CN216998308U - Sulfur recovery system for natural gas desulfurization acid gas - Google Patents
Sulfur recovery system for natural gas desulfurization acid gas Download PDFInfo
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- CN216998308U CN216998308U CN202220469316.5U CN202220469316U CN216998308U CN 216998308 U CN216998308 U CN 216998308U CN 202220469316 U CN202220469316 U CN 202220469316U CN 216998308 U CN216998308 U CN 216998308U
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Abstract
The utility model discloses a sulfur recovery system for natural gas desulfurization acid gas, which is characterized in that: the device comprises four groups of absorption and regeneration devices which are arranged in parallel, a gas outlet at the top of the acid gas separator is divided into four paths which are respectively connected to the four groups of absorption and regeneration devices, each group of absorption and regeneration device comprises an absorption tower, a lean and rich liquid heat exchanger and an oxidation tower, the oxidation tower is a conical bottom, a sulfur slurry pump is arranged at the lowest sulfur slurry outlet of the conical bottom of the oxidation tower, and an outlet of the sulfur slurry pump is connected to a sulfur slurry inlet of the membrane filter press.
Description
Technical Field
The utility model relates to a sulfur recovery system for natural gas desulfurization acid gas, and belongs to the technical field of tail gas treatment equipment of a natural gas pretreatment system.
Background
The acid gas generated in the mined natural gas raw material pretreatment system contains hydrogen sulfide and cannot be directly discharged into the atmosphere, and the acid gas needs to be treated and recovered with elemental sulfur, so that the content of the hydrogen sulfide in tail gas is reduced, and the elemental sulfur is recovered, so that the acid gas has a certain economic value. The traditional treatment process has the disadvantages of complex equipment structure, limited desulfurization effect, poor recycling of the desulfurization agent, high agent consumption and high sulfur recovery cost.
Disclosure of Invention
Aiming at the defects in the prior art, the utility model provides a sulfur recovery system for natural gas desulfurization acid gas, which has the advantages of reasonable structural design, good sulfur recovery effect, low medicament consumption and capability of reducing sulfur recovery cost
In order to achieve the purpose, the technical scheme of the utility model is as follows:
the utility model provides a sulfur recovery system of natural gas desulfurization sour gas which characterized in that: the device comprises an acid-gas separator, absorption and regeneration devices, a magnetic suspension fan, a membrane filter press and a purification-gas separator, wherein the absorption and regeneration devices are four groups and are arranged in parallel, gas outlets at the top of the acid-gas separator are divided into four paths which are respectively connected to the four groups of absorption and regeneration devices, each group of absorption and regeneration device comprises an absorption tower, a lean-rich liquid heat exchanger and an oxidation tower, a gas outlet at the top of the acid-gas separator is connected to a gas inlet at the lower part of the absorption tower, a liquid outlet at the bottom of the absorption tower flows into a rich liquid channel of the lean-rich liquid heat exchanger through a rich liquid pump, a rich liquid outlet of the lean-rich liquid heat exchanger is connected to the top of the oxidation tower, and a purified gas outlet at the top of the absorption tower is connected to an emptying pipe after passing through the purification-gas separator; the device comprises an oxidation tower, a lean solution channel, an absorption tower, at least two magnetic suspension fans, an air cooler, an air distributor, a sulfur slurry pump, a sulfur slurry inlet, a sulfur slurry outlet, a bypass pipeline and an exhaust pipeline, wherein the lean solution outlet at the lower part of the oxidation tower is connected to the lean solution channel of the lean and rich solution heat exchanger through a lean solution pump; and a filtrate tank is arranged below the membrane filter press, filtrate collected in the filtrate tank is pumped into the bypass pipeline through a filtrate pump and then flows back to the oxidation tower, and a screw conveyor is also arranged below the membrane filter press in a matched manner and is used for bagging the separated sulfur paste into a sulfur melting kettle.
Further, a gas distributor is arranged in the absorption tower and is connected with a gas inlet at the lower part of the absorption tower.
Further, a liquid inlet pipeline of the barren pump is connected with a medicament adding system through a metering pump.
Further, a first nozzle connected with a lean solution pipeline is arranged above the middle in the absorption tower; and a second nozzle connected with a rich liquid pipeline is arranged above the inside of the oxidation tower.
The method has the advantages that the equipment works stably, the method can be adapted to a natural gas pretreatment system to continuously recover the sulfur in the acid gas, the medicament is recycled, and the sulfur recovery cost is reduced.
Drawings
Fig. 1 is a schematic structural view of the present invention.
Detailed Description
The present invention will be described in further detail with reference to the following embodiments and the accompanying drawings.
