CN113713558A - Sulfur dioxide adsorption process - Google Patents

Sulfur dioxide adsorption process Download PDF

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Publication number
CN113713558A
CN113713558A CN202010456586.8A CN202010456586A CN113713558A CN 113713558 A CN113713558 A CN 113713558A CN 202010456586 A CN202010456586 A CN 202010456586A CN 113713558 A CN113713558 A CN 113713558A
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reactor
regeneration
gas
adsorption
concentration
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朱荣海
常宏岗
何金龙
陈昌介
刘宗社
熊钢
李金金
杨威
温崇荣
余军
许娟
张素娟
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Petrochina Co Ltd
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    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
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    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/508—Sulfur oxides by treating the gases with solids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/112—Metals or metal compounds not provided for in B01D2253/104 or B01D2253/106
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
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    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
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    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
    • B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
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Abstract

The application discloses sulfur dioxide adsorption technology belongs to the technical field of gas adsorption. The sulfur dioxide adsorption process provided by the embodiment of the application realizes the adsorption of sulfur dioxide in tail gas and the regeneration of the adsorbent through the first reactor and the at least one second reactor, and the adsorption reactor and the regeneration reactor can be exchanged according to the adsorption condition and the regeneration condition of the adsorbent, so that the regeneration while adsorption is realized.

Description

Sulfur dioxide adsorption process
Technical Field
The application relates to the technical field of gas adsorption. In particular to a sulfur dioxide adsorption process.
Background
Sulfur dioxide is a common atmospheric pollutant, and reducing the emission of sulfur dioxide and controlling atmospheric pollution become one of the important subjects of environmental protection in China. With the stricter environmental protection standards of all countries in the world, the emission of sulfur dioxide generated by a sulfur recovery device is also required to be stricter.
In the related art, a reduction absorption type tail gas treatment process (such as SCOT) or an oxidation absorption type treatment process (such as Cansolv) is mainly adopted to reduce the sulfur dioxide emission concentration in the tail gas of the sulfur recovery device, and after the emission standard is reached, the residual tail gas is discharged. For example, in the reduction absorption type tail gas treatment process, a mixed gas of claus tail gas and hydrogen is heated by an online combustion furnace, an electric heater, steam heat exchange and other modes, then the mixed gas is introduced into a reactor, and hydrogen and sulfur-containing gas including sulfur dioxide in the tail gas react in the reactor to obtain hydrogen sulfide-containing hydrogenation tail gas. Then cooling the hydrogenation tail gas by a quench tower, introducing the cooled hydrogenation tail gas into an absorption tower, absorbing hydrogen sulfide in the absorption tower by amine liquid, introducing the absorbed saturated amine liquid into a regeneration tower for regeneration, stripping the hydrogen sulfide in the amine liquid by raising the temperature, and then conveying the hydrogen sulfide back to a sulfur recovery device.
However, the treatment process in the related art has the disadvantages of complicated process flow, complex device, high investment, high operation cost and poor economy when the device scale is low.
Disclosure of Invention
The embodiment of the application provides a sulfur dioxide adsorption process, which can reduce energy consumption, save investment and reduce operation cost. The specific technical scheme is as follows:
the embodiment of the application provides a sulfur dioxide adsorption process, which comprises the following steps:
introducing tail gas into an adsorption reactor, adsorbing sulfur dioxide in the tail gas through an adsorbent in the adsorption reactor, introducing a regeneration gas with a first preset temperature into a regeneration reactor, and regenerating the adsorbent in the regeneration reactor through a reducing gas in the regeneration gas; the regeneration reactor comprises a first reactor, the adsorption reactor comprises at least one second reactor, when the number of the second reactors is multiple, two adjacent second reactors are connected in series through a first valve, and the first reactor is connected with a first second reactor and a last second reactor in the series sequence in the at least one second reactor through second valves;
detecting the concentration of sulfur dioxide at the outlet of the adsorption reactor and the concentration of sulfur-containing gas at the outlet of the regeneration reactor, wherein the sulfur-containing gas at the outlet of the regeneration reactor is generated by the reaction of the reducing gas and the adsorbent;
when the concentration of sulfur dioxide at the outlet of the adsorption reactor does not reach a first preset concentration, discharging tail gas from which the sulfur dioxide is removed;
when the concentration of the sulfur-containing gas at the outlet of the regeneration reactor is lower than a second preset concentration, selecting a second reactor from the at least one second reactor as a regeneration reactor, using the remaining second reactors of the first reactor and the at least one second reactor as adsorption reactors, executing the step of introducing tail gas into the adsorption reactors, adsorbing sulfur dioxide in the tail gas through an adsorbent in the adsorption reactors, introducing regeneration gas at a first preset temperature into the regeneration reactors, and regenerating the adsorbent in the regeneration reactors through reducing gas in the regeneration gas until each second reactor is used as a regeneration reactor for regeneration;
and taking the first reactor as a regeneration reactor, taking the at least one second reactor as an adsorption reactor, executing the steps of introducing tail gas into the adsorption reactor, adsorbing sulfur dioxide in the tail gas through an adsorbent in the adsorption reactor, introducing a regeneration gas with a first preset temperature into the regeneration reactor, and regenerating the adsorbent in the regeneration reactor through a reducing gas in the regeneration gas.
In one possible implementation, the at least one second reactor comprises: a third reactor and a fourth reactor, the third reactor and the fourth reactor being connected in series through the first valve, the first reactor being connected in series with the third reactor and the fourth reactor through the second valve;
the step of introducing tail gas into the adsorption reactor comprises the following steps:
introducing the tail gas into the third reactor and the fourth reactor, wherein the tail gas firstly enters the third reactor and then enters the fourth reactor;
the selecting one of the at least one second reactor as a regeneration reactor, and using the remaining second reactor of the first reactor and the at least one second reactor as an adsorption reactor, includes:
the third reactor is used as a regeneration reactor, and the first reactor and the fourth reactor are used as adsorption reactors.
In another possible implementation, the regeneration gas further includes: an inert gas;
the method comprises the following steps of introducing a regeneration gas with a first preset temperature into a regeneration reactor, and regenerating an adsorbent in the regeneration reactor through a reducing gas in the regeneration gas, wherein the regeneration gas comprises:
introducing the inert gas into the regeneration reactor, and removing residual tail gas in the regeneration reactor through the inert gas;
and introducing the reducing gas into the regeneration reactor, and regenerating the adsorbent in the regeneration reactor by using the reducing gas.
