CN113088331A - Process and system for sweetening alcohol and decarbonylation sulfur - Google Patents
Process and system for sweetening alcohol and decarbonylation sulfur Download PDFInfo
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- CN113088331A CN113088331A CN202110387634.7A CN202110387634A CN113088331A CN 113088331 A CN113088331 A CN 113088331A CN 202110387634 A CN202110387634 A CN 202110387634A CN 113088331 A CN113088331 A CN 113088331A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D36/00—Filter circuits or combinations of filters with other separating devices
- B01D36/003—Filters in combination with devices for the removal of liquids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D36/00—Filter circuits or combinations of filters with other separating devices
- B01D36/04—Combinations of filters with settling tanks
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
- C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
- C10G70/06—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes by gas-liquid contact
Abstract
The invention discloses a process and a system for removing mercaptans and carbonyl sulfides, which comprises the steps of carrying out primary treatment on liquefied gas based on a first alkaline washing pump and a first alkaline washing fiber membrane contactor; dehydrating the liquefied gas and hydrolyzing carbonyl sulfide by a dehydrating tower and a liquefied gas carbonyl sulfide hydrolyzing tower; performing secondary treatment on the liquefied gas based on a second alkali washing pump and a second alkali washing fiber membrane contactor; and washing the liquefied gas based on a washing fiber membrane contactor and a washing settling tank and discharging. The maximization of the contact area in the same volume of the fiber membrane contactor is realized; the efficiency of the two-phase chemical reaction and single-stage fiber membrane contactor can reach more than 98 percent; for pure physical extraction, the single-stage fiber membrane contactor can achieve more than 95% of efficiency; the uniform configuration of the fiber bundles is realized, the problem of rapid increase of pressure drop is avoided, and the internal pressure can be reduced to 70KPa in a three-year operation period, so that the fiber bundles are not easy to damage.
Description
Technical Field
The invention relates to the field of mass transfer equipment, in particular to a process and a system for removing mercaptans and carbonyl sulfide.
Background
The fiber membrane contactor is a novel mass transfer device, can be used for mass transfer processes such as reaction, extraction and extraction in the industries such as chemical industry, pharmacy, papermaking and environmental protection, and the use method is to distribute the secondary distribution phase on the fibrous filler to form a liquid membrane, so that the main distribution phase is distributed outside the liquid membrane; in the process of the two distribution phases flowing in the same direction, the two distribution phases have large contact mass transfer area and short mass transfer distance, thereby improving the mass transfer reaction efficiency. For the fiber membrane contactor, the contact area of the fiber filaments, the suspension mode of the fiber filaments and the mode of each distribution phase entering the fiber filaments seriously affect the efficiency and the service cycle of the fiber membrane contactor; if the contact area of the fiber filaments, the suspension mode of the fiber filaments and the mode of each distribution phase entering the fiber filaments are not designed reasonably, not only is the efficiency of the fiber membrane contactor low or even ineffective, but also the pressure drop of the fiber membrane contactor is possibly too large to be used, or the service cycle is possibly shortened greatly. In practical application, whether imported or domestic fiber membrane contactors, many cases prove that the service life of the existing equipment is easily shortened greatly due to overlarge pressure drop, so that the production cost is increased.
Disclosure of Invention
The invention aims to provide a process and a system for removing mercaptans and carbonyl sulfide, and aims to solve the problem that the existing equipment is easy to greatly shorten the service cycle due to overlarge pressure drop, so that the production cost is increased.
