CN108786441B - Sulfur preparation process by electromigration desulfurization of coke oven flue gas - Google Patents
Sulfur preparation process by electromigration desulfurization of coke oven flue gas Download PDFInfo
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- CN108786441B CN108786441B CN201810556138.8A CN201810556138A CN108786441B CN 108786441 B CN108786441 B CN 108786441B CN 201810556138 A CN201810556138 A CN 201810556138A CN 108786441 B CN108786441 B CN 108786441B
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- C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
- C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
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Abstract
The invention discloses a sulfur preparation process by electromigration desulfurization of coke oven flue gas, belonging to the energy-saving and environment-friendly field of the coking industry. The coke oven flue gas from the coke oven horizontal flue enters a sulfur dioxide electromigration membrane separator to be separated to obtain SO-rich flue gas2Gas and SO removal2Post-processing of flue gas, removal of SO2Heating the flue gas in a heater, feeding the flue gas into an SCR denitration reactor to complete denitration, and recycling waste heat of the denitrated flue gas and then feeding the flue gas into a chimney for discharging; rich in SO2Gas and H-rich from hydrogen sulfide stripping column2S gas is sent into a Claus furnace together to react to generate Claus tail gas containing sulfur steam, the Claus tail gas containing sulfur steam enters a sulfur condenser to be cooled and recover sulfur, the Claus tail gas is divided into 3 parts after being cooled, one part enters a tail gas cooling section of the Claus furnace to be subjected to heat exchange and temperature rise and then enters a hydrogen sulfide analysis tower to serve as H2And the other part of the S desorption tower is dedusted and then enters a sulfur dioxide electromigration membrane separator to be used as the coke oven flue gas electromigration desulfurization carrier gas, and the rest part of the S desorption tower is merged into a coke oven raw gas pipe network. The process designed by the invention can effectively recycle sulfur pollutants in the coke oven smoke.
Description
Technical Field
The invention relates to coke oven flue gas desulfurization and sulfur resource recycling, belongs to the field of energy conservation and environmental protection in the coking industry, and particularly relates to a process for preparing sulfur by performing electromigration desulfurization on coke oven flue gas.
Background
At present, the coke oven flue gas desulfurization and denitrification process operated in China comprises the following steps: the integrated process of semi-dry desulfurization and low-temperature SCR selective catalytic reduction denitration dust removal, the integrated desulfurization and denitration technology (active coke method), the moving bed dry desulfurization and low-temperature SCR denitration technology, the novel catalytic flue gas desulfurization and denitration technology and the ammonia desulfurization and ozone oxidation denitration technology are all the process technologies of firstly desulfurizing and then denitrating, and the overall operation is stable although the process has the same problem in operation.
The method is characterized in that an arrangement mode of firstly desulfurizing and then denitrating is selected, SCR denitration processes can be configured and selected by dry-method and semi-dry-method desulfurization processes, and if enterprises select the wet-method desulfurization processes, the current technology has two schemes: one is that the flue gas temperature is 60-80 ℃ after being treated by the desulfurization device, the flue gas temperature is firstly increased to more than 180 ℃ through the heat exchange device and then enters the flue gas SCR denitration device for treatment, and the scheme is not preferable from the aspect of energy consumption and is also not preferable in economical efficiency. The second scheme is a wet desulfurization process and an ozone oxidation denitration process, and the scheme can meet the arrangement sequence of first desulfurization and then denitration, and can effectively remove SO in the flue gas pollutants2NOx control is within the acceptable range, but no successful operational case report has been found so far.
The selection of the coke oven flue gas desulfurization and denitrification configuration sequence must be careful for enterprises, because the selection relates to whether the desulfurization and denitrification device can continuously and stably operate and whether the emission concentration of flue gas pollutants can stably reach the standard, and the characteristics of the coke oven flue gas are one of the decisive factors.