In another possible implementation manner, before the selecting a second reactor from the at least one second reactor as the regeneration reactor and using the remaining second reactors of the first reactor and the at least one second reactor as the adsorption reactors when the concentration of the sulfur-containing gas at the outlet of the regeneration reactor is lower than the second preset concentration, the process further includes:
and continuously introducing the inert gas into the regeneration reactor, and stopping introducing the reducing gas into the regeneration reactor.
In another possible implementation, the concentration of the reducing gas in the regeneration gas is between 1% and 99%.
In another possible implementation manner, the introducing of the regeneration gas at the first preset temperature into the regeneration reactor includes:
exchanging heat between the tail gas from which the sulfur dioxide is removed and the regeneration gas which is not introduced into the regeneration reactor;
if the temperature of the regenerated gas after heat exchange does not reach the first preset temperature, heating the regenerated gas to the first preset temperature through an electric heater or an online furnace;
and introducing the regeneration gas with the first preset temperature into the regeneration reactor.
In another possible implementation, the process further includes:
and conveying the sulfur-containing gas back to a main combustion furnace, a primary Claus reactor or a secondary Claus reactor in the sulfur recovery device through a conveying pipeline.
In another possible implementation manner, an oxygen concentration detector and a reducing gas concentration detector are arranged on the conveying line;
before the sulfur-containing gas is transported back to a main combustion furnace, a primary claus reactor or a secondary claus reactor in a sulfur recovery plant through a transport line, the process further comprises:
detecting the concentration of oxygen in the sulfur-containing gas by the oxygen concentration detector;
detecting the concentration of the reducing gas in the sulfur-containing gas by the reducing gas concentration detector;
when the concentration of oxygen in the sulfur-containing gas is lower than a third preset concentration and the concentration of reducing gas in the sulfur-containing gas is lower than a fourth preset concentration, the step of conveying the sulfur-containing gas back to a main combustion furnace, a primary claus reactor or a secondary claus reactor in a sulfur recovery device through a conveying line is performed.
In another possible implementation manner, the number of the second reactors is 1-4.
In another possible implementation, the reducing gas includes: at least one of hydrogen, methane and carbon monoxide.
The technical scheme provided by the embodiment of the application has the following beneficial effects:
according to the sulfur dioxide adsorption process provided by the embodiment of the application, tail gas is introduced into an adsorption reactor, sulfur dioxide in the tail gas is adsorbed by an adsorbent in the adsorption reactor, regeneration gas with a first preset temperature is introduced into a regeneration reactor, and the adsorbent in the regeneration reactor is regenerated by reducing gas in the regeneration gas; detecting the concentration of sulfur dioxide at the outlet of the adsorption reactor and the concentration of sulfur-containing gas at the outlet of the regeneration reactor; when the concentration of the sulfur dioxide does not reach a first preset concentration, discharging the tail gas from which the sulfur dioxide is removed; when the concentration of the sulfur-containing gas is lower than a second preset concentration, selecting a second reactor from at least one second reactor as a regeneration reactor, taking the first reactor and the rest second reactors in the at least one second reactor as adsorption reactors, introducing tail gas into the adsorption reactors, adsorbing sulfur dioxide in the tail gas by using an adsorbent in the adsorption reactors, introducing a regeneration gas at a first preset temperature into the regeneration reactors, and regenerating the adsorbent in the regeneration reactors by using a reducing gas in the regeneration gas until each second reactor is used as a regeneration reactor for regeneration; the method comprises the steps of taking a first reactor as a regeneration reactor, taking at least one second reactor as an adsorption reactor, introducing tail gas into the adsorption reactor, adsorbing sulfur dioxide in the tail gas through an adsorbent in the adsorption reactor, introducing regeneration gas with a first preset temperature into the regeneration reactor, and regenerating the adsorbent in the regeneration reactor through reducing gas in the regeneration gas until each second reactor is taken as a regeneration reactor for regeneration. The process realizes the adsorption of sulfur dioxide in the tail gas and the regeneration of the adsorbent through the first reactor and the at least one second reactor, and the adsorption reactor and the regeneration reactor can be interchanged according to the adsorption condition and the regeneration condition of the adsorbent, so that the regeneration while adsorption is realized.
Drawings
FIG. 1 is a flow diagram of a sulfur dioxide adsorption process provided in an embodiment of the present application;
fig. 2 is a process diagram of an adsorption reactor with the number of 2 provided in the examples of the present application.
Detailed Description
In order to make the technical solutions and advantages of the present application more clear, the following describes the embodiments of the present application in further detail.
The embodiment of the present application provides a sulfur dioxide adsorption process, referring to fig. 1, the process includes:
step 101: and introducing tail gas into the adsorption reactor, and adsorbing sulfur dioxide in the tail gas by using an adsorbent in the adsorption reactor.
The tail gas is generated by a sulfur recovery device, and the tail gas at least comprises sulfur dioxide and oxygen.
When the second reactors are multiple, two adjacent second reactors are connected in series through the first valve. The number of adsorption reactors may be set and changed as necessary, and is not particularly limited in the examples of the present application. For example, the number of second reactors is 1, 2, 3 or 4.
When the number of adsorption reactors is 2, the at least one second reactor comprises: the third reactor and the fourth reactor are connected in series through a first valve; the method comprises the following steps: and introducing tail gas into the third reactor and the fourth reactor, wherein the tail gas firstly enters the third reactor and then enters the fourth reactor.
When the number of adsorption reactors is 3, the at least one second reactor comprises: the third reactor and the fourth reactor are connected in series through a first valve, and the fourth reactor and the fifth reactor are connected in series through a first valve; the method comprises the following steps: and introducing tail gas into the third reactor, the fourth reactor and the fifth reactor, wherein the tail gas sequentially enters the third reactor, the fourth reactor and the fifth reactor.
When the number of adsorption reactors is 4, the at least one second reactor comprises: the system comprises a third reactor, a fourth reactor, a fifth reactor and a sixth reactor, wherein the third reactor and the fourth reactor are connected in series through a first valve; the method comprises the following steps: and introducing tail gas into the third reactor, the fourth reactor, the fifth reactor and the sixth reactor, wherein the tail gas sequentially enters the third reactor, the fourth reactor, the fifth reactor and the sixth reactor.
In the embodiment of the application, the treatment capacity of sulfur dioxide can be improved by increasing the number of the adsorption reactors, and the controllable emission of sulfur dioxide with different concentrations is realized.
