CN220078985U - Liquefied gas desulfurization device and system - Google Patents
Liquefied gas desulfurization device and system Download PDFInfo
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- CN220078985U CN220078985U CN202321453865.4U CN202321453865U CN220078985U CN 220078985 U CN220078985 U CN 220078985U CN 202321453865 U CN202321453865 U CN 202321453865U CN 220078985 U CN220078985 U CN 220078985U
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- gas desulfurization
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 85
- 230000023556 desulfurization Effects 0.000 title claims abstract description 85
- 239000007788 liquid Substances 0.000 claims abstract description 91
- 230000002745 absorbent Effects 0.000 claims abstract description 45
- 239000002250 absorbent Substances 0.000 claims abstract description 45
- 230000002093 peripheral effect Effects 0.000 claims abstract description 12
- 238000010521 absorption reaction Methods 0.000 claims description 15
- 238000011084 recovery Methods 0.000 claims description 12
- 230000004308 accommodation Effects 0.000 claims 1
- 238000007599 discharging Methods 0.000 claims 1
- 238000012546 transfer Methods 0.000 abstract description 12
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 230000008901 benefit Effects 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 108
- 238000000034 method Methods 0.000 description 25
- 230000003009 desulfurizing effect Effects 0.000 description 13
- 239000012071 phase Substances 0.000 description 11
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 10
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 8
- 239000003546 flue gas Substances 0.000 description 8
- 239000003795 chemical substances by application Substances 0.000 description 7
- 230000000694 effects Effects 0.000 description 7
- 230000008569 process Effects 0.000 description 7
- 229910052717 sulfur Inorganic materials 0.000 description 7
- 230000009471 action Effects 0.000 description 6
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 6
- 125000001741 organic sulfur group Chemical group 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 239000007791 liquid phase Substances 0.000 description 5
- 239000003345 natural gas Substances 0.000 description 5
- 239000002002 slurry Substances 0.000 description 5
- 239000007921 spray Substances 0.000 description 5
- 238000003780 insertion Methods 0.000 description 4
- 230000037431 insertion Effects 0.000 description 4
- 239000003915 liquefied petroleum gas Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 230000002378 acidificating effect Effects 0.000 description 3
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical class OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 3
- 239000000428 dust Substances 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical class S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 230000001174 ascending effect Effects 0.000 description 2
- 230000005587 bubbling Effects 0.000 description 2
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- 238000000926 separation method Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 238000009279 wet oxidation reaction Methods 0.000 description 2
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
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- 239000003513 alkali Substances 0.000 description 1
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Abstract
The utility model relates to petrochemical equipment, in particular to a liquefied gas desulfurization device, which comprises a cylinder (302) and a jacket (303) sleeved on the outer peripheral surface of the cylinder (302), wherein the upper end of the cylinder (302) is provided with an air inlet (306), the necking angle of the air inlet (306) is 0-25 degrees, the inner wall of the jacket (303) and the outer wall of the cylinder (302) enclose a cavity for containing an alkaline absorbent (9), and the outer peripheral surface of the cylinder (302) in the cavity is provided with a plurality of micropores (307) so that the alkaline absorbent (9) is sprayed into the cylinder (302). In addition, the utility model also relates to a liquefied gas desulfurization system. The liquefied gas desulfurization device has the advantages of high gas-liquid mass transfer efficiency, high desulfurization rate, low investment cost and low energy consumption in subsequent operation.
Description
Technical Field
The utility model relates to petrochemical equipment, in particular to a liquefied gas desulfurization device. In addition, the utility model also relates to a liquefied gas desulfurization system.
Background
There are many impurities in untreated liquefied petroleum gas, in addition to H 2 S and CO 2 Besides the acidic components, the sulfur-containing oil-gas refining agent also comprises organic sulfur components such as mercaptan and the like, and the sulfur components can adversely affect the processing and production environment protection work of petroleum and natural gas refining products. The liquefied petroleum and natural gas must be desulfurized during the application process of chemical production, so the development and improvement of the liquefied petroleum and natural gas desulfurization technology are becoming key technologies in the chemical industry of China.
At present, the domestic and foreign desulfurization technology is continuously developed, and the methods for desulfurizing the liquefied petroleum and natural gas are increasingly increased, and mainly comprise dry desulfurization, wet desulfurization, membrane separation desulfurization and biological desulfurization.