The SCR denitration and ammonia desulphurization process is selected in a coking plant in Shaanxi, a denitration device cannot continuously and stably operate all the time, and the problem of how to continuously and stably operate the denitration device arranged at the front end of the desulphurization device always troubles enterprises. The problem is mainly that the temperature of the coke oven flue gas is low and is generally below 300 ℃, and when the SCR denitration process is selected, a low-temperature catalyst is generally selected from the economic aspect. Due to the presence of SO in the flue gas2Part of SO being present in the presence of an SCR catalyst2Will be converted into SO3. Ammonia gas and SO at 180-230 deg.C3The reaction is easy to generate ammonium bisulfate. The ammonium bisulfate is extremely easy to deliquesce, the melting point temperature is 147 ℃, and the boiling point is 350 ℃. The material is very sticky and difficult to remove, adheres to the surface of the catalyst, and seriously affects the use efficiency of the catalyst.
Na-method desulfurization (SDA) and medium-low-temperature selective catalytic reduction denitration (SCR) process of Zhanjiang Baojian steel and Baoshan base by rotary spraying methodA technical route; coke oven flue gas of Jingdezhen and Tangshanhuofeng coking company3Oxidation, NH3A method flue gas desulfurization and denitrification integrated process route; low-temperature selective catalytic reduction denitration (SCR) + NH in inner Mongolia Bao steel Qinghua3Wet desulphurization process route, etc. The exploration in these engineerings is through the trial run, purification efficiency is unstable and chimney heat has all appeared and has been equipped with the scheduling problem, especially desulfurization earlier, when carrying out the SCR denitration again, because desulfurization process requires the flue gas temperature lower, denitration process requires the flue gas temperature higher, lead to the flue gas cooling, heat the relapse of process such as intensification, need to cool down the flue gas in order to solve when desulfurization earlier denitration again, the equipment investment that the intensification leads to is big, the problem that the energy consumption is high, need to develop the desulfurization technique under the higher flue gas temperature urgently.
In summary, the coke oven flue gas desulfurization and denitrification process mainly has the following technical problems:
(1) in the existing coke oven flue gas SDA + SCR desulfurization and denitrification process, desulfurization byproducts are solid wastes, so that resource utilization cannot be carried out, and secondary pollution is caused to the environment;
(2) in the existing coke oven flue gas SDA + SCR desulfurization and denitrification process, the desulfurization process is a semi-dry method, the system is frequently blocked, and the operation stability is poor;
(3) in the existing coke oven flue gas carbon-based catalytic desulfurization combined SCR denitration process, although the desulfurization by-product is dilute sulfuric acid with low concentration and sulfur pollutants are recycled, the utilization value is low, and further concentration or mixing with concentrated sulfuric acid is needed. Meanwhile, when the process is used for denitration, the flue gas heating energy consumption is high, so that the investment for desulfurization and denitration is large and the operation cost is high.
Disclosure of Invention
In order to solve the technical problem, the invention discloses a process for preparing sulfur by coke oven flue gas electro-migration desulfurization, which can effectively recycle sulfur pollutants in the coke oven flue gas.
In order to achieve the aim, the invention discloses a sulfur preparation process by electromigration desulfurization of coke oven flue gas, which comprises SO-containing sulfur from a horizontal flue of a coke oven2The coke oven flue gas with NOx enters a sulfur dioxide electromigration film separator to be separated through electromigration to obtain SO-rich2Gas and SO removal2Post-flue gas, said de-SO2The flue gas enters a heater for heating and temperature rise and then is sent into an SCR denitration reactor for denitration, and the flue gas after denitration is sent into a chimney for discharge after waste heat recovery;
said rich in SO2Gas and H-rich from hydrogen sulfide stripping column2The method comprises the following steps of feeding S gases into a combustion section of a Claus furnace together to react to generate Claus tail gas containing sulfur steam, feeding the Claus tail gas containing the sulfur steam into a sulfur condenser to separate liquid sulfur and the Claus tail gas after temperature reduction, feeding one part of the Claus tail gas after temperature reduction into a tail gas cooling section of the Claus furnace, heating the tail gas after heat exchange, feeding the other part of the Claus tail gas after dust removal into a hydrogen sulfide desorption tower to serve as a gas stripping gas source and a heat source, feeding the other part of the Claus tail gas after dust removal into a sulfur dioxide electro-migration membrane separator to serve as a carrier gas for electro-migration desulfurization.
Further, the claus tail gas after the temperature reduction in the sulfur condenser is used for removing tar and sulfur in the claus tail gas through an electric tar precipitator.
Preferably, the electrical tar precipitator is an electrostatic precipitator.