In the embodiment of the application, the adsorption reactor is filled with an adsorbent, and the adsorbent can adsorb sulfur dioxide. The type of sulfur dioxide adsorbed by the adsorbent is chemical adsorption, namely, under the action of the adsorbent, sulfur dioxide is converted into sulfate and fixed on the adsorbent. The adsorption process can be represented by the following reaction formula:
MxO+SO2+1/2O2→MxSO4
the adsorbent may be set and modified as needed, and is not particularly limited in the embodiments of the present application. For example, the adsorbent is at least one of a CeCuLiAl mixed oxide, a FeZnNaAl mixed oxide, and a CrNiNaAl mixed oxide.
The introduced tail gas can be the tail gas output from the sulfur recovery device and burned by the incinerator, and can also be the tail gas after heat is recovered by the waste heat boiler. In the embodiments of the present application, this is not particularly limited. The space velocity of the introduced tail gas can be set and changed according to the requirement, and is not particularly limited in the embodiment of the present application. For example, the space velocity of the tail gas is 1000-5000 h-1. The temperature of the exhaust gas may be set and changed as needed, and is not particularly limited in the embodiment of the present application. For example, the temperature of the exhaust gas is 250 to 600 ℃.
Step 102: and introducing a regeneration gas with a first preset temperature into the regeneration reactor, and regenerating the adsorbent in the regeneration reactor through the reducing gas in the regeneration gas.
The regeneration reactor comprises a first reactor, and the first reactor is connected with a first second reactor and a last second reactor in series sequence in at least one second reactor in series through a second valve.
When the number of adsorption reactors is 2, that is, at least one second reactor comprises: and when the reactor is a third reactor and a fourth reactor, the first reactor, the third reactor and the fourth reactor are connected in series through a second valve.
When the number of adsorption reactors is 3, that is, at least one second reactor comprises: and when the reactor is a third reactor, a fourth reactor and a fifth reactor, the first reactor, the third reactor and the fifth reactor are connected in series through a second valve.
When the number of adsorption reactors is 4, that is, at least one second reactor comprises: and when the reactor is a third reactor, a fourth reactor, a fifth reactor and a sixth reactor, the first reactor, the third reactor and the sixth reactor are connected in series through a second valve.
In this application embodiment, through establishing ties first reactor and at least one second reactor, reached every reactor and all can regard as adsorption reactor to adsorb sulfur dioxide, also can regard as regeneration reactor to carry out regenerated effect simultaneously to the realization is to the incessant absorption of sulfur dioxide, has improved tail gas treatment efficiency.
In the embodiment of the present application, the regeneration gas includes a reducing gas and may further include an inert gas.
In a possible implementation, when the regenerating gas comprises a reducing gas, the step is: and introducing reducing gas into the regeneration reactor, and regenerating the adsorbent in the regeneration reactor by the reducing gas.
In another possible implementation, when the regeneration gas includes a reducing gas and an inert gas, the step is: introducing inert gas into the regeneration reactor, and removing residual tail gas in the regeneration reactor through the inert gas; and introducing a reducing gas into the regeneration reactor, and regenerating the adsorbent by using the reducing gas.
In the implementation mode, the inert gas is firstly introduced, and the residual tail gas in the regeneration reactor is removed through the inert gas, so that the regeneration reactor is kept in an inert gas environment, the regeneration process of the adsorbent is facilitated, and the safety in the regeneration process of the adsorbent is ensured.
In the step, the reducing gas and the absorbent absorbing sulfur dioxide are subjected to oxidation-reduction reaction to generate sulfur-containing gas after the reaction. The sorbent regeneration process can be represented by the following equation:
MxSO4+H2→MxO+SO2+H2O
the sulfur-containing gas includes sulfur dioxide and may also include hydrogen sulfide.
The reducing gas may be set and modified as needed, and this is not particularly limited in the embodiments of the present application. For example, the reducing gas is at least one of hydrogen, methane, and carbon monoxide. The space velocity of the introduced reducing gas may be set and changed as necessary, and is not particularly limited in the examples of the present application. For example, the space velocity of the reducing gas is 10 to 1000h-1. The source of the reducing gas may be set and changed as needed, and is not particularly limited in the examples of the present application. For example, the reducing gas is from the outlet of the absorption column of the gas generator or the hydrogenation reduction absorber.
The first preset temperature may be set and changed as needed, and is not particularly limited in the embodiment of the present application. For example, the first predetermined temperature is 250 to 600 ℃, that is, the temperature of the regeneration gas is 250 to 600 ℃.
In addition, the reducing gas can be introduced through the gas conveying pipeline in the step, and when the concentration of the reducing gas is insufficient, the reducing gas can be supplemented in time through the gas conveying pipeline, so that the requirement of the regeneration reactor is met.
It should be noted that steps 101 and 102 are not in sequence, and steps 101 and 102 may be performed simultaneously when performing sulfur dioxide adsorption.
Step 103: detecting the concentration of sulfur dioxide at the outlet of the adsorption reactor, and detecting the concentration of sulfur-containing gas at the outlet of the regeneration reactor.
The sulfur-containing gas at the outlet of the regeneration reactor is produced by reacting a reducing gas with an adsorbent.
In one possible implementation, a sampling port may be provided at the outlet of the adsorption reactor, where sulfur dioxide is collected and then the concentration of sulfur dioxide is detected. In another possible implementation, a sulfur dioxide concentration detector may also be provided at the outlet of the adsorption reactor, by which the concentration of sulfur dioxide at the outlet of the adsorption reactor is detected. In the embodiments of the present application, this is not particularly limited.
In one possible implementation, a sampling port may be provided at the outlet of the regeneration reactor, at which the sulfur-containing gas is collected, and then the concentration of the sulfur-containing gas is detected. In another possible implementation, a concentration detector may also be provided at the outlet of the regeneration reactor, by which the concentration of the sulfur-containing gas at the outlet of the adsorption reactor is detected. In the embodiments of the present application, this is not particularly limited.
It should be noted that, at the beginning of the adsorption process, sulfur dioxide is completely adsorbed by the adsorbent, and therefore, almost no sulfur dioxide is detected at the outlet of the adsorption reactor. And with the saturation of the adsorbent, the capacity of the adsorbent for adsorbing sulfur dioxide is poorer and poorer, and the concentration of the sulfur dioxide at the outlet of the adsorption reactor is gradually increased. And the absorbent absorbing sulfur dioxide reacts with the reducing gas to generate sulfur-containing gas at the beginning of the regeneration process, so that the concentration of the sulfur-containing gas at the outlet of the regeneration reactor is higher, and the absorbent is gradually regenerated along with the reaction, namely the absorbent absorbing sulfur dioxide is gradually reduced, and the concentration of the generated sulfur-containing gas is also gradually reduced.