Wet desulfurization is generally classified into absorption method and wet oxidation method, and absorption method can be classified into chemical absorption method and physical absorption method according to the difference of absorption principleAbsorption methods and chemical-physical absorption methods. The chemical absorption method is to utilize proper desulfurizing agent to react with H in normal temperature environment 2 S and CO 2 The method can realize the recycling of the desulfurizing agent. Physical absorption processes are based primarily on the physical absorption of acidic components in petroleum and natural gas by organic solvents, which are typically carried out at high pressure and at relatively low temperatures, as the rich liquid pressure decreases, whereupon the absorbed acidic components are evolved. The chemical-physical absorption method is a method in which a chemical absorbent and a physical absorbent are used in combination. The wet oxidation method is to make H under the action of desulfurizing agent 2 S is oxidized to sulfide first and then reduced to elemental sulfur. The wet desulfurizing tower mainly comprises a filler tower, a spray tower, a bubbling tower and a liquid column tower. The filling tower has strong adaptability, small pressure drop and liquid retention, but has high manufacturing cost, heavy weight and large investment, and moreover, the grid filling plate of the filling tower is easy to scale and block, so that the system resistance is large; the spray tower is generally arranged in a way of countercurrent contact of flue gas and slurry, a plurality of layers of nozzles are arranged at the upper part of the spray tower, the desulfurizing agent slurry forms liquid mist through the atomizing nozzles, and SO is formed when the flue gas and the slurry liquid mist are in countercurrent full contact 2 The gas-liquid contact area of the spray tower is large, but the spray nozzle is easy to wear and block; the bubbling tower has lower requirements on the dust content of the flue gas, can better run and obtain higher desulfurization efficiency under high dust concentration, but has larger back mixing in the liquid phase, larger system resistance and higher requirements on the output of a wind-smoke system device, and the pipe orifice position is easy to cause structural phenomenon, so that the occupied area is large; the tower body of the liquid column tower is of a square steel structure, a single-layer main pipe is adopted for configuration, the guniting pipe is arranged at the bottom of the tower body, the circulating pump sends the absorbent into the guniting main pipe, and the absorbent is dispersed into each parallel branch pipe for ejection, so that a liquid column covering the cross section of the whole desulfurizing tower is formed. The flue gas radially enters the tower from the lower part of the desulfurizing tower and upwards passes through the liquid column, in the ascending process, the flue gas is firstly contacted with the slurry liquid column sprayed upwards in a concurrent flow manner, the slurry column spreads after reaching the highest point and forms uniformly distributed downward liquid drops, the uniformly distributed downward liquid drops are contacted with the flue gas in a countercurrent manner from top to bottom again, and simultaneously, the tiny falling liquid drops and the liquid drops carried by the ascending flue gas enterThe column collision, renew mass transfer surface, form intensive liquid drop layer, improved the mixing of flue gas and absorption liquid for gas-liquid two-phase high-efficient contact, the liquid column tower advantage lies in simple structure, orifice aperture are great, be difficult for the jam, but its water consumption, electricity consumption, resistance loss are great.
At present, the desulfurization method and technology adopted in the chemical industry in China are complex, the cost is high, the mechanism of the liquefied gas desulfurization process is studied deeply on the basis of the existing technology and equipment, the desulfurization precision is improved, the alkaline residue emission is greatly reduced, and the method has positive significance for improving the environmental protection and economy of the device, and further improving the technical level of liquefied gas desulfurization of domestic refineries on the whole.
Therefore, there is an urgent need in industry to develop a device and a system for desulfurizing liquefied gas, which are low in cost, low in energy consumption, simple in process, and simplified in system, and are safe and efficient.
Disclosure of Invention
In view of the above, an aspect of the present utility model is to provide a liquefied gas desulfurization apparatus, which has high gas-liquid mass transfer efficiency, high desulfurization rate and low pressure drop.
Another technical problem to be solved by the utility model is to provide a liquefied gas desulfurization system which has low investment cost, small occupied area and low operation energy consumption.
In order to achieve the above purpose, according to one aspect of the present utility model, there is provided a liquefied gas desulfurization apparatus, including a cylinder and a jacket sleeved on an outer circumferential surface of the cylinder, wherein an air inlet is provided at an upper end of the cylinder, a necking angle of the air inlet is 0-25 °, an inner wall of the jacket and an outer wall of the cylinder enclose a cavity for accommodating an alkaline absorbent, and a plurality of micropores are provided on the outer circumferential surface of the cylinder in the cavity, so that the alkaline absorbent is injected into the cylinder.