And further, coal gas and air for improving reaction heat are supplemented to a combustion section of the Claus furnace, and the reaction temperature of the combustion section is 1300 ℃.
Furthermore, the sulfur dioxide electromigration membrane separator is provided with a separation SO2The temperature resistance of the gaseous membrane material is more than or equal to 400 ℃ or less than or equal to 200 ℃;
when the temperature resistance of the membrane material is less than or equal to 200 ℃, SO is contained in the horizontal flue of the coke oven2The coke oven flue gas containing NOx enters a sulfur dioxide electromigration membrane separator after heat is recovered by a first waste heat boiler;
when the temperature resistance of the membrane material is more than or equal to 400 ℃, SO is contained in the horizontal flue of the coke oven2And the coke oven flue gas of NOx directly enters the sulfur dioxide electromigration membrane separator.
Further, the SO removal2The flue gas is heated by a heater after exchanging heat with the gas in the heat exchanger, and then is sent into an SCR denitration reactor, and the denitrated flue gasThe gas enters a heat exchanger to be used as and remove SO2The gas of the heat exchange of the back flue gas.
Furthermore, the denitrated flue gas is recycled by the waste heat of the second waste heat boiler and then is discharged out of a chimney.
The beneficial effects of the invention are mainly embodied in the following aspects:
1. the sulfur pollutant separated from the coke oven flue gas by the process designed by the invention is rich in SO2In combination with H removed from the coking process gas2S gas generates sulfur products with high added value in a Claus furnace, and sulfur pollutants in the coke oven smoke are effectively recycled;
2. the sulfur dioxide electrotransport membrane separator in the design process has wide temperature application range, coke oven flue gas can directly enter the sulfur dioxide electrotransport membrane separator for membrane separation of sulfur pollutants without any temperature adjustment, the flue gas temperature reduction in the desulfurization process is small, the flue gas heating energy consumption in the subsequent denitration process is saved, and the desulfurization and denitration cost of the coke oven flue gas is reduced;
3. the sulfur dioxide electromigration membrane separator in the design process of the invention separates and removes SO in the coke oven flue gas2No solid waste or waste liquid is generated, no desulfurizer is needed in the desulfurization process, the desulfurization cost is low, the process control is simple, the operation is convenient, the desulfurization efficiency reaches more than 90 percent, partial NOx in the flue gas can be removed while the electro-migration desulfurization is carried out, and the denitration efficiency is more than 40 percent.
4. The process designed by the invention takes part of Claus tail gas as the gas source for stripping the desorbed rich liquor after the coke oven gas is desulfurized, effectively recycles the waste heat of the part of Claus tail gas, reduces the generation amount of coking wastewater and improves the H content compared with the prior system which adopts steam as the desorption gas source2Recovery of S (SO in tail gas)2And CO2The pH value of the two gases in water is far lower than that of H2S dissolved in water, and the two gases dissolved in water reduce H during gas stripping2S solubility in water, improving desorption effect).
Drawings
FIG. 1 is a process flow diagram of the sulfur production by electromigration desulfurization of coke oven flue gas according to the present invention;
FIG. 2 is a process flow chart of the sulfur production by electromigration desulfurization of coke oven flue gas according to the present invention;
wherein, the parts in fig. 1 and 2 are numbered as follows:
a coke oven 100 (wherein, the coke oven flue gas outlet 110) and a first waste heat boiler 100 a;
a sulfur dioxide electromigration membrane separator 200 (wherein, the first flue gas inlet 210, the first flue gas outlet 220, the carrier gas inlet 230 and the carrier gas outlet 240), a heater 200a, a heat exchanger 200b (the second flue gas inlet 200b-1, the second flue gas outlet 200b-2, the third flue gas inlet 200b-3 and the third flue gas outlet 200 b-4);
a hydrogen sulfide treatment device 300 (wherein, a hydrogen sulfide analysis tower 310 (wherein, a hydrogen sulfide gas outlet 311, a first tail gas inlet 312) and a hydrogen sulfide absorption tower 320);
a Claus furnace 400 (wherein: a combustion section 410, a vaporization cooling section 420, a tail gas cooling section 430 (wherein: a recycled Claus tail gas inlet 440, a recycled Claus tail gas outlet 450));
a sulfur condenser 500, an electrical tar precipitator 500 a;
an SCR denitration reactor 600, a second exhaust-heat boiler 600 a;
coke oven horizontal flues 700 (coke oven combustion chamber outlet section horizontal flue 700a, chimney inlet section horizontal flue 700b, regulating valve 700c), chimney 700 d.