In order to achieve the above object, in a first aspect, the present invention provides a desulfurization alcohol and decarbonylation sulfur system, comprising a primary treatment component, a secondary treatment component and a water washing treatment component, wherein the primary treatment component comprises a filter, a primary alkaline washing settling tank, a primary alkaline washing fiber membrane contactor and a primary alkaline washing pump, the primary alkaline washing fiber membrane contactor is connected with the filter, the primary alkaline washing settling tank is connected with the primary alkaline washing fiber membrane contactor, the primary alkaline washing pump is communicated with the primary alkaline washing settling tank and the primary alkaline washing fiber membrane contactor, the secondary treatment component comprises a dehydration tower, a carbonyl sulfur hydrolysis tower, a secondary alkaline washing fiber membrane contactor, a secondary alkaline washing settling tank and a secondary alkaline washing pump, the dehydration tower is connected with the primary alkaline washing settling tank, the liquefied carbonyl sulfur hydrolysis tower is connected with the dehydration tower, the second grade alkali wash fibre membrane contactor with liquefied gas carbonyl sulphur hydrolysis tower is connected, the second grade alkali wash settling cask with the second grade alkali wash fibre membrane contactor is connected, the second grade alkali wash pump with second grade alkali wash fibre membrane contactor and second grade alkali wash settling cask intercommunication, the washing processing subassembly includes washing fibre membrane contactor and washing settling cask, washing fibre membrane contactor with the second grade alkali wash settling cask is connected, the washing settling cask with washing fibre membrane contactor is connected.
The primary treatment assembly further comprises a first liquid level controller, and the first liquid level controller is connected with the primary alkali washing settling tank.
The primary treatment component further comprises a first flow control valve, and the first flow control valve is connected with the primary alkali washing pump and the primary alkali washing fiber membrane contactor and is positioned between the primary alkali washing pump and the primary alkali washing fiber membrane contactor.
The secondary treatment component further comprises a second liquid level controller, and the second liquid level controller is connected with the secondary alkali washing settling tank.
The second-stage treatment component further comprises a second flow control valve, and the second flow control valve is connected with the second-stage alkaline washing pump and the second-stage alkaline washing fiber membrane contactor and is positioned between the second-stage alkaline washing pump and the second-stage alkaline washing fiber membrane contactor.
Wherein, the washing processing assembly further comprises a coalescer, and the coalescer is connected with the washing settling tank.
Wherein, the washing processing assembly still includes the washing pump, the washing pump with the washing settling cask with washing fibre membrane contactor intercommunication, and be located the washing settling cask with between the washing fibre membrane contactor.
In a second aspect, the present invention also provides a sweetening and decarbonylation process comprising: carrying out primary treatment on the liquefied gas based on a first alkaline washing pump and a first alkaline washing fiber membrane contactor; dehydrating the liquefied gas and hydrolyzing carbonyl sulfide by a dehydrating tower and a liquefied gas carbonyl sulfide hydrolyzing tower; performing secondary treatment on the liquefied gas based on a second alkali washing pump and a second alkali washing fiber membrane contactor; and washing the liquefied gas based on a washing fiber membrane contactor and a washing settling tank and discharging.
According to the process and the system for removing the mercaptan and the carbonyl sulfide, firstly, the liquefied gas is filtered by the filter to remove impurities, then enters the top of the primary alkali washing fiber membrane contactor, and is contacted with the alkali liquor circularly sent by the primary alkali washing pump at the top. Wherein the alkali liquor is circulated before start-up, firstly wetting the metal fibers in the contactor, flowing downwards along the fiber filaments, the liquefied gas flows in parallel along the fiber bundle and the alkali liquor in the same direction, so that a layer of flowing film is formed between the liquefied gas and the alkali liquor on the fiber bundle, thereby increasing the mass transfer area and improving the mass transfer rate, the hydrogen sulfide and the mercaptan are extracted into the alkali, the alkali liquor containing the sodium sulfide and the sodium hydrosulfide is separated from the fibers and settled at the bottom of the primary alkaline washing settling tank, the separated alkali liquor can be continuously circulated through the primary alkaline washing pump, the liquefied gas after primary alkaline washing flows out from the top of the primary alkaline washing settling tank and enters the bottom of the dehydration tower for dehydration, then flows out from the top of the dehydration tower and enters the bottom of the liquefied gas carbonyl sulfide hydrolysis tower, and carbonyl sulfide is hydrolyzed into the hydrogen sulfide and carbon dioxide in the liquefied gas carbonyl sulfide hydrolysis tower under the action of the carbonyl sulfide