Preferably, an air outlet pipe is arranged in the cylinder body, the air outlet pipe extends upwards, and the upper end face of the air outlet pipe is higher than the upper end face of the cylinder body.
Preferably, the outer peripheral surface of the jacket is provided with a liquid inlet pipe.
Preferably, a liquid outlet is arranged at the lower part of the cylinder.
More preferably, the upper part of the cylinder is formed in a cylindrical structure, the middle part is formed in an inverted cone structure, and the lower part is formed in a cylindrical structure.
Specifically, the diameter of the micropores is 0.5-5mm.
The utility model also provides a liquefied gas desulfurization system, which comprises a liquefied gas tank, an air supply device, a liquefied gas desulfurization device, a liquid supply device, an alkaline absorbent accommodating tank and a recovery liquid tank, wherein gas in the liquefied gas tank enters the liquefied gas desulfurization device tangentially after being pressurized by the air supply device, alkaline absorbent in the alkaline absorbent accommodating tank enters the liquefied gas desulfurization device after being pressurized by the liquid supply device, and absorption liquid in the liquefied gas desulfurization device is suitable for being discharged into the recovery liquid tank.
Preferably, the air supply device includes an air pump and a frequency converter electrically connected to the air pump.
More preferably, the liquefied gas tank is connected to the gas supply device, the gas supply device is connected to the liquefied gas desulfurization device, the liquefied gas desulfurization device is connected to the liquid supply device, the liquid supply device is connected to the alkaline absorbent storage tank, and the liquefied gas desulfurization device is connected to the recovery tank through pipelines.
Preferably, the liquefied gas desulfurization device is connected in series in a multistage manner, and the number of stages is 2-5.
Compared with the prior art, the liquefied gas desulfurization device and the liquefied gas desulfurization system have the following three beneficial effects:
(1) The liquefied gas desulfurizing device comprises a cylinder body and a jacket sleeved on the cylinder body, wherein a liquid inlet pipe is arranged on the outer peripheral surface of the jacket, a cavity with a certain volume is formed by the inner wall of the jacket and the outer wall of the cylinder body, and a plurality of rows of micropores are arranged on the outer peripheral surface of the cylinder body in the cavity. After the alkaline absorbent is injected into the cavity from the liquid inlet pipe, under the action of pressure, the alkaline absorbent is divided into a plurality of jet flow columns to enter the cylinder body under the action of pressure, and the liquefied gas tangentially enters the cylinder body from the air inlet on the side surface of the top of the cylinder body, and a downward spiral strong-rotation airflow field is formed in the cylinder body, the jet flow columns are cut and split into liquid drops by the strong-rotation airflow field and then are mixed with the liquefied gas, and the liquid drops of the alkaline absorbent are subjected to high-frequency oscillation to be secondarily broken when the gas-liquid mixture moves along with the downward spiral movement of the strong-rotation airflow field, so that the liquid drops are fully contacted with the liquefied gas and react to absorb sulfide, and the purpose of desulfurization is achieved. The liquefied gas desulfurization device has simple structure, small usage amount of alkaline absorbent and high desulfurization efficiency;
(2) The necking angle of the air inlet is set to be 0-25 degrees, and a certain necking angle is increased, so that the tangential speed of the liquefied gas entering the cylinder is increased, the gas swirling field formed by the liquefied gas entering the cylinder is more stable, and a better gas-liquid mass transfer effect is obtained;
(3) The liquefied gas desulfurization system has the advantages of small occupied area, long service life, high desulfurization efficiency, low operation energy consumption and low investment cost.
Additional features and advantages of the utility model will be set forth in the detailed description which follows.
Drawings
The accompanying drawings, which are included to provide a further understanding of the utility model and are incorporated in and constitute a part of this specification, illustrate and together with the description serve to explain, but do not limit the utility model. In the drawings:
FIG. 1 is a schematic diagram of one embodiment of a liquefied gas desulfurization system of the present utility model;
FIG. 2 is a schematic plan view of an embodiment of a liquid gas desulfurization apparatus according to the present utility model;
FIG. 3 is a schematic perspective view of an embodiment of a liquid gas desulfurization apparatus according to the present utility model;
fig. 4 is a schematic top view of an embodiment of an air intake according to the present utility model.
