CN114317054A - Device and method for eliminating back-vulcanization effect in liquefied gas desulfurization process - Google Patents
Device and method for eliminating back-vulcanization effect in liquefied gas desulfurization process Download PDFInfo
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- CN114317054A CN114317054A CN202111634081.7A CN202111634081A CN114317054A CN 114317054 A CN114317054 A CN 114317054A CN 202111634081 A CN202111634081 A CN 202111634081A CN 114317054 A CN114317054 A CN 114317054A
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Abstract
The invention discloses a device and a method for eliminating the resulfurization effect in the liquefied gas desulfurization process, and the device comprises at least one eliminating system, an input pipeline, an output pipeline and a composite desulfurizer tank, wherein each eliminating system comprises a liquid film desulfurization contactor, a desulfurization separation tank, a desulfurization circulating pump and a first desulfurizer pipeline; like this, can return the different selection elimination system's of sulphur degree according to the alkali wash back liquefied gas of pending number to the effectual influence that eliminates liquefied gas desulfurization process and return sulphur, the very big liquefied gas amine of reduction washes the process and avoids the requirement of mercaptan side reaction and takes off the alkali lye of mercaptan alkali lye oxidation regeneration process and the requirement of byproduct disulfide separation, and then can effectual reduction liquefied gas desulfurization process's running cost, simplified operation process.
Description
Technical Field
The invention relates to a device and a method for eliminating the effect of back-vulcanization in the process of liquefied gas desulfurization.
Background
With the continuous development of the petrochemical industry, the liquefied petroleum gas has been paid more and more attention as a chemical basic raw material and a novel fuel. In chemical engineering, the liquefied petroleum gas is deeply processed and separated to obtain ethylene, propylene, butylene and the like, so as to synthesize plastics, rubber, fibers and the like. Therefore, with the more remarkable importance of the liquefied petroleum gas in deep processing and high value-added product utilization rate, the requirement on the sulfur content of the liquefied petroleum gas is more and more strict, so that the requirements of downstream products are met.
For the mercaptan removal by alkali washing, sodium hydroxide and mercaptan in alkali liquor are reacted to generate sodium hydroxide and disulfide, the sodium hydroxide containing sodium hydroxide reacts with oxygen in the air under the action of a sulfonated cobalt phthalocyanine catalyst, the disulfide and the alkali liquor are separated by a mode of carrying a large amount of tail gas and frequently replacing the alkali liquor in the traditional process, the disulfide and the alkali liquor are separated by reverse extraction of solvents such as naphtha and the like in recent ten years, or the disulfide and the alkali liquor are separated by a technology of separating and recovering the disulfide by liquid phase of the inventor, so that the alkali liquor after the disulfide separation can be recycled for mercaptan removal, but no matter what process, the separation effect of the disulfide and the alkali liquor is not complete, hundreds of ppm of disulfide still remain in the alkali liquor, and the disulfide in the alkali liquor is extracted by liquefied petroleum gas in the process of recycling the mercaptan removal to cause the back addition of sulfur, resulting in an increase in the total sulfur of the final lpg product.
Although the prior art for removing hydrogen sulfide and mercaptan from liquefied petroleum gas is mature and the application effect is approved by refineries, the phenomenon of resulfurization of liquefied petroleum gas caused by side reactions always exists, and the quality is difficult to effectively guarantee for increasingly severe product indexes in recent years. In order to ensure the quality, only alkali can be frequently replaced or amine liquid can be supplemented, which not only causes the emission of three wastes and increases the environmental pollution, but also causes the increase of the desulfurization cost of the liquefied petroleum gas.
Disclosure of Invention
The invention aims to solve the technical problem of providing a device and a method for eliminating the effect of sulfur addition in the process of liquefied gas desulfurization, which solve the problem that the total sulfur of the product liquefied gas is difficult to reach the standard due to the sulfur addition in the process of liquefied gas desulfurization, and realize the requirement of deep desulfurization of the liquefied gas.