Step 104: and when the concentration of the sulfur dioxide at the outlet of the adsorption reactor does not reach a first preset concentration, discharging the tail gas from which the sulfur dioxide is removed.
When the concentration of the sulfur dioxide at the outlet of the adsorption reactor does not reach the first preset concentration, the adsorbent is not saturated, and before the saturation, the tail gas from which the sulfur dioxide is removed can be conveyed to a chimney through a tail gas conveying pipeline and is discharged through the chimney. And when the concentration of the sulfur dioxide at the outlet of the adsorption reactor reaches or even exceeds the first preset concentration, the adsorbent is basically saturated, and the adsorption process is finished.
In a possible implementation mode, the temperature of the tail gas after sulfur dioxide removal is higher, the tail gas and the regeneration gas can be subjected to heat exchange, the heat of the tail gas is fully utilized to heat the regeneration gas, the heat of the tail gas is recovered, and therefore energy consumption is saved. Accordingly, step 102 may be:
exchanging heat between the tail gas from which the sulfur dioxide is removed and the regeneration gas which is not introduced into the regeneration reactor;
if the temperature of the regenerated gas after heat exchange does not reach a first preset temperature, heating the regenerated gas to the first preset temperature through an electric heater or an online furnace;
and introducing a regeneration gas with a first preset temperature into the regeneration reactor.
The tail gas after heat exchange and sulfur dioxide removal can be conveyed to a chimney through a tail gas conveying pipeline and then discharged through the chimney. Wherein, before the tail gas after sulfur dioxide is removed through chimney discharge, can also detect through sulfur dioxide concentration detector, confirm whether the concentration of sulfur dioxide in this tail gas is up to standard, further guaranteed sulfur dioxide's up to standard emission.
Step 105: when the concentration of the sulfur-containing gas at the outlet of the regeneration reactor is lower than a second preset concentration, selecting a second reactor from at least one second reactor as a regeneration reactor, taking the rest second reactors of the first reactor and the at least one second reactor as adsorption reactors, introducing tail gas into the adsorption reactors, adsorbing sulfur dioxide in the tail gas through an adsorbent in the adsorption reactors, introducing regeneration gas with a first preset temperature into the regeneration reactors, and regenerating the adsorbent in the regeneration reactors through reducing gas in the regeneration gas until each second reactor is used as a regeneration reactor for regeneration.
When the concentration of the sulfur-containing gas at the outlet of the regeneration reactor is lower than the second predetermined concentration, it is indicated that the regeneration process is substantially complete. The regeneration process is performed in a shorter time and faster speed than the adsorption process, and therefore, in one possible implementation, the step may be performed when the regeneration process is completed, that is, the first second reactor in the series sequence is selected as the regeneration reactor, the first reactor and the remaining second reactors are selected as the adsorption reactors, and then the step 101-. When the regeneration of the first second reactor in the series sequence is completed and the adsorption of the first reactor and the remaining second reactors are completed, the second reactor in the series sequence is selected as the regeneration reactor, the first reactor and the remaining second reactors are selected as the adsorption reactors, and then step 101-. And so on until the last second reactor in the series sequence is used as a regeneration reactor, the first reactor and the remaining second reactors are used as adsorption reactors, and then step 101-104 are performed. After step 104 is performed, step 106 is performed.
In another possible implementation, step 105 may be performed again when the regeneration process is completed and the adsorption process is completed. In the embodiments of the present application, this is not particularly limited.
In one possible implementation, the inert gas may be continuously introduced into the regeneration reactor and the introduction of the reducing gas into the regeneration reactor may be stopped before the regeneration process is completed and step 105 is performed.
In this implementation, when regeneration process was accomplished, continue to let in inert gas, blow out the reducing gas in the regeneration reactor through this inert gas to follow-up when regarding this regeneration reactor as the adsorption reactor, can directly let in tail gas, avoid remaining reducing gas to influence going on of adsorption process.
In one possible implementation, when the sorbent regeneration is performed in the regeneration reactor to produce the sulfur-containing gas, the sulfur-containing gas may be directly transported back to the main burner, the primary claus reactor or the secondary claus reactor in the sulfur recovery unit through the transport line.
In another possible implementation manner, an oxygen concentration detector and a reducing gas concentration detector are arranged on the conveying pipeline, the concentration of oxygen in the sulfur-containing gas is detected through the oxygen concentration detector, the concentration of the reducing gas in the sulfur-containing gas is detected through the reducing gas concentration detector, and when the concentration of oxygen in the sulfur-containing gas is lower than a third preset concentration and the concentration of the reducing gas in the sulfur-containing gas is lower than a fourth preset concentration, the sulfur-containing gas is conveyed back to a main combustion furnace, a first-stage claus reactor or a second-stage claus reactor in the sulfur recovery device through the conveying pipeline.
In this implementation, through setting up oxygen concentration detector and reducing gas concentration detector, can prevent that excessive oxygen and reducing gas from taking place the reaction in the sour gas, cause the explosion, lead to the incident, protection staff and equipment safety.
The first preset concentration and the second preset concentration may be set and changed as needed, and this is not particularly limited in the embodiment of the present application. For example, the first predetermined concentration is 50mg/m3、100mg/m3Or 200mg/m3And the second preset concentration is 0. The third preset concentration and the fourth preset concentration may be set and changed as needed, and this is not particularly limited in the embodiment of the present application.
In a possible implementation, when the number of adsorption reactors is 2, i.e. at least one second reactor comprises: in the case of the third reactor and the fourth reactor, the step of selecting one of the at least one second reactor as a regeneration reactor and using the remaining second reactor of the first reactor and the at least one second reactor as an adsorption reactor may comprise: the third reactor was used as a regeneration reactor, and the first reactor and the fourth reactor were used as adsorption reactors.
And when the regeneration of the third reactor is finished and the adsorption of the first reactor and the fourth reactor is finished, taking the fourth reactor as a regeneration reactor and taking the first reactor and the third reactor as adsorption reactors. When the regeneration of the fourth reactor is completed and the adsorption of the first reactor and the third reactor is completed, step 106 is performed.
