CN111947167A - Combined treatment system and process method for nitrogen-containing waste gas and waste liquid of ethylene glycol device - Google Patents
Combined treatment system and process method for nitrogen-containing waste gas and waste liquid of ethylene glycol device Download PDFInfo
- Publication number
- CN111947167A CN111947167A CN201910407012.9A CN201910407012A CN111947167A CN 111947167 A CN111947167 A CN 111947167A CN 201910407012 A CN201910407012 A CN 201910407012A CN 111947167 A CN111947167 A CN 111947167A
- Authority
- CN
- China
- Prior art keywords
- gas
- ammonia
- waste
- liquid
- ethylene glycol
- 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.)
- Withdrawn
Links
Images
Classifications
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
- B01D47/06—Spray cleaning
-
- 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
- B01D53/14—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 absorption
- B01D53/1456—Removing acid components
-
- 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
- B01D53/14—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 absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- 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
-
- 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
- B01D53/8659—Removing halogens or halogen compounds
- B01D53/8662—Organic halogen compounds
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
- F22D1/00—Feed-water heaters, i.e. economisers or like preheaters
-
- 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
-
- 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
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Abstract
The invention discloses a combined treatment system and a combined treatment process method for nitrogen-containing waste gas and waste liquid of an ethylene glycol device. The combined processing system comprises: a combustion device, a mixing device, an SCR combined reactor and a washing device. The combined treatment process method comprises the following steps: (1) burning waste gas and waste liquid generated in the coal-to-ethylene glycol in a combustion device; (2) mixing ammonia gas and air preheated by an air preheater in a mixing tank to obtain diluted ammonia gas; (3) spraying the diluted ammonia gas obtained in the step (2) into the flue gas incinerated in the step (1) through an ammonia spraying grid, and then introducing the flue gas into an SCR combined reactor; (4) and the gas reacted by the SCR combined reactor enters a washing device for washing and then is discharged. The invention can realize the clean treatment of waste gas and waste liquid and ensure that tail gas meets the environmental standard and reaches the standard, and simultaneously can generate a byproduct steam product, thereby solving the problem that the waste gas and waste liquid generated in the existing glycol production process pollutes the environment.
Description
Technical Field
The invention relates to a combined treatment system and a combined treatment process for nitrogen-containing waste gas and waste liquid of an ethylene glycol device.
Background
Ethylene glycol is an important organic chemical raw material, is mainly used for producing polyester series products and automobile antifreeze, can also be used as a surfactant, a deicer and a chemical intermediate product, and has wide application in the chemical industry due to the active chemical property of the ethylene glycol with dihydroxyl. At present, the consumption of glycol in the polyester industry in China is about 93%, and the consumption of glycol used for producing antifreeze, surfactant, adhesive, cold-resistant lubricating oil, paint solvent and the like is about 7%.
The process for preparing the ethylene glycol from the coal takes the coal as a raw material and can be divided into three types according to different process flows: direct processes, oxalate processes and olefin processes. However, in any process technology, the coal must be gasified, transformed and purified to produce synthesis gas, and finally ethylene glycol is produced. The three process routes of the coal-to-ethylene glycol produce waste gas and waste liquid in the production process, and the produced waste gas mainly contains Methyl Nitrite (MN) and NO as Nitrogen Oxide (NO)X)、CO、H2S、NH3And the like, wherein NOx is one of main pollution sources causing air pollution and can cause damages such as photochemical smog, acid rain, ozone layer cavities and the like; the generated waste liquid contains Methyl Nitrite (MN) and alcohol ester substances, and the waste cannot be directly discharged and also pollutes the environment after being discharged.
Currently, a joint treatment technology for waste gas and liquid in a coal-to-ethylene glycol process is rarely reported, and with the improvement of environmental requirements, environmental protection departments and production enterprises pay more and more attention to the treatment of the waste gas and liquid in the process.
Disclosure of Invention
The invention aims to overcome the defect that a scheme for jointly treating the nitrogen-containing waste gas and waste liquid of the ethylene glycol device is lacked in the prior art, and provides a system and a process method for jointly treating the nitrogen-containing waste gas and waste liquid of the ethylene glycol device.