In order to solve the technical problems, the invention provides a device for eliminating the effect of adding sulfur in the process of liquefied gas desulfurization, which comprises at least one eliminating system, an input pipeline, an output pipeline and a composite desulfurizing agent tank, wherein the input pipeline is connected with the output pipeline;
every elimination system all includes a liquid film desulfurization contactor, a desulfurization knockout drum, a desulfurization circulating pump and a first desulfurizer pipeline, liquid film desulfurization contactor's feed inlet and input pipeline be linked together, liquid film desulfurization contactor's discharge gate be linked together with the feed inlet of desulfurization knockout drum, the discharge gate that sets up at output pipeline and desulfurization knockout drum be linked together, the discharge gate that sets up in the bottom of desulfurization knockout drum be linked together through first desulfurizer pipeline and liquid film desulfurization contactor's feed inlet, the desulfurization circulating pump set up on first desulfurizer pipeline, the input of desulfurization circulating pump be linked together with the discharge gate of desulfurization knockout drum liquid film bottom, the output of desulfurization circulating pump be linked together with the feed inlet of desulfurization contactor.
Preferably, each eliminating system is connected with a second desulfurizer pipeline and a rich desulfurizer discharging line for replacing the desulfurizer, the second desulfurizer pipeline and the rich desulfurizer discharging line are communicated with a discharge hole at the bottom of the desulfurization separation tank, and the composite desulfurizer tank is communicated with the input end of the desulfurization circulating pump through the second desulfurizer pipeline.
Preferably, the liquid film desulfurization contactor is filled with a wire mesh filler and a stainless steel wire, and the wire mesh filler and the stainless steel wire are arranged in a separated manner.
Preferably, the discharge port of the liquid film desulfurization contactor is fixedly connected with the feed port of the desulfurization separation tank through a flange.
A method for eliminating the effect of back-adding sulfur in the process of liquefied gas desulfurization is characterized in that: the method comprises the following steps:
(1) fully and uniformly mixing the composite desulfurizer and the desalted water in the composite desulfurizer tank to prepare the desulfurizer;
(2) conveying the desulfurizer in the composite desulfurizer tank to the top of a liquid film desulfurization contactor through a desulfurization circulating pump, conveying the alkali-washed liquefied gas to be treated to the top of the liquid film desulfurization contactor through a liquefied gas pipeline, mixing the alkali-washed liquefied gas to be treated with the desulfurizer by using the liquid film desulfurization contactor, thereby forming a mixed liquid of the liquefied gas and the desulfurizer, and completing the elimination of the back-vulcanization effect in the liquid film desulfurization contactor;
(3) conveying the mixed liquid of the liquefied gas and the desulfurizer to the inside of a desulfurization separation tank through a liquid film desulfurization contactor, and performing sedimentation separation on the mixed liquid of the liquefied gas and the desulfurizer by using the desulfurization separation tank to obtain a sulfide-containing rich desulfurizer and the liquefied gas for eliminating the effect of returning sulfur;
(4) and withdrawing the sulfide-containing rich desulfurization agent using a desulfurization circulating pump, and transferring the withdrawn rich desulfurization agent to the top of the membrane desulfurization contactor, thereby completing one cycle.
Preferably, in the step, the concentration of the tert-butylamine ethoxy ethanol TBEE in the composite desulfurizer is 20-30 wt%, the concentration of the 1, 3, 5-tri-hexa-amino-s-triazine is 20-25 wt%, the concentration of the oxazolidine compound is 10-20 wt%, the concentration of the N-methyl pyrrolidone is 3-5 wt%, the concentration of the polyethylene glycol dimethyl ether is 3-5 wt%, the concentration of the N-methyl morpholine is 3-5 wt%, the concentration of the penetrating agent is 1-2 wt%, the concentration of the defoaming agent is 0.5-1 wt%, and the concentration of the antioxidant is 0.5-1 wt%.
Preferably, in the step, the concentration of the composite desulfurizer in the desulfurizer is 25 to 45 wt%.
Preferably, in step (a), the liquefied gas has a pressure ranging from 0.8 to 3.5MPaG and a temperature ranging from 10 to 60 ℃; the mass flow rate range of the mixture of the desulfurizer and the alkali-washed liquefied gas to be treated in the liquid film desulfurization contactor is 10-40%; the apparent linear velocity of the liquid gas subjected to alkali cleaning and to be treated in the liquid film desulfurization contactor is 0.2-0.6 m/s, and the apparent linear velocity of the desulfurizing agent is 0.02-0.16 m/s.
Preferably, in the step, the retention time of the mixed liquid of the liquefied gas and the desulfurizer in the desulfurization separation tank is 10-40 min.
Preferably, in the step, when the sulfur content in the liquefied gas obtained after the sedimentation separation exceeds 10mg/m3 or the sulfur content in the desulfurizer exceeds 10g/L, the desulfurizer is replaced by a second desulfurizer pipeline and a desulfurizer-rich discharge line in the elimination system.
