CN111097284A - Method for heating flue gas entering denitration system by using heat of conversion section - Google Patents
Method for heating flue gas entering denitration system by using heat of conversion section Download PDFInfo
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- CN111097284A CN111097284A CN201811266262.7A CN201811266262A CN111097284A CN 111097284 A CN111097284 A CN 111097284A CN 201811266262 A CN201811266262 A CN 201811266262A CN 111097284 A CN111097284 A CN 111097284A
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- flue gas
- tail gas
- heat exchanger
- denitration
- heat
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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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
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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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- 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
- Y02E20/30—Technologies for a more efficient combustion or heat usage
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Engineering & Computer Science (AREA)
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- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
A method for heating denitration flue gas by utilizing self heat of a conversion system is characterized in that a denitration device is arranged behind a secondary absorption tower, a tail gas heat exchanger is additionally arranged in an original conversion system, the shell side inlet flue gas of the tail gas heat exchanger is tail gas absorbed by the secondary absorption tower, the tube side inlet flue gas of the tail gas heat exchanger is flue gas converted from a tube side outlet of a third heat exchanger, the tube side outlet flue gas enters a primary absorption tower again for absorption, the shell side outlet flue gas after heat exchange has the temperature of 130-150 ℃ and the pressure of 3-7 KPa, and the flue gas condition meets the requirement of introducing a denitration reaction system. After the flue gas enters a denitration system for treatment, NO in the tail gas can be removedXThe content of the active carbon is controlled to be less than or equal to 50mg/m3. The invention can not only ensure that the nitrogen oxide in the tail gas can reach the national emission standard, but also utilize the self heat, thereby greatly reducing the emission of nitrogen oxide from the outside of the systemThe investment of heat sources and equipment is supplemented, and the practicability and the obvious economic benefit are very good. The added flow has simple and clear principle, clear pipeline and strong operability.
Description
Technical Field
The invention belongs to the technical field of chemical environmental protection, and relates to a method for heating flue gas entering a denitration system by using heat of a conversion working section.
Background
In various acid making devices in China, if the processes of regenerating flue gas by cracking alkylated waste acid, making acid by flue gas, making acid by sulfur and the like are involved, a large amount of nitrogen oxides are generated due to high-temperature oxidation combustion reaction of a cracking furnace and an incinerator, so that the treatment work of the nitrogen oxides is emphasized at present, and the denitration treatment is continued on the basis. However, the denitration apparatus is installed, and it is more appropriate to place the denitration apparatus at any stage of the acid production system, and the denitration apparatus is also in a search stage.
At present, some devices are arranged on a flue gas pipeline of a purification section into a dry suction section, which inevitably leads to partial SO2And SO3The loss, i.e., the decrease in the amount of acid produced, may also have a toxic effect on the denitration catalyst, someArranged in the line before the start of the conversion reaction in the conversion section, which may have a major impact on the cost of the temperature-sensitive conversion section and may result in a loss of part of the SO2。
Disclosure of Invention
The invention provides a method for heating flue gas entering a denitration system by using heat of a conversion section aiming at various acid making devices.
In order to ensure the acid production of the acid making device and reduce SO as much as possible3The process of the invention is to arrange the denitration device behind the second absorption tower. A tail gas heat exchanger is added in an original conversion system, the temperature of tail gas at the inlet of a shell pass of the tail gas heat exchanger is about 60 ℃, the pressure of the tail gas is about 6-7 KPa, the temperature of the flue gas at the inlet of a tube pass of the tail gas heat exchanger is about 230-250 ℃, the pressure of the flue gas at the outlet of a tube pass of a conversion third heat exchanger is about 18-19 KPa, the flue gas at the outlet of the tube pass enters a first absorption tower again for absorption, the temperature of the flue gas at the outlet of the shell pass after heat exchange is about 130-150 ℃, the pressure of the flue gas at the outlet of the shell pass is 3-7 KPa, and the condition of. After the flue gas enters a denitration system for treatment, NO in the tail gas can be removedXThe content of the active carbon is controlled to be less than or equal to 50mg/m3To NO of ChinaXThe emission requirements of (2).
The main technical scheme of the invention is as follows: a method for heating flue gas entering a denitration system by using heat of a conversion section is characterized in that a denitration device is arranged on a tail gas pipeline absorbed by a secondary absorption tower; and a tail gas heat exchanger is added in the conversion section of the original acid system.
Furthermore, the flue gas at the shell pass inlet of the tail gas heat exchanger is tail gas absorbed by the secondary absorption tower.
The flue gas at the shell pass inlet of the tail gas heat exchanger is tail gas absorbed by a secondary absorption tower, the temperature is 50-65 ℃, and the flue gas pressure is about 6-7 KPa.
The flue gas at the tube side inlet of the tail gas heat exchanger is the flue gas at the tube side outlet of the third heat exchanger.
The flue gas at the tube side inlet of the tail gas heat exchanger is converted into the flue gas at the tube side outlet of the third heat exchanger, the temperature is about 230-250 ℃, and the pressure is about 18-19 Kpa.
And the flue gas at the tube pass outlet enters an absorption tower again for absorption.
The temperature of the tail gas of the secondary absorption tower after heat exchange is 130-150 ℃, and the pressure is 3-7 KPa, so that the tail gas meets the requirement of entering a denitration device.
After the flue gas enters the denitration system for treatment, NO in tail gasXThe content of the active carbon is controlled to be less than or equal to 50mg/m3。
The method of the invention can not only ensure that the nitrogen oxide in the tail gas can reach the national emission standard, but also utilize the self heat, greatly reduce the investment of supplementing heat sources and equipment from the outside of the system, and has very good practicability and obvious economic benefit. The added flow has simple and clear principle, clear pipeline and strong operability.
Drawings
FIG. 1 is a schematic flow diagram of the process of the present invention.
In the figure, 1, a third conversion heat exchanger, 2, a tail gas heat exchanger, 3, a three-section outlet flue gas pipeline of the converter, 4, a flue gas pipeline for removing the first conversion heat exchanger, 5, a flue gas pipeline for removing the first absorption tower, 6, a flue gas pipeline for removing the second absorption tower, 7, a flue gas pipeline for removing the first absorption tower, 8 and a flue gas pipeline for removing the denitration device.
Detailed Description
The present invention will be described in detail below with reference to examples and the accompanying drawings. The drawings are only for purposes of illustrating the implementations of the invention in connection with the above description and are not intended to limit the scope of the invention.
Examples
The method for heating flue gas entering a denitration system by using heat of a conversion section mainly comprises the following steps with reference to the attached drawing 1: (1) the denitration device is arranged on the tail gas pipeline absorbed by the secondary absorption tower, SO that SO can be completely avoided3The catalyst has toxic action on the catalyst of the denitration device, and can ensure that the acid production is not influenced.
(2) A tail gas heat exchanger is added in the conversion section of the original acid production system.
(3) The flue gas at the shell pass inlet of the tail gas heat exchanger is tail gas absorbed by a secondary absorption tower, the temperature is about 60 ℃, and the flue gas pressure is about 6-7 Kpa.
(4) The flue gas at the tube side inlet of the tail gas heat exchanger is converted into the flue gas at the tube side outlet of the third heat exchanger, the temperature is about 230-250 ℃, and the pressure is about 18-19 Kpa.
(5) And the flue gas at the tube pass outlet enters an absorption tower again for absorption.
(6) The shell pass outlet flue gas after heat exchange is required to be at the temperature of 130-150 ℃ and the pressure of 3-6 KPa, and the flue gas condition can reach the condition of introducing a denitration reaction system.
In the embodiment, after the flue gas enters the denitration system for treatment, NO in the tail gas can be removedXThe content of the active carbon is controlled to be less than or equal to 50mg/m3To NO of ChinaXThe emission requirements of (2).
The method of the invention can not only ensure that the nitrogen oxide in the tail gas can reach the national emission standard, but also utilize the self heat, greatly reduce the investment of supplementing heat sources and equipment from the outside of the system, and has very good practicability and obvious economic benefit. The added flow has simple and clear principle, clear pipeline and strong operability.
Claims (8)
1. A method for heating flue gas entering a denitration system by using heat of a conversion section is characterized in that a denitration device is arranged on a tail gas pipeline absorbed by a second absorption tower; and a tail gas heat exchanger is added in the conversion section of the original acid system.
2. The method according to claim 1, wherein the shell side inlet flue gas of the tail gas heat exchanger is tail gas absorbed by a secondary absorption tower.
3. The method according to claim 2, wherein the flue gas at the shell side inlet of the tail gas heat exchanger is tail gas absorbed by a secondary absorption tower, the temperature is 50-65 ℃, and the flue gas pressure is about 6-7 KPa.
4. The method of claim 1 wherein the tail gas heat exchanger tube side inlet flue gas is a flue gas from the tube side outlet of the reforming third heat exchanger.
5. The method according to claim 4, wherein the flue gas at the inlet of the tube side of the tail gas heat exchanger is flue gas at the outlet of the tube side of the third heat exchanger, and the temperature is about 230-250 ℃ and the pressure is about 18-19 Kpa.
6. The process of claim 5 wherein the tube side outlet flue gas is re-introduced into a suction tower for absorption.
7. The method according to claim 1, wherein the temperature of the tail gas of the second absorption tower after heat exchange is 130-150 ℃, and the pressure is 3-7 KPa, so as to meet the requirement of entering a denitration device.
