CN108704474B - Coke oven flue gas and Claus tail gas combined treatment process - Google Patents
Coke oven flue gas and Claus tail gas combined treatment process Download PDFInfo
- Publication number
- CN108704474B CN108704474B CN201810553377.8A CN201810553377A CN108704474B CN 108704474 B CN108704474 B CN 108704474B CN 201810553377 A CN201810553377 A CN 201810553377A CN 108704474 B CN108704474 B CN 108704474B
- Authority
- CN
- China
- Prior art keywords
- gas
- coke oven
- tail gas
- flue gas
- claus
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/90—Injecting reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—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
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/004—Systems for reclaiming waste heat
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- 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
- B01D2253/102—Carbon
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Abstract
The invention discloses a combined treatment process of coke oven smoke and Claus tail gas, belonging to the field of energy conservation and environmental protection in the coking industry. The method comprises the steps that coke oven flue gas from a horizontal flue of a coke oven is sent into a coke oven flue gas desulfurization and denitrification device after waste heat is recovered, and NOx in the coke oven flue gas is catalytically reduced into nitrogen and then discharged; SO in coke oven flue gas2Adsorbing and resolving to obtain SO-rich product2The gas and the rich H from the hydrogen sulfide desorption tower2S gas is sent into a Claus furnace together to react to generate Claus tail gas containing sulfur steam, the Claus tail gas containing the sulfur steam enters a sulfur condenser to separate liquid sulfur and the Claus tail gas after temperature reduction, and a part of the Claus tail gas after temperature reduction enters the Claus furnace to be heated and then enters a hydrogen sulfide desorption tower to be used as desorption H2And (4) a gas stripping gas source and a heat source of the S, wherein a part of the cooled Claus tail gas enters a tail gas combustion device and is sent to a coke oven flue gas desulfurization and denitrification device after waste heat recovery. The process thoroughly eliminates the secondary pollution of the desulfurization by-products in the traditional coke oven flue gas treatment.
Description
Technical Field
The invention relates to coke oven flue gas desulfurization and sulfur resource recovery, belongs to the field of energy conservation and environmental protection in the coking industry, and particularly relates to a combined treatment process of coke oven flue gas and Claus tail gas.
Background
According to statistics, the annual SO of the whole country in nearly two years2The total amount of NOx and the emission is 1800 million tons, coal coking is one of the main pollution sources in the field of industrial coal, coke oven flue gas is the most main waste gas pollution source in a coking enterprise, and about 60 percent of SO2And 90% NOx from this.
The coke oven flue gas (coke oven gas for short) is a coke ovenThe product of gas combustion contains CO as main component2、H2O、N2、SO2NOx, etc., wherein SO2NOx is a pollutant that has an impact on the environment. Because the coke oven waste gas is continuously discharged in an organized overhead point source, the coking enterprises are the industries with serious pollution at present.
The environmental protection department of 6 months 2012 issued a new standard for the emission of atmospheric pollutants in the coking industry, and stipulated SO in the combustion tail gas of coke oven chimney from 20152The concentration is less than 50mg/m3NOx concentration < 500mg/m3Dust concentration is less than 30mg/m3。
Is limited by the restriction of various factors such as the production process condition of the coke oven, the blow-by of the oven body and the like, and the coking enterprises can ensure that the exhaust emission reaches the standard only by using the flue gas desulfurization and denitrification device.
Although the flue gas desulfurization and denitrification belong to mature technologies in industries such as electric power and the like, in the conventional coking industry, various problems exist in the aspects of process optimization, investment and operation cost, the problem of secondary waste treatment exists, and particularly, no good solution exists in the aspect of safe operation of a coking plant (emergency switching of a coke oven and safe guarantee of chimney suction).
