomer sulfur on the tower wall and the filler can be melted and washed by spraying steam, and the sulfur between the loosened filler layers can be washed away by the steam.
The air outlet is movably connected with more than two wire mesh filters 18. The stainless steel wire mesh filter in the absorption tower is changed into an independent device outside the tower, so that the maintenance and shutdown times of tower equipment are reduced. When the wire mesh filter is blocked, the whole filter can be taken out for cleaning. Reaction gas enters from the upper part of the silk screen filter, and exits from the bottom, more than two devices can ensure the start-up and standby states, and sulfur is switched to be cleaned after being blocked, so that the shutdown of the whole device is avoided.
The top on the silk screen filter is a quick-opening flange structure, a cylindrical framework 1801 with the thickness of 3mm is arranged in the silk screen filter, the opening of the framework faces to the air inlet of the silk screen filter, the quick-opening flange structure covers the opening of the cylindrical framework, and the framework is provided with an opening
The through holes are densely distributed, two layers of stainless steel wire nets 1802 are laid on the outer side of the framework, one layer is arranged on the inner side of the framework and the other layer is arranged on the outer side of the framework, the inner layer is 40 meshes, the outer layer is 20 meshes, the framework and the stainless steel wire nets are of an integral structure, and all parts need to be welded in a stainless steel sealing mode.
The gas-liquid mixture distributor 4 is arranged at the gas-liquid inlet pipe and is disc-shaped, the axis of the gas-liquid mixture distributor is coincident with the axis of the cylinder, the diameter of the gas-liquid mixture distributor is one third of the diameter of the cylinder, and the height of the gas-liquid mixture distributor is 200-400 mm. Round holes with the diameter of 4 mm-6 mm are uniformly arranged at the bottom and the side surface, the distance between the holes is 10mm, and the round holes are uniformly distributed. The material is 316 stainless steel material, and the wall thickness is 3 mm-4 mm. The material enters from the center of the upper part of the disc and exits from the side and the bottom, and the gas-liquid mixture distributor enables the feeding to be distributed more uniformly in the tower.
Example 1
A certain refinery enterprise is provided with a set of liquid-phase direct oxidation-reduction desulfurization device, and the amount of the acid gas to be treated is 6000Nm 3 The hydrogen sulfide content is 0.1 percent, and the process flow is as follows: pressurizing the acid gas with the temperature of 40 ℃ by a fan, then feeding the acid gas and the iron agent slurry into a Venturi mixer, mixing the acid gas and the iron agent slurry, feeding the gas-liquid mixture into a gas-liquid mixture distributor in an absorption tower, spraying the gas-liquid mixture out of the gas-liquid mixture distributor in the tower, ascending in the tower, feeding the gas-liquid mixture into a packing layer, and feeding H in a gas phase 2 S is mixed with the iron agent slurry which contains oxygen carrier again to remove H in the natural gas 2 S is oxidized into particle simple substance S, the simple substance S falls to the bottom of the tower along with the iron agent slurry and is discharged through the discharging pipe. Removal of H 2 And (3) feeding the acidic gas after S into a wire mesh filter through the top of the absorption tower, then feeding the acidic gas into an incinerator, feeding the absorbed solution carrying the particle simple substance S into an oxidation regeneration tank by a circulating pump for aeration regeneration, returning part of the solution to the absorption tower, feeding the slurry into a belt filter after the sulfur reaches a certain concentration, and returning the filtrate to the oxidation regeneration tank. The sulfur cake from the filter is accumulated to a certain amount and then enters a sulfur melting kettle for refining, and H in the treated tail gas 2 The S content is less than 10 ppm.
The absorption tower is the key equipment of the device, the diameter of the absorption tower of the device is 800mm, the height is 10 meters, three sections of fillers are 40mm, the fillers are hollow and externally filled with solid round stainless steel, pressure gauges are respectively arranged between the tower top and each section of fillers, a 22KW three-phase motor is arranged on the tower top to drive a stirring shaft and blades, a wire mesh demister is arranged outside the tower, a discharging pipe at the bottom is additionally provided with steam heat tracing and the like, and the device does not block the tower when normally operating for one year.
