CN106552505B - Method for treating sulfur-containing waste gas - Google Patents
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- CN106552505B CN106552505B CN201510639559.3A CN201510639559A CN106552505B CN 106552505 B CN106552505 B CN 106552505B CN 201510639559 A CN201510639559 A CN 201510639559A CN 106552505 B CN106552505 B CN 106552505B
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Abstract
Hair brushThe invention relates to a method for treating sulfur-containing waste gas, belonging to the technical field of petrochemical waste gas treatment. The method for treating the sulfur-containing waste gas comprises the steps of introducing one or two of flue gas of a sulfur recovery device or S Zorb regeneration flue gas and regeneration air of a catalytic cracking device into a regeneration unit in the catalytic cracking device for a coking reaction, wherein unreacted SO-containing gas2The gas and the flue gas generated by the coking reaction are sequentially subjected to separation and heat exchange and then enter a desulfurization and denitrification unit in a catalytic cracking device for treatment, and the purified tail gas is obtained and then discharged. The invention relies on the existing device to realize the SO content2The treatment of waste gas, especially sulfur plant flue gas and S Zorb regeneration flue gas, has the advantages of low investment and low operating cost, and realizes environmental protection and waste gas treatment.
Description
Technical Field
The invention relates to a method for treating sulfur-containing waste gas, belonging to the technical field of petrochemical waste gas treatment.
Background
SO2Is one of the most important environmental pollutants and is the most important cause of acid rain. SO (SO)2Can destroy the physiological function of plants, slow down the growth of crops and forests, and enable human bodies to inhale SO with higher concentration2Gas, which causes strong stimulation of the respiratory tract, SO2Has received wide attention as a main emission treatment technology of atmospheric pollutants. In recent years, SO2The discharge causes that 40 percent of the territorial area of China is damaged by acid rain, and the annual loss caused by the discharge is as high as 1100 billion yuan. SO emitted by the oil refining industry by 2020 according to the current emission control level2Will reach 126993 t/a. Thus, pollution control and SO reduction2The emission is an important task for sustainable development of the economic society of China.
The sulfur emission requirement of industrially developed countries is very strict, and the regulations of the environmental protection agency of the federal government of the United states stipulate heating furnace flue gas, sulfur tail gas and catalytic cracking regeneration flue gas SO of petroleum refining industry2The emission concentration limit is 50ppm (v) and is about 143mg/m3. Year 2015, month 4China releases GB31570-2015 discharge Standard for Industrial pollutants for Petroleum refining, which stipulates: the limit value of the sulfur dioxide emission concentration of the sulfur recovery device is 400mg/m3Special limit of 100mg/m for specific area3The existing enterprise is executed in 2017 in 1 month and 1 day, and the new enterprise is executed in 2015 in 7 months and 1 day. This standard is currently the most stringent emission standard in the world.
SO in flue gas of most of sulfur recovery devices in China at present2The content is 960mg/m3In the following, the flue gas SO can be achieved by optimizing operation and selecting catalyst with excellent performance for part of enterprises2The discharge is less than 400mg/m3But some enterprises still can not reach the emission standard. Special limit value for special area of 100mg/m3The emission requirement is difficult to achieve by adopting the existing sulfur recovery process. Therefore, new exhaust gas treatment methods must be developed to meet national emission standards.
In addition, with the increasingly strict environmental regulations in China, the quality requirement on the vehicle gasoline is continuously improved. China petrochemical industry introduced and bought off the S Zorb gasoline adsorption desulfurization patent technology developed by the United states Kangfei company, and carries out secondary innovation to produce clean gasoline with low sulfur content. In the S Zorb technology, the adsorbent needs to be regenerated circularly after saturation, and sulfur adsorbed on the catalyst is converted into SO2And the catalyst is sent out of the device along with the regenerated flue gas and recycled, SO the regenerated flue gas contains more SO2Of which SO2The volume content is up to 5 percent. Foreign countries usually adopt a lye absorption mode to remove SO2However, the S Zorb gasoline adsorption desulfurization process pack does not contain a treatment technology of the S Zorb regeneration flue gas.