After adopting the structure, compared with the prior art, the invention has the following advantages: the number of the eliminating systems can be selected according to different degrees of sulfur return of the liquefied gas after alkaline washing to be treated, so that the system can be eliminated by a mixed liquid consisting of the liquefied gas and a desulfurizing agent more than once according to requirements, and the obtained liquefied gas is ensured to meet the industrial requirements; the bottom of the desulfurization separation tank is communicated with the top of the liquid film desulfurization contactor through the first desulfurizer pipeline, and a desulfurization circulating pump is arranged on the first desulfurizer pipeline to form a desulfurizer circulation loop, so that the desulfurization efficiency of the desulfurizer is improved, the shearing emulsification of liquefied gas and the desulfurizer is avoided, the entrainment is reduced, the residence time of mixed liquid in the desulfurization separation tank is greatly reduced, the equipment size of the desulfurization separation tank is further reduced, the production cost and the occupied area of the equipment are reduced, meanwhile, the composite desulfurizer capable of being fed into an MDEA regeneration system for regeneration is adopted, the device in the prior art is convenient to upgrade, optimize and reform, and the difficulty and the cost of the device in the prior art in technical upgrading and reforming are also reduced.
Drawings
FIG. 1 is a schematic structural diagram of the present invention.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.
The device for eliminating the effect of the added sulfur in the process of desulfurizing liquefied gas, which is shown in figure 1, comprises at least one eliminating system 10 and an input pipeLine 21, an output line 22 and a composite desulfurizer tank 30; each eliminating system 10 comprises a liquid film desulfurization contactor 11, a desulfurization separation tank 12, a desulfurization circulating pump 13 and a first desulfurizer pipeline 14, the feed inlet of the liquid film desulfurization contactor 11 is communicated with an input pipeline 21, the discharge outlet of the liquid film desulfurization contactor 11 is communicated with the feed inlet of the desulfurization separation tank 12, the discharge outlet of the liquid film desulfurization contactor 11 is fixedly connected with the feed inlet of the desulfurization separation tank 12 through a flange, an output pipeline 22 is communicated with the discharge outlet arranged at the top of the desulfurization separation tank 12, the discharge outlet arranged at the bottom of the desulfurization separation tank 12 is communicated with the feed inlet of the liquid film desulfurization contactor 11 through the first desulfurizer pipeline 14, the desulfurization circulating pump 13 is arranged on the first desulfurizer pipeline 14, the input end of the desulfurization circulating pump 13 is communicated with the discharge outlet at the bottom of the desulfurization separation tank 12, the output end of the desulfurization circulating pump 13 is communicated with the feed inlet of the liquid film desulfurization contactor 11, wherein a plurality of elimination systems 10 are connected in series, and a liquid film desulfurization contactor 11 in the next elimination system 10 between two adjacent elimination systems 10 is connected with a liquefied gas outlet arranged on the top of a desulfurization separation tank 12 in the previous elimination system 10, so that, can be specifically set according to the different sulfur return effects of the liquefied gas after alkali washing to be treated so as to be suitable for the liquefied gas with sulfur return in different degrees, the system 10 can be eliminated by a mixed liquid composed of liquefied gas and a desulfurizer more than once according to the requirement, and finally the liquefied gas obtained after being processed by a device for eliminating the sulfur effect in the process of liquefied gas desulfurization meets the process requirement, namely, the total sulfur content of the liquefied gas after alkali cleaning is not more than 10mg/m after being processed by the eliminating system 10.3And a desulfurizer circulation is formed in the elimination system 10 through the desulfurization circulating pump 13, so that the use amount of the desulfurizer is reduced, the utilization rate of the desulfurizer is improved, the cost is saved, and the emulsification of the desulfurizer is avoided.
Every elimination system 10 is last all to be connected with a second desulfurizer pipeline 15 and a rich desulfurizer row's line 16 that is used for replacing the desulfurizer, second desulfurizer pipeline 15 and rich desulfurizer row's line 16 all be linked together with the discharge gate of desulfurization knockout drum 12 bottom, compound desulfurizer jar 30 be linked together through the input of second desulfurizer pipeline 15 with desulfurization circulating pump 13, compound amine liquid desulfurizer jar 30 for the pressure vessel who takes the stirring, compound desulfurizer jar 30 is used in eliminating liquefied gas desulfurization process and returns the sulphur effect device and specifically is used for compound desulfurizer and the abundant mixing of demineralized water to obtain required desulfurizer to avoid influencing the effect of elimination process.