When the number of adsorption reactors is 3, that is, at least one second reactor comprises: in the case of the third reactor, the fourth reactor and the fifth reactor, the step of selecting one second reactor from the at least one second reactor as a regeneration reactor and using the remaining second reactors of the first reactor and the at least one second reactor as adsorption reactors may be: the third reactor was used as a regeneration reactor, and the first, fourth and fifth reactors were used as adsorption reactors.
When the regeneration of the third reactor is finished and the adsorption of the first reactor, the fourth reactor and the fifth reactor is finished, taking the fourth reactor as a regeneration reactor and taking the first reactor, the third reactor and the fifth reactor as adsorption reactors; and when the regeneration of the fourth reactor is finished and the adsorption of the first reactor, the third reactor and the fifth reactor is finished, taking the fifth reactor as a regeneration reactor and taking the first reactor, the third reactor and the fourth reactor as adsorption reactors. When the regeneration of the fifth reactor is completed and the adsorption of the first reactor, the third reactor and the fourth reactor is completed, step 106 is performed.
When the number of adsorption reactors is 4, that is, at least one second reactor comprises: the third reactor, the fourth reactor, the fifth reactor and the sixth reactor, wherein one of the at least one second reactor is selected as a regeneration reactor, and the step of using the remaining second reactor of the first reactor and the at least one second reactor as an adsorption reactor may be: the third reactor was used as a regeneration reactor, and the first reactor, the fourth reactor, the fifth reactor and the sixth reactor were used as adsorption reactors.
When the regeneration of the third reactor is finished and the adsorption of the first reactor, the fourth reactor, the fifth reactor and the sixth reactor is finished, taking the fourth reactor as a regeneration reactor and taking the first reactor, the third reactor, the fifth reactor and the sixth reactor as adsorption reactors; when the regeneration of the fourth reactor is finished and the adsorption of the first reactor, the third reactor, the fifth reactor and the sixth reactor is finished, taking the fifth reactor as a regeneration reactor and taking the first reactor, the third reactor, the fourth reactor and the sixth reactor as adsorption reactors; and when the fifth reactor is regenerated, the first reactor, the third reactor, the fourth reactor and the sixth reactor are taken as adsorption reactors to complete adsorption, the sixth reactor is taken as a regeneration reactor, and the first reactor, the third reactor, the fourth reactor and the fifth reactor are taken as adsorption reactors. When the regeneration of the sixth reactor is completed and the adsorption of the first reactor, the third reactor, the fourth reactor and the fifth reactor is completed, step 106 is performed.
Step 106: the method comprises the steps of taking a first reactor as a regeneration reactor, taking at least one second reactor as an adsorption reactor, introducing tail gas into the adsorption reactor, adsorbing sulfur dioxide in the tail gas through an adsorbent in the adsorption reactor, introducing a regeneration gas with a first preset temperature into the regeneration reactor, and regenerating the adsorbent in the regeneration reactor through a reducing gas in the regeneration gas.
In this application embodiment, can realize the absorption to sulfur dioxide in the tail gas through the adsorption reactor, can realize the regeneration of adsorbent through the regeneration reactor. The regeneration of the adsorbent can be realized when the adsorption reactor is saturated in the follow-up adsorption, and the adsorption can be continuously carried out after the regeneration of the regeneration reactor is finished, so that the uninterrupted adsorption of sulfur dioxide in the tail gas is realized, the reaction of gas and solid is realized no matter in the regeneration reactor or the adsorption reactor, the investment and operation cost is low, and no extra three wastes are generated. In addition, in the related technology, the sulfur recovery device is in the shutdown stage, the concentration of the generated sulfur dioxide is high, and the pollution is serious. And through the process that this application embodiment provided, can adsorb the sulfur dioxide that sulfur recovery unit start-stop stage produced, avoid a large amount of sulfur dioxide to discharge in the environment, cause the pollution to the environment.
The sulfur dioxide adsorption process provided by the embodiment of the application realizes the adsorption of sulfur dioxide in tail gas and the regeneration of the adsorbent through the first reactor and the at least one second reactor, and the adsorption reactor and the regeneration reactor can be exchanged according to the adsorption condition and the regeneration condition of the adsorbent, so that the regeneration while adsorption is realized.
The technical solution of the present application will be described in detail by specific examples below.
Example 1
This example will be described by taking the number of adsorption reactors as 1.
Step 1: introducing the tail gas into an adsorption reactor, adsorbing sulfur dioxide in the tail gas by using a FeZnNaAl mixed oxide adsorbent in the adsorption reactor, introducing a regeneration gas into a regeneration reactor, and regenerating the adsorbent in the regeneration reactor by using hydrogen in the regeneration reactor. Wherein the tail gas is sulfurThe flow rate of the tail gas after incineration of the sulfur recovery device is 30000m3Per hour, the sulfur dioxide concentration is 300mg/m3. The regeneration gas comprises 1% hydrogen and 99% nitrogen. Wherein the bed temperature of the adsorption reactor and the regeneration reactor is 250 ℃. The regeneration reactor comprises reactor R1 and the adsorption reactor comprises reactor R2.
Step 2: detecting the concentration of sulfur dioxide at the outlet of the adsorption reactor, and detecting the concentration of sulfur-containing gas at the outlet of the regeneration reactor.
And step 3: when the concentration of sulfur dioxide at the outlet of the adsorption reactor does not reach 50mg/m3And meanwhile, discharging the tail gas after removing the sulfur dioxide.
And 4, step 4: when no sulfur-containing gas is detected at the outlet of the regeneration reactor, taking the reactor R2 as the regeneration reactor, taking the reactor R1 as the adsorption reactor, introducing the tail gas into the adsorption reactor, adsorbing sulfur dioxide in the tail gas by using a FeZnNaAl mixed oxide adsorbent in the adsorption reactor, introducing a regeneration gas into the regeneration reactor, and regenerating the adsorbent in the regeneration reactor by using hydrogen in the regeneration reactor.
After each reactor completes one regeneration, one adsorption regeneration period is considered to be completed, and then the next period is entered, that is, step 5 is executed.
And 5: taking the reactor R1 as an adsorption reactor, taking the reactor R2 as an adsorption reactor, introducing the tail gas into the adsorption reactor, adsorbing sulfur dioxide in the tail gas by a FeZnNaAl mixed oxide adsorbent in the adsorption reactor, introducing a regeneration gas into the regeneration reactor, and regenerating the adsorbent in the regeneration reactor by hydrogen in the regeneration reactor.
Example 2
This example will be described by taking the number of adsorption reactors as 2.