Particularly, after the mechanical stirring device is additionally arranged, when the pressure difference between the top pressure and the bottom pressure exceeds 350pa, the mechanical stirring device is started, the loosening time is 30min each time, the motor drives the stirring shaft to rotate left and right in the clockwise direction and the anticlockwise direction through a DCS operation program, so that the blades are in a swinging state in the axial direction, each blade rotates left and right at a low speed in the respective direction, the rotation angle is less than 120 degrees, and the rotation frequency is not more than 6 times per minute. The round fillers are staggered with each other by rotating the blades left and right, and sulfur particles between the fillers loosen and fall off. The steam coil pipe at the bottom of the filler is started by the mechanical stirring device to start to spray steam, sweep sulfur between the round fillers, and clean the surfaces of the fillers.
Two wire mesh filters connected in parallel are arranged outside the air outlet of the absorption tower, and one wire mesh filter is provided with one opening. If the wire mesh filter is blocked by sulfur, the pressure of the system is increased, the valve of the air outlet is switched to enter the spare wire mesh filter, and the blocked wire mesh filter is overhauled without stopping working. The bottom discharging pipe is welded with a steam jacket, and the temperature of the pipe wall of the discharging pipe exceeds 120 ℃ and exceeds the melting point of sulfur, so that the blocking of the discharging pipe is prevented.
Example 2
6000Nm of natural gas production of a certain oil and gas well 3 The hydrogen sulfide content was 1.46%, and desulfurization was carried out by direct oxidation-reduction. The natural gas enters the raw material gas separation tank after being pressurized by the fan, and after condensate liquid is separated out, the condensate liquid is mixed with iron ion liquid desulphurization barren solution through the Venturi mixer and then enters the lower part of the absorption tower. In the absorption tower, iron ion liquid desulfurizing agent barren liquor is divided into two paths and respectively enters the absorption tower from a gas-liquid mixture distributor, and is sprayed from the upper part of the absorption tower through an iron agent solution inlet to enter the absorption tower to be in full contact reaction with sulfur-containing waste gas. The sulfur-containing waste gas is in reverse contact with the desulfurization barren solution in the spherical random packing in the absorption tower, the hydrogen sulfide in the natural gas is absorbed and reacts, most of the absorbed hydrogen sulfide is converted into sulfur with tiny particles, and the purified gas flows out from a gas outlet at the upper part of the absorption tower and is converged into a natural gas main pipe.
And the iron ion liquid desulfurizing agent in the absorption tower absorbs hydrogen sulfide to form ion liquid desulfurizing rich liquid, and the desulfurizing rich liquid is pressurized by a rich liquid circulating pump, mixed with purified air (air) and then enters an oxidation regeneration tank. The ion liquid desulfurizing agent rich liquid and the purified air enter the lower part of the oxidation regeneration tank through the gas-liquid distributor. In the oxidation regeneration tank, the purified air and the desulfurization rich solution continue to generate oxidation regeneration reaction in a bubbling mixing mode. The residual small amount of sulfide in the desulfurization rich solution is completely oxidized into sulfur. The rich solution of the desulfurizer is regenerated into lean solution, and redundant air is discharged through an evacuation port at the top of the oxidation regeneration tank. The sulfur in the oxidation regeneration tank floats upwards along with purified wind to form sulfur foam which flows into a sulfur settling tank for further treatment.
The key equipment of the device is an absorption tower, the diameter is 600mm, the height is 8 meters, 2 sections of fillers are filled, the fillers are hollow and solid round stainless steel with the diameter of 32mm, pressure gauges are respectively arranged between the top of the tower and each section of fillers, a 18.5KW three-phase motor is arranged at the top of the tower to drive a mechanical stirring device, a wire mesh demister is arranged outside the tower, and a discharging pipe at the bottom is additionally provided with steam heat tracing.