The liquid film desulfurization contactor 11 is filled with a wire mesh filler 111 and a stainless steel wire 112, wherein the wire mesh packing 111 and the stainless steel wire 112 are separately provided, and the liquid film desulfurization contactor 11 is filled with the wire mesh packing 111 at the upper portion and the stainless steel wire 112 at the lower portion, so that, when the eliminating system 10 is used, the contact reaction of the desulfurizer and the sulfur returning substance in the liquefied gas at an oil-water interface is realized under the action of liquid film mass transfer, so that the sulfur returning substance in the liquefied gas and the desulfurizer form or dissolve chemical substances, then flows into the desulfurization separation tank 12 to stay for a period of time for sedimentation separation, thereby layering the liquefied gas and the desulfurizer containing sulfide, since the density of the desulfurizing agent is greater than that of the liquefied gas, the desulfurizing agent is deposited at the bottom of the desulfurization separation tank 12, and the liquefied gas is accumulated at the top of the desulfurization separation tank 12.
In order to realize the scheme, the method for eliminating the back sulfur effect in the liquefied gas desulfurization process comprises the following steps:
(1) the composite desulfurizer and the desalted water are fully and uniformly mixed in the composite desulfurizer tank 30, so that the desulfurizer with the required concentration is prepared;
(2) conveying the desulfurizer in the composite desulfurizer tank 30 to the top of the liquid film desulfurization contactor 11 through a desulfurization circulating pump 13, conveying the alkali-washed liquefied gas to be treated to the top of the liquid film desulfurization contactor 11 through a liquefied gas pipeline 20, mixing the alkali-washed liquefied gas to be treated with the desulfurizer by using the liquid film desulfurization contactor 11, thereby forming a mixed solution of the liquefied gas and the desulfurizer, and completing the elimination of the back-vulcanization effect in the liquid film desulfurization contactor 11;
(3) the mixed liquid of the liquefied gas and the desulfurizer is conveyed to the inside of a desulfurization separation tank 12 through a liquid film desulfurization contactor 11, the mixed liquid of the liquefied gas and the desulfurizer is subjected to sedimentation separation by using the desulfurization separation tank 12, and the liquefied gas is separated by the desulfurization separation tank 12 to obtain the sulfide-containing desulfurizer rich in desulfurizer and the liquefied gas for eliminating the effect of adding sulfur;
(4) the sulfide-containing rich desulfurization agent is withdrawn by the desulfurization circulating pump 13, and the withdrawn rich desulfurization agent is fed to the top of the membrane desulfurization contactor 11, thereby completing one cycle.
In the step 1, the concentration of tert-butylamine ethoxy ethanol TBEE in the composite desulfurizer is 20-30 wt%, the concentration of 1, 3, 5-tri 2-hydroxyethyl-hexamine-s-triazine is 20-25 wt%, the concentration of oxazolidine compounds is 10-20 wt%, the concentration of N-methyl pyrrolidone is 3-5 wt%, the concentration of polyethylene glycol dimethyl ether is 3-5 wt%, the concentration of N-methyl morpholine is 3-5 wt%, the concentration of penetrant is 1-2 wt%, the concentration of defoaming agent is 0.5-1 wt%, and the concentration of antioxidant is 0.5-1 wt%; the concentration of the composite desulfurizer in the desulfurizer is 25-45 wt%; in the step 2, the pressure range of the liquefied gas is 0.8-3.5MPaG, and the temperature range is 10-60 ℃; the mass flow rate range of the mixture of the desulfurizer and the alkali-washed liquefied gas to be treated in the liquid film desulfurization contactor 11 is 10-40%; the apparent linear velocity of the liquid gas subjected to alkali washing in the liquid film desulfurization contactor is 0.2-0.6 m/s, and the apparent linear velocity of the desulfurizer is 0.02-0.16 m/s; in the step 3, the retention time of the mixed liquid of the liquefied gas and the desulfurizer in the desulfurization separation tank 12 is 10-40 min; when the sulfur content in the liquefied gas obtained after the settling separation exceeds 10mg/m3 or the sulfur content in the desulfurizer exceeds 10g/L, the desulfurizer is replaced by a second desulfurizer pipeline 15 and a desulfurizer-rich discharge line 16 in the elimination system 10.