hydrolysis agent, and then the liquefied gas is discharged from the top of the liquefied gas carbonyl sulfide hydrolysis tower and enters the secondary alkali washing fiber membrane contactor, the top of the liquefied gas carbonyl sulfide hydrolysis tower is contacted with alkali liquor conveyed by a secondary alkali washing pump, the residual mercaptan, hydrogen sulfide and carbon dioxide in the liquefied gas are further removed, after sedimentation and separation, the alkali liquor at the bottom of the tank is recycled for secondary mercaptan removal of the liquefied gas or for the primary alkali washing fiber membrane contactor, the liquefied gas is discharged from the secondary alkali washing settling tank and enters the water washing fiber membrane contactor, then the liquefied gas enters the water washing settling tank, alkali drops possibly carried in the liquefied gas are washed, and then the liquefied gas enters a downstream process. Therefore, the maximization of the contact area in the same volume of the fiber membrane contactor is realized, and the minimization of equipment with the same treatment capacity can be ensured; the efficiency of the two-phase chemical reaction and single-stage fiber membrane contactor can reach more than 98 percent; for pure physical extraction, the single-stage fiber membrane contactor can achieve more than 95% of efficiency; the uniform configuration of the fiber bundles is realized, the problem of rapid increase of pressure drop is avoided, and the internal pressure drop can be reduced to 70KPa in a three-year operation period; the method has the advantages that the removal efficiency of liquefied gas mercaptan is realized, the total sulfur removal efficiency of the liquefied gas is guaranteed, the total sulfur of the liquefied gas after removal can be guaranteed to be less than 10ppm, the service life of the equipment is easily shortened greatly due to overlarge pressure drop, and the production cost is improved.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a block diagram of a desulfurization alcohol and decarbonylation system of the present invention;
FIG. 2 is a block diagram of a primary processing module of the present invention;
FIG. 3 is a block diagram of a secondary processing component of the present invention;
FIG. 4 is a block diagram of a water wash treatment assembly of the present invention;
FIG. 5 is a flow diagram of a desulfurized alcohol and decarbonylthio process of the invention.
1-first-stage treatment component, 2-second-stage treatment component, 3-water washing treatment component, 11-filter, 12-first-stage alkaline washing settling tank, 13-first-stage alkaline washing fiber membrane contactor, 14-first-stage alkaline washing pump, 15-first liquid level controller, 16-first flow control valve, 21-dehydration tower, 22-liquefied gas carbonyl sulfide hydrolysis tower, 23-second-stage alkaline washing fiber membrane contactor, 24-second-stage alkaline washing settling tank, 25-second-stage alkaline washing pump, 26-second liquid level controller, 27-second flow control valve, 31-water washing fiber membrane contactor, 32-water washing settling tank, 33-coalescer, 34-water washing pump, 35-third liquid level controller and 36-third flow control valve.
Detailed Description
Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings, wherein like or similar reference numerals refer to the same or similar elements or elements having the same or similar function throughout. The embodiments described below with reference to the drawings are illustrative and intended to be illustrative of the invention and are not to be construed as limiting the invention.
In a first aspect, referring to FIGS. 1-4, the present invention provides a system for removing mercaptans and carbonyl sulfide, comprising:
the device comprises a primary treatment component 1, a secondary treatment component 2 and a water washing treatment component 3, wherein the primary treatment component 1 comprises a filter 11, a primary alkali washing settling tank 12, a primary alkali washing fiber membrane contactor 13 and a primary alkali washing pump 14, the primary alkali washing fiber membrane contactor 13 is connected with the filter 11, the primary alkali washing settling tank 12 is connected with the primary alkali washing fiber membrane contactor 13, the primary alkali washing pump 14 is communicated with the primary alkali washing settling tank 12 and the primary alkali washing fiber membrane contactor 13, the secondary treatment component 2 comprises a dewatering tower 21, a liquefied gas carbonyl sulfide hydrolysis tower 22, a secondary alkali washing fiber membrane contactor 23, a secondary alkali washing settling tank 24 and a secondary alkali washing pump 25, the dewatering tower 21 is connected with the primary alkali washing settling tank 12, the liquefied gas carbonyl sulfide hydrolysis tower 22 is connected with the dewatering tower 21, the secondary alkali washing fiber membrane contactor 23 is connected with the liquefied gas carbonyl sulfide hydrolysis tower 22, the second grade alkali wash settling cask 24 with second grade alkali wash fibre membrane contactor 23 is connected, second grade alkali wash pump 25 and second grade alkali wash fibre membrane contactor 23 and second grade alkali wash settling cask 24 intercommunication, the washing processing subassembly includes washing fibre membrane contactor 31 and washing settling cask 32, washing fibre membrane contactor 31 with second grade alkali wash settling cask 24 is connected, washing settling cask 32 with washing fibre membrane contactor 31 is connected.