Sulfur recovery process
Gas phase flow: and (4) allowing acid gas released after the regeneration of the MDEA solution to enter a complex iron desulfurization device. The separated free water and MDEA solution enter an absorption tower 2 to react with the complex iron poor solution, the wet purified gas with hydrogen sulfide removed is separated from the carried liquid by a purification and gas separator 7, and is discharged through a discharge pipeline after reaching the discharge standard (the content of hydrogen sulfide is less than or equal to 13 ppm).
Liquid phase flow: the desulfurization lean solution is pressurized by a lean solution pump 9 and then is conveyed into an absorption tower 2, the inside of the absorption tower 2 and H2S in acid gas are subjected to chemical reaction, rich solution absorbing H2S flows out of the bottom of the absorption tower 2 and then enters an oxidation tower 6, air is blown into the oxidation tower 6 by a magnetic suspension fan 3 to regenerate the solution, one part of the regenerated lean solution is pumped back to the absorption tower 2 through the lean solution pump 9 for recycling, the other part of the regenerated lean solution is input to the top of the oxidation tower 6 through an injection pump and is uniformly sprayed onto the surface of the solution through a nozzle, and the spray can destroy foam or floating sulfur accumulated on the surface of the solution.
Sulfur slurry flow: the solid sulfur is precipitated at the conical bottom of the oxidation tower 6, the sulfur slurry is pumped out from the conical bottom through a sulfur slurry pump 12, one part of the sulfur slurry is circularly conveyed to the oxidation tower 6, the other part of the sulfur slurry is conveyed to a membrane filter press 4, and sulfur paste with 20-30% of water is obtained by filtering through the filter press 4.
Example 1
The sulfur recovery apparatus shown in FIG. 1 comprises an absorption system, a regeneration system, a filtration system, and a chemical addition system.
Absorption system
The sour gas containing sulfur enters a sulfur recovery device. An emergency vent valve and a pneumatic switch valve are arranged in front of the acid-gas separator 1, under the normal operation condition, the emergency vent valve leading to a vent pipeline is closed, the sulfur-containing gas enters the acid-gas separator 1, and when the overpressure linkage system acts, the acid gas is directly discharged to the vent pipeline and the pneumatic switch valve is closed. After the acid gas passes through the acid-gas separator 1, free water and MDEA solution are removed, and the liquid level switch valve is controlled by the remote liquid level meter of the acid-gas separator 1 to discharge sewage.
The acid gas is metered by a flowmeter after leaving the acid gas separator 1, and then averagely enters the four-row absorption tower 2 by four paths, the four-row flow is the same, and a three-purpose one-standby structure is adopted. Each column flow is the same and only the first column flow is described. The acid gas enters the absorption tower 2 and reversely contacts with the complexing iron barren solution from the oxidation tower 6, the complexing iron barren solution is pumped into the absorption tower 2 from the oxidation tower 6 through a barren solution pump 9, and the hydrogen sulfide in the acid gas is converted into elemental sulfur and water (Fe) by iron ions+3Is reduced to Fe+2And converting the complex iron barren solution into a complex iron rich solution). Purified gas (less than or equal to 13 ppmH)2S) is gathered at the top of the absorption tower 2, then purified gas enters the purification gas separator 7 through the flow regulating valve to remove the rich liquid of the desulfurizer, is discharged out of the system, and enters the emptying vertical pipe, and the flow regulating valve is controlled by the outlet flow meter of each row of acid-gas separators 1 to regulate the flow entering each row of absorption towers 2. The rich liquid of the desulfurizing agent discharged by the gas purification separator 7 flows into the filtrate tank 13 to be reused in the system again.
Regeneration system
The regeneration system is carried out in the oxidation tower 6, and each flow scheme is the same, and only the first flow scheme is described. Regeneration of the rich desulfurization solution (containing divalent iron ions) is performed in the oxidation tower 6. Under the action of a rich liquid pump 8, a solution at the bottom of an absorption tower 2 enters an oxidation tower 6 after the conical bottom of the absorption tower 2 is adjusted by the flow of a frequency converter of the rich liquid pump 8, hydrogen sulfide is absorbed to be an exothermic reaction, because the temperature of a desulfurization solution is high, the rich liquid of the Luo river iron needs to enter a lean rich liquid heat exchanger 5, the desulfurization solution enters the oxidation tower 6 in a spraying mode through the top of the oxidation tower 6 after heat exchange and temperature reduction, so that sulfur foam floating on the surface of the solution is destroyed, and the flow of the rich liquid pump 8 is subjected to frequency modulation control by a liquid level meter of the absorption tower 2.