When the pressure difference between the top pressure and the bottom pressure exceeds 350pa, the mechanical stirring device is started, the gas contains high sulfur content, the loosening time is 40min each time, the motor drives the stirring shaft to rotate left and right in the clockwise direction and the anticlockwise direction through a DCS operation program, so that the blades are in a swinging state in the axial direction, each blade slowly rotates left and right in the respective direction, the rotation angle is less than 120 degrees, and the rotation frequency is 6 per minute. The round fillers are staggered with each other by rotating the blades left and right, and sulfur particles between the fillers loosen and fall off. The steam coil pipe at the bottom of the filler is started by the mechanical stirring device to start to spray steam, sweep sulfur between the round fillers, and clean the surfaces of the fillers.
Two wire mesh filters connected in parallel are arranged outside the gas outlet of the desulfurization system, and one wire mesh filter is provided with one filter. If the wire mesh filter is blocked by sulfur, the pressure of the system is increased, the valve of the air outlet is switched to enter the spare wire mesh filter, and the blocked wire mesh filter is overhauled without stopping working. The bottom discharging pipe is welded with a steam jacket, and the temperature of the pipe wall of the discharging pipe exceeds 120 ℃ and exceeds the melting point of sulfur, so that the blocking of the discharging pipe is prevented.
It should be understood that the above description is only a preferred embodiment of the present invention, and not intended to limit the present invention, and although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications and equivalents may be made in the technical solutions described in the foregoing embodiments, or some technical features may be substituted. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. An absorption tower for treating hydrogen sulfide gas by using a wet oxidation method comprises a cylindrical barrel (3), wherein a gas outlet (17) is formed in the top of the barrel (3), one or more than two iron agent solution inlets (9) are formed in the upper portion inside the barrel (3), a plurality of support grid plates (8) are arranged below the iron agent solution inlets (9), fillers (10) are placed on the support grid plates (8), a gas-liquid inlet pipe (14) is formed in the lower portion of the barrel (3), and a discharging pipe (2) is arranged at the bottom of the barrel (3), and the absorption tower is characterized in that a mechanical stirring device is arranged inside the barrel (3) and comprises a transmission part (12), a sealing part (11), a stirring shaft (6) and blades (7); the transmission component (12) is arranged at the top end of the cylinder body (3), the transmission component (12) is isolated from the inner cavity of the cylinder body (3) through the sealing element (11), and the transmission component (12) drives the stirring shaft (6) to rotate in the inner cavity of the cylinder body (3); the stirring shaft (6) is fixedly connected with a plurality of layers of blades (7) from top to bottom, the blades (7) rotate around the axis of the cylinder body (3), and the filler (10) is stirred;
A plurality of stirring shaft support frames (5) are fixed in the inner cavity of the cylinder body (3), and the stirring shaft support frames (5) are in sliding connection with the stirring shaft (6) through sliding bearings;
the top of each supporting grid plate (8) is also provided with a steam coil (16), the diameter DN 50-DN 100 of the pipeline of the steam coil (16) is 12-20 nozzles, and the installation angle of the nozzles faces to the intersection of the filler (10) and the inner wall of the barrel body (3).
2. The absorption tower for treating hydrogen sulfide gas by using the wet oxidation method according to claim 1, wherein the number of the blades (7) in each section of the packing (10) is three, each layer of the blades (7) comprises three radially distributed blade tubes (701), the included angle between every two layers of the blade tubes (701) is 120 degrees, and the included angle between every two layers of the blade tubes (701) of the three layers of the blades (7) is 30 degrees.
3. The absorption tower for treating the hydrogen sulfide gas by the wet oxidation method as claimed in claim 2, wherein the filler (10) is spherical, the inner hollow diameter is 35 mm-40 mm, the material is stainless steel or 150 ℃ resistant plastic, and the thickness of each layer of the filler (10) is not more than 2000 mm.
4. The absorption tower for treating hydrogen sulfide gas by wet oxidation according to claim 3, wherein the paddle tube (701) is made of a corrosion-resistant hard material of DN 14-DN 20.
5. The absorption tower for treating the hydrogen sulfide gas by the wet oxidation method according to claim 1, wherein the discharge pipe (2) is a cross straight pipe, two ends of the straight pipe are sealed by flanges, and a steam sleeve (201) is arranged outside the discharge pipe (2).
