CN100460483C - Method and device for lye extraction desulfurization - Google Patents
Method and device for lye extraction desulfurization Download PDFInfo
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- CN100460483C CN100460483C CNB2005101322997A CN200510132299A CN100460483C CN 100460483 C CN100460483 C CN 100460483C CN B2005101322997 A CNB2005101322997 A CN B2005101322997A CN 200510132299 A CN200510132299 A CN 200510132299A CN 100460483 C CN100460483 C CN 100460483C
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Abstract
The invention provides a method and device for desulfurization from hydrocarbon flow thorough alkaline liquid suction. It is to add a gas- removal system between oxidation system and phase separation system, and introduce inert gas into gas- removal system to exchange oxidative gas and then effectivelyt promote the separation of sulfur dioxide or sulfur dioxide- containing solvent from regenerative alkaline liquid in phase separation system, and the thiol in hydrocarbon flow can be inhibited from oxidation by oxidative gas in suction system, which enables thorough desulfurization by alkaline liquid suction.
Description
Technical field
The invention belongs to the field of refinement of hydrocarbon material.Particularly, the present invention relates to a kind of fluid that passes through the alkali lye extracting to hydrocarbon material, promptly hydrocarbon stream carries out the method and apparatus of desulfurization.
Background technology
The alkali lye extracting is a kind of traditional method of refining hydrocarbon material, and the mercaptan removal that is widely used in hydrocarbon materials such as liquefied petroleum gas (LPG), gasoline, diesel oil, petroleum naphtha, alkane, alkene is refining.This method is the fluid with hydrocarbon material, and promptly hydrocarbon stream contacts with alkali lye, and the mercaptan in the hydrocarbon stream is by generating thiolate with alkaline reaction and removing from oil product.
Directly discharge the both uneconomical environmental requirement that also do not meet if contain the alkali lye of thiolate.Thereby adopting oxidation style that thiolate is oxidized to disulphide usually makes the alkali lye that contains thiolate obtain regeneration (consulting U.S. Pat 2853432).Particularly, this method makes the thiolate that is dissolved in the alkali lye be oxidized to disulphide, thereby alkali lye is regenerated by inject oxidizing gas and oxide catalyst in used alkali lye.After this, by settlement separate or organic hydrocarbon solvent extraction regeneration alkali lye is separated with the alkali lye of will regenerating with wherein disulphide and continue on for removing mercaptan in the hydrocarbon stream, significantly reduce the discharging of salkali waste thus.
Therefore, existing lye extraction desulfurization method comprises following basic step: (1) extracting, and (2) oxidation, (3) are separated.In extraction system, alkali lye (comprising regeneration alkali lye) contacts with the hydrocarbon stream that contains mercaptan, and generates thiolate with thiol reactant; In oxidation system, the alkali lye that contains thiolate from extraction system mixes with oxidizing gas that is injected and oxide catalyst, make the thiolate in the alkali lye be oxidized to disulphide, thereby alkali lye is regenerated, wherein oxide catalyst is the metal phthalocyanine of widely knowing, as the sulfonate of phthalocyanine cobalt, common metal phthalocyanine catalyst is along with fresh alkali lye intermittence or inject oxidation system continuously; In phase-separation system, be separated from each other by sedimentation from the regeneration alkali lye of oxidation system and the mixture of disulphide, perhaps will by sedimentation regeneration alkali lye be separated with the solvent phase that contains disulphide after this mixture and the organic hydrocarbon solvent, the regeneration alkali lye of handling through being separated is back to extraction system to be continued to use.
Obviously, if disulphide separates not exclusively, making still remainingly in the regeneration alkali lye has disulphide, and the alkali lye of regenerating so is being back to extraction system when continuing to use, and disulphide wherein just might be carried to hydrocarbon stream by back suction.Therefore, the improvement of this method is mainly concentrated on separate (the consulting U.S. Pat 4705620, US4362614 and US3574093) of disulphide and regeneration alkali lye.In addition, U.S. Pat 2921020 also utilizes oxygen residual in the regeneration alkali lye and oxide catalyst that the hydrocarbon stream of handling through extracting is carried out secondary treatment, further to remove mercaptan remaining in the hydrocarbon stream.