Meanwhile, the desulfurization and denitrification integrated technology is generally divided into two types: firstly, the existing single desulfurization and denitrification technologies are combined; secondly, based on redox mechanism, SO is generated by using oxidant2And NO are oxidized to SO respectively3And NO2Then the absorption is carried out. The common simultaneous desulfurization and denitrification technologies mainly comprise the following technologies:
an integrated technology of activated carbon adsorption and desulfurization and denitrification is a mature process technology which can simultaneously remove SO2、NOxHeavy metals and other pollutants, and is particularly suitable for high SO2Treating the flue gas with concentration. However, the temperature of the flue gas adsorbed by the activated carbon is preferably 120-160 ℃, and the temperature of the coke oven flue gas is usually in the range of 170-230 ℃, so the temperature condition of the coking flue gas is not suitable.
The wet limestone/lime-gypsum process (WFGD) and Selective Catalytic Reduction (SCR) are both mature desulfurization and denitrification process technologies. Therefore, the two processes are combined to form a WFGD + SCR simultaneous desulfurization and denitrification integrated technology, which is a common method and has a plurality of engineering applications in China. However, the treatment methods have the problem that the desulfurization by-products cannot be recycled.
Feeding the heated coke oven flue gas into a denitration reactor for denitration by an SCR + active coke method; and (4) enabling the flue gas after denitration to enter an active coke desorption tower, and performing desorption regeneration on the desulfurized active coke in the tower. The active coke has good pore structure and high specific surface area, and can react with SO in flue gas2Physical adsorption and chemical adsorption occur. SO in the absence of water in the flue gas2The active coke is adsorbed in the microporous structure to generate physical adsorption; in the presence of water in the flue gas, the activated coke can adsorb SO2And sulfuric acid and sulfurous acid are generated by reaction to generate chemical adsorption.
High-efficiency oxidation absorption desulfurization and denitrification method for removing O3、H2O2As an oxidant for NO, ammonia is used as an absorbent. Part of NO in flue gas is enclosed by O3Oxidizing, and allowing the rest NO to enter a secondary oxidation system to be oxidized by H2O2And (4) oxidizing. The oxidation product enters an absorption tower along with the flue gas to react with SO2Absorbed together by the ammonia. Because the temperature of the flue gas reaches 100 ℃, O3Will be completely decomposed, which seriously affects the oxidation efficiency of NO and leads to instability of the purification efficiency of NO. On the other hand, O is generated3The generation device is difficult to be upsized, and is one of the key factors for limiting the technology.
The tracking analysis of the operation conditions of a plurality of sets of SDA + SCR coke oven flue gas desulfurization and denitrification devices which are put into operation at present shows that the main problems are system blockage and secondary pollution caused by sulfur pollutants. Therefore, how to successfully transplant the mature desulfurization and denitrification technologies in the industries such as electric power and the like to the coking industry or develop a new coke oven flue gas desulfurization and denitrification technology is a common problem of a coking plant and also becomes a key factor which seriously restricts the implementation of a new environment-friendly standard.
On the other hand, most coke plants remove H when desulfurizing coke oven gas2S produces either sulfuric acid or sulfur. Whether living or notThe produced by-products are all generated by waste gas in the production process, and the waste gas is generally merged into a raw gas pipe network, so that the corrosion of the pipe network is caused, and the quality of the gas is also influenced.