Detailed Description
The invention discloses a sulfur preparation process by electromigration desulfurization of coke oven flue gas, which comprises SO-containing flue gas from a horizontal flue 700 of a coke oven as shown in figures 1 and 22The coke oven flue gas with NOx enters a sulfur dioxide electromigration film separator 200 to be separated by electromigration to obtain SO-rich2Gas and SO removal2Post-flue gas, said de-SO2And the flue gas enters a heater 200a for heating and temperature rise, and then is sent into an SCR denitration reactor 600 for denitration, and the flue gas after denitration is sent into a chimney 700d for discharge after waste heat recovery.
In the sulfur dioxide electromigration membrane separator 200 of the invention, separated SO is placed2A film material of a gas, saidThe temperature resistance of the membrane material is more than or equal to 400 ℃ or less than or equal to 200 ℃;
as shown in figure 1, when the temperature resistance of the membrane material is less than or equal to 200 ℃, SO is contained in the horizontal flue 700 of the coke oven2The coke oven flue gas containing NOx enters a sulfur dioxide electromigration membrane separator 200 after heat is recovered by a first waste heat boiler 100 a;
as shown in figure 2, when the temperature resistance of the membrane material is more than or equal to 400 ℃, SO is contained in the horizontal flue 700 from the coke oven2And NOx directly into the sulfur dioxide electromigration membrane separator 200.
Furthermore, the SO-rich2The gas and the H-rich gas in the hydrogen sulfide stripping tower 310 from the hydrogen sulfide processing apparatus 3002The S gas is sent into the combustion section 410 of the Claus furnace 400 together to react and generate sulfur steam, coal gas and air for improving reaction heat are supplemented to the combustion section 410 of the Claus furnace 400, the reaction temperature of the combustion section 410 is about 1300 ℃, H is H2S gas, SO2The gas, coal gas and air are used for obtaining sulfur under the action of a catalyst; the balance is Claus tail gas, the sulfur steam and the Claus tail gas enter a sulfur condenser 500 to separate liquid sulfur and the Claus tail gas after cooling, preferably, the Claus tail gas after cooling in the sulfur condenser 500 is used for removing tar and sulfur in the Claus tail gas through an electric tar precipitator 500a (preferably an electrostatic precipitator), and then, a part of the Claus tail gas after cooling enters a tail gas cooling section 430 of the Claus furnace 400 to be heated and enters a hydrogen sulfide desorption tower 310 to be used as desorption H2A supplementary gas source and a heat source of S gas, wherein part of the cooled Claus tail gas enters the sulfur dioxide electromigration membrane separator 200 to be used as SO-rich gas2And (3) conveying the gas carrier and a part of the cooled Claus tail gas into a raw gas pipeline.
Preferably, the hydrogen sulfide treatment apparatus 300 includes a hydrogen sulfide analysis tower 310 and a hydrogen sulfide absorption tower 320, wherein the hydrogen sulfide absorption tower 320 contains an absorption liquid, and a saturated liquid after absorbing hydrogen sulfide flows into the hydrogen sulfide analysis tower 310 to re-precipitate hydrogen sulfide gas under the action of a certain temperature and other gases.
Preferably, the claus furnace 400 includes a combustion section 410, a vaporization cooling section 420 and a tail gas cooling section 430, and cooling soft water is additionally provided to the vaporization cooling section 420.
In order to better explain the invention, the following further illustrate the main content of the invention in connection with specific examples, but the content of the invention is not limited to the following examples.
Wherein, in the embodiment of the invention, the smoke gas amount of a coke oven plant of 2 multiplied by 6 meters is about 250000Nm3And h, respectively enabling the coke oven smoke from each combustion chamber to enter a machine and a smoke distributing channel on two sides of coke to be converged and then enter a horizontal flue of the coke oven.