Step 1: introducing the tail gas into an adsorption reactor, adsorbing sulfur dioxide in the tail gas by a CeCuLiAl mixed oxide adsorbent in the adsorption reactor, introducing a regeneration gas into a regeneration reactor, and introducing hydrogen in the regeneration reactorRegenerating the adsorbent. Wherein the tail gas is the tail gas after the incineration of the sulfur recovery device, and the flow rate is 8000m3Per hour, the sulfur dioxide concentration is 4000mg/m3. The regeneration gas comprises 15% hydrogen and 85% nitrogen. Wherein the bed temperature of the adsorption reactor and the regeneration reactor is both 500 ℃. The regeneration reactor comprises reactor R1 and the adsorption reactor comprises reactors R2 and R3.
Step 2: detecting the concentration of sulfur dioxide at the outlet of the adsorption reactor, and detecting the concentration of sulfur-containing gas at the outlet of the regeneration reactor.
And step 3: when the concentration of sulfur dioxide at the outlet of the adsorption reactor does not reach 100mg/m3And meanwhile, discharging the tail gas after removing the sulfur dioxide.
And 4, step 4: when no sulfur-containing gas is detected at the outlet of the regeneration reactor, the reactor R2 is used as a regeneration reactor, the reactors R1 and R3 are connected in series to be used as adsorption reactors, the tail gas is introduced into the adsorption reactors, the CeCuLiAl mixed oxide adsorbent in the adsorption reactors adsorbs sulfur dioxide in the tail gas, the regeneration gas is introduced into the regeneration reactors, and the adsorbent in the regeneration reactors is regenerated by the hydrogen in the regeneration reactors until each reactor is used as a regeneration reactor for regeneration.
When the regeneration of the reactor R2 is completed and the adsorption of the reactors R1 and R3 is completed, the regeneration reactor is used as R3, and the adsorption reactors are connected in series by using R1 and R2. After each reactor completes one regeneration, one adsorption regeneration period is considered to be completed, and then the next period is entered, that is, step 5 is executed.
And 5: taking the reactor R1 as an adsorption reactor, taking the reactor R2 as an adsorption reactor, introducing the tail gas into the adsorption reactor, adsorbing sulfur dioxide in the tail gas by a CeCuLiAl mixed oxide adsorbent in the adsorption reactor, introducing a regeneration gas into the regeneration reactor, and regenerating the adsorbent in the regeneration reactor by hydrogen in the regeneration reactor.
Referring to fig. 2, reactor R1 in fig. 2 is a regeneration reactor, reactors R2 and R3 are connected in series to serve as adsorption reactors, and tail gas enters reactor R2 through valve V4, and enters reactor R3 through valve V6 from the outlet of reactor R2. Sulfur dioxide in the tail gas was adsorbed by a CeCuLiAl mixed oxide adsorbent in reactors R2 and R3. Meanwhile, a valve V13 is opened to convey hydrogen through a hydrogen conveying pipeline, the hydrogen and nitrogen are mixed and then exchange heat with tail gas after sulfur dioxide removal through a heat exchanger E4, the hydrogen and nitrogen after heat exchange enter an electric heater E1 to be heated, and when the temperature is heated to 500 ℃, the hydrogen and nitrogen enter a reactor R1 through a valve H1.
In reactor R1, the hydrogen reacts with the sorbent having absorbed sulfur dioxide to produce a sulfur-containing gas which can be fed to the primary burner, primary claus reactor or secondary claus reactor of the sulfur recovery unit via valve V10. The oxygen concentration and the reducing gas concentration in the sulfur-containing gas may be detected by an oxygen concentration detector E2 and a reducing gas concentration detector E3, respectively, before being fed to the main combustion furnace, the primary claus reactor, or the secondary claus reactor in the sulfur recovery apparatus. The concentration of sulfur dioxide at the outlet of the reactor R3 was measured through a sampling port Q6, and the concentration of sulfur-containing gas was measured through a sampling port Q2. When the concentration of sulfur dioxide at the outlet of the reactor R3 does not reach 100mg/m3During the process, the tail gas from which the sulfur dioxide is removed exchanges heat with hydrogen and nitrogen through a valve V8, the tail gas from which the sulfur dioxide is removed after heat exchange is conveyed to a chimney, and the tail gas is discharged through the chimney.
When no sulfur-containing gas was detected at the outlet of the reactor R1, the reactor R2 was used as a regeneration reactor, and the reactors R1 and R3 were connected in series via a valve V9 and used as adsorption reactors. The tail gas firstly enters the reactor R3 through a valve V7, and is output from the outlet of the reactor R3 to enter the reactor R1 through a valve V9. Sulfur dioxide in the tail gas is adsorbed by the CeCuLiAl mixed oxide adsorbent in the reactors R1 and R3. At the same time, valve H1 was closed, valve H2 was opened, and hydrogen and nitrogen were fed into reactor R2 through valve H2. In reactor R2, the hydrogen reacts with the sorbent having absorbed sulfur dioxide to produce a sulfur-containing gas which can be fed to the primary burner, primary Claus reactor or secondary Claus reaction in the sulfur recovery unit via valve V11In the device. The oxygen concentration and the reducing gas concentration in the sulfur-containing gas may be detected by an oxygen concentration detector E2 and a reducing gas concentration detector E3, respectively, before being fed to the main combustion furnace, the primary claus reactor, or the secondary claus reactor in the sulfur recovery apparatus. The concentration of sulfur dioxide at the outlet of the reactor R1 was measured through a sampling port Q2, and the concentration of sulfur-containing gas was measured through a sampling port Q4. When the concentration of sulfur dioxide at the outlet of the reactor R1 does not reach 100mg/m3During the process, the tail gas from which the sulfur dioxide is removed exchanges heat with hydrogen and nitrogen through a valve V2, the tail gas from which the sulfur dioxide is removed after heat exchange is conveyed to a chimney, and the tail gas is discharged through the chimney.