The number of the magnetic suspension fans 3 is three, and the two-purpose one-standby structure is adopted. 3000Nm of single air volume3And h, cooling to 40-50 ℃ through the air cooler 10, and respectively conveying the cooled air to each row of oxidation towers 6 through flow regulating valves. After entering the oxidation tower 6, the air is uniformly distributed on the cross section of the whole oxidation tower 6 through an oxidation air distributor 11. The bubbles meet the rich complex iron solution from the absorption tower 2 during the rising process, and the ferrous ions in the rich complex iron solution are oxidized into ferric ions (the rich complex iron solution is converted into a poor complex iron solution). The redundant air rises to the top of the oxidation tower to be emptied, and the main components of the air-discharging body are air, carbon dioxide and water vapor.
The iron complex barren solution is extracted from the bottom of the oxidation zone above the conical bottom of the oxidation tower 6 and is conveyed to a barren solution pump 9 at 150m3The flow rate/h enters the absorption column 2.
The concentration of sulfur precipitate allowed in the conical bottom of the oxidation tower 6 is 5-15%. In order to maintain the normal flow of the sulfur slurry, a blowing wind and a flushing device are added around the cone sleeve, the blowing wind continuously blows to the cone part at a fixed time period to prevent the cone from sulfur caking, and the flushing water continuously blows to the cone part manually to prevent the sulfur caking in the cone.
Filtration system
The sulfur slurry pump 12 pumps the sulfur slurry from the conical hopper of the oxidation tower 6 with the length of 12m3The flow rate of the/h enters a membrane filter press 4 for filtration, and the number of the membrane filter presses 4 is two, and the membrane filter presses can be used intermittently or one is used for standby. The unloading time is 3 times per day of full load. The flow of the membrane filter press comprises feeding, squeezing, discharging and conveying.
Feeding: one path of the sulfur slurry from the sulfur slurry pump 12 enters the membrane filter press 4, and the other path of the sulfur slurry is controlled by a bypass pipeline backflow diaphragm valve to ensure that the maximum pressure entering the membrane filter press 4 is 0.6Mpa, and when the sulfur in the inner cavity of the membrane filter press 4 is more and more, the redundant sulfur slurry flows back to the oxidation tower 6 through the bypass. While the sulfur paste is fully filter-pressed, a sulfur slurry pump 12 and a membrane filter press 4 are protected, and filtrate flows back to an oxidation tower 6 through a blind flow. When the feeding pressure is kept at 0.6Mpa for a period of time, the feeding valve of the membrane filter press 4 is closed, the membrane filter press is switched to a standby membrane filter press, the sulfur slurry enters the standby membrane filter press or an outlet bypass valve is opened, and the sulfur slurry flows back to the oxidation tower 6.
Squeezing: after feeding is finished, 1.6Mpa desalted water is opened, the diaphragm is flushed, when the squeezing pressure is 1.6Mpa, a desalted water loop valve is opened, the squeezing pressure is kept at 1.6Mpa manually, and after 5-10min, water feeding is closed, and desalted water in the diaphragm is decompressed.
Unloading: when the squeezing force is 0, the turning plate is closed, the automatic plate pulling function of the membrane filter press 4 is controlled, and plate pulling and unloading are started. A small amount of liquid enters the filtrate tank 13 through a turning plate arranged at the lower part of the membrane filter press 4, the turning plate is opened, the sulfur paste falls into the screw conveyer 15, and the screw conveyer 15 conveys the sulfur paste to a ton bag for bagging.
Medicament adding system
The consumed chemicals, complexing agent, iron ions and KOH chemicals are supplemented to each row of oxidation towers 6 by chemical metering pumps, and the supplement amount is related to the sulfur load of the device; the surfactant is supplemented to the liquid inlet pipeline of each row of barren pumps 9 by a chemical metering pump.
The start-up initiator and the defoamer are added only periodically during initial operation and normal operation. The defoaming agent injection is installed on the inlet pipeline of each row of the barren liquor pump 9, and the defoaming agent or surfactant is added in batches in a desalted water pressure injection mode. During initial operation, the defoaming agent and the surfactant can be added according to needs; and can be added periodically after the system is operating normally.
Although each pump has a designed additive amount, the actual flow rate of the pump is determined and whether the pump is in a working state or not by manually calibrating the column for 2-3 times per day.