The above-mentioned SO-containing2The emission of exhaust gases into the atmosphere, on the one hand, can cause serious environmental pollution problems and, on the other hand, can also cause poisoning events. Thus, a reasonably reliable SO-containing2The development of a waste gas treatment method is imminent, and the method can meet the requirements of the tail gas of a sulfur device for reaching the standard and the treatment of S Zorb regenerated flue gas at the same time, and can also meet the requirement of the independent treatment of two gases.
The patent CN102441326 discloses a method for treating gas containing hydrocarbon and sulfur, which comprises the steps of firstly enabling the gas containing hydrocarbon and sulfur to enter an absorption tower to be absorbed and dealkylated by low-temperature diesel oil, then enabling the gas to enter a catalytic oxidation reactor, and enabling the gas to pass through catalytic oxidation desulfurization and catalytic oxidation hydrocarbon supporting beds in sequence to purify tail gas and achieve emission standard. The method has the advantages of complex process flow and high operation cost.
Patent CN103316578 discloses a method for absorbing sulfur dioxide and co-producing sulfur. The method comprises the steps of mixing calcium sulfite or/and calcium sulfate with a carbon-based reducing agent to prepare calcium sulfide, reacting the calcium sulfide with introduced SO2 gas under a certain condition, and separating to obtain sulfur and a mixture containing the calcium sulfite and the calcium sulfate after the reaction is finished. The process flow is complex, calcium sulfate, carbon-based reducing agent and the like are required to be consumed, and the operation cost of the device is high.
Disclosure of Invention
The invention aims to provide a method for treating sulfur-containing waste gas, which realizes SO-containing by relying on the existing device2The treatment of waste gas, especially sulfur plant flue gas and S Zorb regeneration flue gas, has the advantages of low investment and low operating cost, and realizes environmental protection and waste gas treatment.
The method for treating the sulfur-containing waste gas comprises the steps of introducing one or two of flue gas of a sulfur recovery device or S Zorb regenerated flue gas and regenerated air of a catalytic cracking device into a regeneration unit in the catalytic cracking device for a coking reaction, separating and exchanging heat of unreacted SO 2-containing gas and flue gas generated by the coking reaction in sequence, and then introducing the gas into a desulfurization and denitrification unit in the catalytic cracking device for treatment to obtain purified tail gas for emission.
The temperature of the flue gas of the sulfur recovery device is 280-350 ℃, and SO in the flue gas of the sulfur recovery device2The volume content is 100-800mg/m3The volume content of oxygen is 2-5%.
The temperature of the S Zorb regeneration flue gas is 110-22-5% of volume content, 0.2-5% of oxygen volume content and the balance of nitrogen.
And the flue gas of the sulfur recovery device or the S Zorb regeneration flue gas is introduced into a regeneration unit in the catalytic cracking device through a pipeline.
The regeneration air of the catalytic cracking unit is introduced into a regeneration unit in the catalytic cracking unit through a fan.
The regeneration unit in the catalytic cracking device comprises a coking tank and a regenerator, is a catalyst regeneration place in the catalytic cracking device, and mainly has the functions of carrying out a coking reaction at the temperature of 650-720 ℃, burning off coke on a coked catalyst to recover the activity of the catalyst, so that the catalyst is regenerated, wherein in the process, a gas phase firstly participates in the coking reaction in the lower coking tank and then enters the upper regenerator.
The volume content of oxygen in the flue gas generated by the scorching reaction is controlled to be 2-9%.
SO in the purified tail gas2The content is less than 50mg/m3。
One or two of the flue gas of the sulfur recovery device or the S Zorb regeneration flue gas are introduced into a catalytic cracking device through a pipeline, and are mixed with air introduced by a fan and then introduced into a coking tank. In a coking tank, the catalytic cracking catalyst reacts with oxygen at the high temperature of 650-720 ℃ to coke the catalyst, thereby realizing the regeneration of the catalyst, simultaneously, the oxygen in the flue gas of the sulfur recovery device and the S Zorb regeneration flue gas is reacted, and the residual SO2The gas separates catalyst particles through a cyclone separator arranged in a regenerator along with catalytic cracking regeneration flue gas. The regeneration flue gas at 630-700 ℃ is introduced into a three-stage cyclone separator to further separate entrained catalyst particles, and then enters a waste heat boiler to recover heat. The flue gas is cooled to below 180 ℃ by a waste heat boiler and then is introduced into a flue gas desulfurization and denitration unit of the device, and most of SO in the flue gas is absorbed in an absorption tower of the unit2Absorbed, the generated wastewater is subjected to subsequent treatment, and the residual SO2The content is less than 50mg/m3The tail gas is discharged through a chimney.