In conclusion, the prior coke oven flue gas treatment process has the following technical problems:
(1) the Claus tail gas generated after the sulfur is prepared by the desulfurization of the coke oven gas is generally washed, cooled and merged into a raw gas pipe network, and the tail gas is brought into SO during the subsequent gas desulfurization2The sulfur-containing gas enters the absorption liquid, so that the salt content of the desulfurization waste liquid is increased, the loss of sulfur resources is caused, and the consumption of a gas desulfurizer is increased;
(2) the existing coke oven flue gas activated carbon desulfurization and denitrification process is generally matched with a sulfuric acid preparation system, the investment is large, and a treatment system for acid wastewater generated in the acid preparation process is also required to be matched with the existing coke oven flue gas activated carbon desulfurization and denitrification process. Tail gas after acid preparation is mixed into coke oven flue gas before an active carbon desulfurization and denitrification tower, and certain corrosion is caused to a flue gas pipeline in the front area of the tower;
(3) 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;
(4) 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;
(5) 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 (the dilute sulfuric acid with the concentration of about 10 percent can not be directly used as a sulfuric acid raw material in a coking ammonium sulfate procedure and can be used only by further concentration or mixing with concentrated sulfuric acid). 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;
(6) the Claus tail gas amount after the sulfur is prepared by the existing coke oven gas desulfurization is about 10% of the coal gas amount, and after the tail gas is merged into a raw coke oven gas pipe network, the operation load of a coke oven gas purification system is increased, and the heat value of the coke oven gas is reduced.
Disclosure of Invention
In order to solve the technical problems, the invention discloses a coke oven flue gas and Claus tail gas combined treatment process which can realize resource utilization of sulfur pollutants in the coke oven flue gas and thoroughly eliminate secondary pollution of desulfurization byproducts in the traditional coke oven flue gas treatment.
In order to realize the aim, the invention discloses a combined treatment process of coke oven flue gas and Claus tail gas, which comprises SO-containing gas from a horizontal flue of a coke oven2The coke oven flue gas containing NOx is sent into a coke oven flue gas desulfurization and denitrification device after waste heat recovery, and the NOx in the coke oven flue gas is catalytically reduced into nitrogen and then sent into a chimney for discharge; SO in coke oven flue gas2Adsorbing and resolving to obtain SO-rich product2Gas and H-rich gas in hydrogen sulfide stripping column from hydrogen sulfide treatment apparatus2S gas is sent into a combustion section of a Claus furnace together to react to generate Claus tail gas containing sulfur steam, the Claus tail gas containing the sulfur steam enters a sulfur condenser to separate liquid sulfur and the Claus tail gas after temperature reduction, and a part of the Claus tail gas after temperature reduction enters a tail gas cooling section of the Claus furnace to be heated and then enters a hydrogen sulfide desorption tower to be used as desorption H2And (3) a gas stripping gas source and a heat source of the S, wherein a part of the cooled Claus tail gas enters a tail gas combustion device to be mixed with supplemented air or combustion-supporting flue gas introduced from a horizontal flue of the coke oven and then is combusted, and the mixture is sent to a desulfurization and denitrification device after waste heat recovery.
Further, the claus tail gas after the temperature reduction in the sulfur condenser is used for removing tar, sulfur and carbon residue in the claus tail gas through an electric tar precipitator.
And furthermore, the coke oven flue gas desulfurization and denitrification device adopts an activated carbon adsorption desulfurization and catalytic denitrification process.
Furthermore, the combustion section of the claus furnace is supplemented with gas and air for increasing the heat of reaction, the reaction temperature of the combustion section being 1300 ℃.
Furthermore, the Claus furnace further comprises a vaporization cooling section, and cooling soft water is supplemented to the vaporization cooling section.
The process of the invention has the following beneficial effects:
(1) the process designed by the invention avoids the quality reduction of the coke oven gas and the corrosion of a pipe network caused by the merging of the existing coking Claus tail gas into the raw coke oven gas pipe network;
(2) the process designed by the invention saves the investment and the operation cost of an acid preparation system required by the original coke oven flue gas activated carbon adsorption catalysis glue sulfur denitration process, and eliminates the acid wastewater pollution of the original acid preparation system;
(3) 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 stripping2The solubility of S in water is improved, and the desorption effect is improved);
(4) the process designed by the invention adopts the mixing of the Claus tail gas and the coke oven flue gas for treatment, thereby saving the treatment cost of the original Claus tail gas, and the treated sulfur pollutant enters the Claus furnace as SO required by the Claus reaction2And the recovery rate and high-valued utilization rate of sulfur pollutants are improved.