In the present embodiment, the chemical reactions of mercaptan, hydrogen sulfide, and carbon dioxide in the liquefied gas by alkaline cleaning (desorption) are as follows:
RSH+NaOH→NaSR+H2O
H2S+NaOH→NaHS+H2O
CO2+2NaOH→Na2CO3+H2O
the chemical reactions of carbonyl sulfide and carbon disulfide hydrolysis in the liquefied gas are as follows:
COS+H2O＝H2S+CO2
CS2+2H2O＝2H2S+CO2
firstly, the liquefied gas is filtered by the filter 11 to remove impurities, and then enters the top of the primary alkali washing fiber membrane contactor 13, and the top of the primary alkali washing fiber membrane contactor is contacted with alkali liquor circularly sent by the primary alkali washing pump 14. Wherein the alkali liquor is circulated before the start-up, firstly the metal fiber in the contactor is wetted, and the alkali liquor flows downwards along the fiber yarn, the liquefied gas flows along the fiber bundle and the alkali liquor in parallel, so that a layer of flowing film is formed between the liquefied gas and the alkali liquor on the fiber bundle, thereby increasing the mass transfer area and improving the mass transfer rate, the hydrogen sulfide and the mercaptan are extracted into the alkali, the alkali liquor containing the sodium sulfide and the sodium mercaptan is separated from the fiber and settled at the bottom of the primary alkaline washing settling tank 12, the separated alkali liquor can be continuously circulated through the primary alkaline washing pump 14, the liquefied gas after the primary alkaline washing flows out from the top of the primary alkaline washing settling tank 12 and enters the bottom of the dehydrating tower 21 for dehydration, then the liquefied gas flows out from the top of the dehydrating tower 21 and enters the bottom of the carbonyl sulfide hydrolyzing tower 22, and is subjected to the action of the carbonyl sulfide hydrolyzing agent in the liquefied gas carbonyl sulfide hydrolyzing tower, hydrolyzing carbonyl sulfide into hydrogen sulfide and carbon dioxide, discharging liquefied gas from the top of the liquefied gas carbonyl sulfide hydrolysis tower 22, entering the secondary alkali washing fiber membrane contactor 23, contacting the top with alkali liquor sent by a secondary alkali washing pump 25, further removing residual mercaptan, hydrogen sulfide and carbon dioxide in the liquefied gas, after settling and separating, recycling the alkali liquor at the bottom of the tank for secondary mercaptan removal of the liquefied gas or entering the primary alkali washing fiber membrane contactor 13, discharging the liquefied gas from the secondary alkali washing settling tank 24, entering the water washing fiber membrane contactor 31, then entering the water washing settling tank 32, washing alkali drops possibly carried in the liquefied gas, and then entering a downstream process. Therefore, the maximization of the contact area in the same volume of the fiber membrane contactor is realized, and the minimization of equipment with the same treatment capacity can be ensured; the efficiency of the two-phase chemical reaction and single-stage fiber membrane contactor can reach more than 98 percent; for pure physical extraction, the single-stage fiber membrane contactor can achieve more than 95% of efficiency; the uniform configuration of the fiber bundles is realized, the problem of rapid increase of pressure drop is avoided, and the internal pressure drop can be reduced to 70KPa in a three-year operation period; the method has the advantages that the removal efficiency of liquefied gas mercaptan is realized, the total sulfur removal efficiency of the liquefied gas is guaranteed, the total sulfur of the liquefied gas after removal can be guaranteed to be less than 10ppm, the service life of the equipment is easily shortened greatly due to overlarge pressure drop, and the production cost is improved.