The invention has the following beneficial effects:
(1) provides a more economical sulfur recovery device SO2The method for discharging concentration depends on the existing catalytic cracking device, and SO can be realized without increasing the investment of a sulfur recovery device2The discharge concentration is reduced to 50mg/m3The method meets the requirements of new environmental protection laws and regulations, saves the investment of devices, and creates huge investment for enterprisesThe social benefit of (2);
(2) provides a reasonable method for treating the regenerated flue gas of S Zorb, SO in the regenerated flue gas of S Zorb2The content is high, the method realizes the treatment of the regenerated flue gas of the S Zorb by means of the existing catalytic cracking device, saves the investment and solves the worries of the future for upgrading the quality of the gasoline.
Drawings
FIG. 1 is a process flow diagram of the present invention;
in the figure: 1. flue gas of a sulfur recovery device; 2. s Zorb regeneration flue gas; 3. regenerating air in a catalytic cracking unit; 4. a coke burning tank; 5. a regenerator; 6. a tertiary cyclone separator; 7. a waste heat boiler; 8. an absorption tower; 9. waste water; 10. tail gas; 11. and (4) a chimney.
Detailed Description
The present invention is further illustrated by the following examples, which are not intended to limit the practice of the invention.
Example 1
The process flow is shown in figure 1, and the flue gas 1 (the temperature is 315 ℃, SO) of the sulfur recovery device is used2The content is 500mg/m3，O23.2 percent of the sulfur and S Zorb regeneration flue gas 2 (the temperature is 125 ℃, and SO)2Content of 3.5%, O2The content is 3.8 percent) are respectively led into a catalytic cracking device through a pipeline, and are mixed with the regeneration air 3 of the catalytic cracking device led in by a fan and then are led into a coking tank 4. In a coking tank 4, the catalytic cracking catalyst reacts with oxygen at high temperature of 680 ℃ to carry out catalyst coking, SO that the catalyst is regenerated, meanwhile, oxygen in the flue gas 1 of the sulfur recovery device and the S Zorb regenerated flue gas 2 is reacted, and the residual SO2The gas separates catalyst particles through a cyclone separator arranged in a regenerator 5 along with catalytic cracking regeneration flue gas. 668 deg.C regenerated flue gas is introduced into a three-stage cyclone separator 6 to further separate entrained catalyst particles, and then enters a waste heat boiler 7 to recover heat. The flue gas is cooled to 168 ℃ by a waste heat boiler 7 and then is introduced into a flue gas desulfurization and denitration unit of the device, and most of SO in the flue gas is absorbed in an absorption tower 8 of the unit2Absorbed, the generated wastewater 9 is subjected to subsequent treatment, and the residual SO2The content is less than 50mg/m3Of the tail gas10 are discharged through a chimney 11.
SO in tail gas 10 of the process2The concentration is 25mg/m3Meets the 1SO of the flue gas of the sulfur recovery device2The content is less than 100mg/m3Simultaneously reasonably processing the S Zorb regeneration flue gas 2.
Example 2
The process flow is shown in figure 1, and the flue gas 1 (the temperature is 280 ℃, and the SO) of the sulfur recovery device is used2The content is 150mg/m3，O2Content of 5%) and S Zorb regeneration flue gas 2 (temperature of 160 ℃, SO)2Content of 5%, O2The content is 5 percent) are respectively led into a catalytic cracking device through a pipeline, and are mixed with the regeneration air 3 of the catalytic cracking device led in by a fan and then are led into a coking tank 4. In a coking tank 4, the catalytic cracking catalyst reacts with oxygen at the high temperature of 720 ℃ to coke the catalyst, SO as to realize the regeneration of the catalyst, meanwhile, the oxygen in the flue gas 1 of the sulfur recovery device and the S Zorb regeneration flue gas 2 is reacted, and the residual SO2The gas separates catalyst particles through a cyclone separator arranged in a regenerator 5 along with catalytic cracking regeneration flue gas. The regenerated flue gas at 700 ℃ is introduced into a three-stage cyclone separator 6 to further separate entrained catalyst particles, and then enters a waste heat boiler 7 to recover heat. The flue gas is cooled to 180 ℃ by a waste heat boiler 7 and then is introduced into a flue gas desulfurization and denitration unit of the device, and most of SO in the flue gas is absorbed in an absorption tower 8 of the unit2Absorbed, the generated wastewater 9 is subjected to subsequent treatment, and the residual SO2The content is less than 50mg/m3The tail gas 10 is discharged through a chimney 11.