8. The method according to claim 1 or 7, wherein NO in the tail gas is treated by the denitration systemXThe content of the active carbon is controlled to be less than or equal to 50mg/m3。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811266262.7A CN111097284B (en) | 2018-10-29 | 2018-10-29 | Method for heating flue gas entering denitration system by using heat of conversion section |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811266262.7A CN111097284B (en) | 2018-10-29 | 2018-10-29 | Method for heating flue gas entering denitration system by using heat of conversion section |
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| CN111097284A true CN111097284A (en) | 2020-05-05 |
| CN111097284B CN111097284B (en) | 2022-03-08 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111841310A (en) * | 2020-07-02 | 2020-10-30 | 宁波科新化工工程技术有限公司大连分公司 | Acid making waste heat utilization and tail gas comprehensive treatment process and device |
| 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 |
Citations (10)
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|---|---|---|---|---|
| EP0191725A2 (en) * | 1985-01-16 | 1986-08-20 | Ciba-Geigy Ag | Process for separating sulfur dioxyde from gases and for obtaining concentrated sulfuric acid |
| EP0873777B1 (en) * | 1997-04-21 | 2003-07-23 | Mitsubishi Heavy Industries, Ltd. | Flue gas treating process |
| US20110008230A1 (en) * | 2004-09-30 | 2011-01-13 | Babcock Power Inc. | Systems and methods for high efficiency regenerative selective catalytic reduction |
| CN105688566A (en) * | 2016-03-02 | 2016-06-22 | 钢研晟华工程技术有限公司 | Desulfurization and denitrification device and method for sintering flue gas |
| CN105983331A (en) * | 2015-02-06 | 2016-10-05 | 上海东化环境工程有限公司 | Industrial sulfur-containing tail gas desulphurization technology |
| CN106731826A (en) * | 2016-12-27 | 2017-05-31 | 江苏科瑞工程设计有限公司 | One kind reduces NO in spent acid cracker tail gasXThe method of concentration |
| CN107540038A (en) * | 2017-08-25 | 2018-01-05 | 金川集团股份有限公司 | A kind of device and method that tower exiting flue gas concentrated acidic waste water is inhaled using two |
| CN107774121A (en) * | 2016-08-24 | 2018-03-09 | 江苏新天鸿集团有限公司 | New catalytic method flue gas treating process |
| CN207175469U (en) * | 2017-07-05 | 2018-04-03 | 长沙有色冶金设计研究院有限公司 | A kind of Flue Gas of Nonferrous Smelting relieving haperacidity high-temperature residual heat utilization device |
| CN108167844A (en) * | 2018-01-05 | 2018-06-15 | 江苏科瑞工程设计有限公司 | A kind of method of the air preheat of spent acid cracking technology |
-
2018
- 2018-10-29 CN CN201811266262.7A patent/CN111097284B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0191725A2 (en) * | 1985-01-16 | 1986-08-20 | Ciba-Geigy Ag | Process for separating sulfur dioxyde from gases and for obtaining concentrated sulfuric acid |
| EP0873777B1 (en) * | 1997-04-21 | 2003-07-23 | Mitsubishi Heavy Industries, Ltd. | Flue gas treating process |
| US20110008230A1 (en) * | 2004-09-30 | 2011-01-13 | Babcock Power Inc. | Systems and methods for high efficiency regenerative selective catalytic reduction |
| CN105983331A (en) * | 2015-02-06 | 2016-10-05 | 上海东化环境工程有限公司 | Industrial sulfur-containing tail gas desulphurization technology |
| CN105688566A (en) * | 2016-03-02 | 2016-06-22 | 钢研晟华工程技术有限公司 | Desulfurization and denitrification device and method for sintering flue gas |
| CN107774121A (en) * | 2016-08-24 | 2018-03-09 | 江苏新天鸿集团有限公司 | New catalytic method flue gas treating process |
| CN106731826A (en) * | 2016-12-27 | 2017-05-31 | 江苏科瑞工程设计有限公司 | One kind reduces NO in spent acid cracker tail gasXThe method of concentration |
| CN207175469U (en) * | 2017-07-05 | 2018-04-03 | 长沙有色冶金设计研究院有限公司 | A kind of Flue Gas of Nonferrous Smelting relieving haperacidity high-temperature residual heat utilization device |
| CN107540038A (en) * | 2017-08-25 | 2018-01-05 | 金川集团股份有限公司 | A kind of device and method that tower exiting flue gas concentrated acidic waste water is inhaled using two |
| CN108167844A (en) * | 2018-01-05 | 2018-06-15 | 江苏科瑞工程设计有限公司 | A kind of method of the air preheat of spent acid cracking technology |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111841310A (en) * | 2020-07-02 | 2020-10-30 | 宁波科新化工工程技术有限公司大连分公司 | Acid making waste heat utilization and tail gas comprehensive treatment process and device |
| 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 |
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| Publication number | Publication date |
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| CN111097284B (en) | 2022-03-08 |
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