When no sulfur-containing gas was detected at the outlet of the reactor R2, the reactor R3 was used as a regeneration reactor, and the reactors R1 and R2 were connected in series via a valve V3 and used as adsorption reactors. The tail gas firstly enters the reactor R1 through a valve V1, and is output from the outlet of the reactor R1 to enter the reactor R2 through a valve V1. Sulfur dioxide in the tail gas is adsorbed by the CeCuLiAl mixed oxide adsorbent in the reactors R1 and R2. At the same time, valve H2 was closed, valve H3 was opened, and hydrogen and nitrogen were fed into reactor R3 through valve H3. In reactor R3, the hydrogen reacts with the sorbent having absorbed sulfur dioxide to produce a sulfur-containing gas which can be fed to the primary burner, primary claus reactor or secondary claus reactor of the sulfur recovery unit via valve V12. The oxygen concentration and the reducing gas concentration in the sulfur-containing gas may be detected by an oxygen concentration detector E2 and a reducing gas concentration detector E3, respectively, before being fed to the main combustion furnace, the primary claus reactor, or the secondary claus reactor in the sulfur recovery apparatus. The concentration of the sulfur-containing gas at the outlet of the reactor R3 was detected through a sampling port Q6, and the concentration of sulfur dioxide at the outlet of the reactor R2 was detected through a sampling port Q4. When the concentration of sulfur dioxide at the outlet of the reactor R2 does not reach 100mg/m3During the process, the tail gas from which the sulfur dioxide is removed exchanges heat with hydrogen and nitrogen through a valve V5, the tail gas from which the sulfur dioxide is removed after heat exchange is conveyed to a chimney, and the tail gas is discharged through the chimney.
After each reactor completes one regeneration, one adsorption regeneration period is considered to be completed, and then the next period is entered, namely R1 is used as a regeneration reactor again, R2 and R3 are connected in series to be used as adsorption reactors, and the subsequent steps are carried out.
In a possible realization, the inlet of each reactor is also provided with sampling ports, respectively Q1, Q2 and Q3. Sampling at the sampling port allows the concentration of the gas entering the reactor to be detected. For example, when the reactor R1 is used as a regeneration reactor, the concentration of the reducing gas entering the reactor R1 can be detected through the sampling port Q1; when the reactor R1 is used as an adsorption reactor, the concentration of sulfur dioxide entering the reactor R1 can be detected through the sampling port Q1.
Example 3
This example is illustrated with the number of adsorption reactors being 4.
Step 1: introducing the tail gas into an adsorption reactor, adsorbing sulfur dioxide in the tail gas by a CrNiNaAl mixed oxide adsorbent in the adsorption reactor, introducing a regeneration gas into a regeneration reactor, and regenerating the adsorbent in the regeneration reactor by hydrogen in the regeneration reactor. Wherein the tail gas is the tail gas after the incineration of the sulfur recovery device, and the flow rate is 5000m3H, the sulfur dioxide concentration is 75mg/m3. The regeneration gas comprises 90% hydrogen and 10% nitrogen. Wherein the bed temperature of the adsorption reactor and the regeneration reactor is 600 ℃. The regeneration reactor comprises reactor R1 and the adsorption reactor comprises reactors R2, R3, R4 and R5.
Step 2: detecting the concentration of sulfur dioxide at the outlet of the adsorption reactor, and detecting the concentration of sulfur-containing gas at the outlet of the regeneration reactor.
And step 3: when the concentration of sulfur dioxide at the outlet of the adsorption reactor does not reach 200mg/m3And meanwhile, discharging the tail gas after removing the sulfur dioxide.
And 4, step 4: when no sulfur-containing gas is detected at the outlet of the regeneration reactor, taking the reactor R2 as a regeneration reactor, serially connecting the reactors R1, R3, R4 and R5 as adsorption reactors, introducing the tail gas into the adsorption reactors, adsorbing sulfur dioxide in the tail gas by a CrNiNaAl mixed oxide adsorbent in the adsorption reactors, introducing regeneration gas into the regeneration reactors, and regenerating the adsorbent in the regeneration reactors by hydrogen in the regeneration reactors until each reactor is taken as a regeneration reactor for regeneration.
When the regeneration of the reactor R2 is completed and the adsorption of the reactors R1, R3, R4 and R5 is completed, the reactor R3 is used as a regeneration reactor, and the reactors R1, R2, R4 and R5 are connected in series to be used as adsorption reactors. When the regeneration of the reactor R3 is completed and the adsorption of the reactors R1, R2, R4 and R5 is completed, the reactor R4 is used as a regeneration reactor, and the reactors R1, R2, R3 and R5 are connected in series to be used as adsorption reactors. When the regeneration of the reactor R4 is completed and the adsorption of the reactors R1, R2, R3 and R5 is completed, the reactor R5 is used as a regeneration reactor, and the reactors R1, R2, R3 and R4 are connected in series to be used as adsorption reactors. After each reactor completes one regeneration, one adsorption regeneration period is considered to be completed, and then the next period is entered, that is, step 5 is executed.
And 5: taking the reactor R1 as an adsorption reactor, taking the reactor R2 as an adsorption reactor, introducing the tail gas into the adsorption reactor, adsorbing sulfur dioxide in the tail gas by a CrNiNaAl mixed oxide adsorbent in the adsorption reactor, introducing a regeneration gas into the regeneration reactor, and regenerating the adsorbent in the regeneration reactor by hydrogen in the regeneration reactor.
As can be seen from the above examples: the process can interchange the adsorption reactor and the regeneration reactor according to the regeneration condition of the adsorption condition of the adsorbent, realizes the regeneration while adsorbing, and has the advantages of low energy consumption, low investment and low operation cost.
The above description is only for facilitating the understanding of the technical solutions of the present application by those skilled in the art, and is not intended to limit the present application. Any modification, equivalent replacement, improvement and the like made within the spirit and principle of the present application shall be included in the protection scope of the present application.

Claims (10)

1. A sulfur dioxide adsorption process, characterized in that the process comprises:
introducing tail gas into an adsorption reactor, adsorbing sulfur dioxide in the tail gas through an adsorbent in the adsorption reactor, introducing a regeneration gas with a first preset temperature into a regeneration reactor, and regenerating the adsorbent in the regeneration reactor through a reducing gas in the regeneration gas; the regeneration reactor comprises a first reactor, the adsorption reactor comprises at least one second reactor, when the number of the second reactors is multiple, two adjacent second reactors are connected in series through a first valve, and the first reactor is connected with a first second reactor and a last second reactor in the series sequence in the at least one second reactor through second valves;
detecting the concentration of sulfur dioxide at the outlet of the adsorption reactor and the concentration of sulfur-containing gas at the outlet of the regeneration reactor, wherein the sulfur-containing gas at the outlet of the regeneration reactor is generated by the reaction of the reducing gas and the adsorbent;
when the concentration of sulfur dioxide at the outlet of the adsorption reactor does not reach a first preset concentration, discharging tail gas from which the sulfur dioxide is removed;
when the concentration of the sulfur-containing gas at the outlet of the regeneration reactor is lower than a second preset concentration, selecting a second reactor from the at least one second reactor as a regeneration reactor, using the remaining second reactors of the first reactor and the at least one second reactor as adsorption reactors, executing the step of introducing tail gas into the adsorption reactors, adsorbing sulfur dioxide in the tail gas through an adsorbent in the adsorption reactors, introducing regeneration gas at a first preset temperature into the regeneration reactors, and regenerating the adsorbent in the regeneration reactors through reducing gas in the regeneration gas until each second reactor is used as a regeneration reactor for regeneration;
and taking the first reactor as a regeneration reactor, taking the at least one second reactor as an adsorption reactor, executing the steps of introducing tail gas into the adsorption reactor, adsorbing sulfur dioxide in the tail gas through an adsorbent in the adsorption reactor, introducing a regeneration gas with a first preset temperature into the regeneration reactor, and regenerating the adsorbent in the regeneration reactor through a reducing gas in the regeneration gas.