SO in tail gas 10 of the process2The concentration is 38mg/m3Meets the 1SO of the flue gas of the sulfur recovery device2The content is less than 100mg/m3Simultaneously reasonably processing the S Zorb regeneration flue gas 2.
Example 3
The process flow is shown in figure 1, and the flue gas 1 (the temperature is 350 ℃, and the SO) of the sulfur recovery device is used2The content is 800mg/m3，O22 percent of the flue gas and S Zorb regeneration flue gas 2 (the temperature is 110 ℃, SO)2Content of 2%, O2Content of 0.2%) are introduced into a catalytic cracking unit via lines, respectively, withThe regenerated air 3 of the catalytic cracking device introduced by the fan is mixed and then introduced into the coke burning tank 4. In a coking tank 4, a catalytic cracking catalyst reacts with oxygen at a high temperature of 650 ℃ to coke the catalyst, SO that the catalyst is regenerated, meanwhile, oxygen in the flue gas 1 of the sulfur recovery device and the S Zorb regeneration flue gas 2 is reacted, and the residual SO2The gas separates catalyst particles through a cyclone separator arranged in a regenerator 5 along with catalytic cracking regeneration flue gas. The regeneration flue gas at 630 ℃ is introduced into a three-stage cyclone separator 6 to further separate entrained catalyst particles, and then enters a waste heat boiler 7 to recover heat. The flue gas is cooled to 162 ℃ by a waste heat boiler 7 and then is introduced into a flue gas desulfurization and denitration unit of the device, and most of SO in the flue gas is absorbed in an absorption tower 8 of the unit2Absorbed, the generated wastewater 9 is subjected to subsequent treatment, and the residual SO2The content is less than 50mg/m3The tail gas 10 is discharged through a chimney 11.
SO in tail gas 10 of the process2The concentration is 33mg/m3Meets the 1SO of the flue gas of the sulfur recovery device2The content is less than 100mg/m3Simultaneously reasonably processing the S Zorb regeneration flue gas 2.
Example 4
The process flow is shown in figure 1, and the flue gas 1 (the temperature is 295 ℃ and the SO temperature is higher) of the sulfur recovery device2The content is 338mg/m3，O23.9 percent) and S Zorb regeneration flue gas 2 (the temperature is 140 ℃, SO)2Content of 3.0%, O2Content is 1.8%) are respectively led into a catalytic cracking device through a pipeline, and are mixed with catalytic cracking device regeneration air 3 led in by a fan and then are led into a coking tank 4. In a coking tank 4, the catalytic cracking catalyst reacts with oxygen at the high temperature of 691 ℃ to coke the catalyst, SO as to realize the regeneration of the catalyst, meanwhile, the oxygen in the flue gas 1 of the sulfur recovery device and the S Zorb regeneration flue gas 2 is reacted, and the residual SO2The gas separates catalyst particles through a cyclone separator arranged in a regenerator 5 along with catalytic cracking regeneration flue gas. The regeneration flue gas at 683 ℃ is introduced into a three-stage cyclone separator 6 to further separate entrained catalyst particles and then enters a waste heat boiler 7 to recover heat. The flue gas is cooled to 165 ℃ by a waste heat boiler 7 and then is introduced into a flue gas desulfurization and denitration unit of the deviceMost of SO in flue gas in the absorption tower 82Absorbed, the generated wastewater 9 is subjected to subsequent treatment, and the residual SO2The content is less than 50mg/m3The tail gas 10 is discharged through a chimney 11.