Drawings
FIG. 1 is a process flow diagram of the combined treatment of coke oven flue gas and Claus tail gas of the present invention;
wherein, the parts in fig. 1 are numbered as follows:
a coke oven 100 (wherein: a coke oven flue gas outlet 110);
a coke oven flue gas desulfurization and denitrification device 200 (wherein, the adsorption reaction tower 210 (wherein, the first flue gas inlet 211, the first flue gas outlet 212, the reaction tower discharge hole 213 and the reaction tower feed inlet 214), the sulfur dioxide analysis tower 220 (wherein, the sulfur dioxide gas outlet 221, the analysis tower feed inlet 222 and the analysis tower discharge hole 223)), and a first waste heat boiler 200 a;
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;
a tail gas combustion device 600;
the coke oven horizontal flue 700 (wherein, the coke oven combustion chamber outlet section horizontal flue 700a, the chimney inlet section horizontal flue 700b, the adjusting valve 700c) and the chimney 700 d.
Detailed Description
The invention adopts a coke oven of 2 x 6 meters in a certain coke-oven plant as an example, the smoke gas quantity of the original coke oven 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. Coke oven gas content about 50000Nm3Per, Claus tail size of about 5000Nm3H is used as the reference value. Contains 5 to 7g/Nm3H of (A) to (B)2The S component raw gas passes through an absorption tower and passes through a desulfurization barren solution (K)2CO3Solution or ammonia solution) containing more than 95% of H2The S component is absorbed and absorbs H2The rich solution of S enters a regeneration tower, and H is separated under the heating and stripping action of superheated steam2The S component is desorbed and enters a Claus furnace.
As shown in FIG. 1, the invention discloses a combined treatment process of coke oven flue gas and Claus tail gas, which comprises controlling an adjusting valve 700c on a horizontal flue 700 of a coke oven, and discharging SO-containing gas from a coke oven flue gas outlet 110 of a coke oven 1002The coke oven flue gas with NOx enters a coke oven combustion chamber outlet section horizontal flue 700a of the coke oven horizontal flue 700, and the SO-containing flue gas2The coke oven flue gas containing NOx is sent into the coke oven flue gas desulfurization and denitrification device 200 after being recovered by the waste heat of the first waste heat boiler 200a, the coke oven flue gas desulfurization and denitrification device 200 adopts an activated carbon adsorption desulfurization and catalytic denitrification process, specifically, the coke oven flue gas desulfurization and denitrification device 200 comprises an adsorption reaction tower 210 for adsorbing sulfur dioxide, nitrogen oxides and catalytic reaction nitrogen oxides and a sulfur dioxide desorption tower 220, wherein the adsorption reaction tower 210 is provided with an adsorption reaction tower 210Be equipped with first exhanst gas outlet 212, reaction tower discharge gate 213 and reaction tower feed inlet 214, the air inlet that first exhanst gas outlet 212 connects chimney entry section horizontal flue 700b is used for discharging tail gas, be equipped with desorption tower feed inlet 222 and analysis tower discharge gate 223 on the desorption tower 220, analysis tower feed inlet 222 is connected to reaction tower discharge gate 213, analysis tower discharge gate 223 is connected reaction tower feed inlet 214, and preferred contain active carbon and catalyst in the adsorption reaction tower 210, the concrete reaction process among the SOx/NOx control device 200 is: sulfur dioxide and nitrogen oxides in the coke oven flue gas are adsorbed by activated carbon, the nitrogen oxides react with ammonia gas introduced into the adsorption reaction tower at a certain temperature in a catalyst to obtain nitrogen, the nitrogen and other tail gases are discharged along a first flue gas outlet 212, the activated carbon saturated with adsorbed sulfur dioxide is conveyed to the sulfur dioxide desorption tower 220 along a reaction tower discharge port 213 and a desorption tower feed port 222 to complete desorption, the desorbed activated carbon is conveyed to the adsorption reaction tower 210 along a desorption tower discharge port 223 and a reaction tower feed port 214 to complete cyclic utilization, and sulfur dioxide gas obtained by enrichment in the sulfur dioxide desorption tower 220 enters the claus furnace 400 along a sulfur dioxide gas outlet 221 arranged on the sulfur dioxide desorption tower 220.