Though aforesaid method has bigger improvement aspect the mercaptan removing, and if suitable operation (for example, the amount of the oxidizing gas of injection is moderate, and can discharge fully, and in phase-separation system, regeneration alkali lye can separate fully with disulphide), also can have tangible sweetening effectiveness.But should be noted that, in the prior art, particularly in actual applications, because the variation of mercaptans content in the hydrocarbon stream, make the mercaptans content be absorbed in the alkali lye change thereupon, therefore complete for the alkali liquid regeneration that guarantees to contain mercaptan, need in oxidation system, to inject the oxidizing gas that is higher than theory measurement far away usually, and excessive oxidizing gas flows in the phase-separation system with alkali lye usually, and is difficult to discharge fully in phase-separation system.
This just causes two defectives: the one, and the oxidizing gas that flows into phase-separation system easily forms aeration regeneration alkali lye and disulphide mutually or contain solvent phase settlement separate of disulphide in alkali lye, make the solvent that still is entrained with disulphide in the regeneration alkali lye or contains disulphide, when regeneration alkali lye turns back to extraction system and recycles, the disulphide back suction can be carried to hydrocarbon stream, be caused sweetening effectiveness not obvious; The 2nd, the oxidizing gas that remains in the alkali lye is back to extraction system with regeneration alkali lye, at least a portion mercaptan in the hydrocarbon stream generates disulphide under this oxidizing gas and the effect with alkali lye round-robin oxide catalyst, described disulphide not with alkaline reaction, and remain in the hydrocarbon stream, therefore can't realize handling hydrocarbon stream to carry out the purpose of desulfurization with alkali lye, sweetening effectiveness is not obvious at least.
Prior art has been ignored the oxidizing gas carried secretly in the alkali lye to being separated and extractive disadvantageous effect, causes sweetening effectiveness not obvious.The present invention is directed to above-mentioned defective prior art is improved, with the purpose of abundant realization lye extraction desulfurization.
Summary of the invention
One of purpose of the present invention is to provide a kind of method of lye extraction desulfurization, comprises the steps:
Extracting contacts in extraction system with alkali lye even contain the hydrocarbon stream of mercaptan, generates thiolate in the alkali lye so that the mercaptan in the hydrocarbon stream is absorbed into, and exports as product through the hydrocarbon stream of desulfurization;
Oxidation, the alkali lye that contains thiolate that is about to generate in the extraction system is delivered to oxidation system, and the thiolate in the described alkali lye is oxidized to disulphide through oxidizing gas under the effect of catalyzer, thereby makes alkali liquid regeneration;
The degassing is about to the regeneration alkali lye of oxidation system and the mixture of disulphide and oxidizing gas and delivers to degas system, and removes oxidizing gas therein;
Be separated, be about to deliver to phase-separation system, regeneration alkali lye is separated with disulphide by sedimentation or organic solvent extracting through the regeneration alkali lye of degas system processing and the mixture of disulphide;
At last, will be back to extraction system from the regeneration alkali lye of phase-separation system recycles.
The method of lye extraction desulfurization of the present invention is introduced degassing step between original oxidation and phase separation step, to remove the oxidizing gas of carrying secretly in the regeneration alkali lye, thereby the solvent phase that effectively promotes disulphide or contain disulphide in phase-separation system with the separating of regeneration alkali lye, and the oxidizing gas oxidation of further avoiding the mercaptan in the hydrocarbon stream in extraction system, to be carried secretly by alkali lye, with the purpose of abundant realization lye extraction desulfurization.
Another object of the present invention is to provide a kind of equipment that is used for lye extraction desulfurization, this equipment comprises extraction system, oxidation system, degas system and phase-separation system.The equipment of lye extraction desulfurization provided by the invention increases the degas system that is used to remove oxidizing gas between oxidation system and phase-separation system, to remove the oxidizing gas of carrying secretly in the regeneration alkali lye, thereby avoid that effectively oxidizing gas is introduced phase-separation system and extraction system causes disadvantageous effect, improve the effect of lye extraction desulfurization.
Description of drawings
Fig. 1 has exemplarily represented a preferred embodiment of the present invention.
Fig. 2 is the schematic flow sheet of lye extraction desulfurization method in the prior art.
Embodiment
The invention provides a kind of method of lye extraction desulfurization, comprise the steps:
Extracting contacts in extraction system with alkali lye even contain the hydrocarbon stream of mercaptan, generates thiolate in the alkali lye so that the mercaptan in the hydrocarbon stream is absorbed into, and exports as product through the hydrocarbon stream of desulfurization;
Oxidation, the alkali lye that contains thiolate that is about to generate in the extraction system is delivered to oxidation system, and the thiolate in the described alkali lye is oxidized to disulphide through oxidizing gas under the effect of catalyzer, thereby makes alkali liquid regeneration;
The degassing is about to the regeneration alkali lye of oxidation system and the mixture of disulphide and oxidizing gas and delivers to degas system, and removes oxidizing gas therein;
Be separated, be about to deliver to phase-separation system, regeneration alkali lye is separated with disulphide by sedimentation or organic solvent extracting through the regeneration alkali lye of degas system processing and the mixture of disulphide;
At last, will be back to extraction system from the regeneration alkali lye of phase-separation system recycles.
The method of lye extraction desulfurization of the present invention is introduced degassing step between original oxidation and phase separation step, to remove the oxidizing gas of carrying secretly in the regeneration alkali lye, thereby the solvent phase that effectively promotes disulphide or contain disulphide in phase-separation system with the separating of regeneration alkali lye, and the oxidizing gas oxidation of further avoiding the mercaptan in the hydrocarbon stream in extraction system, to be carried secretly by alkali lye, with the purpose of abundant realization lye extraction desulfurization.
Described method can be used for processing and comprises liquefied petroleum gas (LPG), gasoline, diesel oil, petroleum naphtha, C
1～C
5Alkane and C
2～C
4Alkene is at interior hydrocarbon stream.The required alkali lye of extracting hydrocarbon stream is the alkali lye commonly used that is used for the extracting hydrocarbon stream, is replenished in oxidation system usually.Except importing fresh alkali lye, generally also need add catalyzer, as the sulfonate of phthalocyanine cobalt to guarantee the regeneration effect of alkali lye.The employed oxidizing gas of oxidation system is generally air or contains the mixed gas of oxygen.
Described degassing step can adopt usually and vacuumize and/or mode such as heating.In one embodiment, the degassing is operating as and adopts vacuum pump that the pressure of degas system is reduced to 0.2～0.8MPa.In a further preferred embodiment, when the degassing is operating as degas system is heated to 50～100 ℃, the pressure of operating system is reduced to 0.2～0.5MPa.
Preferably, degassing step adopts inert gas flow replace oxygen voltinism gas, and this replacement process can carry out separately, also can vacuumize and/or mode such as heating combine and carries out with above-mentioned, separates out from alkali lye with promotion disulphide.Described inert gas flow be nitrogen, hydrogen, organic hydrocarbon gas etc. immiscible with alkali lye, be difficult to the gas that reacts with mercaptan, preferred nitrogen, hydrogen or its mixture.Its consumption is generally 1/500～10/1 of alkali lye volume, is preferably 1/200～1/1 of alkali lye volume, and more preferably 1/200～1/12 of the alkali lye volume.This rare gas element discharges at degas system, and does not flow into phase-separation system with regeneration alkali lye, thus the solvent phase that can effectively promote disulphide or contain disulphide in phase-separation system with the separating of regeneration alkali lye.
More preferably, the top of degas system can be provided with conventional condenses retrieving arrangement, to reclaim the light hydrocarbon component of carrying secretly in institute's emission gases that contains disulphide.Because alkali lye when extraction system is delivered to degas system via oxidation system, can be entrained with light hydrocarbon component usually, these light hydrocarbon components evaporate and are entrained with disulphide at degas system from alkali lye, and directly discharging will pollute atmosphere.Therefore, be environmentally friendly in degassing step condenses recovering liquid.The gas that degas system discharges also can be delivered to processing unit again and handle.Above-mentioned condenses retrieving arrangement and gas processing unit again are known to those skilled in the art.
The present invention also provides a kind of equipment that is used for lye extraction desulfurization, and this equipment comprises extraction system, oxidation system, degas system and phase-separation system.This equipment also can comprise the pipeline that is used for importing to oxidation system fresh alkali lye and catalyzer.
The equipment of lye extraction desulfurization provided by the invention increases the degas system that is used to remove oxidizing gas between oxidation system and phase-separation system, to remove the oxidizing gas of carrying secretly in the regeneration alkali lye, thereby avoid that effectively oxidizing gas is introduced phase-separation system and extraction system causes disadvantageous effect, improve the effect of lye extraction desulfurization.Usually, degas system is positioned at the upstream of phase-separation system, can possess vacuum extractor and/or heating unit, is used for handled liquid is vacuumized and/or heats, to help the degassing.Degas system generally comprise vertical tower or jar and the pipeline that is used to import the pipeline of rare gas element and is used to discharge gas.Preferably, the top of degas system can be provided with conventional condenses retrieving arrangement, to reclaim the light hydrocarbon component of carrying secretly in institute's emission gases that contains disulphide.