SO in tail gas 10 of the process2The concentration is 31mg/m3Meets the 1SO of the flue gas of the sulfur recovery device2The content is less than 100mg/m3Simultaneously reasonably processing the S Zorb regeneration flue gas 2.
Example 5
The process flow is shown in figure 1, and the flue gas 1 of the sulfur recovery device (the temperature is 326 ℃, SO)2The content is 710mg/m3，O21.0 percent) and S Zorb regeneration flue gas 2 (the temperature is 142 ℃, SO)2Content of 2.8%, O2The content is 2.2 percent) are respectively led into a catalytic cracking device through a pipeline, and are mixed with regeneration air 3 of the catalytic cracking device led in by a fan and then are led into a coking tank 4. In a coking tank 4, a catalytic cracking catalyst reacts with oxygen at the high temperature of 713 ℃ to coke the catalyst, SO that the regeneration of the catalyst is realized, meanwhile, oxygen in the flue gas 1 of the sulfur recovery device and the S Zorb regeneration flue gas 2 is reacted, and the residual SO2The gas separates catalyst particles through a cyclone separator arranged in a regenerator 5 along with catalytic cracking regeneration flue gas. The 672 ℃ regenerated flue gas is introduced into a three-stage cyclone separator 6 to further separate entrained catalyst particles, and then enters a waste heat boiler 7 to recover heat. The flue gas is cooled to 170 ℃ by a waste heat boiler 7 and then is introduced into a flue gas desulfurization and denitration unit of the device, and most of SO in the flue gas is absorbed in an absorption tower 8 of the unit2Absorbed, the generated wastewater 9 is subjected to subsequent treatment, and the residual SO2The content is less than 50mg/m3The tail gas 10 is discharged through a chimney 11.
SO in tail gas 10 of the process2The concentration is 39mg/m3Meets the 1SO of the flue gas of the sulfur recovery device2The content is less than 100mg/m3Simultaneously reasonably processing the S Zorb regeneration flue gas 2.
Example 6
The process flow is shown in figure 1, and the flue gas 1 (the temperature is 308 ℃, SO) of the sulfur recovery device is used2The content is 239mg/m3，O23.7 percent) and S Zorb regeneration flue gas 2 (the temperature is 133 ℃, SO)2Content of 4.2%, O2The content is 4.5 percent) are respectively led into a catalytic cracking device through a pipeline, and are mixed with the regeneration air 3 of the catalytic cracking device led in by a fan and then are led into a coking tank 4. In a coking tank 4, the catalytic cracking catalyst reacts with oxygen at the high temperature of 678 ℃ to coke the catalyst, SO as to realize the regeneration of the catalyst, meanwhile, the oxygen in the flue gas 1 of the sulfur recovery device and the regeneration flue gas 2 of the S Zorb are reacted, and the residual SO2The gas separates catalyst particles through a cyclone separator arranged in a regenerator 5 along with catalytic cracking regeneration flue gas. The 656 ℃ regeneration flue gas is introduced into a three-stage cyclone separator 6 to further separate entrained catalyst particles and then enters a waste heat boiler 7 to recover heat. The flue gas is cooled to 163 ℃ by a waste heat boiler 7 and then is introduced into a flue gas desulfurization and denitration unit of the device, and most of SO in the flue gas is absorbed in an absorption tower 8 of the unit2Absorbed, the generated wastewater 9 is subjected to subsequent treatment, and the residual SO2The content is less than 50mg/m3The tail gas 10 is discharged through a chimney 11.
SO in tail gas 10 of the process2The concentration is 30mg/m3Meets the 1SO of the flue gas of the sulfur recovery device2The content is less than 100mg/m3Simultaneously reasonably processing the S Zorb regeneration flue gas 2.