The technical solutions provided by the embodiments of the present invention are described in detail above, and the principles and embodiments of the present invention are explained herein by using specific examples, and the descriptions of the embodiments are only used to help understanding the principles of the embodiments of the present invention; meanwhile, for a person skilled in the art, according to the embodiments of the present invention, there may be variations in the specific implementation manners and application ranges, and in summary, the content of the present description should not be construed as a limitation to the present invention.
Claims (4)
1. The utility model provides a sulfur recovery system of natural gas desulfurization sour gas which characterized in that: comprises acid-gas separators (1), absorption and regeneration devices, magnetic suspension fans (3), a membrane filter press (4) and purification-gas separators (7), wherein the number of the absorption and regeneration devices is four, and are arranged in parallel, a gas outlet at the top of the acid-gas separator (1) is divided into four paths which are respectively connected to four groups of absorption and regeneration devices, each group of absorption and regeneration devices comprises an absorption tower (2), a lean and rich liquid heat exchanger (5) and an oxidation tower (6), a gas outlet at the top of the acid-gas separator (1) is connected to a gas inlet at the lower part of the absorption tower (2), a liquid outlet at the bottom of the absorption tower (2) flows into a rich solution channel of the lean-rich solution heat exchanger (5) through a rich solution pump (8), a rich liquid outlet of the lean-rich liquid heat exchanger (5) is connected to the top of the oxidation tower (6), a purified gas outlet at the top of the absorption tower (2) passes through the purified gas separator (7) and then is connected to an emptying pipe; a barren liquor outlet at the lower part of the oxidation tower (6) is connected to a barren liquor channel of the barren and rich liquor heat exchanger (5) through a barren liquor pump (9), the lean solution outlet of the lean-rich solution heat exchanger (5) is also connected to the upper part of the absorption tower (2), the number of the magnetic suspension fans (3) is at least two, an air outlet of each magnetic suspension fan (3) is connected with an air cooler (10), the air outlet of the air cooler (10) is respectively connected to the oxidation air distributor (11) at the inner lower part of each group of the oxidation tower (6) through a flow regulating valve, the oxidation tower (6) is a conical bottom, a sulfur slurry pump (12) is arranged at the lowest sulfur slurry outlet of the conical bottom of the oxidation tower (6), the outlet of the sulfur slurry pump (12) is connected to the sulfur slurry inlet of the membrane filter press (4), a bypass line is arranged on the outlet line of the sulfur slurry pump (12) and returns to the oxidation tower (6); the membrane filter press is characterized in that a filtrate tank (13) is arranged below the membrane filter press (4), filtrate collected in the filtrate tank (13) is pumped into a bypass pipeline through a filtrate pump (14) and then flows back to the oxidation tower (6), and a spiral conveyor (15) is further arranged below the membrane filter press (4) in a matched mode and used for bagging separated sulfur paste into a sulfur melting kettle.
2. The system for recovering sulfur from natural gas desulfurization acid gas according to claim 1, characterized in that: and a gas distributor is arranged in the absorption tower (2) and is connected with a gas inlet at the lower part of the absorption tower.
3. The system for recovering sulfur from natural gas desulfurization acid gas according to claim 1, characterized in that: and a liquid inlet pipeline of the barren pump (9) is connected with a medicament adding system through a metering pump.
4. The system for recovering sulfur from natural gas desulfurization acid gas according to claim 1, characterized in that: a first nozzle connected with a barren liquor pipeline is arranged above the middle in the absorption tower (2); and a second nozzle connected with a rich liquid pipeline is arranged above the inner part of the oxidation tower (6).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202220469316.5U CN216998308U (en) | 2022-03-04 | 2022-03-04 | Sulfur recovery system for natural gas desulfurization acid gas |
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| CN202220469316.5U CN216998308U (en) | 2022-03-04 | 2022-03-04 | Sulfur recovery system for natural gas desulfurization acid gas |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116836742A (en) * | 2023-07-31 | 2023-10-03 | 合肥万豪能源设备有限责任公司 | High-sulfur natural gas purifying and sulfur recycling system |
| CN117603744A (en) * | 2024-01-24 | 2024-02-27 | 山西国化能源有限责任公司 | Automatic natural gas desulfurization system |
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2022
- 2022-03-04 CN CN202220469316.5U patent/CN216998308U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116836742A (en) * | 2023-07-31 | 2023-10-03 | 合肥万豪能源设备有限责任公司 | High-sulfur natural gas purifying and sulfur recycling system |
| CN117603744A (en) * | 2024-01-24 | 2024-02-27 | 山西国化能源有限责任公司 | Automatic natural gas desulfurization system |
| CN117603744B (en) * | 2024-01-24 | 2024-04-09 | 山西国化能源有限责任公司 | Automatic natural gas desulfurization system |
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