The working principle is as follows: liquefied gas in the liquefied gas pipeline 20 is conveyed to the liquid film desulfurization contactor 11, is mixed with a desulfurizer pumped and discharged by the desulfurization circulating pump 13 and flows into the liquid film desulfurization contactor 11, and then flows to the desulfurization separation tank 12 through the liquid film desulfurization contactor 11 to be stopped and separated, wherein the liquefied gas and the desulfurizer perform liquid film mass transfer action through a wire mesh filler 111 and a stainless steel wire 112 arranged in the liquid film desulfurization contactor 11, so that sulfides generated by adding sulfur back in the liquefied gas enter the desulfurizer through chemical reaction and physical dissolution, and then are settled and separated in the desulfurization separation tank 12, and thus, the elimination effect of the elimination system 10 on the sulfur adding back effect of the liquefied gas desulfurization is realized. Wherein elimination system 10 during operation, desulfurization circulating pump 13 can draw the desulfurizer in the desulfurization knockout drum 12 then arrange and send to in liquid film desulfurization contactor 11, realize the circulation circuit of desulfurizer, can understand, the circulation flow of desulfurizer among the elimination system 10, can reduce and eliminate back the required desulfurizer use amount when returning the sulphur effect to returning sulphur liquefied gas, and avoid the desulfurizer emulsification, greatly reduce the separation dwell time between desulfurizer and liquefied gas, and then reduce the equipment size of desulfurization knockout drum 12, reduction in production cost and device's use area.
The present application is described in further detail below with reference to specific examples, which should not be construed as limiting the scope of the invention as claimed.
The first embodiment is as follows:
the properties of the liquefied gas required for eliminating the additional sulfur effect in the process of desulfurizing the liquefied gas by the device and the method are shown in the table below.
Liquefied gas properties and degree of reversion.
After the mercaptan is removed by alkali washing, the liquefied gas enters a liquid film desulfurization contactor through a liquefied gas pipeline to contact with a circulating desulfurizer with the mass being 15% of the liquefied gas, the elimination of the back-added sulfur effect is completed, then the liquefied gas stays in a desulfurization separation tank for 30 minutes to carry out sedimentation separation, the desulfurizer is extracted from the bottom of the desulfurization separation tank under the action of a desulfurization circulating pump and is discharged to the liquid film desulfurization contactor, so that a circulating loop is formed, the cyclic use of the desulfurizer is realized, and the separated liquefied gas is ejected out of the desulfurization separation tank and is sent to subsequent facilities.
Wherein the apparent velocity of the liquefied gas in the liquid film desulfurization contactor is 0.4m/s, the apparent velocity of the desulfurizer is 0.03m/s, and the concentration of the desulfurizer is 30% wt.
Example two:
the properties of the liquefied gas required for eliminating the additional sulfur effect in the process of desulfurizing the liquefied gas by the device and the method are shown in the table below.
Liquefied gas properties and degree of reversion.
The difference between the embodiment and the first embodiment is that after the mercaptan is removed by alkali washing, the liquefied gas enters a liquid film desulfurization contactor through a liquefied gas pipeline to contact with a circulating desulfurizer with the mass of 25% of the liquefied gas to complete the elimination of the effect of the added sulfur, and a desulfurization separation tank stays for 35 minutes to perform settling separation, wherein the apparent velocity of the liquefied gas in the liquid film desulfurization contactor is 0.3m/s, the apparent velocity of the desulfurizer is 0.04m/s, and the concentration of the desulfurizer is 35% wt.
Example three:
the properties of the liquefied gas required for eliminating the additional sulfur effect in the process of desulfurizing the liquefied gas by the device and the method are shown in the table below.
Liquefied gas properties and degree of reversion.
The difference between the embodiment and the first embodiment is that after the alkali washing and mercaptan removal, the liquefied gas enters a first-stage liquid film desulfurization contactor through a liquefied gas pipeline to contact with a circulating desulfurizer with the mass of 35% of the liquefied gas to complete the elimination of the back-addition sulfur effect, then stays in the first-stage desulfurization separation tank for 30 minutes to perform sedimentation separation, the desulfurizer is extracted from the bottom of the desulfurization separation tank under the action of a desulfurization circulating pump and is discharged to the liquid film desulfurization contactor to form a circulating loop to realize the recycling of the desulfurizer, the separated liquefied gas is ejected out of the desulfurization separation tank, enters a second-stage liquid film desulfurization contactor through the liquefied gas pipeline to contact with the circulating desulfurizer with the mass of 35% of the liquefied gas to complete the elimination of the back-addition sulfur effect, then stays in the second-stage desulfurization separation tank for 30 minutes to perform sedimentation separation, the desulfurizer is extracted from the bottom of the desulfurization separation tank under the action of the desulfurization circulating pump and is discharged to the liquid film desulfurization contactor, so as to form a circulation loop to realize the recycling of the desulfurizer, and the separated liquefied gas is ejected out of the desulfurization separation tank and enters subsequent facilities.
