CN104593070A - Refinery plant liquefied gas desulphurization device and refinery plant liquefied gas desulphurization method - Google Patents
Refinery plant liquefied gas desulphurization device and refinery plant liquefied gas desulphurization method Download PDFInfo
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Abstract
The invention relates to a refinery plant liquefied gas desulphurization device and a refinery plant liquefied gas desulphurization method. The refinery plant liquefied gas desulphurization device comprises a first-stage liquid film hydrogen sulfide removing reactor, a first-stage hydrogen sulfide removing separation tank, a second-stage liquid film hydrogen sulfide removing reactor, a second-stage hydrogen sulfide removing separation tank, a fiber type coalescer, a first-stage liquid film mercaptan removing reactor, a first-stage mercaptan removing separation tank, a second-stage liquid film mercaptan removing reactor, a second-stage mercaptan removing separation tank, a liquid film washing contactor, a washing separation tank, a plurality of filters, a plurality of circulating pumps, a plurality of liquid inlets and a plurality of liquid outlets, wherein the plurality of filters, the plurality of circulating pumps, the plurality of liquid inlets and the plurality of liquid outlets are connected with one ore more of the above parts. The refinery plant liquefied gas desulphurization device disclosed by the invention has the beneficial effects of being reasonable in design, solving the problems of amine solution emulsification entrainment, amine solution foaming and the like of an extraction tower by improving a desulphurization device and a desulphurization method, ensuring that liquefied gas can be effectively removed in hydrogen sulfide, reducing the consumption of an amine solution and an alkali solution and reducing the circulating amount of the amine solution and the alkali solution, thereby reducing the electricity consumption of a machine pump and the energy consumption of regenerated steam. The total sulfur of refined liquefied gas subjected to desulphurization treatment through the method is lower than 20 ppm.
Description
Technical field
The present invention relates to a kind of refinery desulfuration of liquefied gas device and method.
Background technology
Refinery's liquefied gas is the hydrocarbon gas of petroleum refinery's by-product, and it is mainly derived from the processes such as crude distillation, catalytic cracking, thermally splitting, petroleum coking, hydrocracking, catalytic reforming, hydrofining.The main component of refinery's liquefied gas comprises C3, C4, a small amount of C2, C5 component, and hydrogen sulfide, mercaptan and thioether sulfides.And due to the source of refinery's liquefied gas different, the sulfide content therefore contained by it and composition also there are differences, but main component is hydrogen sulfide and mercaptan.Along with the raising that oil product resource deep processing and utilization requires, as refinery's liquefied gas of downstream unit industrial chemicals, its total sulfur requires also higher, and general requirement is no more than 20ppm.
Current refinery uses alkanolamine solution to remove hydrogen sulfide usually in extraction tower, and adopts mixing tank alkali cleaning mode mercaptan removal.Because hydrogen sulfide, mercaptans content and impurity contained in refinery's liquefied gas of different sources all there are differences, and prior art is poor for applicability, hydrogen sulfide fluctuation in refinery's liquefied gas after extracting is frequent and amplitude is large, the Con trolling index of Yuan Chao refinery 10ppm, and existing extraction tower easily blocks and runs amine, while hydrogen sulfide stripping effect reduces, also cause alkanolamine solution to enter caustic washing system, increase the consumption of follow-up caustic washing system alkali lye, also cause liquefied gas total sulfur to exceed standard.In addition, existing extraction tower depriving hydrogen sulphide and the alkanolamine solution internal circulating load needed for mixing tank mercaptan removal (being generally the 150-200%wt of flow of lpg) and alkali lye internal circulating load (being generally the 40-60%wt of flow of lpg) very big, cause pump energy consumption and steam energy consumption higher, be unfavorable for energy-conserving and environment-protective.
Summary of the invention
The object of this invention is to provide a kind of refinery desulfuration of liquefied gas device and method, to overcome currently available technology above shortcomings.
The object of the invention is to be achieved through the following technical solutions:
According to an aspect of the present invention, a kind of refinery desulfuration of liquefied gas device is provided.
A kind of refinery desulfuration of liquefied gas device, comprise one-level liquid film depriving hydrogen sulphide reactor, first grade desulfurizing hydrogen separating tank, secondary liquid film depriving hydrogen sulphide reactor, two-grade desulfurizing hydrogen separating tank, fiber type coalescer, one-level liquid film sweetening reaction device, first grade desulfurizing alcohol separating tank, secondary liquid film sweetening reaction device, two-grade desulfurizing alcohol separating tank, liquid film washing contactor, washing separating tank and with one or more some strainers be connected in above-mentioned each parts, some recycle pumps, some fluid inlets and some liquid outlets, described one-level liquid film depriving hydrogen sulphide reactor bottom is connected with first grade desulfurizing hydrogen separating tank top inlet, the outlet of described first grade desulfurizing hydrogen separating tank top is connected with secondary liquid film depriving hydrogen sulphide reactor top end entrance, described secondary liquid film depriving hydrogen sulphide reactor bottom is connected with two-grade desulfurizing hydrogen separating tank top inlet, the outlet of described two-grade desulfurizing hydrogen separating tank top is connected with fiber type coalescer top inlet, described fiber type coalescer side outlet is connected with one-level liquid film sweetening reaction device top inlet, be connected with first grade desulfurizing alcohol separating tank top inlet bottom described one-level liquid film sweetening reaction device, the outlet of described first grade desulfurizing alcohol separating tank top is connected with secondary liquid film sweetening reaction device top inlet, be connected with two-grade desulfurizing alcohol separating tank top inlet bottom described secondary liquid film sweetening reaction device, the outlet of described two-grade desulfurizing alcohol separating tank top is washed contact top end entrance with liquid film and is connected, be connected with washing separating tank top inlet bottom described liquid film washing contactor.