Referring again to fig. 1, the hydrogen sulfide treatment apparatus 300 includes a hydrogen sulfide analysis column 310 and a hydrogen sulfide absorption column 320, wherein the hydrogen sulfide absorption column 320 contains an absorption liquid (K) for absorbing hydrogen sulfide2CO3Solution or ammonia solution), the saturated liquid after absorbing hydrogen sulfide flows into the hydrogen sulfide analysis tower 310 along the inlet and outlet between the hydrogen sulfide analysis tower 310 and the hydrogen sulfide absorption tower 320, and hydrogen sulfide is re-precipitated under the action of certain temperature and other gases. The hydrogen sulfide desorption tower 310 is provided with a hydrogen sulfide gas outlet 311 and a first tail gas inlet 312, the hydrogen sulfide gas outlet 311 and the sulfur dioxide gas outlet 221 are both connected with a combustion section 410 of the claus furnace 400, the claus furnace 400 further comprises a vaporization cooling section 420 and a tail gas cooling section 430, coal gas and air are supplemented to the tail gas cooling section 430, and cooling soft water is supplemented to the vaporization cooling section 420; the hydrogen sulfide gas entering the Claus furnace 400 is rich in sulfur dioxideThe gas and the coal gas supplemented along the gas inlet of the claus furnace 400 are subjected to claus reaction with the air at the temperature of 1300 ℃ and under the action of a catalyst to obtain claus tail gas of high-temperature sulfur-containing steam, as shown in fig. 1, a circulating claus tail gas inlet 440 and a circulating claus tail gas outlet 450 are further arranged on a tail gas cooling section 430, and the tail gas cooling section 430 of the claus furnace 400 is connected with the gas inlet of a sulfur condenser 500; wherein, the high temperature sulfur steam in the claus tail gas containing sulfur steam is cooled to liquid sulfur in the sulfur condenser 500 and flows out along the liquid outlet arranged at the lower part of the sulfur condenser 500, in this embodiment, preferably, an electric tar precipitator 500a is arranged at the gas outlet of the sulfur condenser 500, the electric tar precipitator is an electrostatic precipitator, used for removing micro-dust such as tar, sulfur, carbon residue and the like in the Claus tail gas, the gas outlet of the electrical tar precipitator 500a is connected with two gas pipelines, one gas pipeline is connected with the gas inlet of the tail gas combustion device 600, so that part of the Claus tail gas after the electrostatic precipitator removes the micro-dust such as tar, sulfur and carbon residue enters the tail gas combustion device 600, and the gas is mixed with air supplemented from the air inlet of the tail gas combustion device 600 and combustion-supporting flue gas introduced from the horizontal flue 700 of the coke oven and then is further combusted, hydrogen sulfide gas in the claus tail gas is converted into sulfur dioxide, and the sulfur dioxide is sent to the desulfurization and denitrification device 200 after waste heat recovery. The other gas pipeline is connected with a circulating claus tail gas inlet 440 of the tail gas cooling section 430, and the circulating claus tail gas outlet 450 is connected with the first tail gas inlet 312 of the hydrogen sulfide processing device 300, so that a part of claus tail gas enters the hydrogen sulfide desorption tower 310 after being subjected to heat exchange and temperature rise in the tail gas cooling section 430 to provide a gas stripping gas source and a supplementary heat source for desorption of hydrogen sulfide gas.