Wherein the apparent velocity of the liquefied gas in the liquid film desulfurization contactor is 0.5m/s, the apparent velocity of the desulfurizer is 0.09m/s, and the concentration of the desulfurizer is 40% wt.
Example results:
the implementation results of the embodiment show that the device and the method for eliminating the effect of the added sulfur in the liquefied gas desulfurization process can eliminate the phenomenon of the added sulfur in the liquefied gas, meet the industrial requirements, and even eliminate the added sulfur and simultaneously remove other sulfur. While the sulfur content of the third-stage sulfur addition of the embodiment exceeds 150mg/m3In the case of (2), only two abatement systems are required to meet a total sulfur of not more than 10mg/m3The requirements of (1). Therefore, the invention has simple and convenient operation, greatly improves the utilization rate of the desulfurizer, reduces the loss of the desulfurizer, further reduces the operation cost, and also reduces the difficulty of upgrading and transforming the existing liquefied gas desulfurization process technology.
Therefore, the device and the method for eliminating the additional sulfur effect in the liquefied gas desulfurization process greatly reduce the requirement of avoiding mercaptan side reaction in the liquefied gas amine washing process and the requirement of separating alkali liquor and byproduct disulfide in the oxidation regeneration process of the sweetening alkali liquor, and further can effectively reduce the operation cost of the liquefied gas desulfurization process and simplify the operation process. The invention overcomes and solves the harm caused by adding sulfur in the byproduct disulfide in the liquefied gas desulfurization process in the prior art, and ensures that the total sulfur of the liquefied gas meets the industrial requirement.
The above description is only about the preferred embodiment of the present invention, but it should not be understood as limiting the claims, and the present invention may be modified in other structures, not limited to the above structures. In general, all changes which come within the scope of the invention as defined by the independent claims are intended to be embraced therein.
Claims (12)
1. A device for eliminating the effect of the added sulfur in the process of liquefied gas desulfurization is characterized by comprising at least one eliminating system (10), an input pipeline (21), an output pipeline (22) and a composite desulfurizing agent tank (30);
each eliminating system (10) comprises a liquid film desulfurization contactor (11), a desulfurization separation tank (12), a desulfurization circulating pump (13) and a first desulfurizer pipeline (14), the feed inlet of the liquid film desulfurization contactor (11) is communicated with an input pipeline (21), the discharge outlet of the liquid film desulfurization contactor (11) is communicated with the feed inlet of the desulfurization separation tank (12), an output pipeline (22) is communicated with the discharge outlet arranged at the top of the desulfurization separation tank (12), the discharge outlet arranged at the bottom of the desulfurization separation tank (12) is communicated with the feed inlet of the desulfurization contactor (11) through the first desulfurizer pipeline (14), the desulfurization circulating pump (13) is arranged on the first desulfurizer pipeline (14), the input end of the desulfurization circulating pump (13) is communicated with the discharge outlet at the bottom of the desulfurization separation tank (12), the output end of the desulfurization circulating pump (13) is communicated with the feed inlet of the liquid film desulfurization contactor (11).
2. The device for eliminating the effect of the added sulfur in the desulfurization process of liquefied gas according to claim 1, wherein each eliminating system (10) is connected with a second desulfurizer pipeline (15) for replacing the desulfurizer and a rich desulfurizer discharging line (16), the second desulfurizer pipeline (15) and the rich desulfurizer discharging line (16) are both communicated with a discharge port at the bottom of the desulfurization separation tank (12), and the composite desulfurizer tank (30) is communicated with the input end of the desulfurization circulating pump (13) through the second desulfurizer pipeline (15).
3. The device for eliminating the effect of sulfur addition in the desulfurization process of liquefied gas according to claim 1, wherein the liquid film desulfurization contactor (11) is filled with a wire mesh filler (111) and a stainless steel wire (112), and the wire mesh filler (111) and the stainless steel wire (112) are arranged separately.