Description of the reference numerals
1 liquefied gas tank 2 air supply device
3 liquefied gas desulfurization device 301 outlet duct
302 barrel 303 jacket
304 liquid inlet pipe 305 liquid outlet
306 air inlet 307 micro-holes
4 liquid feeding device 5 alkaline absorbent tank
6 recovery liquid tank 7 liquefied gas
8 desulphurized liquefied gas 9 alkaline absorbent
Detailed Description
The following detailed description of the embodiments of the utility model is provided in connection with the accompanying drawings, it being understood that the embodiments described herein are for purposes of illustration and explanation only, and the scope of the utility model is not limited to the following embodiments.
In the description of the present utility model, it should be noted that, unless explicitly stated and limited otherwise, the terms "disposed," "mounted," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; either directly or indirectly via an intermediate medium, or in communication with each other or in interaction with each other. The specific meaning of the above terms in the present utility model can be understood by those of ordinary skill in the art according to the specific circumstances.
In the description of the present utility model, it should be understood that the terminology of orientation is based on the orientation or positional relationship shown in the accompanying drawings, which is for the purpose of describing the present utility model only and simplifying the description, and is not intended to indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore should not be construed as limiting the utility model.
Referring to fig. 2, the utility model provides a liquefied gas desulfurization device, which comprises a cylinder 302 and a jacket 303 sleeved on the outer peripheral surface of the cylinder 302, wherein an air inlet 306 is arranged at the upper end of the cylinder 302, the necking angle of the air inlet 306 is 0-25 degrees, the inner wall of the jacket 303 and the outer wall of the cylinder 302 enclose a cavity for containing an alkaline absorbent 9, and a plurality of micropores 307 are arranged on the outer peripheral surface of the cylinder 302 in the cavity, so that the alkaline absorbent 9 is sprayed into the cylinder 302.
Referring to fig. 3 and 4, in the present utility model, the upper end of the cylinder 302 is provided with the air inlet 306, the air inlet 306 is located at the circumferential tangent of the cylinder 302, and the necking angle of the air inlet 306 is 0-25 °, preferably, the necking angle of the air inlet 306 is 20 °, so that the tangential velocity of the liquefied gas 7 entering the cylinder 302 is further increased, the gas swirling field formed by the liquefied gas 7 entering the cylinder 302 can be maintained to be more stable, more liquid phase jet flows can be involved into the gas phase to form a liquid dispersed phase, and the contact area of the two phases is greatly increased, thereby obtaining better gas-liquid mass transfer effect. The jacket 303 is sleeved on the outer peripheral surface of the middle section of the cylinder 302, the liquid inlet pipe 304 is arranged on the outer peripheral surface of the jacket 303, the inner wall of the jacket 303 and the outer wall of the cylinder 302 enclose a cavity with a certain volume, and a plurality of rows of micropores 307 are arranged on the outer peripheral surface of the cylinder 302 within the range of the cavity. After the alkaline absorbent 9 is injected into the cavity 302 from the liquid inlet pipe 304, under the action of pressure, the alkaline absorbent 9 is divided into a plurality of jet flows to enter the cylinder 302 when passing through the micropores 307, so that the jet flows are divided into innumerable liquid drops and mixed with the liquefied gas 7 under the action of the gas swirling field, and the gas-liquid mixture spirally moves downwards along with the strong swirling flow field, and meanwhile, the alkaline absorbent liquid drops are subjected to high-frequency oscillation to be secondarily broken, so that the alkaline absorbent liquid drops fully contact with the liquefied gas and react to absorb sulfides, and the purpose of desulfurization is achieved. The necking angle of the present utility model refers to an angle θ in fig. 4.
As a preferred embodiment of the present utility model, the air outlet 301 is provided in the cylinder 302, the air outlet 301 extends upward, and the upper end surface of the air outlet 301 is higher than the upper end surface of the cylinder 302. The insertion depth of the gas outlet 301 affects the motion pattern of the gas flow field, and thus the mass transfer process of the gas-liquid two phases. Along with the increase of the insertion depth of the air outlet pipe 301, the velocity component of the air flow in the tangential direction is gradually increased, a spiral flow field in the form of a spiral upward rigid vortex is gradually formed in the space spiral flow field of the cone, the strength of the rigid vortex field is high, the carrying capacity of liquid in the spiral flow field can be increased, the movement duration of the air flow can be also increased, and however, along with the increase of the insertion depth of the air outlet pipe 301, the pressure drop of the gas phase and the energy consumption in the mass transfer process can be increased. Therefore, the user can select a proper insertion depth of the outlet pipe 301 in consideration of the requirements of the energy consumption and mass transfer performance of the apparatus.
Preferably, the outer circumferential surface of the jacket 303 is provided with a liquid inlet pipe 304. In this embodiment, the liquid inlet pipe 304 is disposed in the middle of the jacket 303.
More preferably, a liquid outlet 305 is provided in the lower portion of the cylinder 302.
In addition, the upper portion of the cylinder 302 is formed in a columnar structure, the middle portion is formed in an inverted cone structure, and the lower portion is formed in a columnar structure. In the annular cavity formed by the cylinder 302 and the air outlet pipe 301, the air flow mainly rotates in a quasi-free vortex mode, the cone section is a main body area for separating gas phase from liquid phase, the air flow optimally rotates in a quasi-forced vortex mode in the cone section, and the carrying quantity of liquid drops can be effectively reduced, so that secondary pollution is avoided. The design of cone height influences pressure drop and separation efficiency of the liquefied gas desulfurization device, and a user can adopt cones with different heights according to use requirements. The middle space of the cylinder 302 is of an inverted cone structure, compared with a traditional cylindrical structure, the cylinder 302 with the combined cylindrical cone has higher tangential velocity in the gas-liquid swirling flow field, the gas-phase swirling flow field has stronger atomization dispersing effect on radial jet flow, and the jet flow can be deformed, crushed and atomized earlier, so that a coupling state with stronger gas-liquid mass transfer effect is formed. The columnar structure of the lower part of the cylinder 302 is a liquid outlet 305.
Further preferably, the diameter of the micropores 307 is 0.5 to 5mm. The arrangement of the micro holes 307 on the cylinder 302 is a square arrangement. The diameter of the micro-holes 307 may be selected according to the flow rate desired to be treated, the diameter of the cylinder 302, etc.
The operation pressure drop of the liquefied gas desulfurization device is 10-50KPa, and the treatment capacity is 10-100m 3 /h。
Referring to fig. 1, the utility model further provides a liquefied gas desulfurization system, which comprises a liquefied gas tank 1, a gas feeding device 2, a liquefied gas desulfurization device 3, a liquid feeding device 4, an alkaline absorbent accommodating tank 5 and a recovery liquid tank 6, wherein liquefied gas 7 in the liquefied gas tank 1 is pressurized by the gas feeding device 2 and then enters the liquefied gas desulfurization device 3 tangentially, alkaline absorbent 9 in the alkaline absorbent accommodating tank 5 is pressurized by the liquid feeding device 4 and then enters the liquefied gas desulfurization device 3, and absorption liquid in the liquefied gas desulfurization device 3 is suitable for being discharged into the recovery liquid tank 6. The air supply device 2 of the present utility model is preferably an air pump, and the air pump is electrically connected to a frequency converter, so that the flow rate of the liquefied gas 7 fed into the liquefied gas desulfurization device 3 can be adjusted. The liquid feeding means 4 is preferably a water pump adapted to be connected to a regulating valve by means of which the alkaline absorbent 9 is fed to the liquid inlet pipe 304, and by means of which the flow rate of the alkaline absorbent 9 into the jacket 303 is regulated. The liquefied gas 7 tangentially enters the cylinder 302 through the air inlet 306 to form a strong cyclone flow field, the alkaline absorbent 9 entering the cavity of the jacket 303 is injected into the cylinder 302 through the micropores 307 on the side wall of the cylinder 302, the radially injected alkaline absorbent 9 is continuously cut by the liquefied gas 7 rotating at a high speed in a tangential direction, so that the liquid drops of the alkaline absorbent 9 are dispersed into mist-like liquid drops, the mist-like liquid drops are applied with shearing force by the high-speed airflow field, and the rapid rupture and surface update of the liquid drops are caused, and meanwhile, the liquid drops move to the wall surface under the centrifugal force of the airflow field to form a supergravity mass transfer effect. The two-phase fluid mixture continues to rotate downwards, finally, the two-phase fluid mixture is separated at the cone part of the cylinder 302, the liquid serving as heavy components is thrown to the inner wall of the cylinder 302 under the action of centrifugal force and then slides downwards, the liquid flows out from the liquid outlet 305 to the recovery liquid tank 6, the rotating air flow contracts in the cylinder 302 and flows towards the center, a secondary vortex is formed upwards, the desulfurization liquefied gas 8 serving as a light component is discharged from the gas outlet pipe 301 along with the secondary vortex, the gas outlet pipe 301 is connected with the desulfurization liquefied gas chamber through a pipeline, and the desulfurization liquefied gas 8 is stored in the desulfurization liquefied gas chamber. The absorption liquid in the recovery liquid tank 6 can be processed for the second time to produce the needed chemical raw materials, and the alkaline absorbent can be desorbed to realize recycling.
The air supply device 2 of the present utility model includes an air pump and a frequency converter, and the frequency converter is electrically connected to the air pump. The user can adjust the flow of the liquefied gas 7 entering the liquefied gas desulfurization device 3 according to the frequency converter, so that the gas flow with the optimal gas-liquid mass transfer effect is obtained.
Preferably, the liquefied gas tank 1 is connected with the gas supply device 2, the gas supply device 2 is connected with the liquefied gas desulfurization device 3, the liquefied gas desulfurization device 3 is connected with the liquid supply device 4, the liquid supply device 4 is connected with the alkaline absorbent accommodating groove 5, and the liquefied gas desulfurization device 3 is connected with the recovery liquid groove 6 through pipelines. The pipeline of the utility model comprises, but is not limited to, pipes, pipe fittings, valves, flanges, gaskets, fasteners and other pipeline components, and the pipe materials also comprise, but are not limited to, metal pipes, rubber pipes, plastic pipes, glass pipes and other materials, and a user can select the pipe materials according to the characteristics and the use requirements of the alkaline absorbent. The pipeline arrangement of the liquefied gas desulfurization system of the utility model meets the principles that cold and hot pipelines are arranged separately, the pipelines with corrosive materials are arranged on the lower side or the outer side of the parallel pipelines, the pipelines are as little bent as possible, and the valves are arranged on the parts convenient to operate.
Preferably, the liquefied gas desulfurization apparatus 3 is multi-stage series connection, the number of stages is 2-5. The user can set the liquefied gas desulfurization device 3 to be used in series in multiple stages according to the treatment capacity of the liquefied gas and the treatment requirement of the components in the liquefied gas 7. For example, a water washing device can be connected in series, and the desulfurized liquefied gas 8 is conveyed to the water washing device to remove alkali liquor impurities carried in the desulfurized liquefied gas 8, so that the desulfurized liquefied gas 8 is neutral.
The liquefied gas 7 generally contains H 2 S、CO 2 COS, mercaptans (RSH), and the like. For H contained in the liquefied gas 7 to be removed 2 S and CO 2 In the case where the component is relatively large and the organic sulfur (e.g., COS) component is relatively low, the alkaline absorbent 9 used in the present utility model is preferably a solvent such as Monoethanolamine (MEA), modified diethanolamine (SNPA-DEA), or N-Methyldiethanolamine (MDEA). In the case where the liquefied gas 7 to be removed contains a high content of organic sulfur (e.g., COS), the alkaline absorbent 9 used in the present utility model is preferably a UDS high-efficiency desulfurizing agent. The Monoethanolamine (MEA) method uses 15% -25% of monoethanolamine aqueous solution, the modified diethanolamine (SNPA-DEA) method uses 40% -50% of diethanolamine aqueous solution, and the N-Methyldiethanolamine (MDEA) method uses methyldiethanolamine solutionThe liquid, UDS high-efficiency desulfurizing agent is prepared by taking MDEA as a main solvent, and adding active components for improving the reaction rate of organic sulfur and a sulfur-philic compound component for improving the physical solubility of the organic sulfur to improve the organic sulfur removal performance of the solvent. The type of the alkaline absorbent 9 can be arbitrarily selected by the user according to the sulfur content in the liquefied gas 8.
The gas phase of the present utility model is liquefied gas 7, and the liquid phase is alkaline absorbent 9. In addition, the continuous operation of the liquefied gas desulfurization system is not less than 5 years, the equipment design life is 20 years, and the total sulfur removal efficiency of the liquefied gas is more than 99%.
The utility model can effectively solve the following two important problems:
the upper part of the cylinder 302 in the liquefied gas desulfurization device 3 is designed to be in a columnar structure, the middle part of the cylinder is designed to be in an inverted conical structure, and when the airflow passes through a narrower space, the tangential velocity is increased, so that the liquid phase jet flow is deformed, crushed and atomized earlier, and the gas-liquid mass transfer effect is enhanced;
the second, inventive system for desulfurizing a liquefied gas can form the liquefied gas desulfurization apparatus 3 to be used in series in multiple stages, thereby enabling the inventive system to treat a larger flow of the liquefied gas 7 or to treat more components in the liquefied gas 7, such as dust particles and CO in the liquefied gas 2 The components are as follows.
The preferred embodiments of the present utility model have been described in detail above with reference to the accompanying drawings, but the present utility model is not limited to the specific details of the above embodiments, and various simple modifications can be made to the technical solution of the present utility model within the scope of the technical concept of the present utility model, and all the simple modifications belong to the protection scope of the present utility model.
In addition, the specific features described in the above embodiments may be combined in any suitable manner without contradiction. The various possible combinations of the utility model are not described in detail in order to avoid unnecessary repetition.
Moreover, any combination of the various embodiments of the utility model can be made without departing from the spirit of the utility model, which should also be considered as disclosed herein.
Claims (10)
1. The utility model provides a liquefied gas desulfurization device, its characterized in that includes barrel (302) and cup joints jacket (303) on barrel (302) outer peripheral face, the upper end of barrel (302) is provided with air inlet (306), just the throat angle of air inlet (306) is 0-25, jacket (303) inner wall with barrel (302) outer wall encloses the cavity that synthesizes and hold alkaline absorbent (9), just be equipped with a plurality of micropore (307) on barrel (302) outer peripheral face in the cavity, so that alkaline absorbent (9) jet into inside barrel (302).
2. The liquefied gas desulfurization apparatus as claimed in claim 1, wherein an air outlet pipe (301) is provided inside the cylinder (302), the air outlet pipe (301) extends upward and an upper end surface of the air outlet pipe (301) is higher than an upper end surface of the cylinder (302).
3. The liquefied gas desulfurization apparatus as claimed in claim 1, wherein a liquid inlet pipe (304) is provided on an outer circumferential surface of the jacket (303).
4. The liquefied gas desulfurization apparatus as claimed in claim 1, wherein a liquid outlet (305) is provided at a lower portion of the cylinder (302).
5. The liquefied gas desulfurization apparatus as claimed in claim 4, wherein an upper portion of the cylinder (302) is formed in a cylindrical structure, a middle portion is formed in an inverted cone structure, and a lower portion is formed in a cylindrical structure.
6. The device according to claim 1, characterized in that the diameter of the micropores (307) is 0.5-5mm.
7. The utility model provides a liquefied gas desulfurization system, its characterized in that includes liquefied gas jar (1), air feed device (2), liquefied gas desulfurization device (3), liquid feed device (4), alkaline absorbent holding tank (5) and recovery cistern (6), gaseous (7) in liquefied gas jar (1) are through in gas feed device (2) pressure boost back tangential entering liquefied gas desulfurization device (3), alkaline absorbent (9) in alkaline absorbent holding tank (5) are through liquid feed device (4) pressure boost back entering liquefied gas desulfurization device (3) in, the absorption liquid in liquefied gas desulfurization device (3) is suitable for discharging into recovery cistern (6).
8. The liquefied gas desulfurization system according to claim 7, wherein the gas supply device (2) includes an air pump and a frequency converter electrically connected to the air pump.
9. The liquefied gas desulfurization system according to claim 8, wherein the liquefied gas tank (1) and the gas supply device (2), the gas supply device (2) and the liquefied gas desulfurization device (3), the liquefied gas desulfurization device (3) and the liquid supply device (4), the liquid supply device (4) and the alkaline absorbent accommodation tank (5), and the liquefied gas desulfurization device (3) and the recovery liquid tank (6) are connected by pipelines.
10. The liquefied gas desulfurization system according to any one of claims 7 to 9, wherein the liquefied gas desulfurization apparatus (3) is multistage in series, the number of stages being 2 to 5.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321453865.4U CN220078985U (en) | 2023-06-08 | 2023-06-08 | Liquefied gas desulfurization device and system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321453865.4U CN220078985U (en) | 2023-06-08 | 2023-06-08 | Liquefied gas desulfurization device and system |
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| CN220078985U true CN220078985U (en) | 2023-11-24 |
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| CN202321453865.4U Active CN220078985U (en) | 2023-06-08 | 2023-06-08 | Liquefied gas desulfurization device and system |
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| CN (1) | CN220078985U (en) |
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