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, and compared with the original activated carbon method, the method saves the investment of desulfurization and denitrification of the coke oven flue gas by more than 30 percent and saves the annual cost of desulfurization, denitrification and Claus tail gas treatment and operation by more than 2000 ten thousand yuan.
In conclusion, the process of the invention not only avoids the quality reduction of the coke oven gas and the corrosion of the pipe network caused by the incorporation of the existing coking Claus tail gas into the raw gas pipe network of the coke oven gas, but also realizes the resource utilization of the sulfur pollutants in the coke oven gas.
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 coke oven flue gas and Claus tail gas combined treatment process is characterized in that: comprising SO-containing flue gas from a horizontal flue (700) of a coke oven2And NOxThe coke oven flue gas is sent into a coke oven flue gas desulfurization and denitrification device (200) after waste heat recovery, and NO in the coke oven flue gasxThe nitrogen is sent to a chimney (700d) for discharging after being catalytically reduced into nitrogen; SO in coke oven flue gas2Adsorbing and resolving to obtain SO-rich product2The gas is mixed with H-rich gas from the hydrogen sulfide stripping tower (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, the Claus tail gas containing the sulfur steam enters a sulfur condenser (500) to separate liquid sulfur and the Claus tail gas after being cooled, and one part of the Claus tail gas after being cooled enters a tail gas cooling section (430) of the Claus furnace (400) to be heated and then enters a hydrogen sulfide desorption tower (310) to be used as desorption H2A part of the cooled Claus tail gas enters a tail gas combustion device (600) to be mixed with supplemented air or combustion-supporting flue gas introduced from a horizontal flue (700) of the coke oven and then is combusted, and the mixture is sent to a coke oven flue gas desulfurization and denitrification device (200) after waste heat recovery; after the temperature reduction in the sulfur condenser (500) is completed, the Claus tail gas is used for removing tar, sulfur and carbon residue in the Claus tail gas through an electrical tar precipitator (500 a).
2. The coke oven flue gas and claus tail gas combined treatment process of claim 1, characterized in that: the coke oven flue gas desulfurization and denitrification device (200) adopts an activated carbon adsorption desulfurization and catalytic denitrification process.
3. The coke oven flue gas and claus tail gas combined treatment process according to claim 1 or 2, characterized in that: 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 coke oven flue gas and claus tail gas combined treatment process according to claim 1 or 2, characterized in that: the claus furnace (400) further comprises a vaporization cooling section (420) for supplementing cooling soft water to the vaporization cooling section (420).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810553377.8A CN108704474B (en) | 2018-05-31 | 2018-05-31 | Coke oven flue gas and Claus tail gas combined treatment process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810553377.8A CN108704474B (en) | 2018-05-31 | 2018-05-31 | Coke oven flue gas and Claus tail gas combined treatment process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108704474A CN108704474A (en) | 2018-10-26 |
| CN108704474B true CN108704474B (en) | 2021-03-19 |
Family
ID=63870989
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810553377.8A Active CN108704474B (en) | 2018-05-31 | 2018-05-31 | Coke oven flue gas and Claus tail gas combined treatment process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108704474B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109529621B (en) * | 2019-01-12 | 2024-03-12 | 西安交通大学 | Semi-dry desulfurization, denitrification and demercuration device and method based on catalytic oxidation and deep condensation |
| CN114432842A (en) * | 2020-10-20 | 2022-05-06 | 中国石油化工股份有限公司 | Method and device for coupling desulfurization and preparing sulfur |