Further, the primary treatment assembly 1 further comprises a first liquid level controller 15, and the first liquid level controller 15 is connected with the primary alkaline washing settling tank 12.
In this embodiment, the first liquid level controller 15 can detect the liquid level in the primary caustic wash settling tank 12, so that the excess liquid can be automatically discharged.
Further, the primary treatment assembly 1 further comprises a first flow control valve 16, and the first flow control valve 16 is connected with the primary alkali washing pump 14 and the primary alkali washing fiber membrane contactor 13 and is located between the primary alkali washing pump 14 and the primary alkali washing fiber membrane contactor 13.
In this embodiment, the flow rate of the first alkaline washing pump can be detected by the first flow rate control valve 16, so that the control is more convenient.
Further, the secondary treatment component 2 further comprises a second level controller 26, and the second level controller 26 is connected with the secondary caustic washing settling tank 24.
In this embodiment, the liquid level in the secondary alkaline washing settling tank 24 can be detected by the second liquid level controller 26, so that the excessive liquid can be automatically discharged.
Further, the secondary treatment component 2 further comprises a second flow control valve 27, and the second flow control valve 27 is connected with the secondary alkaline washing pump 25 and the secondary alkaline washing fiber membrane contactor 23 and is located between the secondary alkaline washing pump 25 and the secondary alkaline washing fiber membrane contactor 23.
In this embodiment, the flow rate of the second alkaline washing pump can be detected by the second flow rate control valve 27, so that the control is more convenient.
Further, the water washing processing assembly 3 further comprises a coalescer 33, and the coalescer 33 is connected with the water washing settling tank 32.
In the present embodiment, the coalescer 33 can rapidly collect the liquefied gas after the treatment, thereby improving the treatment efficiency.
Further, the washing processing component 3 further comprises a washing pump 34, the washing pump 34 is communicated with the washing settling tank 32 and the washing fiber membrane contactors 31, and is positioned between the washing settling tank 32 and the washing fiber membrane contactors 31.
In the present embodiment, the water in the water washing settling tank 32 can be circularly introduced into the water washing fiber membrane contactor 31 by the water washing pump 34, so that the liquefied gas is more sufficiently contacted, and the reaction efficiency is improved.
Further, the water washing processing assembly 3 further comprises a third liquid level controller 35, and the third liquid level controller 35 is connected with the water washing settling tank 32.
In the present embodiment, the liquid level in the water wash settling tank 32 can be detected by the third liquid level controller 35, and thus, the excess liquid can be automatically discharged.
Further, the water washing processing assembly 3 comprises a third flow control valve 36, and the third flow control valve 36 is connected with the water washing pump 34 and the water washing fiber membrane contactor 31 and is located between the water washing pump 34 and the water washing fiber membrane contactor 31.
In the present embodiment, the third flow rate control valve 36 can detect the flow rate of the washing pump 34, thereby facilitating control.
In a second aspect, referring to fig. 5, the present invention also provides a desulfurization alcohol and decarbonylation process, comprising:
s101, carrying out primary treatment on the liquefied gas based on a first alkaline washing pump and a first alkaline washing fiber membrane contactor;
firstly, the liquefied gas is filtered by the filter 11 to remove impurities, and then enters the top of the primary alkali washing fiber membrane contactor 13, and the top of the primary alkali washing fiber membrane contactor is contacted with alkali liquor circularly sent by the primary alkali washing pump 14. The alkali liquor is circulated before the start-up, the metal fibers in the contactor are wetted firstly, the alkali liquor flows downwards along the fiber filaments, the liquefied gas flows in parallel along the fiber bundles and the alkali liquor in the same direction, a layer of flowing film is formed between the liquefied gas and the alkali liquor on the fiber bundles, the mass transfer area is increased, the mass transfer rate is improved, the hydrogen sulfide and the mercaptan are extracted into the alkali, and the alkali liquor containing the sodium sulfide and the sodium mercaptan is separated from the fibers and is settled at the bottom of the primary alkali washing settling tank 12.