Example 1
As shown in FIG. 1, the SO-containing gas discharged along the coke oven flue gas outlet 110 of the coke oven 100 is adjusted by adjusting the adjusting valve 700c on the horizontal flue 700 of the coke oven2The coke oven flue gas with NOx enters the sulfur dioxide electrotransport membrane separator 200 along the horizontal flue 700a of the outlet section of the coke oven combustion chamber, the first flue gas inlet 210 of the sulfur dioxide electrotransport membrane separator 200, and the separated SO placed in the sulfur dioxide electrotransport membrane separator 200 in the embodiment2The temperature resistance of the membrane material of the gas is less than or equal to 200 ℃, SO that the heat is recovered by the first waste heat boiler 100a and then enters the sulfur dioxide electromigration membrane separator 200 preferentially, and most of SO in the coke oven flue gas2The gas enters the other side of the separation membrane under the action of electromigration to obtain the SO-rich gas2Gas of the rich SO2The gas flows out of a carrier gas outlet 240 of the sulfur dioxide electromigration membrane separator 200 under the action of the part of the Claus tail gas which flows in along the carrier gas inlet 230 of the sulfur dioxide electromigration membrane separator 200 and is cooled and serves as a carrier gas, and the gas and the H-rich tail gas which is discharged along a hydrogen sulfide gas outlet 311 of a hydrogen sulfide desorption tower 3102The S gas is sent into a combustion section 410 of a Claus furnace 400 together, the Claus furnace 400 comprises the combustion section 410, a vaporization cooling section 420 and a tail gas cooling section 430, the tail gas cooling section 430 is also provided with a circulating Claus tail gas inlet 440 and a circulating Claus tail gas outlet 450, the combustion section 410 is supplemented with coal gas and air for improving reaction heat, and the vaporization cooling section 420 is supplemented with cooling soft water; the gas entering the Claus furnace 400 is rich in hydrogen sulfide gas, sulfur dioxide gas and along the gas inlet of the Claus furnace 400The supplemented coal gas and air are subjected to Claus reaction at 1300 ℃ and under the action of a catalyst to obtain high-temperature sulfur steam and Claus tail gas, the high-temperature sulfur steam and the Claus tail gas enter a sulfur condenser 500 to be separated into liquid sulfur and the Claus tail gas after being cooled, a part of the Claus tail gas after being cooled enters a tail gas cooling section 430 along a circulating Claus tail gas inlet 440, is subjected to heat exchange and temperature rise, then flows out of the Claus furnace 400 along a circulating Claus tail gas outlet 450, and enters a hydrogen sulfide desorption tower 310 along a first tail gas inlet 312 arranged at the bottom end of the hydrogen sulfide desorption tower 310 to be used as desorption H2A supplementary gas source and a heat source for the S gas; after a part of the Claus tail gas after being cooled is used for removing tar and sulfur in the Claus tail gas through an electrical tar precipitator 500a, the part of the Claus tail gas is sent to a sulfur dioxide electromigration membrane separator 200 to be used as SO-rich2The carrier gas of the gas and a part of the cooled claus tail gas are sent into the raw gas pipeline (the process flow chart of the embodiment does not show the gas trend, but includes the part).
Referring again to FIG. 1, the sulfur dioxide electromigration membrane separator 200 is further provided with a means for discharging the SO2First flue gas outlet 220 for the post-flue gas, SO removal2The back flue gas enters along a second flue gas inlet 200b-1 on a heat exchanger 200b, exchanges heat with the denitrated flue gas entering the heat exchanger 200b in the heat exchanger 200b, is discharged along a second flue gas outlet 200b-2, enters a heater 200a, is continuously heated and heated, and is sent to an SCR denitration reactor 600, ammonia gas is supplemented into the SCR denitration reactor 600, nitrogen oxides and the ammonia gas generate SCR reaction under the action of a denitration catalyst, and the flue gas after high-temperature denitration enters the heat exchanger 200b along a third flue gas inlet 200b-3 to be used as the flue gas for SO removal2The gas after heat exchange of the flue gas is discharged along the third flue gas outlet 200b-4 and then is sent to the chimney 700d along the horizontal flue 700b at the inlet section of the chimney for discharge.
Through the implementation of the scheme, SO in the coke oven flue gas2Down to 50mg/Nm3NOx to 100mg/Nm3SO in flue gas2The recovery utilization rate reaches 95 percent.