Further, described strainer comprises liquefied gas filter device, amine liquid prefilter, amine liquid filter and alkali lye strainer, described liquefied gas filter device is connected with one-level liquid film depriving hydrogen sulphide reactor top end entrance, described amine liquid prefilter is connected with amine liquid filter, described amine liquid filter is connected with secondary liquid film depriving hydrogen sulphide reactor-side end entrance, and described alkali lye strainer is connected with secondary liquid film sweetening reaction device side entrance.
Further, described recycle pump comprises amine liquid recycle pump, NaOH solution circulating pump and water washing cycles pump, described amine liquid pump entry is connected with alkali lye strainer, described amine liquid circulating-pump outlet is connected with described secondary liquid film depriving hydrogen sulphide reactor-side end entrance, described NaOH solution circulating pump entrance is connected with described two-grade desulfurizing alcohol separating tank bottom end outlet, described NaOH solution circulating pump outlet is connected with one-level liquid film sweetening reaction device side entrance, described water washing cycles pump intake is connected with washing separating tank bottom end outlet, described water washing cycles pump discharge and described liquid film are washed contactor side entrance and are connected.
Further, described fluid inlet comprises liquefied gas raw material mouth, fresh amine liquid or poor amine liquid mouth, fresh alkali lye or poor alkali lye mouth and the washing mouth of a river.
Further, described liquid outlet comprises rich amine solution mouth, refining liquefied gas port, alkaline sewage mouth and rich alkali lye mouth.
Further, silk screen coalescing-plate is equipped with in described first grade desulfurizing hydrogen separating tank and two-grade desulfurizing hydrogen separating tank.
Further, described silk screen coalescing-plate is through surface hydrophilic process, and its model is W500 or W700.
According to a further aspect in the invention, provide a kind of said apparatus that utilizes and the method for desulfurization carried out to refinery's liquefied gas, comprise the following steps:
Step 1: utilize described liquefied gas filter device to filter the liquefied gas raw material imported via liquefied gas raw material mouth, and the liquefied gas raw material after filtering is removed hydrogen sulfide with together inputting from the amine liquid of amine liquid recycle pump in one-level liquid film depriving hydrogen sulphide reactor and carry out reaction in one-level liquid film depriving hydrogen sulphide reactor, first grade desulfurizing hydrogen separating tank is utilized to be separated with amine liquid reacted liquefied gas, described liquefied gas and amine liquid stop 30-60min in first grade desulfurizing hydrogen separating tank, amine liquid after separation is derived via bottom first grade desulfurizing hydrogen separating tank, and through rich amine solution mouth take-up gear, by liquefied gas after being separated with to import via fresh amine liquid or poor amine liquid mouth, and the fresh amine liquid filtered through amine liquid prefilter and amine liquid filter or poor amine liquid together input in secondary liquid film depriving hydrogen sulphide reactor, and hydrogen sulfide is removed further, then two-grade desulfurizing hydrogen separating tank is utilized to be separated with amine liquid the liquefied gas through depriving hydrogen sulphide again, described liquefied gas and amine liquid stop 30-60min in two-grade desulfurizing hydrogen separating tank, the liquefied gas of discharging due to the outlet of two-grade desulfurizing hydrogen separating tank top is entrained with amine liquid, fiber type coalescer is utilized to remove carrying amine liquid secretly,
Step 2: by the liquefied gas of discharging from fiber type coalescer side with together to input from the alkali lye of NaOH solution circulating pump in one-level liquid film sweetening reaction device and remove mercaptan in one-level liquid film sweetening reaction device, first grade desulfurizing alcohol separating tank is utilized to be separated with alkali lye reacted liquefied gas, described liquefied gas and alkali lye stop 20-40min in first grade desulfurizing alcohol separating tank, alkali lye after described separation goes out via outlet guide bottom first grade desulfurizing alcohol separating tank and by rich alkali lye mouth take-up gear, by liquefied gas after being separated with to import via fresh alkali lye or poor alkali lye mouth, and together input in secondary liquid film sweetening reaction device through the fresh alkali lye of alkali lye metre filter or poor alkali lye mercaptan is removed further, then two-grade desulfurizing alcohol separating tank is utilized to be separated with alkali lye reacted liquefied gas again, described liquefied gas and alkali lye stop 20-40min in two-grade desulfurizing alcohol separating tank, alkali lye after described separation goes out via outlet guide bottom two-grade desulfurizing alcohol separating tank, utilize NaOH solution circulating pump that the alkali lye after separation is circulated to one-level liquid film sweetening reaction device to recycle,
Step 3: by the liquefied gas of discharging from the outlet of described two-grade desulfurizing alcohol separating tank top with the mouth of a river imports via washing, and through water washing cycles pump circulation washing water together input liquid film washing contactor in liquefied gas is washed, then liquefied gas and washing water are together imported and wash separating tank and be separated, described liquefied gas and washing water stop 25-50min washing in separating tank, water washing cycles pump is utilized to carry out recirculation to the washing water of discharging bottom washing separating tank, and imported liquid film washing contactor in recycle, utilize washing separating tank to be separated the alkali lye carried secretly in liquefied gas after washing and discharge from washing separating tank outlet at bottom, final through alkaline sewage mouth take-up gear, and the liquefied gas after being separated is discharged from the outlet of washing separating tank top, and via refining liquefied gas port by liquefied refinery gas take-up gear.
Further, in described step 1, in first grade desulfurizing hydrogen separating tank and two-grade desulfurizing hydrogen separating tank, position, the boundary scope of liquefied gas and amine liquid is 40-50%.
Further, in described step 1, amine liquid preferred concentration is the methyldiethanolamine solution of 25-35%wt, and described amine liquid and liquefied gas quality are 30-80% than scope.