| CN115143473B (en) * | 2022-09-02 | 2023-02-24 | 臣功环境科技有限公司 | High-temperature dry distillation carbonization incineration device for household garbage |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101422692A (en) * | 2008-11-24 | 2009-05-06 | 袁宝春 | Pulse corona plasma reaction and absorption catalysis desulfurization denitration method and device |
| CN103894047A (en) * | 2014-03-14 | 2014-07-02 | 成都华西堂投资有限公司 | Flue gas pollutant control integrated purifying and recycling process |
| CN107537297A (en) * | 2016-06-29 | 2018-01-05 | 中国石油化工股份有限公司 | The flue gas circulation desulfuration technique of clean environment firendly |
| 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 |
| CN207413149U (en) * | 2017-09-08 | 2018-05-29 | 中冶焦耐(大连)工程技术有限公司 | A kind of claus tail-gas clean-up system |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5864117A (en) * | 1981-10-12 | 1983-04-16 | Hitachi Ltd | Dry stack-gas desulfurization process |
-
2018
- 2018-05-31 CN CN201810553377.8A patent/CN108704474B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101422692A (en) * | 2008-11-24 | 2009-05-06 | 袁宝春 | Pulse corona plasma reaction and absorption catalysis desulfurization denitration method and device |
| CN103894047A (en) * | 2014-03-14 | 2014-07-02 | 成都华西堂投资有限公司 | Flue gas pollutant control integrated purifying and recycling process |
| CN107537297A (en) * | 2016-06-29 | 2018-01-05 | 中国石油化工股份有限公司 | The flue gas circulation desulfuration technique of clean environment firendly |
| CN207413149U (en) * | 2017-09-08 | 2018-05-29 | 中冶焦耐(大连)工程技术有限公司 | A kind of claus tail-gas clean-up system |
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108704474A (en) | 2018-10-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US11529584B2 (en) | Acid gas treatment | |
| CN103894047B (en) | Flue gas pollutant controls integrated purifying recovery process | |
| CN104689679A (en) | Desulfurization and denitrification process for coke oven flue gas | |
| CN108704474B (en) | Coke oven flue gas and Claus tail gas combined treatment process | |
| CN103877839A (en) | Flue gas pollutant control integrated purification process | |
| CN111346605B (en) | Pollutant comprehensive treatment system and method suitable for large-scale coal-fired power plant | |
| CN112191083A (en) | Sintering flue gas active coke desulfurization and denitrification ultralow emission treatment system and method | |
| CN108654363B (en) | Acid making process by coupling waste heat of coke oven flue gas and sulfur pollutants | |
| CN102371110B (en) | Flue gas desulfurization and denitration method | |
| EP3597286A1 (en) | Acid gas treatment | |
| CN108786441B (en) | Sulfur preparation process by electromigration desulfurization of coke oven flue gas | |
| CN208082173U (en) | The processing system of activated coke method coke oven flue gas desulphurization denitration acid vapour is handled with system for preparing sulfuric acid | |
| CN206463781U (en) | A kind of desulfuring and denitrifying apparatus of coke oven flue gas | |
| CN109925859B (en) | Device and process for deep oxidation, desulfurization and denitrification of industrial flue gas | |
| CN110877899A (en) | Method for treating low-concentration sulfur-containing acidic gas | |
| CN104556147A (en) | Process for preparing SCR reducing agent from coking residual ammonia wastewater as raw material | |
| CN110953597A (en) | High-sulfur waste gas rich combustion device and energy utilization method | |
| CN103879970A (en) | Production process for preparing sulfur by recovering sulfur dioxide from flue gas | |
| CN109701383A (en) | A kind of new catalytic method desulfuring and denitrifying apparatus and technique for coke oven flue gas | |
| CN115340887B (en) | Blast furnace gas fine desulfurization and sulfur recycling process | |
| CN107890755A (en) | With the production technology and processing system of system for preparing sulfuric acid processing activated coke method coke oven flue gas desulphurization denitration acid vapour | |
| CN215693083U (en) | Sintering flue gas desulfurization and denitrification system | |
| CN106552505B (en) | Method for treating sulfur-containing waste gas | |
| CN112191073A (en) | Integrated removing device for smoke pollutants | |
| CN116920592A (en) | Catalytic oxidation adsorption treatment system and method for sulfur-containing tail gas of sulfur recovery device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |