CN111841310A - Acid making waste heat utilization and tail gas comprehensive treatment process and device - Google Patents
Acid making waste heat utilization and tail gas comprehensive treatment process and device Download PDFInfo
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- CN111841310A CN111841310A CN202010628537.8A CN202010628537A CN111841310A CN 111841310 A CN111841310 A CN 111841310A CN 202010628537 A CN202010628537 A CN 202010628537A CN 111841310 A CN111841310 A CN 111841310A
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- 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
- B01D53/8603—Removing sulfur compounds
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- 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
- B01D53/8631—Processes characterised by a specific device
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
- F23G5/46—Recuperation of heat
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- 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
- F23G7/04—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste liquors, e.g. sulfite liquors
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L15/00—Heating of air supplied for combustion
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- 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
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- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2206/00—Waste heat recuperation
- F23G2206/10—Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2209/00—Specific waste
- F23G2209/10—Liquid waste
- F23G2209/101—Waste liquor
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
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- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
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- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Biomedical Technology (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
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Abstract
The process comprises the steps of heating tail gas and cooling air from a condensation cooler by using heat of a converter in the process of burning sulfuric acid by using low-quality sulfur generated by wet oxidation and desulfurization of coke oven gas and salt waste liquid containing sulfur as raw materials, enabling the tail gas to reach the operation temperature required by a coke oven flue gas desulfurization and denitrification system, sending the tail gas into the coke oven flue gas desulfurization and denitrification system for comprehensive treatment, preheating the cooling air from the condensation cooler into high-temperature air, and sending the high-temperature air to an incinerator as high-temperature combustion-supporting air. After the reaction heat of the tail gas recovery converter is sent to a coke oven flue gas desulfurization and denitrification system for desulfurization and denitrification comprehensive treatment, the original tail gas washing, activated carbon adsorption and regeneration devices are omitted, and the generation of regenerated dilute acid is avoided. The cooling air of the condensing cooler is heated by the converter and is sent to the incinerator for combustion air, so that the heat efficiency of the system is improved, and the energy consumption is reduced.
Description
Technical Field
The invention relates to the technical field of acid preparation, in particular to a process and a device for utilizing waste heat in acid preparation and comprehensively treating tail gas.
Background
Wet oxidation desulfurization with simple process and desulfurization (H)2S) has the characteristic of high efficiency and is widely applied to the desulfurization process of coke oven gas, the desulfurized low-quality sulfur and the byproduct salt waste liquid are used as important matched environment-friendly facilities of the desulfurization process, the tail gas generated in acid preparation by burning is not directly discharged after being washed as the environmental protection becomes stricter day by day, the existing tail gas treatment, upgrading and modification method is generally activated carbon adsorption treatment, firstly, the investment and operation cost is high, and secondly, the activated carbon is regenerated to generate dilute acid waste liquid.
Disclosure of Invention
The invention aims to provide a process and a device for utilizing waste heat from acid making and comprehensively treating tail gas.
In order to achieve the purpose, the invention adopts the following technical scheme:
the process comprises the steps of heating tail gas and cooling air from a condensation cooler by using heat of a converter in the process of burning sulfuric acid by using low-quality sulfur generated by wet oxidation and desulfurization of coke oven gas and salt waste liquid containing sulfur as raw materials, enabling the tail gas to reach the operation temperature required by a coke oven flue gas desulfurization and denitrification system, sending the tail gas into the coke oven flue gas desulfurization and denitrification system for comprehensive treatment, preheating the cooling air from the condensation cooler into high-temperature air, and sending part or all of the cooling air to an incinerator as high-temperature combustion-supporting air.
Returning the tail gas with the temperature of 90-160 ℃ coming out of the condensation cooler to the bottom of the converter, recovering reaction heat through heat exchange of a heat exchanger and process gas, heating the tail gas to 180-280 ℃ to meet the temperature requirement for low-temperature denitration of coke oven flue gas, and sending the tail gas to a coke oven flue gas desulfurization and denitration system to perform desulfurization and denitration together with the coke oven flue gas SO as to remove trace SO in the tail gas2、SO3And NOX。
And cooling air with the temperature of 170-210 ℃ from the condensation cooler enters the converter, reaction heat is recovered through heat exchange of the heat exchanger and the process gas, the cooling air is heated into high-temperature air with the temperature of 300-400 ℃, and one part of the cooling air is used as high-temperature combustion air and sent to the incinerator.
A device for utilizing acid making waste heat and comprehensively treating tail gas comprises an incinerator, a cooling and purifying system, a converter, a condensing cooler and a coke oven desulfurization and denitrification system; the converter comprises a first section of catalyst layer, a first section of heat exchanger, a second section of catalyst layer, a second section of heat exchanger, a third section of catalyst layer and a third section of heat exchanger, wherein the first section of catalyst layer, the first section of heat exchanger, the second section of catalyst layer, the second section of heat exchanger, the third section of catalyst layer and the third section of heat exchanger are sequentially arranged from top to bottom; the device comprises an incinerator process gas outlet, a cooling and purifying system inlet, a converter process gas inlet, a condenser cooler process gas outlet, a converter three-section heat exchanger tail gas inlet, a converter three-section heat exchanger tail gas outlet, a coke oven flue gas desulfurization and denitrification system, a coke oven; cooling air is fed from a shell pass air inlet of the condensing cooler, a shell pass air outlet of the condensing cooler is connected with an air inlet of a second-stage heat exchanger of the converter through a pipeline, and an air outlet of the second-stage heat exchanger of the converter is connected with an air inlet of the first-stage heat exchanger of the converter through a pipeline; the air outlet of the first-stage heat exchanger of the converter is divided into two paths, one path is connected with the air inlet of the incinerator, and the other path is connected with the tail gas outlet of the tube pass of the condensing cooler.
Compared with the prior art, the invention has the beneficial effects that:
1) the reaction heat of the tail gas recovery converter is preheated to the temperature (above 180 ℃) required by low-temperature denitration, and is sent to a coke oven flue gas desulfurization and denitration system to be subjected to desulfurization and denitration comprehensive treatment together with the coke oven flue gas, so that the original tail gas washing, activated carbon adsorption and regeneration devices are omitted, and the generation of regenerated dilute acid is avoided.
2) The cooling air of the condensing cooler is further heated into high-temperature (300-400 ℃) preheated air through the converter and is sent to the incinerator for combustion air, the heat efficiency of the system is improved, and energy consumption is reduced.
Drawings
FIG. 1 is a process flow diagram of the present invention.
In the figure: the system comprises a 1-incinerator, a 2-cooling purification system, a 3-converter, a 3-1 section of catalyst layer, a 3-2 section of heat exchanger, a 3-3 section of catalyst layer, a 3-4 section of heat exchanger, a 3-5 section of catalyst layer, a 3-6 section of heat exchanger, a 4-condensing cooler, a 5-coke oven desulfurization and denitrification system, 6-tail gas, 7-cooling air, 8-compressed air, 9-process gas, 10-high temperature air, 11-sulfur paddle and 12-coke oven flue gas.
Detailed Description
Embodiments of the invention are further described below with reference to the accompanying drawings:
as shown in figure 1, in the process of burning sulfuric acid by using low-quality sulfur generated by wet oxidation and desulfurization of coke oven gas and salt waste liquid containing sulfur element as raw materials, tail gas 6 and cooling air 7 from a condensation cooler 4 are heated by heat of a converter 3, so that the tail gas 6 reaches the operation temperature required by a coke oven flue gas desulfurization and denitrification system 5 and is sent to the coke oven flue gas desulfurization and denitrification system 5 for comprehensive treatment, and after the cooling air 7 from the condensation cooler is preheated to high-temperature air 10, part or all of the cooling air is sent to a burning furnace 1 as high-temperature combustion-supporting air.
Returning the tail gas 6 with the temperature of 90-160 ℃ coming out of the condensation cooler 4 to the bottom of the converter 3, exchanging heat with the process gas 9 through a heat exchanger to recover reaction heat, heating the tail gas 6 to 180-280 ℃ to meet the temperature requirement for low-temperature denitration of coke oven flue gas, and sending the tail gas 6 to a coke oven flue gas desulfurization and denitration system 5 to perform desulfurization and denitration together with the coke oven flue gas 12 to remove trace SO in the tail gas2、SO3And NOX。
Cooling air 7 with the temperature of 170-210 ℃ coming out of the condensation cooler 4 enters the converter 3, reaction heat is recovered through heat exchange of a heat exchanger and process gas 9, the cooling air 7 is heated into high-temperature air 10 with the temperature of 300-400 ℃, and a part of the cooling air is used as high-temperature combustion-supporting air to be sent to the incinerator 1.
The other part (5-20%) of the high-temperature air 10 from the heat exchanger of the converter is sent to the upper part (tail gas side) of the tube pass of the condensing cooler 4 to be mixed with the discharged tail gas 6, so that the superheat degree of the tail gas from the condensing cooler 4 is improved.
The invention adopts ammonia as alkali source, such as: low-quality sulfur produced by coke oven gas wet oxidation desulfurization process with HPF, PDS and the like as catalysts and salt waste liquid containing sulfur element as raw materials, and process method for waste heat utilization and tail gas comprehensive treatment of process for preparing sulfuric acid by burning sulfur pulp waste liquid
A device for utilizing acid making waste heat and comprehensively treating tail gas comprises an incinerator 1, a cooling and purifying system 2, a converter 3, a condensing cooler 4 and a coke oven desulfurization and denitrification system 5; the converter 3 comprises a first section catalyst layer 3-1, a first section heat exchanger 3-2, a second section catalyst layer 3-3, a second section heat exchanger 3-4, a third section catalyst layer 3-5 and a third section heat exchanger 3-6, wherein the first section catalyst layer 3-1, the first section heat exchanger 3-2, the second section catalyst layer 3-3, the second section heat exchanger 3-4, the third section catalyst layer 3-5 and the third section heat exchanger 3-6 are sequentially arranged from top to bottom; the process gas outlet of the incinerator 1 is connected with the inlet of the cooling and purifying system 2 through a pipeline, the process gas outlet of the cooling and purifying system 2 is connected with the process gas inlet of the converter 3 through a pipeline, the process gas outlet of the converter 3 is connected with the tube pass inlet of the condensing cooler 4 through a pipeline, the tube pass tail gas outlet of the condensing cooler 4 is connected with the tail gas inlet of the three-section heat exchanger 3-6 of the converter through a pipeline, and the tail gas outlet of the three-section heat exchanger 3-6 of the converter is connected with the flue gas desulfurization and denitrification system 5 of the coke oven through a pipeline; cooling air 7 is fed from a shell side air inlet of a condensing cooler 4, a shell side air outlet of the condensing cooler 4 is connected with an air inlet of a second-stage heat exchanger 3-4 of the converter through a pipeline, and an air outlet of the second-stage heat exchanger 3-4 of the converter is connected with an air inlet of a first-stage heat exchanger 3-2 of the converter through a pipeline; the air outlet of the first section heat exchanger 3-2 of the converter is divided into two paths, one path is connected with the air inlet of the incinerator 1, and the other path is connected with the pipe pass tail gas outlet of the condensing cooler 4.
The converter 3 is typically a three-bed catalyst SO2Conversion to SO3The reactor of (1).
The condensate cooler 4 is typically a high temperature sulfuric acid corrosion resistant glass tube condensate cooler with process gas 9 on the tube side and cooling air 7 on the shell side.
The first-stage heat exchanger 3-2, the second-stage heat exchanger 3-4 and the third-stage heat exchanger 3-6 in the converter 3 can also be separately arranged from the converter.
The incinerator 1, the cooling purification system 2 and the coke oven desulfurization and denitrification system 5 are the prior art or devices.
The specific process of the embodiment of the invention is as follows:
1) the sulfur slurry 11 is atomized and sprayed into the incinerator 1 through the compressed air 8 to be mixed with the high-temperature combustion air from the converter 3, and is combusted in the incinerator 1 to generate SO with the temperature of 950-1100 DEG C2The process gas 9 is cooled to 380-420 ℃ by a cooling and purifying system 2, purified and dedusted, and then sent into a converter 3, and SO is converted in the converter 3 under the action of a catalyst2Conversion to SO3SO-containing gas from the converter 33The process gas 9 enters the condensing cooler 4 to be condensed and cooled to separate out concentrated sulfuric acid, and tail gas 6 (with the temperature of 90-110 ℃) is discharged from the top of the condensing cooler 4.
2) The tail gas 6 discharged from the top of the condensing cooler 4 is mixed with part (10%) of high-temperature air 10 from the first-stage heat exchanger 3-2 of the converter 3 to increase the temperature (120-140 ℃) of the tail gas 6, and then the tail gas is sent into the three-stage heat exchanger 3-6 of the converter 3 to exchange heat, heated to 230-270 ℃, sent into the coke oven desulfurization and denitrification system 5 to be mixed with the coke oven flue gas 12 to be subjected to desulfurization and denitrification treatment together.
3) Cooling air 7 (the temperature is 170-210 ℃) from the condensing cooler 4 enters a second-stage heat exchanger 3-4 of the converter 3 and a first-stage heat exchanger 3-2 of the converter 3 for heat exchange to be heated to 350-400 ℃, most (90%) of high-temperature air 10 from the first-stage heat exchanger 3-2 of the converter 3 is sent to the incinerator 1 as combustion air, and a small part (10%) of high-temperature air is sent to a tail gas outlet at the top of a tube pass of the condensing cooler 4 to be mixed with tail gas so as to improve the superheat degree of the tail gas.
Although the embodiments of the present invention have been described with reference to the accompanying drawings, the scope of the present invention is not limited thereto, and various modifications and variations which do not require inventive efforts and which are made by those skilled in the art are within the scope of the present invention.
Claims (4)
1. The process is characterized in that in the process of burning sulfuric acid by using low-quality sulfur generated by wet oxidation and desulfurization of coke oven gas and salt waste liquid containing sulfur as raw materials, the tail gas and cooling air from a condensation cooler are heated by heat of a converter, so that the tail gas reaches the operating temperature required by a coke oven flue gas desulfurization and denitrification system and is sent to the coke oven flue gas desulfurization and denitrification system for comprehensive treatment, and after the cooling air from the condensation cooler is preheated to high-temperature air, part or all of the cooling air is sent to a burning furnace as high-temperature combustion-supporting air.
2. The acid making waste heat utilization and tail gas comprehensive treatment process according to claim 1, wherein the tail gas with the temperature of 90-160 ℃ coming out of the condensation cooler is returned to the converter, the reaction heat is recovered through heat exchange of the heat exchanger and the process gas, the tail gas is heated to 180-280 ℃, and is sent to a coke oven flue gas desulfurization and denitrification system to be desulfurized and denitrified together with the coke oven flue gas so as to remove the tail gasTrace amount of SO2、SO3And NOX。
3. The acid making waste heat utilization and tail gas comprehensive treatment process according to claim 1 or 2, characterized in that cooling air with the temperature of 170-210 ℃ from a condensation cooler enters a converter, reaction heat is recovered through heat exchange of a heat exchanger and process gas, the cooling air is heated into high-temperature air with the temperature of 300-400 ℃, and a part of the cooling air is sent to an incinerator as high-temperature combustion air.
4. The device for utilizing the waste heat in acid making and comprehensively treating the tail gas according to claim 1, which is characterized by comprising an incinerator, a cooling and purifying system, a converter, a condensing cooler and a coke oven desulfurization and denitrification system; the converter comprises a first section of catalyst layer, a first section of heat exchanger, a second section of catalyst layer, a second section of heat exchanger, a third section of catalyst layer and a third section of heat exchanger, wherein the first section of catalyst layer, the first section of heat exchanger, the second section of catalyst layer, the second section of heat exchanger, the third section of catalyst layer and the third section of heat exchanger are sequentially arranged from top to bottom; the device comprises an incinerator process gas outlet, a cooling and purifying system inlet, a converter process gas inlet, a condenser cooler process gas outlet, a converter three-section heat exchanger tail gas inlet, a converter three-section heat exchanger tail gas outlet, a coke oven flue gas desulfurization and denitrification system, a coke oven; cooling air is fed from a shell pass air inlet of the condensing cooler, a shell pass air outlet of the condensing cooler is connected with an air inlet of a second-stage heat exchanger of the converter through a pipeline, and an air outlet of the second-stage heat exchanger of the converter is connected with an air inlet of the first-stage heat exchanger of the converter through a pipeline; the air outlet of the first-stage heat exchanger of the converter is divided into two paths, one path is connected with the air inlet of the incinerator, and the other path is connected with the tail gas outlet of the tube pass of the condensing cooler.
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| CN202010628537.8A CN111841310A (en) | 2020-07-02 | 2020-07-02 | Acid making waste heat utilization and tail gas comprehensive treatment process and device |
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| CN202010628537.8A CN111841310A (en) | 2020-07-02 | 2020-07-02 | Acid making waste heat utilization and tail gas comprehensive treatment process and device |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113144848A (en) * | 2021-04-22 | 2021-07-23 | 湖北陆盛环保工程有限公司 | Method for treating tail gas from acid production by low-temperature SCR (selective catalytic reduction) process by using conversion heat of acid production |
| CN113230876A (en) * | 2021-04-23 | 2021-08-10 | 宁波德普绿创环保科技有限公司 | Tail gas purification device of polyester vacuum cracking furnace |
| CN114699911A (en) * | 2022-04-11 | 2022-07-05 | 苏州晶拓半导体科技有限公司 | Ozone destruction device based on heat recovery and ozone destruction method thereof |
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