Further, in described step 2, in first grade desulfurizing alcohol separating tank and two-grade desulfurizing alcohol separating tank, position, the boundary scope of liquefied gas and alkali lye is 40-50%.
Further, in described step 2, alkali lye preferred concentration is the sodium hydroxide solution of 15-25%wt, and described alkali lye and liquefied gas quality are 8-30% than scope.
Further, position, the boundary scope of washing liquefied gas and water in separating tank in described step 3 is 30-40%
Further, in described step 3, the preferred de-mineralized water of described washing water, described water and liquefied gas quality are 15-30% than scope.
Beneficial effect of the present invention is: reasonable in design, by the improvement to desulfurizer and sulfur method, solve the problems such as the emulsification of extraction tower amine liquid is carried secretly, the foaming of amine liquid, guarantee that liquefied gas can effective elimination hydrogen sulfide, reduce amine liquid and alkali lye consumption, reduce amine liquid and alkali lye internal circulating load simultaneously, thus reduce pump power consumption, regeneration steam energy consumption, the liquefied refinery gas total sulfur after the method desulfurization process is lower than 20ppm.
Accompanying drawing explanation
In order to be illustrated more clearly in the embodiment of the present invention or technical scheme of the prior art, be briefly described to the accompanying drawing used required in embodiment below, apparently, accompanying drawing in the following describes is only some embodiments of the present invention, for those of ordinary skill in the art, under the prerequisite not paying creative work, other accompanying drawing can also be obtained according to these accompanying drawings.
Fig. 1 is the apparatus structure schematic diagram of a kind of refinery desulfuration of liquefied gas device and method according to the embodiment of the present invention 1.
In figure:
1, liquefied gas raw material mouth; 2, fresh amine liquid or poor amine liquid mouth; 3, rich amine solution mouth; 4, fresh alkali lye or poor alkali lye mouth; 5, the mouth of a river is washed; 6, refining liquefied gas port; 7, alkaline sewage mouth; 8, rich alkali lye mouth; 9, one-level liquid film depriving hydrogen sulphide reactor; 10, first grade desulfurizing hydrogen separating tank; 11, secondary liquid film depriving hydrogen sulphide reactor; 12, two-grade desulfurizing hydrogen separating tank; 13, one-level liquid film sweetening reaction device; 14, first grade desulfurizing alcohol separating tank; 15, secondary liquid film sweetening reaction device; 16, two-grade desulfurizing alcohol separating tank; 17, liquid film washing contactor; 18, separating tank is washed; 19, fiber type coalescer; 20, liquefied gas filter device; 21, amine liquid prefilter; 22, amine liquid filter; 23, alkali lye strainer; 24, amine liquid recycle pump; 25, NaOH solution circulating pump; 26, water washing cycles pump; 27, silk screen coalescing-plate.
Embodiment
Be clearly and completely described the technical scheme in the embodiment of the present invention, obviously, described embodiment is only the present invention's part embodiment, instead of whole embodiments.Based on the embodiment in the present invention, the every other embodiment that those of ordinary skill in the art obtain, all belongs to the scope of protection of the invention.
According to the embodiment of the present invention, provide a kind of refinery desulfuration of liquefied gas device and method.
As shown in Figure 1, a kind of refinery desulfuration of liquefied gas device according to the embodiment of the present invention, comprise one-level liquid film depriving hydrogen sulphide reactor 9, first grade desulfurizing hydrogen separating tank 10, secondary liquid film depriving hydrogen sulphide reactor 11, two-grade desulfurizing hydrogen separating tank 12, fiber type coalescer 19, one-level liquid film sweetening reaction device 13, first grade desulfurizing alcohol separating tank 14, secondary liquid film sweetening reaction device 15, two-grade desulfurizing alcohol separating tank 16, liquid film washing contactor 17, washing separating tank 18, some strainers, some recycle pumps, some fluid inlets and some liquid outlets, be connected with first grade desulfurizing hydrogen separating tank 10 top inlet bottom described one-level liquid film depriving hydrogen sulphide reactor 9, the outlet of described first grade desulfurizing hydrogen separating tank 10 top is connected with secondary liquid film depriving hydrogen sulphide reactor 11 top inlet, be connected with two-grade desulfurizing hydrogen separating tank 12 top inlet bottom described secondary liquid film depriving hydrogen sulphide reactor 11, the outlet of described two-grade desulfurizing hydrogen separating tank 12 top is connected with fiber type coalescer 19 top inlet, described fiber type coalescer 19 side outlet is connected with one-level liquid film sweetening reaction device 13 top inlet, be connected with first grade desulfurizing alcohol separating tank 14 top inlet bottom described one-level liquid film sweetening reaction device 13, the outlet of described first grade desulfurizing alcohol separating tank 14 top is connected with secondary liquid film sweetening reaction device 15 top inlet, be connected with two-grade desulfurizing alcohol separating tank 16 top inlet bottom described secondary liquid film sweetening reaction device 15, the outlet of described two-grade desulfurizing alcohol separating tank 16 top is washed contactor 17 top inlet with liquid film and is connected, be connected with washing separating tank 18 top inlet bottom described liquid film washing contactor 17, described strainer comprises liquefied gas filter device 20, amine liquid prefilter 21, amine liquid filter 22, with alkali lye strainer 23, described liquefied gas filter device 20 is connected with one-level liquid film depriving hydrogen sulphide reactor 9 top inlet, described amine liquid prefilter 21 is connected with amine liquid filter 22, described amine liquid filter 22 is connected with secondary liquid film depriving hydrogen sulphide reactor 11 side entrance, described alkali lye strainer 23 is connected with secondary liquid film sweetening reaction device 15 side entrance, described recycle pump comprises amine liquid recycle pump 24, NaOH solution circulating pump 25 and water washing cycles pump 26, described amine liquid recycle pump 24 entrance is connected with alkali lye strainer 23, described amine liquid recycle pump 24 outlet is connected with described secondary liquid film depriving hydrogen sulphide reactor 11 side entrance, described NaOH solution circulating pump 25 entrance is connected with described two-grade desulfurizing alcohol separating tank 16 bottom end outlet, described NaOH solution circulating pump 25 outlet is connected with one-level liquid film sweetening reaction device 13 side entrance, described water washing cycles pump 26 entrance is connected with washing separating tank 18 bottom end outlet, described water washing cycles pump 26 outlet is washed contactor 17 side entrance with described liquid film and is connected, described fluid inlet comprises liquefied gas raw material mouth 1, fresh amine liquid or poor amine liquid mouth 2, fresh alkali lye or poor alkali lye mouth 4 and the washing mouth of a river 5, described liquid outlet comprises rich amine solution mouth 3, refining liquefied gas port 6, alkaline sewage mouth 7 and rich alkali lye mouth 8, silk screen coalescing-plate 27 is equipped with in described first grade desulfurizing hydrogen separating tank 10 and two-grade desulfurizing hydrogen separating tank 12.
Embodiment 1:
Utilize above-mentioned desulfuration of liquefied gas device to carry out the method for desulfurization, comprise the following steps:
Step 1: utilize described liquefied gas filter device 20 to filter the liquefied gas raw material imported via liquefied gas raw material mouth 1, and the liquefied gas raw material after filtering is removed hydrogen sulfide with together inputting from the amine liquid of amine liquid recycle pump 24 in one-level liquid film depriving hydrogen sulphide reactor 9 and carry out reaction in one-level liquid film depriving hydrogen sulphide reactor 9, first grade desulfurizing hydrogen separating tank 10 is utilized to be separated with amine liquid reacted liquefied gas, described liquefied gas and amine liquid stop 30min in first grade desulfurizing hydrogen separating tank 10, amine liquid after separation is derived via bottom first grade desulfurizing hydrogen separating tank 10, and through rich amine solution mouth 3 take-up gear, by liquefied gas after being separated with to import via fresh amine liquid or poor amine liquid mouth 2, and the fresh amine liquid filtered through amine liquid prefilter 21 and amine liquid filter 22 or poor amine liquid together input in secondary liquid film depriving hydrogen sulphide reactor 11, and hydrogen sulfide is removed further, then two-grade desulfurizing hydrogen separating tank 12 is utilized to be separated with amine liquid the liquefied gas through depriving hydrogen sulphide again, described liquefied gas and amine liquid stop 30min in two-grade desulfurizing hydrogen separating tank 12, the liquefied gas of discharging due to the outlet of two-grade desulfurizing hydrogen separating tank 12 top is entrained with amine liquid, fiber type coalescer 19 is utilized to remove carrying amine liquid secretly, position, the boundary scope of described liquefied gas and amine liquid is 40%, described amine liquid preferred concentration is the methyldiethanolamine solution of 25%wt, described amine liquid and liquefied gas quality are 30% than scope,
Step 2: by the liquefied gas of discharging from fiber type coalescer 19 side with together to input from the alkali lye of NaOH solution circulating pump 25 in one-level liquid film sweetening reaction device 13 and remove mercaptan in one-level liquid film sweetening reaction device 13, first grade desulfurizing alcohol separating tank 14 is utilized to be separated with alkali lye reacted liquefied gas, described liquefied gas and alkali lye stop 20min in first grade desulfurizing alcohol separating tank 14, alkali lye after described separation is derived via first grade desulfurizing alcohol separating tank 14 outlet at bottom and is passed through rich alkali lye mouth 8 take-up gear, by liquefied gas after being separated with to import via fresh alkali lye or poor alkali lye mouth 4, and the fresh alkali lye filtered through alkali lye strainer 23 or poor alkali lye together input in secondary liquid film sweetening reaction device 15 and remove further mercaptan, then two-grade desulfurizing alcohol separating tank 16 is utilized to be separated with alkali lye reacted liquefied gas again, described liquefied gas and alkali lye stop 20min in two-grade desulfurizing alcohol separating tank 16, alkali lye after described separation is derived via two-grade desulfurizing alcohol separating tank 16 outlet at bottom, utilize NaOH solution circulating pump 25 that the alkali lye after separation is circulated to one-level liquid film sweetening reaction device 13 to recycle, described first grade desulfurizing alcohol separating tank 14 is 40% with position, the boundary scope of liquefied gas in two-grade desulfurizing alcohol separating tank 16 and alkali lye, described alkali lye preferred concentration is the sodium hydroxide solution of 15%wt, described alkali lye and liquefied gas quality are 8% than scope,
Step 3: by the liquefied gas of discharging from the outlet of described two-grade desulfurizing alcohol separating tank 16 top with the mouth of a river 5 imports via washing, and through water washing cycles pump 26 circulate washing water together input liquid film washing contactor 17 in liquefied gas is washed, then liquefied gas and washing water are together imported and wash separating tank 18 and be separated, in described washing separating tank, position, the boundary scope of liquefied gas and water is 30%, the preferred de-mineralized water of washing water, described water and liquefied gas quality are 15% than scope, described liquefied gas and washing water stop 25min washing in separating tank 18, water washing cycles pump 26 is utilized to carry out recirculation to the washing water of discharging bottom washing separating tank 18, and imported liquid film washing contactor 17 in recycle, utilize washing separating tank 18 to be separated the alkali lye carried secretly in liquefied gas after washing and discharge from washing separating tank 18 outlet at bottom, final through alkaline sewage mouth 7 take-up gear, and the liquefied gas after being separated is discharged from the outlet of washing separating tank 18 top, and via refining liquefied gas port 6 by liquefied refinery gas take-up gear.
Embodiment 2:
Step 1: utilize described liquefied gas filter device 20 to filter the liquefied gas raw material imported via liquefied gas raw material mouth 1, and the liquefied gas raw material after filtering is removed hydrogen sulfide with together inputting from the amine liquid of amine liquid recycle pump 24 in one-level liquid film depriving hydrogen sulphide reactor 9 and carry out reaction in one-level liquid film depriving hydrogen sulphide reactor 9, first grade desulfurizing hydrogen separating tank 10 is utilized to be separated with amine liquid reacted liquefied gas, described liquefied gas and amine liquid stop 45min in first grade desulfurizing hydrogen separating tank 10, amine liquid after separation is derived via bottom first grade desulfurizing hydrogen separating tank 10, and through rich amine solution mouth 3 take-up gear, by liquefied gas after being separated with to import via fresh amine liquid or poor amine liquid mouth 2, and the fresh amine liquid filtered through amine liquid prefilter 21 and amine liquid filter 22 or poor amine liquid together input in secondary liquid film depriving hydrogen sulphide reactor 11, and hydrogen sulfide is removed further, then two-grade desulfurizing hydrogen separating tank 12 is utilized to be separated with amine liquid the liquefied gas through depriving hydrogen sulphide again, described liquefied gas and amine liquid stop 45min in two-grade desulfurizing hydrogen separating tank 12, the liquefied gas of discharging due to the outlet of two-grade desulfurizing hydrogen separating tank 12 top is entrained with amine liquid, fiber type coalescer 19 is utilized to remove carrying amine liquid secretly, position, the boundary scope of described liquefied gas and amine liquid is 45%, described amine liquid preferred concentration is the methyldiethanolamine solution of 30%wt, described amine liquid and liquefied gas quality are 55% than scope,
Step 2: by the liquefied gas of discharging from fiber type coalescer 19 side with together to input from the alkali lye of NaOH solution circulating pump 25 in one-level liquid film sweetening reaction device 13 and remove mercaptan in one-level liquid film sweetening reaction device 13, first grade desulfurizing alcohol separating tank 14 is utilized to be separated with alkali lye reacted liquefied gas, described liquefied gas and alkali lye stop 30min in first grade desulfurizing alcohol separating tank 14, alkali lye after described separation is derived via first grade desulfurizing alcohol separating tank 14 outlet at bottom and is passed through rich alkali lye mouth 8 take-up gear, by liquefied gas after being separated with to import via fresh alkali lye or poor alkali lye mouth 4, and the fresh alkali lye filtered through alkali lye strainer 23 or poor alkali lye together input in secondary liquid film sweetening reaction device 15 and remove further mercaptan, then two-grade desulfurizing alcohol separating tank 16 is utilized to be separated with alkali lye reacted liquefied gas again, described liquefied gas and alkali lye stop 30min in two-grade desulfurizing alcohol separating tank 16, alkali lye after described separation is derived via two-grade desulfurizing alcohol separating tank 16 outlet at bottom, utilize NaOH solution circulating pump 25 that the alkali lye after separation is circulated to one-level liquid film sweetening reaction device 13 to recycle, described first grade desulfurizing alcohol separating tank 14 is 45% with position, the boundary scope of liquefied gas in two-grade desulfurizing alcohol separating tank 16 and alkali lye, described alkali lye preferred concentration is the sodium hydroxide solution of 20%wt, described alkali lye and liquefied gas quality are 19% than scope,
Step 3: by the liquefied gas of discharging from the outlet of described two-grade desulfurizing alcohol separating tank 16 top with the mouth of a river 5 imports via washing, and through water washing cycles pump 26 circulate washing water together input liquid film washing contactor 17 in liquefied gas is washed, then liquefied gas and washing water are together imported and wash separating tank 18 and be separated, in described washing separating tank, position, the boundary scope of liquefied gas and water is 35%, the preferred de-mineralized water of washing water, described water and liquefied gas quality are 22% than scope, described liquefied gas and washing water stop 37min washing in separating tank 18, water washing cycles pump 26 is utilized to carry out recirculation to the washing water of discharging bottom washing separating tank 18, and imported liquid film washing contactor 17 in recycle, utilize washing separating tank 18 to be separated the alkali lye carried secretly in liquefied gas after washing and discharge from washing separating tank 18 outlet at bottom, final through alkaline sewage mouth 7 take-up gear, and the liquefied gas after being separated is discharged from the outlet of washing separating tank 18 top, and via refining liquefied gas port 6 by liquefied refinery gas take-up gear.
Embodiment 3:
Step 1: utilize described liquefied gas filter device 20 to filter the liquefied gas raw material imported via liquefied gas raw material mouth 1, and the liquefied gas raw material after filtering is removed hydrogen sulfide with together inputting from the amine liquid of amine liquid recycle pump 24 in one-level liquid film depriving hydrogen sulphide reactor 9 and carry out reaction in one-level liquid film depriving hydrogen sulphide reactor 9, first grade desulfurizing hydrogen separating tank 10 is utilized to be separated with amine liquid reacted liquefied gas, described liquefied gas and amine liquid stop 60min in first grade desulfurizing hydrogen separating tank 10, amine liquid after separation is derived via bottom first grade desulfurizing hydrogen separating tank 10, and through rich amine solution mouth 3 take-up gear, by liquefied gas after being separated with to import via fresh amine liquid or poor amine liquid mouth 2, and the fresh amine liquid filtered through amine liquid prefilter 21 and amine liquid filter 22 or poor amine liquid together input in secondary liquid film depriving hydrogen sulphide reactor 11, and hydrogen sulfide is removed further, then two-grade desulfurizing hydrogen separating tank 12 is utilized to be separated with amine liquid the liquefied gas through depriving hydrogen sulphide again, described liquefied gas and amine liquid stop 60min in two-grade desulfurizing hydrogen separating tank 12, the liquefied gas of discharging due to the outlet of two-grade desulfurizing hydrogen separating tank 12 top is entrained with amine liquid, fiber type coalescer 19 is utilized to remove carrying amine liquid secretly, position, the boundary scope of described liquefied gas and amine liquid is 50%, described amine liquid preferred concentration is the methyldiethanolamine solution of 35%wt, described amine liquid and liquefied gas quality are 80% than scope,
Step 2: by the liquefied gas of discharging from fiber type coalescer 19 side with together to input from the alkali lye of NaOH solution circulating pump 25 in one-level liquid film sweetening reaction device 13 and remove mercaptan in one-level liquid film sweetening reaction device 13, first grade desulfurizing alcohol separating tank 14 is utilized to be separated with alkali lye reacted liquefied gas, described liquefied gas and alkali lye stop 40min in first grade desulfurizing alcohol separating tank 14, alkali lye after described separation is derived via first grade desulfurizing alcohol separating tank 14 outlet at bottom and is passed through rich alkali lye mouth 8 take-up gear, by liquefied gas after being separated with to import via fresh alkali lye or poor alkali lye mouth 4, and the fresh alkali lye filtered through alkali lye strainer 23 or poor alkali lye together input in secondary liquid film sweetening reaction device 15 and remove further mercaptan, then two-grade desulfurizing alcohol separating tank 16 is utilized to be separated with alkali lye reacted liquefied gas again, described liquefied gas and alkali lye stop 40min in two-grade desulfurizing alcohol separating tank 16, alkali lye after described separation is derived via two-grade desulfurizing alcohol separating tank 16 outlet at bottom, utilize NaOH solution circulating pump 25 that the alkali lye after separation is circulated to one-level liquid film sweetening reaction device 13 to recycle, described first grade desulfurizing alcohol separating tank 14 is 50% with position, the boundary scope of liquefied gas in two-grade desulfurizing alcohol separating tank 16 and alkali lye, described alkali lye preferred concentration is the sodium hydroxide solution of 25%wt, described alkali lye and liquefied gas quality are 30% than scope,
Step 3: by the liquefied gas of discharging from the outlet of described two-grade desulfurizing alcohol separating tank 16 top with the mouth of a river 5 imports via washing, and through water washing cycles pump 26 circulate washing water together input liquid film washing contactor 17 in liquefied gas is washed, then liquefied gas and washing water are together imported and wash separating tank 18 and be separated, in described washing separating tank, position, the boundary scope of liquefied gas and water is 40%, the preferred de-mineralized water of washing water, described water and liquefied gas quality are 30% than scope, described liquefied gas and washing water stop 50min washing in separating tank 18, water washing cycles pump 26 is utilized to carry out recirculation to the washing water of discharging bottom washing separating tank 18, and imported liquid film washing contactor 17 in recycle, utilize washing separating tank 18 to be separated the alkali lye carried secretly in liquefied gas after washing and discharge from washing separating tank 18 outlet at bottom, final through alkaline sewage mouth 7 take-up gear, and the liquefied gas after being separated is discharged from the outlet of washing separating tank 18 top, and via refining liquefied gas port 6 by liquefied refinery gas take-up gear.
Application Example one:
For detecting the sweetening effectiveness of refinery of the present invention desulfuration of liquefied gas device, be applied in by said apparatus in certain Chemical Co., Ltd.'s mixed liquefied gas depriving hydrogen sulphide and mercaptan removal project, and carry out full scale plant data tracking, concrete operations are as follows:
Liquefied gas raw material after liquefied gas filter device filters and circulation amine liquid together enter in one-level liquid film depriving hydrogen sulphide reactor 9, the rich amine solution of discharging bottom first grade desulfurizing hydrogen separating tank 10 enters the recycle of amine liquid regeneration system rapidly, the liquefied gas of discharging from the outlet of first grade desulfurizing hydrogen separating tank 10 top together enters in secondary liquid film depriving hydrogen sulphide reactor 11 with the amine liquid through amine liquid filter, described amine liquid is the poor amine liquid of 30% concentration, the circulation amine liquid of discharging bottom described two-grade desulfurizing hydrogen separating tank 12 is cycled to used in depriving hydrogen sulphide by amine liquid recycle pump 24, liquefied gas is discharged from the outlet of two-grade desulfurizing hydrogen separating tank 12 top, and through fiber type filter 19 coalescent remove carry amine liquid secretly after, enter in one-level liquid film sweetening reaction device 13 together with circulation alkali liquor, bottom first grade desulfurizing alcohol separating tank 14, discharge rich alkali lye enter regeneration system rapidly recycle, the liquefied gas of discharging from the outlet of first grade desulfurizing alcohol separating tank 14 top together enters in secondary liquid film sweetening reaction device 15 with the poor alkali lye from regeneration system rapidly, the concentration of described poor alkali lye is 20%, the circulation alkali liquor of discharging bottom two-grade desulfurizing alcohol separating tank 16 is by NaOH solution circulating pump 25 recycle, can be used for circulation desulfurization alcohol, liquefied gas is discharged from the top outlet of two-grade desulfurizing alcohol separating tank 16, and together enter liquid film with circulation de-mineralized water and wash contactor 17, then washing separating tank 18 is entered, bottom washing separating tank 18, discharge washing water be cycled to used in washing, the liquefied gas that the outlet of described washing separating tank 18 top is discharged is liquefied refinery gas.In actual applications, according to liquefied gas hydrogen sulfide and mercaptans content, secondary liquid film depriving hydrogen sulphide reactor and two-grade desulfurizing hydrogen separating tank can be changed to water elution amine or caustic wash desulfuration alcohol facility.