S102, dehydrating the liquefied gas and hydrolyzing carbonyl sulfide through a dehydrating tower 21 and a liquefied gas carbonyl sulfide hydrolysis tower 22;
the liquefied gas after the primary alkali washing enters the bottom of the dehydrating tower 21 from the top of the primary alkali washing settling tank 12 for dehydration, then enters the bottom of the liquefied gas carbonyl sulfide hydrolysis tower 22 from the top of the dehydrating tower 21, and carbonyl sulfide is hydrolyzed into hydrogen sulfide and carbon dioxide in the liquefied gas carbonyl sulfide hydrolysis tower 22 under the action of a carbonyl sulfide hydrolyzing agent.
S103, carrying out secondary treatment on the liquefied gas based on a second alkali washing pump and a second alkali washing fiber membrane contactor;
liquefied gas is discharged from the top of the liquefied gas carbonyl sulfide hydrolysis tower 22 and enters the secondary caustic washing fiber membrane contactor 23, and the liquefied gas is contacted with alkali liquor sent by a secondary caustic washing pump 25 at the top, so that residual mercaptan, hydrogen sulfide and carbon dioxide in the liquefied gas are further removed.
S104 washes and discharges the liquefied gas with water based on the water-washed fiber membrane contactor 31 and the water-washed settling tank 32.
Liquefied gas is discharged from the secondary caustic washing settling tank 24, enters the water-washing fiber membrane contactor 31, then enters the water-washing settling tank 32, is washed to remove caustic droplets possibly carried in the liquefied gas, and then enters a downstream process.
While the invention has been described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes in form and detail may be made therein without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (8)
1. A desulfurization alcohol and decarbonylation sulfur system is characterized in that,
the device comprises a primary treatment component, a secondary treatment component and a water washing treatment component, wherein the primary treatment component comprises a filter, a primary alkali washing settling tank, a primary alkali washing fiber membrane contactor and a primary alkali washing pump, the primary alkali washing fiber membrane contactor is connected with the filter, the primary alkali washing settling tank is connected with the primary alkali washing fiber membrane contactor, the primary alkali washing pump is communicated with the primary alkali washing settling tank and the primary alkali washing fiber membrane contactor, the secondary treatment component comprises a dehydration tower, a liquefied gas carbonyl sulfide hydrolysis tower, a secondary alkali washing fiber membrane contactor, a secondary alkali washing settling tank and a secondary alkali washing pump, the dehydration tower is connected with the primary alkali washing settling tank, the liquefied gas carbonyl sulfide hydrolysis tower is connected with the dehydration tower, the secondary alkali washing fiber membrane contactor is connected with the liquefied gas carbonyl sulfide hydrolysis tower, the secondary alkali washing settling tank is connected with the secondary alkali washing fiber membrane contactor, the secondary alkali washing pump is communicated with the secondary alkali washing fiber membrane contactor and the secondary alkali washing settling tank, the water washing processing assembly comprises a water washing fiber membrane contactor and a water washing settling tank, the water washing fiber membrane contactor is connected with the secondary alkali washing settling tank, and the water washing settling tank is connected with the water washing fiber membrane contactor.
2. A desulfurization alcohol and decarbonylation sulfur system according to claim 1,
the primary treatment assembly further comprises a first liquid level controller, and the first liquid level controller is connected with the primary alkali washing settling tank.
3. A desulfurization alcohol and decarbonylation sulfur system according to claim 2,
the primary treatment component further comprises a first flow control valve, and the first flow control valve is connected with the primary alkali washing pump and the primary alkali washing fiber membrane contactor and is positioned between the primary alkali washing pump and the primary alkali washing fiber membrane contactor.