The invention solves the technical problems through the following technical scheme:
the invention provides a combined treatment system for nitrogen-containing waste gas and waste liquid of an ethylene glycol device, which comprises: a combustion device, a mixing device, an SCR combined reactor and a washing device;
the combustion device is used for incinerating waste gas and waste liquid generated in the coal-to-ethylene glycol production process;
the mixing device comprises a mixing tank and an ammonia injection grid, the mixing tank is used for mixing ammonia gas and air preheated by an air preheater to obtain diluted ammonia gas, and the ammonia injection grid is used for mixing the diluted ammonia gas and outlet gas of the combustion device and introducing the mixed gas into the SCR combined reactor;
the SCR combined reactor is used for catalytically cracking dioxin in intake air into CO2、H2O and HCl, and simultaneously catalytically reducing nitrogen oxides in the inlet gas to N2And H2O；
And a gas outlet of the SCR combined reactor is connected with the washing device and is discharged after passing through the washing device.
The combined treatment system of the present invention is further described below:
the waste gas and waste liquid generated in the process of preparing the ethylene glycol from the coal have complex components, a certain amount of oxynitride, a small amount of HCl and trace dioxin are generated after the waste gas and the waste liquid are treated by the combustion device, and the oxynitride is selectively catalytically reduced into N after passing through the SCR combined reactor2And H2O, dioxins are then cracked into CO2、H2O and HCl, dust of the flue gas is removed after passing through the washing device, and the HCl is absorbed by washing liquid in the washing device to finally obtain clean tail gas.
In the invention, preferably, the combustion device is further provided with an air inlet, and air is sent into the combustion device for incineration through a blower. The air plays a role in supporting combustion on one hand and controlling the combustion temperature on the other hand in the combustion device, thereby controlling the reaction process in the combustion device. For example, when the temperature in the combustion device is too high, increasing the air flow may reduce the temperature in the combustion device because the air is not preheated.
In the invention, the waste liquid enters the combustion device after being atomized by an atomization device. The atomizing means may be conventional in the art, such as an atomizing nozzle.
In the present invention, preferably, the combustion device is an incinerator, and the waste gas generated in the ethylene glycol production and the waste liquid atomized by the atomization device are incinerated in the incinerator while the air conditioning reaction process is introduced. Preferably, the incinerator adopts atomization incineration and multiple mixing technology, and structurally, the inside of the incinerator body adopts secondary mixing design, so that harmful substances can be completely incinerated and cracked in the hearth.
In the present invention, preferably, the combustion device is further connected to a waste heat recovery device for recovering heat of the high temperature flue gas generated in the combustion device. The waste heat recoverer is connected with the combustion device through a direct connection structure, namely, high-temperature flue gas generated in the combustion device directly enters an inlet of the waste heat recoverer.
Preferably, the heat exchange medium outlet of the waste heat recoverer is further connected with a steam drum to form a waste heat collecting loop. The steam drum is preferably an intermediate pressure steam drum.
In the present invention, preferably, the SCR combined reactor is further connected to a process gas cooler for recovering heat of flue gas in the SCR combined reactor. The process gas cooler and the SCR combined reactor are connected by adopting a direct connection structure, namely, flue gas generated in the SCR combined reactor directly enters the process gas cooler.
Preferably, the process gas cooler is connected with the steam drum, and boiler feed water enters the steam drum after being preheated by the process gas cooler. And the waste heat recoverer and the steam drum realize heat recovery through natural circulation of boiler water supply.
In the invention, preferably, a gas-ammonia pre-mixer is further arranged between the mixing tank and the ammonia injection grid and is used for further uniformly mixing the gas mixed by the mixing tank.
In the invention, preferably, a gas ammonia post-mixer is further arranged between the ammonia injection grid and the SCR combined reactor; the gas ammonia post-mixer at the downstream of the ammonia injection grid further promotes the mixing of the flue gas and the ammonia, and ensures the uniform distribution of the ammonia concentration in the flue gas, thereby being beneficial to the complete reduction of oxynitride and the reduction of the escape amount of the ammonia.
In the invention, preferably, an ammonia batching precise control system is arranged at the upstream of the mixing tank, flue gas detection devices are respectively arranged on outlet pipelines of the waste heat recoverer and the process gas cooler, and the injection amount of the ammonia gas in the ammonia injection grid is precisely controlled by detecting the content of oxynitride in the flue gas in the pipelines, so that the ammonia escape amount is reduced.