Result shows, and in liquefied gas raw material, hydrogen sulfide content is within the scope of 1000-20000 ppm, and mercaptan is within the scope of 100-500 ppm.After the process of this device two-stage liquid film depriving hydrogen sulphide, in liquefied gas, hydrogen sulfide content removes substantially, and average hydrogen sulfide content is lower than 1 ppm, and after the process of this device liquid film sweetening reaction device, liquefied gas total sulfur content is lower than 5 ppm.Wherein methyldiethanolamine internal circulating load is reduced to 35% by 160% before transforming, methyldiethanolamine solvent-oil ratio is reduced to 0.02kg/t liquefied gas by the 0.28kg/t liquefied gas before transforming, and alkali lye consumption is also reduced to 0.543kg/t liquefied gas by the 10kg/t liquefied gas before transforming.
When hydrogen sulfide in liquefied gas is lower than 3000ppm, secondary liquid film depriving hydrogen sulphide reactor and two-grade desulfurizing hydrogen separating tank can be changed to water elution amine, after the process of this device two-stage liquid film depriving hydrogen sulphide, in liquefied gas, hydrogen sulfide content is on average lower than 2ppm, and after the process of this device liquid film sweetening reaction device, liquefied gas total sulfur content is lower than 5ppm, and wherein methyldiethanolamine internal circulating load is only 35%.
In sum, provide a kind of refinery desulfuration of liquefied gas device and method, this apparatus design is reasonable, by the improvement to desulfurizer and sulfur method, solve the emulsification of extraction tower amine liquid to carry secretly, the problems such as amine liquid foaming, guarantee that liquefied gas can effective elimination hydrogen sulfide, reduce amine liquid and alkali lye consumption, reduce amine liquid and alkali lye internal circulating load simultaneously, thus reduce pump power consumption, regeneration steam energy consumption, liquefied refinery gas total sulfur after the method desulfurization process is lower than 20ppm, secondary liquid film depriving hydrogen sulphide reactor in device and two-grade desulfurizing hydrogen separating tank can change to washing or alkali cleaning flexibly according to raw material condition, the consumption of effective reduction alkali lye also guarantees that liquefied refinery gas total sulfur is qualified.
The foregoing is only preferred embodiment of the present invention, not in order to limit the present invention, within the spirit and principles in the present invention all, any amendment done, equivalent replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (10)
1. refinery's desulfuration of liquefied gas device, it is characterized in that, comprise one-level liquid film depriving hydrogen sulphide reactor (9), first grade desulfurizing hydrogen separating tank (10), secondary liquid film depriving hydrogen sulphide reactor (11), two-grade desulfurizing hydrogen separating tank (12), fiber type coalescer (19), one-level liquid film sweetening reaction device (13), first grade desulfurizing alcohol separating tank (14), secondary liquid film sweetening reaction device (15), two-grade desulfurizing alcohol separating tank (16), liquid film washing contactor (17), washing separating tank (18) and with one or more some strainers be connected in above-mentioned each parts, some recycle pumps, some fluid inlets and some liquid outlets, described one-level liquid film depriving hydrogen sulphide reactor (9) bottom is connected with first grade desulfurizing hydrogen separating tank (10) top inlet, the outlet of described first grade desulfurizing hydrogen separating tank (10) top is connected with secondary liquid film depriving hydrogen sulphide reactor (11) top inlet, described secondary liquid film depriving hydrogen sulphide reactor (11) bottom is connected with two-grade desulfurizing hydrogen separating tank (12) top inlet, the outlet of described two-grade desulfurizing hydrogen separating tank (12) top is connected with fiber type coalescer (19) top inlet, described fiber type coalescer (19) side outlet is connected with one-level liquid film sweetening reaction device (13) top inlet, described one-level liquid film sweetening reaction device (13) bottom is connected with first grade desulfurizing alcohol separating tank (14) top inlet, the outlet of described first grade desulfurizing alcohol separating tank (14) top is connected with secondary liquid film sweetening reaction device (15) top inlet, described secondary liquid film sweetening reaction device (15) bottom is connected with two-grade desulfurizing alcohol separating tank (16) top inlet, the outlet of described two-grade desulfurizing alcohol separating tank (16) top is washed contactor (17) top inlet with liquid film and is connected, described liquid film washing contactor (17) bottom is connected with washing separating tank (18) top inlet.
2. desulfuration of liquefied gas device according to claim 1, it is characterized in that, described strainer comprises liquefied gas filter device (20), amine liquid prefilter (21), amine liquid filter (22), with alkali lye strainer (23), described liquefied gas filter device (20) is connected with one-level liquid film depriving hydrogen sulphide reactor (9) top inlet, described amine liquid prefilter (21) is connected with amine liquid filter (22), described amine liquid filter (22) is connected with secondary liquid film depriving hydrogen sulphide reactor (11) side entrance, described alkali lye strainer (23) is connected with secondary liquid film sweetening reaction device (15) side entrance.
3. desulfuration of liquefied gas device according to claim 2, it is characterized in that, described recycle pump comprises amine liquid recycle pump (24), NaOH solution circulating pump (25) and water washing cycles pump (26), described amine liquid recycle pump (24) entrance is connected with alkali lye strainer (23), described amine liquid recycle pump (24) outlet is connected with described secondary liquid film depriving hydrogen sulphide reactor (11) side entrance, described NaOH solution circulating pump (25) entrance is connected with described two-grade desulfurizing alcohol separating tank (16) bottom end outlet, described NaOH solution circulating pump (25) outlet is connected with one-level liquid film sweetening reaction device (13) side entrance, described water washing cycles pump (26) entrance is connected with washing separating tank (18) bottom end outlet, described water washing cycles pump (26) outlet is washed contactor (17) side entrance with described liquid film and is connected.