Example 2
As shown in FIG. 2, the adjusting valve on the horizontal flue 700 of the coke oven is adjusted700c discharging SO-containing gas along the coke oven flue gas outlet 110 of the coke oven 1002The coke oven flue gas with NOx enters the sulfur dioxide electrotransport membrane separator 200 along the horizontal flue 700a of the outlet section of the coke oven combustion chamber, the first flue gas inlet 210 of the sulfur dioxide electrotransport membrane separator 200, and the separated SO placed in the sulfur dioxide electrotransport membrane separator 200 in the embodiment2The temperature resistance of the film material of the gas is more than or equal to 400 ℃, SO SO-containing gas from the horizontal flue 700 of the coke oven is preferably adopted2The coke oven flue gas with NOx directly enters the sulfur dioxide electromigration membrane separator 200, and most of SO in the coke oven flue gas2The gas enters the other side of the separation membrane under the action of electromigration to obtain the SO-rich gas2Gas of the rich SO2The gas flows out of a carrier gas outlet 240 of the sulfur dioxide electromigration membrane separator 200 under the action of the part of the Claus tail gas which flows in along the carrier gas inlet 230 of the sulfur dioxide electromigration membrane separator 200 and is cooled and serves as a carrier gas, and the gas and the H-rich tail gas which is discharged along a hydrogen sulfide gas outlet 311 of a hydrogen sulfide desorption tower 3102The S gas is sent into a combustion section 410 of a Claus furnace 400 together, the Claus furnace 400 comprises the combustion section 410, a vaporization cooling section 420 and a tail gas cooling section 430, the tail gas cooling section 430 is also provided with a circulating Claus tail gas inlet 440 and a circulating Claus tail gas outlet 450, the combustion section 410 is supplemented with coal gas and air for improving reaction heat, and the vaporization cooling section 420 is supplemented with cooling soft water; the gas rich in hydrogen sulfide gas and sulfur dioxide entering the claus furnace 400 and the coal gas and air supplemented along the air inlet of the claus furnace 400 are subjected to claus reaction at the temperature of 1300 ℃ and under the action of a catalyst to obtain high-temperature sulfur steam and claus tail gas, the high-temperature sulfur steam and the claus tail gas enter a sulfur condenser 500 to be separated into liquid sulfur and the claus tail gas after being cooled, a part of the claus tail gas after being cooled enters a tail gas cooling section 430 along a circulating claus tail gas inlet 440, is heated and then flows out of the claus furnace 400 along a circulating claus tail gas outlet 450, and enters a hydrogen sulfide desorption tower 310 along a first tail gas inlet 312 arranged at the bottom end of the hydrogen sulfide desorption tower 310 to be used as desorption H2A supplementary gas source and a heat source for the S gas; part of the Claus tail gas after being cooled is used for removing tar in the Claus tail gas through the electrical tar precipitator 500aSulfur is then fed into sulfur dioxide electromigration membrane separator 200 as SO-rich2The carrier gas of the gas and a part of the cooled claus tail gas are sent into the raw gas pipeline (the process flow chart of the embodiment does not show the gas trend, but includes the part).
Referring again to FIG. 2, the sulfur dioxide electromigration membrane separator 200 is further provided with a means for discharging the SO2First flue gas outlet 220 for the post-flue gas, SO removal2The flue gas after the high-temperature denitration directly enters the heater 200a, is heated and heated, and then is sent to the SCR denitration reactor 600, ammonia gas is supplemented to the SCR denitration reactor 600, nitrogen oxide and ammonia gas are subjected to SCR reaction under the action of a denitration catalyst, and the flue gas after the high-temperature denitration is sent to the chimney 700d along the horizontal flue 700b at the inlet section of the chimney after the heat of the flue gas is recovered by the second waste heat boiler 600 a.
The above examples are merely preferred examples and are not intended to limit the embodiments of the present invention. In addition to the above embodiments, the present invention has other embodiments. All technical solutions formed by adopting equivalent substitutions or equivalent transformations fall within the protection scope of the claims of the present invention.