2. The process according to claim 1, characterized in that said at least one second reactor comprises: a third reactor and a fourth reactor, the third reactor and the fourth reactor being connected in series through the first valve, the first reactor being connected in series with the third reactor and the fourth reactor through the second valve;
the step of introducing tail gas into the adsorption reactor comprises the following steps:
introducing the tail gas into the third reactor and the fourth reactor, wherein the tail gas firstly enters the third reactor and then enters the fourth reactor;
the selecting one of the at least one second reactor as a regeneration reactor, and using the remaining second reactor of the first reactor and the at least one second reactor as an adsorption reactor, includes:
the third reactor is used as a regeneration reactor, and the first reactor and the fourth reactor are used as adsorption reactors.
3. The process of claim 1, wherein the regeneration gas further comprises: an inert gas;
the method comprises the following steps of introducing a regeneration gas with a first preset temperature into a regeneration reactor, and regenerating an adsorbent in the regeneration reactor through a reducing gas in the regeneration gas, wherein the regeneration gas comprises:
introducing the inert gas into the regeneration reactor, and removing residual tail gas in the regeneration reactor through the inert gas;
and introducing the reducing gas into the regeneration reactor, and regenerating the adsorbent in the regeneration reactor by using the reducing gas.
4. The process according to claim 3, wherein when the concentration of the sulfur-containing gas at the outlet of the regeneration reactor is lower than a second preset concentration, selecting one of the at least one second reactor as the regeneration reactor, and before using the remaining second reactors of the first reactor and the at least one second reactor as adsorption reactors, the process further comprises:
and continuously introducing the inert gas into the regeneration reactor, and stopping introducing the reducing gas into the regeneration reactor.
5. The process according to claim 3, characterized in that the concentration of the reducing gas in the regenerating gas is between 1% and 99%.
6. The process of claim 1, wherein the introducing of the regeneration gas into the regeneration reactor at the first predetermined temperature comprises:
exchanging heat between the tail gas from which the sulfur dioxide is removed and the regeneration gas which is not introduced into the regeneration reactor;
if the temperature of the regenerated gas after heat exchange does not reach the first preset temperature, heating the regenerated gas to the first preset temperature through an electric heater or an online furnace;
and introducing the regeneration gas with the first preset temperature into the regeneration reactor.
7. The process of claim 1, further comprising:
and conveying the sulfur-containing gas back to a main combustion furnace, a primary Claus reactor or a secondary Claus reactor in the sulfur recovery device through a conveying pipeline.
8. The process of claim 7, wherein the transfer line is provided with an oxygen concentration detector and a reducing gas concentration detector;
before the sulfur-containing gas is transported back to a main combustion furnace, a primary claus reactor or a secondary claus reactor in a sulfur recovery plant through a transport line, the process further comprises:
detecting the concentration of oxygen in the sulfur-containing gas by the oxygen concentration detector;
detecting the concentration of the reducing gas in the sulfur-containing gas by the reducing gas concentration detector;
when the concentration of oxygen in the sulfur-containing gas is lower than a third preset concentration and the concentration of reducing gas in the sulfur-containing gas is lower than a fourth preset concentration, the step of conveying the sulfur-containing gas back to a main combustion furnace, a primary claus reactor or a secondary claus reactor in a sulfur recovery device through a conveying line is performed.
9. The process according to claim 1, wherein the number of the second reactors is 1 to 4.
10. The process of claim 1, wherein the reducing gas comprises: at least one of hydrogen, methane and carbon monoxide.
CN202010456586.8A 2020-05-26 2020-05-26 Sulfur dioxide adsorption process Pending CN113713558A (en)

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1363164A (en) * 1971-02-19 1974-08-14 Shell Int Research Process an plant for removing sulphur oxides from gases
NL7505940A (en) * 1975-05-21 1976-11-23 Shell Int Research Sulphur dioxide removal from flue gas - and conversion to sulphur by reducing with gas contg. sulphur cpds.
WO2001052974A1 (en) * 2000-01-17 2001-07-26 Stork Engineers & Contractors B.V. Method for removing sulfur compounds from gas mixtures
CN103480252A (en) * 2012-06-13 2014-01-01 中国石油天然气股份有限公司 Hydrogen sulfide-containing acid gas treatment method
CN104209084A (en) * 2013-06-05 2014-12-17 中国石油天然气股份有限公司 Claus tail gas SO2 sorbent and preparation and use thereof
CN109351183A (en) * 2018-11-27 2019-02-19 中国石油大学(北京) A kind of regeneration fume from catalytic cracking dry desulfurization dedusting technique

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1363164A (en) * 1971-02-19 1974-08-14 Shell Int Research Process an plant for removing sulphur oxides from gases
NL7505940A (en) * 1975-05-21 1976-11-23 Shell Int Research Sulphur dioxide removal from flue gas - and conversion to sulphur by reducing with gas contg. sulphur cpds.
WO2001052974A1 (en) * 2000-01-17 2001-07-26 Stork Engineers & Contractors B.V. Method for removing sulfur compounds from gas mixtures
CN103480252A (en) * 2012-06-13 2014-01-01 中国石油天然气股份有限公司 Hydrogen sulfide-containing acid gas treatment method
CN104209084A (en) * 2013-06-05 2014-12-17 中国石油天然气股份有限公司 Claus tail gas SO2 sorbent and preparation and use thereof
CN109351183A (en) * 2018-11-27 2019-02-19 中国石油大学(北京) A kind of regeneration fume from catalytic cracking dry desulfurization dedusting technique

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