4. A desulfurization alcohol and decarbonylation sulfur system according to claim 1,
the secondary treatment component also comprises a second liquid level controller, and the second liquid level controller is connected with the secondary alkali washing settling tank.
5. A desulfurization alcohol and decarbonylation sulfur system according to claim 4,
the second-stage treatment component also comprises a second flow control valve, and the second flow control valve is connected with the second-stage alkaline washing pump and the second-stage alkaline washing fiber membrane contactor and is positioned between the second-stage alkaline washing pump and the second-stage alkaline washing fiber membrane contactor.
6. A desulfurization alcohol and decarbonylation sulfur system according to claim 1,
the water washing treatment assembly further comprises a coalescer, and the coalescer is connected with the water washing settling tank.
7. A desulfurization alcohol and decarbonylation sulfur system according to claim 6,
the washing processing assembly further comprises a washing pump, wherein the washing pump is communicated with the washing settling tank and the washing fiber membrane contactors and is positioned between the washing settling tank and the washing fiber membrane contactors.
8. A desulfurization alcohol and decarbonylation process applied to a desulfurization alcohol and decarbonylation system according to any one of claims 1 to 7,
the method comprises the following steps: carrying out primary treatment on the liquefied gas based on a first alkaline washing pump and a first alkaline washing fiber membrane contactor;
dehydrating the liquefied gas and hydrolyzing carbonyl sulfide by a dehydrating tower and a liquefied gas carbonyl sulfide hydrolyzing tower;
performing secondary treatment on the liquefied gas based on a second alkali washing pump and a second alkali washing fiber membrane contactor;
and washing the liquefied gas based on a washing fiber membrane contactor and a washing settling tank and discharging.
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| CN202110387634.7A CN113088331A (en) | 2021-04-09 | 2021-04-09 | Process and system for sweetening alcohol and decarbonylation sulfur |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202110387634.7A CN113088331A (en) | 2021-04-09 | 2021-04-09 | Process and system for sweetening alcohol and decarbonylation sulfur |
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| CN204058377U (en) * | 2014-09-02 | 2014-12-31 | 徐振华 | A kind of mercaptan oxidation and alkali liquor oxidized regenerating unit |
| CN105885937A (en) * | 2016-06-21 | 2016-08-24 | 宁波章甫能源科技有限公司 | Fine desulfurization method for liquid hydrocarbon |
| CN205676426U (en) * | 2016-06-21 | 2016-11-09 | 宁波章甫能源科技有限公司 | A kind of device of liquid hydrocarbon fine de-sulfur |
| CN106365944A (en) * | 2016-08-30 | 2017-02-01 | 宁波中金石化有限公司 | Method for preparing polymerization-grade propylene through liquefied petroleum gas separation |
| CN112221324A (en) * | 2020-09-28 | 2021-01-15 | 南京金炼科技有限公司 | Process for removing carbonyl sulfide in liquefied gas |
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2021
- 2021-04-09 CN CN202110387634.7A patent/CN113088331A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN204058377U (en) * | 2014-09-02 | 2014-12-31 | 徐振华 | A kind of mercaptan oxidation and alkali liquor oxidized regenerating unit |
| CN105885937A (en) * | 2016-06-21 | 2016-08-24 | 宁波章甫能源科技有限公司 | Fine desulfurization method for liquid hydrocarbon |
| CN205676426U (en) * | 2016-06-21 | 2016-11-09 | 宁波章甫能源科技有限公司 | A kind of device of liquid hydrocarbon fine de-sulfur |
| CN106365944A (en) * | 2016-08-30 | 2017-02-01 | 宁波中金石化有限公司 | Method for preparing polymerization-grade propylene through liquefied petroleum gas separation |
| CN112221324A (en) * | 2020-09-28 | 2021-01-15 | 南京金炼科技有限公司 | Process for removing carbonyl sulfide in liquefied gas |
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Application publication date: 20210709 |
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