Example 7
The process flow is shown in figure 1, and the flue gas 1 (the temperature is 318 ℃ and the SO temperature is higher) of the sulfur recovery device2The content is 268mg/m3，O2The content is 3.5 percent) is introduced into a catalytic cracking device through a pipeline, and is mixed with regeneration air 3 of the catalytic cracking device introduced by a fan and then is introduced into a coking tank 4. In a coking tank 4, the catalytic cracking catalyst reacts with oxygen at high temperature of 680 ℃ to carry out catalyst coking, SO that the catalyst is regenerated, meanwhile, oxygen in the flue gas 1 of the sulfur recovery device and the S Zorb regenerated flue gas 2 is reacted, and the residual SO2The gas separates catalyst particles through a cyclone separator arranged in a regenerator 5 along with catalytic cracking regeneration flue gas. The regenerated flue gas at 666 ℃ is introduced into a three-stage cyclone separator 6 to further separate entrained catalyst particles, and then enters a waste heat boiler 7 to recover heat. Waste of flue gasThe hot boiler 7 is introduced into a flue gas desulfurization and denitration unit after being cooled to 160 ℃, and most of SO in the flue gas is absorbed in an absorption tower 8 of the unit2Absorbed, the generated wastewater 9 is subjected to subsequent treatment, and the residual SO2The content is less than 50mg/m3The tail gas 10 is discharged through a chimney 11.
SO in tail gas 10 of the process2The concentration is 24mg/m3Meets the 1SO of the flue gas of the sulfur recovery device2The content is less than 100mg/m3Meets the requirements of new environmental protection regulations.
Example 8
The technological process is shown in figure 1, and S Zorb regeneration flue gas 2 (temperature is 143 ℃, SO)2Content of 4.6%, O2Content is 4.0 percent) is introduced into a catalytic cracking device through a pipeline, and is mixed with catalytic cracking device regeneration air 3 introduced by a fan and then is introduced into a coking tank 4. In a coking tank 4, the catalytic cracking catalyst reacts with oxygen at 685 ℃ to coke the catalyst, SO that the regeneration of the catalyst is realized, meanwhile, oxygen in the flue gas 1 of the sulfur recovery device and the regeneration flue gas 2 of the S Zorb are reacted, and the residual SO2The gas separates catalyst particles through a cyclone separator arranged in a regenerator 5 along with catalytic cracking regeneration flue gas. The 671 deg.C regeneration flue gas is introduced into a three-stage cyclone separator 6 for further separation of entrained catalyst particles, and then enters a waste heat boiler 7 for heat recovery. The flue gas is cooled to 168 ℃ by a waste heat boiler 7 and then is introduced into a flue gas desulfurization and denitration unit of the device, and most of SO in the flue gas is absorbed in an absorption tower 8 of the unit2Absorbed, the generated wastewater 9 is subjected to subsequent treatment, and the residual SO2The content is less than 50mg/m3The tail gas 10 is discharged through a chimney 11.
SO in tail gas 10 of the process2The concentration is 31mg/m3And reasonably processing the S Zorb regeneration flue gas 2.
Comparative example 1
A Claus + SCOT sulfur recovery process adopted by a certain 8 million tons/year sulfur device in China. The specific process flow is as follows: part of hydrogen sulfide in the acid gas and air are combusted at high temperature in a sulfur production furnace to generate sulfur dioxide and elemental sulfur, and the rest hydrogen sulfide and the generated sulfur dioxide undergo a Claus reaction to generate elemental sulfur. High-temperature process gas containing hydrogen sulfide, sulfur dioxide and sulfur steam generated by the sulfur production furnace is heated by a waste heat boiler 7 and then enters a primary sulfur condenser to recover elemental sulfur, and process gas at the outlet of the condenser sequentially passes through a primary sulfur production reactor and a secondary sulfur production reactor through the process gas to generate Claus and hydrolysis reactions under the action of a catalyst. The Claus tail gas generated by the sulfur production unit enters a tail gas hydrogenation unit for treatment, and sulfur steam and SO in the Claus tail gas in a tail gas hydrogenation reactor2And the COS respectively generates hydrogen sulfide through hydrogenation and hydrolysis reactions, the purified tail gas generated after part of the hydrogen sulfide is absorbed by the Claus tail gas containing the hydrogen sulfide through the amine liquid absorption system is incinerated by the incinerator and then discharged through a device chimney 11, and finally SO in the flue gas of the sulfur device2The discharge concentration is 512mg/m3And the requirements of the latest national environmental protection regulation GB31570-2015 discharge Standard of pollutants for oil refining industry cannot be met.
Comparative example 2
A certain domestic refining enterprise introduces the S Zorb regenerated flue gas 2 into a sulfur production furnace of a 10 ten thousand ton/year sulfur recovery device for treatment. The specific process flow is as follows: acid gas, S Zorb tail gas and air are respectively introduced into the sulfur production furnace through a burner. SO in SZorb regeneration flue gas 2 in sulfur production furnace2The sulfur and hydrogen sulfide in the acid gas are subjected to a Claus reaction to generate elemental sulfur, and meanwhile, oxygen in the sulfur is burnt; part of hydrogen sulfide in the acid gas and air are combusted at high temperature to generate sulfur dioxide and elemental sulfur, and the rest hydrogen sulfide and the generated sulfur dioxide are subjected to a Claus reaction to generate the elemental sulfur. High-temperature process gas containing hydrogen sulfide, sulfur dioxide and sulfur steam generated by the sulfur production furnace is heated by a waste heat boiler 7 and then enters a primary sulfur condenser to recover elemental sulfur, and process gas at the outlet of the condenser sequentially passes through a primary sulfur production reactor and a secondary sulfur production reactor through the process gas to generate Claus and hydrolysis reactions under the action of a catalyst. The Claus tail gas generated by the sulfur production unit enters a tail gas hydrogenation unit for treatment, and finally SO in the flue gas of the sulfur device2The discharge concentration was 635mg/m3And the requirements of the latest national environmental protection regulation GB31570-2015 discharge Standard of pollutants for oil refining industry cannot be met. More importantly, the furnace temperature is reduced due to the introduction of the S Zorb regeneration flue gas 2 when the furnace temperature of the sulfur making furnace is up to over 1000 ℃,so that the energy consumption of the device is greatly increased, and when the load of the sulfur recovery device is lower than 70 percent, the S Zorb regeneration flue gas 2 must be cut off. In addition, the higher oxygen content in the S Zorb regeneration flue gas 2 easily causes sulfation of the catalyst in the first-order converter, which reduces the catalytic activity, and more seriously may cause catalyst deactivation, which seriously affects the normal operation of the sulfur recovery device.
Claims (1)
1. A method for treating sulfur-containing waste gas is characterized in that: one or two of the sulfur recovery device flue gas (1) or the S Zorb regeneration flue gas (2) and the regeneration air (3) of the catalytic cracking device are introduced into a regeneration unit of the catalytic cracking device for a coking reaction, and unreacted SO-containing gas2The gas and the flue gas generated by the coking reaction are sequentially subjected to separation and heat exchange and then enter a desulfurization and denitrification unit in a catalytic cracking device for treatment, and the purified tail gas (10) is obtained and then discharged;
the temperature of the flue gas (1) of the sulfur recovery device is 280-350 ℃, and SO in the flue gas (1) of the sulfur recovery device2The volume content is 100-800mg/m3The volume content of oxygen is 2-5%;
the temperature of the S Zorb regeneration flue gas (2) is 110-22-5% of volume content, 0.2-5% of oxygen volume content and the balance of nitrogen;
introducing the sulfur recovery unit flue gas (1) or S Zorb regeneration flue gas (2) into a regeneration unit in a catalytic cracking unit through a pipeline;
introducing the regenerated air (3) of the catalytic cracking unit into a regeneration unit in the catalytic cracking unit through a fan;
the regeneration unit in the catalytic cracking device comprises a coke burning tank (4) and a regenerator (5);
the temperature of the scorching reaction is 650-720 ℃;
controlling the volume content of oxygen in the flue gas generated by the scorching reaction to be 2-9%;
SO in cleaned tail gas (10)2The content is less than 50mg/m3。
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| CN1253848A (en) * | 1998-11-13 | 2000-05-24 | 中国石油化工集团公司 | Method for treating industrial waste gas containing sulphur oxide |
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| CN1253848A (en) * | 1998-11-13 | 2000-05-24 | 中国石油化工集团公司 | Method for treating industrial waste gas containing sulphur oxide |
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| Title |
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| 影响硫磺回收装置ＳＯ２排放浓度的因素分析;李鹏等;《石油炼制与化工》;20130430;第75-79页 * |
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