In a preferred embodiment, the present invention is used for the equipment of lye extraction desulfurization, and its degas system comprises vacuum pump, heating jacket, vertical tower, be used to the condenses retrieving arrangement importing the pipeline of rare gas element and be used to discharge the pipeline of gas and be positioned at the top.
Below in conjunction with accompanying drawing the present invention is further described.Accompanying drawing only is intended to usually represent the flow process of a preferred embodiment of the present invention, and do not plan to provide the details such as operating device of relevant container, well heater, water cooler, pump, compressor, valve, technological process, these are basic equipment to knowing those skilled in the art.
Hydrocarbon stream enters extraction system 3 through pipeline 1, and contains catalyzer, and for example the alkali lye of metal phthalocyanine catalyst enters extraction system 3 through pipeline 2.Usually, alkali lye is preferably the aqueous solution of alkali metal hydroxide, for example the aqueous solution of sodium hydroxide, potassium hydroxide, lithium hydroxide etc.If necessary, also can use the aqueous solution of alkaline earth metal hydroxides, for example calcium hydroxide, hydrated barta etc.The particularly preferred alkali lye of the present invention is that weight percent is 1～50% aqueous sodium hydroxide solution, and more preferably operating weight per-cent is 5～25% aqueous sodium hydroxide solution.Extraction system 3 normally is equipped with the vertical tower of suitable contact device, and for example contact device such as flapper disk, tower tray is used so that two kinds of fluid-tights contacts of injecting.Hydrocarbon stream contacts in extraction system 3 convection current with alkali lye.Hydrocarbon stream through lye extraction desulfurization leaves extraction system 3 by pipeline 4.The temperature of extraction system 3 is between 25～100 ℃, preferably between 30～75 ℃.The pressure of extraction system 3 can be through selecting to make hydrocarbon stream keep liquid phase state, usually between 0.1～2.0MPa.
The alkali lye that is rich in thiolate flows into oxidation systems 8 through pipeline 5, and and mixes through the oxidizing gas that pipeline 7 enters oxidation system 8.Oxidation system preferably uses air as oxidizing gas, and the amount of air equals at least to make that mercaptan salt is oxidized to the required stoichiometry of disulphide in the alkali lye, is generally stoichiometric 2～4 times.The pressure of oxidation system 8 and generally is starkly lower than the pressure of extraction system 3 between 0.1～2.0MPa, in a typical embodiment, optimum operation pressure is between 0.2～0.5MPa.The temperature of oxidation system 8 is between 25～100 ℃, preferably between 30～75 ℃.Usually, if desired, fresh alkali lye and catalyzer can be through pipeline 6 inputs.
Flow into degas system 10 from residual oxidizing gas, the disulphide of oxidation system 8 and the mixture of the alkali lye of regenerating through pipeline 9.Degas system 10 can adopt simple vertical tower, jar or similar containers, also can adopt the vertical tower, jar or the similar containers that contain suitable contact device.Flow into degas system 10 from the regeneration alkali lye of oxidation system 8, rare gas element is flowed through pipeline 11 from the bottom up by degas system 10, and with discharging from the oxidizing gas of oxidation system 8 pipeline 12 from degas system 10 tops.Preferably, gas phase is when flowing through pipeline 12, and the light hydrocarbon component of wherein carrying secretly that contains disulphide that evaporates from alkali lye is recycled to the condenses retrieving arrangement at pipeline 12 tops through condensation, thereby has avoided the pollution to environment.And in the prior art, residual oxidizing gas is normally discharged through pipeline 17 ' in phase-separation system 15 '.The temperature of degas system 10 is usually between 25～100 ℃, preferably between 30～75 ℃.The pressure of degas system 10 and generally is lower than the pressure of extraction system 3 between 0.1～2.0MPa.In a typical embodiment, optimum operation pressure is 0.2～0.5MPa.