Claims (4)
1. A process for preparing sulfur by electromigration desulfurization of coke oven flue gas is characterized in that: comprising SO-containing flue gas from a horizontal flue (700) of a coke oven2And NOxThe coke oven flue gas enters a sulfur dioxide electromigration film separator (200) to be separated through electromigration to obtain SO-rich gas2 Gas and SO removal2Post-flue gas, said de-SO2The flue gas after denitration is sent into an SCR denitration reactor (600) to complete denitration after being subjected to heat exchange with the gas in the heat exchanger (200b) and then being heated by a heater (200a), and the flue gas after denitration is sent into the heat exchanger (200b) to be used for SO removal2Gas of heat exchange of the back flue gas; the denitrated flue gas is sent to a chimney (700d) for discharging after being subjected to waste heat recovery by a second waste heat boiler (600 a); said rich in SO2The gas is mixed with H-rich gas from a hydrogen sulfide stripping column (310)2S gas is sent into a combustion section (410) of a Claus furnace (400) together to react to generate Claus tail gas containing sulfur steam, and the Claus tail gas containing the sulfur steam enters a sulfur condenser (500) to be separatedAnd (3) discharging liquid sulfur and the cooled Claus tail gas, wherein one part of the cooled Claus tail gas enters a tail gas cooling section (430) of a Claus furnace (400), is subjected to heat exchange and temperature rise, then enters a hydrogen sulfide desorption tower (310) to serve as a gas stripping gas source and a heat source, the other part of the cooled Claus tail gas enters a sulfur dioxide electro-migration membrane separator (200) to serve as a carrier gas for electro-migration desulfurization of coke oven flue gas, and the rest part of the cooled Claus tail gas is merged into a coke oven raw gas pipe network.
2. The electromigration desulfurization sulfur preparation process for the coke oven flue gas as set forth in claim 1, wherein: after the temperature reduction is finished in the sulfur condenser (500), the Claus tail gas is used for removing tar and sulfur in the Claus tail gas through an electric tar precipitator (500 a).
3. The electromigration desulfurization sulfur preparation process for the coke oven flue gas as set forth in claim 1, wherein: the combustion section (410) of the claus furnace (400) is also supplemented with gas and air for increasing the heat of reaction, the reaction temperature of the combustion section (410) being 1300 ℃.
4. The electromigration desulfurization sulfur preparation process for the coke oven flue gas according to any one of claims 1 to 3 is characterized in that: the sulfur dioxide electromigration membrane separator (200) is provided with separated SO2The temperature resistance of the gaseous membrane material is more than or equal to 400 ℃ or less than or equal to 200 ℃; when the temperature resistance of the membrane material is less than or equal to 200 ℃, SO is contained in the horizontal flue (700) of the coke oven2And NOxThe coke oven flue gas enters a sulfur dioxide electro-migration membrane separator (200) after heat is recovered by a first waste heat boiler (100 a); when the temperature resistance of the membrane material is more than or equal to 400 ℃, SO is contained in the horizontal flue (700) of the coke oven2And NOxThe coke oven flue gas directly enters a sulfur dioxide electromigration membrane separator (200).
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| JP2745099B2 (en) * | 1993-03-23 | 1998-04-28 | 三菱化工機株式会社 | Klaus tail gas treatment equipment |
| CN102198363A (en) * | 2010-03-25 | 2011-09-28 | 中国石油化工股份有限公司 | Film based recovery method of sulfur in flue gas |
| CN104962333A (en) * | 2015-05-29 | 2015-10-07 | 西安建筑科技大学 | Membrane separation biogas biological desulfurization method and device |
| CN107875838A (en) * | 2017-12-15 | 2018-04-06 | 马鞍山钢铁股份有限公司 | With the production technology and processing system of compound claus oven processing activated coke method coke oven flue gas desulphurization denitration acid vapour |
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| JP2745099B2 (en) * | 1993-03-23 | 1998-04-28 | 三菱化工機株式会社 | Klaus tail gas treatment equipment |
| CN102198363A (en) * | 2010-03-25 | 2011-09-28 | 中国石油化工股份有限公司 | Film based recovery method of sulfur in flue gas |
| CN104962333A (en) * | 2015-05-29 | 2015-10-07 | 西安建筑科技大学 | Membrane separation biogas biological desulfurization method and device |
| CN107875838A (en) * | 2017-12-15 | 2018-04-06 | 马鞍山钢铁股份有限公司 | With the production technology and processing system of compound claus oven processing activated coke method coke oven flue gas desulphurization denitration acid vapour |
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