4. desulfuration of liquefied gas device according to claim 3, is characterized in that, described fluid inlet comprises liquefied gas raw material mouth (1), fresh amine liquid or poor amine liquid mouth (2), fresh alkali lye or poor alkali lye mouth (4) and the washing mouth of a river (5).
5. desulfuration of liquefied gas device according to claim 4, is characterized in that, described liquid outlet comprises rich amine solution mouth (3), refining liquefied gas port (6), alkaline sewage mouth (7) and rich alkali lye mouth (8).
6. desulfuration of liquefied gas device according to claim 5, is characterized in that, is equipped with silk screen coalescing-plate (27) in described first grade desulfurizing hydrogen separating tank (10) and two-grade desulfurizing hydrogen separating tank (12).
7. refinery's liquefied gas is carried out to a method for desulfurization, it is characterized in that, by the desulfuration of liquefied gas device in claim 1 to 5 described in any one, desulfurization is carried out to refinery's liquefied gas, and the method for described desulfurization comprises:
Step 1: utilize described liquefied gas filter device (20) to filter the liquefied gas raw material imported via liquefied gas raw material mouth (1), and the liquefied gas raw material after filtering is removed hydrogen sulfide with together inputting from the amine liquid of amine liquid recycle pump (24) in one-level liquid film depriving hydrogen sulphide reactor (9) and carry out reaction in one-level liquid film depriving hydrogen sulphide reactor (9), first grade desulfurizing hydrogen separating tank (10) is utilized to be separated with amine liquid reacted liquefied gas, described liquefied gas and amine liquid stop 30-60min in first grade desulfurizing hydrogen separating tank (10), amine liquid after separation is derived via first grade desulfurizing hydrogen separating tank (10) bottom, and through rich amine solution mouth (3) take-up gear, by liquefied gas after being separated with to import via fresh amine liquid or poor amine liquid mouth (2), and the fresh amine liquid filtered through amine liquid prefilter (21) and amine liquid filter (22) or poor amine liquid together input in secondary liquid film depriving hydrogen sulphide reactor (11), and hydrogen sulfide is removed further, then two-grade desulfurizing hydrogen separating tank (12) is utilized to be separated with amine liquid the liquefied gas through depriving hydrogen sulphide again, described liquefied gas and amine liquid stop 30-60min in two-grade desulfurizing hydrogen separating tank (12), the liquefied gas of discharging due to the outlet of two-grade desulfurizing hydrogen separating tank (12) top is entrained with amine liquid, fiber type coalescer (19) is utilized to remove carrying amine liquid secretly,
Step 2: by the liquefied gas of discharging from fiber type coalescer (19) side with together to input from the alkali lye of NaOH solution circulating pump (25) in one-level liquid film sweetening reaction device (13) and remove mercaptan in one-level liquid film sweetening reaction device (13), first grade desulfurizing alcohol separating tank (14) is utilized to be separated with alkali lye reacted liquefied gas, described liquefied gas and alkali lye stop 20-40min in first grade desulfurizing alcohol separating tank (14), alkali lye after described separation is derived via first grade desulfurizing alcohol separating tank (14) outlet at bottom and is passed through rich alkali lye mouth (8) take-up gear, by liquefied gas after being separated with to import via fresh alkali lye or poor alkali lye mouth (4), and the fresh alkali lye filtered through alkali lye strainer (23) or poor alkali lye together input in secondary liquid film sweetening reaction device (15) and remove further mercaptan, then two-grade desulfurizing alcohol separating tank (16) is utilized to be separated with alkali lye reacted liquefied gas again, described liquefied gas and alkali lye stop 20-40min in two-grade desulfurizing alcohol separating tank (16), alkali lye after described separation is derived via two-grade desulfurizing alcohol separating tank (16) outlet at bottom, utilize NaOH solution circulating pump (25) that the alkali lye after separation is circulated to one-level liquid film sweetening reaction device (13) to recycle,
Step 3: by the liquefied gas of discharging from the outlet of described two-grade desulfurizing alcohol separating tank (16) top with the mouth of a river (5) imports via washing, and together input in liquid film washing contactor (17) through the washing water that water washing cycles pump (26) circulates liquefied gas is washed, then liquefied gas and washing water are together imported and wash separating tank (18) and be separated, described liquefied gas and washing water stop 25-50min washing in separating tank (18), water washing cycles pump (26) is utilized to carry out recirculation to the washing water of discharging from washing separating tank (18) bottom, and imported in liquid film washing contactor (17) and recycle, washing separating tank (18) is utilized to be separated the alkali lye carried secretly in liquefied gas after washing and to discharge from washing separating tank (18) outlet at bottom, final through alkaline sewage mouth (7) take-up gear, and the liquefied gas after being separated is discharged from the outlet of washing separating tank (18) top, and via refining liquefied gas port (6) by liquefied refinery gas take-up gear.
8. liquefied gas desulfurizing method according to claim 7, is characterized in that, in described step 1, position, the boundary scope of first grade desulfurizing hydrogen separating tank (10) and two-grade desulfurizing hydrogen separating tank (12) interior liquefied gas and amine liquid is 40-50%.
9. liquefied gas desulfurizing method according to claim 8, is characterized in that, in described step 2, first grade desulfurizing alcohol separating tank (14) is 40-50% with position, the boundary scope of two-grade desulfurizing alcohol separating tank (16) interior liquefied gas and alkali lye.
10. liquefied gas desulfurizing method according to claim 9, is characterized in that, position, the boundary scope of washing separating tank (18) interior liquefied gas and water in described step 3 is 30-40%.
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| CN110013751A (en) * | 2019-02-15 | 2019-07-16 | 宁波中一石化科技股份有限公司 | A kind of wet process takes off the device and method of non-mercaptan sulfur and mercaptan in liquefied gas |
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