In phase-separation system 15, flow into through pipeline 13 from the regeneration alkali lye that is mixed with disulphide of degas system 10.And because residual oxidizing gas discharges through pipeline 12 at the top of degas system 10, the fluid that therefore enters phase-separation system 15 mainly is a liquid phase fluid.The temperature that phase-separation system 15 is adopted is a normal temperature, and the pressure that is adopted is less than or equal to the pressure of degas system 10.Liquid phase fluid in the phase-separation system 15 flows out by two different pipelines according to its character: the immiscible substantially disulphide of (1) and alkali lye directly flows out through pipeline 18 mutually, perhaps with organic hydrocarbon solvent (the organic hydrocarbon solvent mixes with the alkali lye of regenerating through pipeline 14) through pipeline 18 outflows; (2) alkali lye flows out and is back to extraction system through pipeline 2 through pipeline 16 and recycles.The organic hydrocarbon solvent of extracting disulphide can be selected petroleum naphtha, aviation jet fuel etc. for use.Simultaneously, the pipeline 17 of phase-separation system 15 links to each other with the pipeline 12 of degas system 10, with the pressure of the pressure stabilizing device stable phase separation system by pipeline 12, in case the pressure of phase-separation system surpasses set(ting)value, and can be by pipeline 17 decompressions.In phase-separation system 15, use usually as fillers such as steel wire, sand, glass and gather into independent phase with promotion disulphide as coalescing agent.The residence time is generally 0.5～2.0 hour, is separated with further promotion.
Further describe the present invention below by example.Given embodiment is intended to illustrate the present invention, and and does not limit the present invention in any way.
Embodiment
Embodiment 1
Hydrocarbon stream to be desulfurization is the catalytically cracked gasoline cut, and its essential property is as shown in table 1.Wherein, the mensuration of sulphur content adopts the microcoulomb method, and the mensuration of mercaptan adopts potentiometric titration.
Table 1
| Raw material | Boiling range (℃) | Sulphur content (ppm) | Mercaptan sulfur content (ppm) |
| FCCG1 | 33～98 | 139 | 71 |
| FCCG2 | 34～114 | 73 | 20 |
Adopt the hydrocarbon stream FCCG1 and the FCCG2 of schema his-and-hers watches 1 shown in Figure 1 to carry out the desulfurization processing.Working concentration is the NaOH solution of 15% (weight), and the content of sulfonated phthalocyanine cobalt is 100ppm in the alkali lye.In extraction system, the volume ratio of alkali lye and hydrocarbon stream is 1:9, and temperature is a normal temperature, pressure 0.50MPa.In the oxidation system, the injection rate of air and alkali lye volume ratio are 1:4.5, and temperature is 50 ℃, and pressure is 0.40MPa.In the degas system, pressure is 0.34MPa, and the injection rate of nitrogen and alkali lye volume ratio are 1:90.The pressure of phase-separation system is 0.20MPa.The desulfurization result is as shown in table 2.
The result shows that after annotating nitrogen treatment, hydrocarbon stream has obtained sweetening effectiveness preferably in mercaptan removal.
Comparative Examples
Adopt the hydrocarbon stream raw material FCCG2 of schema his-and-hers watches 1 shown in Figure 2 to carry out the desulfurization processing.Employed operational condition is identical with embodiment 1, just nitrogen injection displaced air not.Air discharges in phase-separation system.The desulfurization result is as shown in table 2.
The result shows that without the hydrocarbon stream of annotating nitrogen treatment, though the content of mercaptan reduces greatly, sweetening effectiveness is undesirable.
Table 2
It should be understood that various concrete degassing operation of the present invention and de-gassing vessel can make up in any way.In addition, under the situation that does not depart from purport of the present invention and scope, the various improvement that the present invention did also are encompassed in the scope of claims of the present invention.
Claims (14)
1. the method for a lye extraction desulfurization comprises the steps:
Extracting contacts in extraction system with alkali lye even contain the hydrocarbon stream of mercaptan, generates thiolate in the alkali lye so that the mercaptan in the hydrocarbon stream is absorbed into, and exports as product through the hydrocarbon stream of desulfurization;
Oxidation, the alkali lye that contains thiolate that is about to generate in the extraction system is delivered to oxidation system, and the thiolate in the described alkali lye is oxidized to disulphide through oxidizing gas under the effect of catalyzer, thereby makes alkali liquid regeneration;
Be separated, the mixture of be about to regenerate alkali lye and disulphide is delivered to phase-separation system, by sedimentation or organic solvent extracting regeneration alkali lye is separated with disulphide;
At last, will be back to extraction system from the regeneration alkali lye of phase-separation system recycles;
It is characterized in that, between oxidation and phase separation step, introduce degassing step, be about to the regeneration alkali lye of oxidation system and the mixture of disulphide and oxidizing gas and deliver to degas system, and remove oxidizing gas therein.