6. The absorption tower for treating hydrogen sulfide gas by wet oxidation according to any one of claims 1 to 5, wherein the gas outlet (17) is movably connected with more than two wire mesh filters (18).
7. The absorption tower for treating the hydrogen sulfide gas by the wet oxidation method according to claim 6, wherein a cylindrical skeleton (1801) which is open towards the air inlet direction is arranged inside the wire mesh filter (18), through holes ranging from 12mm to 20mm are formed in the skeleton (1801), two layers of stainless steel wire meshes (1802) are laid on the outer side of the skeleton (1801), the inner layer is 40 meshes, the outer layer is 20 meshes, and the skeleton (1801) and the stainless steel wire meshes (1802) are of an integral structure.
8. The absorption tower for treating the hydrogen sulfide gas by the wet oxidation method according to claim 6, wherein the gas-liquid mixture distributor (4) is arranged at the gas-liquid inlet pipe (14), the gas-liquid mixture distributor (4) is disc-shaped, the axes of the gas-liquid mixture distributor (4) and the cylinder (3) are coincided, the diameter of the gas-liquid mixture distributor is one third of the diameter of the cylinder (3), and round holes are uniformly formed in the bottom and the side surface of the gas-liquid mixture distributor.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4999172A (en) * | 1988-06-29 | 1991-03-12 | Simons Paul B | Absorber packing and method |
| CN104043326A (en) * | 2014-06-04 | 2014-09-17 | 北京化工大学 | Apparatus for high gravity removal of hydrogen sulfide of novel industrial gas, and technology thereof |
| JP6170197B1 (en) * | 2016-02-29 | 2017-07-26 | 荏原実業株式会社 | Desulfurization system and desulfurization method |
| CN107511045A (en) * | 2016-06-18 | 2017-12-26 | 湖北徐风环保科技有限公司 | A kind of method of hydrogen sulfide in removing gas |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5286466A (en) * | 1991-04-08 | 1994-02-15 | Ari Technologies, Inc. | Multi-bed cocurrent downflow mass transfer column with spherical packing |
| CN101890286B (en) * | 2010-08-04 | 2012-11-14 | 姜辉 | Method and device for removing hydrogen sulfide from gas by using suspension of ferric oxide powder |
| CN104645920A (en) * | 2013-11-15 | 2015-05-27 | 天津市东鼎源建筑装饰工程有限公司 | A coating producing device |
| CN105498470A (en) * | 2014-09-25 | 2016-04-20 | 中国石油化工股份有限公司 | Microorganism desulfurizing and sulfur recycling method |
| CN107537302A (en) * | 2016-06-29 | 2018-01-05 | 中国石油化工股份有限公司 | Sulfur recovery facility tail gas from absorption tower handling process and its absorbing liquid used |
| CN106669402A (en) * | 2016-11-23 | 2017-05-17 | 四川沃兹凯兰科技有限公司 | Gas field sulfur-containing waste gas treatment method |
| CN206783622U (en) * | 2017-05-23 | 2017-12-22 | 四川西油致诚石油技术有限公司 | A kind of selexol process process unit |
| CN208711383U (en) * | 2018-06-29 | 2019-04-09 | 广西博世科环保科技股份有限公司 | A kind of packed tower block clearing anti-block apparatus of fluid and machine driving synergistic effect |
| CN109943376B (en) * | 2019-04-02 | 2021-07-23 | 乐山力朴能源环保科技有限公司 | Biogas biological desulfurization device and desulfurization method |
-
2019
- 2019-08-02 CN CN201910712330.6A patent/CN112295382B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4999172A (en) * | 1988-06-29 | 1991-03-12 | Simons Paul B | Absorber packing and method |
| CN104043326A (en) * | 2014-06-04 | 2014-09-17 | 北京化工大学 | Apparatus for high gravity removal of hydrogen sulfide of novel industrial gas, and technology thereof |
| JP6170197B1 (en) * | 2016-02-29 | 2017-07-26 | 荏原実業株式会社 | Desulfurization system and desulfurization method |
| CN107511045A (en) * | 2016-06-18 | 2017-12-26 | 湖北徐风环保科技有限公司 | A kind of method of hydrogen sulfide in removing gas |
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