4. The device for eliminating the effect of sulfur addition in the desulfurization process of liquefied gas according to claim 1, wherein the discharge port of the liquid film desulfurization contactor (11) is fixedly connected with the feed port of the desulfurization separation tank (12) through a flange.
5. A method for eliminating the effect of back-adding sulfur in the process of liquefied gas desulfurization is characterized in that: the method comprises the following steps:
(1) the composite desulfurizer and the demineralized water are fully and uniformly mixed in a composite desulfurizer tank (30) to prepare the desulfurizer;
(2) conveying a desulfurizer in a composite desulfurizer tank (30) to the top of a liquid film desulfurization contactor (11) through a desulfurization circulating pump (13), conveying a to-be-treated alkali-washed liquefied gas to the top of the liquid film desulfurization contactor (11) through a liquefied gas pipeline (20), mixing the to-be-treated alkali-washed liquefied gas with the desulfurizer by using the liquid film desulfurization contactor (11), thereby forming a mixed solution of the liquefied gas and the desulfurizer, and completing the elimination of a back-sulfur effect in the liquid film desulfurization contactor (11);
(3) conveying the mixed liquid of the liquefied gas and the desulfurizer to the inside of a desulfurization separation tank (12) through a liquid film desulfurization contactor (11), and performing sedimentation separation on the mixed liquid of the liquefied gas and the desulfurizer by using the desulfurization separation tank (12) to obtain a sulfide-containing desulfurizer-rich agent and a liquefied gas for eliminating the effect of adding sulfur back;
(4) and withdrawing the sulfide-containing rich desulfurization agent by using a desulfurization circulating pump (13), and feeding the withdrawn rich desulfurization agent to the top of the membrane desulfurization contactor (11), thereby completing one cycle.
6. The method for eliminating the effect of sulfur back-feeding in the desulfurization process of liquefied gas according to claim 5, wherein in step (1), the concentration of TBEE in the composite desulfurizing agent is 20-30 wt%, the concentration of 1, 3, 5-tris (2-hydroxyethyl) -hexa-amino-s-triazine is 20-25 wt%, the concentration of oxazolidine compounds is 10-20 wt%, the concentration of N-methylpyrrolidone is 3-5 wt%, the concentration of dimethyl polyglycol ether is 3-5 wt%, the concentration of N-methylmorpholine is 3-5 wt%, the concentration of penetrant is 1-2 wt%, the concentration of defoaming agent is 0.5-1 wt%, and the concentration of antioxidant is 0.5-1 wt%.
7. The method for eliminating the effect of sulfur addition in the desulfurization process of liquefied gas according to claim 5, wherein in the step (1), the concentration of the composite desulfurizing agent in the desulfurizing agent is 25 to 45 wt%.
8. The method for eliminating the effect of sulfur addition in the desulfurization process of liquefied gas according to claim 5, wherein in the step (2), the pressure of the liquefied gas is in the range of 0.8-3.5MPaG, and the temperature is in the range of 10-60 ℃.
9. The method for eliminating the effect of sulfur addition in the desulfurization process of liquefied gas according to claim 5, wherein in the step (2), the mass flow ratio of the desulfurizer to the alkali-washed liquefied gas to be treated in the liquid film desulfurization contactor (11) is in the range of 10-40%.
10. The method for eliminating the effect of sulfur addition in the desulfurization process of liquefied gas according to claim 5, wherein in the step (2), the apparent linear velocity of the alkali-washed liquefied gas to be treated in the liquid film desulfurization contactor is 0.2-0.6 m/s, and the apparent linear velocity of the desulfurizing agent is 0.02-0.16 m/s.
11. The method for eliminating the effect of sulfur addition in the desulfurization process of liquefied gas according to claim 5, wherein in the step (3), the retention time of the mixed liquid of the liquefied gas and the desulfurizing agent in the desulfurization separation tank (12) is 10-40 min.
12. The method for eliminating the effect of sulfur addition in the desulfurization process of liquefied gas according to claim 5, wherein in the step (3), when the sulfur content in the liquefied gas obtained after the settling separation exceeds 10mg/m3 or the sulfur content in the desulfurizing agent exceeds 10g/L, the desulfurizing agent is replaced by the second desulfurizing agent pipeline (15) and the desulfurizing agent-rich discharging line (16) in the eliminating system (10).
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