2. the method for claim 1 is characterized in that, described hydrocarbon stream comprises liquefied petroleum gas (LPG), gasoline, diesel oil, petroleum naphtha, C
1～C
5Alkane and C
2～C
4At least a in the alkene.
3. the method for claim 1 also comprises fresh alkali lye and the catalyzer of input in oxidation system.
4. the method for claim 1 is characterized in that, described degassing step is by vacuumizing and/or heating and/or realize with the mode of inert gas flow replace oxygen voltinism gas.
5. the method for claim 4 is characterized in that, inert gas flow is nitrogen, hydrogen, organic hydrocarbon gas or its mixture.
6. the method for claim 4 is characterized in that, the consumption of inert gas flow is 1/500～10/1 of an alkali lye volume.
7. the method for claim 6 is characterized in that, the consumption of inert gas flow is 1/200～1/1 of an alkali lye volume.
8. the method for claim 4 is characterized in that, the pressure of degas system is lower than the pressure of extraction system, is greater than or equal to the pressure of phase-separation system.
9. the method for claim 4, the step that it is characterized in that outgasing comprise that also condensation reclaims the light hydrocarbon component that contains disulphide that evaporates from alkali lye.
10. an equipment that is used for lye extraction desulfurization comprises extraction system (3), oxidation system (8), degas system (10) and phase-separation system (15).
11. the equipment of claim 10 also comprises the pipeline (6) that is used for importing to oxidation system fresh alkali lye and catalyzer.
12. the equipment of claim 10 is characterized in that, degas system (10) comprises vacuum extractor and/or heating unit.
13. the equipment of one of claim 10～12 is characterized in that, degas system (10) comprise vertical tower or jar and be used to import the pipeline (11) of rare gas element and be used to discharge the pipeline (12) of oxidizing gas.
14. the equipment of claim 13 is characterized in that, degas system (10) also comprises the condenses retrieving arrangement.
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| CN104371786B (en) * | 2013-08-14 | 2017-05-24 | 中国石油化工股份有限公司 | Alkali lye desulfurization method and device of liquefied petroleum gas |
| CN104371785B (en) * | 2013-08-14 | 2018-04-13 | 中国石油化工股份有限公司 | The lye sulfur method of liquefied petroleum gas |
| CN104623929B (en) * | 2013-11-13 | 2016-09-07 | 中国石油天然气股份有限公司 | Method for removing dissolved oxygen in alkali liquor |
| CN107974275B (en) * | 2016-10-25 | 2020-05-19 | 中国石油化工股份有限公司 | Method for removing mercaptan from light gasoline |
| FR3063497B1 (en) * | 2017-03-01 | 2019-04-05 | Axens | IMPROVED METHOD FOR REGENERATING AN ALKALINE SOLUTION USED IN A PROCESS FOR EXTRACTING SULFUR COMPOUNDS COMPRISING A WASHING STEP |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2853432A (en) * | 1954-12-28 | 1958-09-23 | Universal Oil Prod Co | Regeneration of used alkaline reagents by oxidizing the same in the presence of a phthalocyanine catalyst |
| US4705620A (en) * | 1986-12-16 | 1987-11-10 | Uop Inc. | Mercaptan extraction process |
| CN1510109A (en) * | 2002-12-20 | 2004-07-07 | 中国石油天然气股份有限公司 | Combined method for deeply desulfurizing liquefied petroleum gas and light hydrocarbon by adopting solid alkali and agent-alkali |
| CN1632072A (en) * | 2004-12-01 | 2005-06-29 | 中国石油天然气股份有限公司 | Combined device for light oil product alkaline extraction-fixed bed catalytic oxidation sweetening |
-
2005
- 2005-12-27 CN CNB2005101322997A patent/CN100460483C/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2853432A (en) * | 1954-12-28 | 1958-09-23 | Universal Oil Prod Co | Regeneration of used alkaline reagents by oxidizing the same in the presence of a phthalocyanine catalyst |
| US4705620A (en) * | 1986-12-16 | 1987-11-10 | Uop Inc. | Mercaptan extraction process |
| CN1510109A (en) * | 2002-12-20 | 2004-07-07 | 中国石油天然气股份有限公司 | Combined method for deeply desulfurizing liquefied petroleum gas and light hydrocarbon by adopting solid alkali and agent-alkali |
| CN1632072A (en) * | 2004-12-01 | 2005-06-29 | 中国石油天然气股份有限公司 | Combined device for light oil product alkaline extraction-fixed bed catalytic oxidation sweetening |
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