In the present invention, preferably, the washing apparatus includes a quencher and a quench tower connected in sequence, and the outlet gas of the SCR combined reactor passes through the quencher from top to bottom and enters the quench tower from the lower portion. The upper portions of the quencher and the quench tower are respectively provided with a washing liquid inlet, the outlet gas of the SCR combined reactor firstly enters the quencher, a strand of circulating washing liquid is sprayed into the quencher through the washing liquid inlet arranged at the upper portion of the quencher, the sprayed washing liquid is atomized into small liquid drops, quenching and humidifying of flue gas are facilitated, and meanwhile dust in the flue gas is combined with the liquid drops to achieve the purpose of dust removal. Flue gas and washing liquid enter the lower part of quench tower through the quench cooler bottom, spout into washing liquid simultaneously at quench tower upper portion, flue gas and the washing liquid that sprays from quench tower upper portion contact against current in the quench tower, and HCl in the flue gas is fully absorbed by the washing liquid, and clean flue gas is sent into the aiutage from the quench tower top and is discharged into the atmosphere.
Preferably, the quenching tower is also provided with a washing liquid circulating pump, washing liquid sprayed from the upper parts of the quencher and the quenching tower directly enters the bottom of the quenching tower, and a small amount of washing liquid is sent out of the battery limit to a downstream sewage treatment device after the washing liquid is pressurized by the washing liquid circulating pump; other washing liquid is divided into two streams after heat exchange and cooling, one stream is sent back to the quencher to cool the flue gas, and the other stream is sent to the top of the quenching tower to be sprayed as the washing liquid.
Preferably, the upper part of the quenching tower is provided with a demister, and a small amount of washing liquid carried by the flue gas is captured by the demister at the upper part of the quenching tower. The mist and mist eliminator can be of the type conventional in the art, including but not limited to plate mist eliminators, wire mesh demister, vane mist eliminator, electric demister, and the like. Preferably, the upper part of the demister is also provided with a spray opening through which desalted water is regularly sprayed, so that the liquid level of the quench tower is supplemented on one hand, and the demister is washed on the other hand.
The invention also provides a combined treatment process method of the nitrogen-containing waste gas and waste liquid of the glycol device, which is carried out by adopting the combined treatment system of the nitrogen-containing waste gas and waste liquid of the glycol device, and comprises the following steps:
(1) burning waste gas and waste liquid generated in the coal-to-ethylene glycol in a combustion device;
(2) mixing ammonia gas and air preheated by an air preheater in a mixing tank to obtain diluted ammonia gas;
(3) spraying the diluted ammonia gas obtained in the step (2) into the flue gas incinerated in the step (1) through an ammonia spraying grid, and then introducing the flue gas into an SCR combined reactor;
(4) the gas reacted by the SCR combined reactor enters a washing device for washing and then is discharged;
wherein, the sequence of the steps (1) and (2) is not limited.
The combined treatment process of the present invention is further described below:
in the invention, when the combustion device is provided with an air inlet, air is sent into the combustion device through the air blower for incineration, and the temperature of the air is normal temperature (-10-30 ℃).
In the invention, the waste liquid generated in the coal-to-ethylene glycol is atomized in the forms of steam atomization, air atomization or mechanical atomization and the like, sprayed into an atomization device for atomization, and then mixed with the waste gas for incineration.
In the present invention, the combustion temperature in the combustion apparatus is preferably 1000 to 1300 ℃.
The waste gas and the waste liquid component generated in the process of preparing the ethylene glycol from the coal are complex, the reaction can be carried out without additionally introducing fuel gas when the ethylene glycol is burnt in a combustion device, and the specific reaction comprises the following reaction formula:
the main reactions of the exhaust gases in the combustion device are as follows:
4CH3ONO+5O2→4CO2+4NO+6H2heat of reaction (A)
In addition, the waste gas also contains a certain content of CO and hydrocarbon substances, and a small amount of CH3OH, trace of chlorinated organic CH3Cl, the following reactions will occur simultaneously:
2CO+O2→2CO2+ Heat of reaction (B)
CnHm+(n+m/4)O2→m/2H2O+nCO2+ Heat of reaction (C)
m and n are independently integers of 1-15
2CH3OH+3O2→2CO2+4H2Heat of reaction (D)
2CH3Cl+3O2→2CO2+2H2O +2HCl + heat of reaction (E)
The main reactions of the waste liquid in the incinerator are as follows:
4CxHyOz+(4x+y-2z)O2→4xCO2+2yH2heat of reaction (F)
x and y are independently integers of 1 to 15, and z is an integer of 0 to 10
In the invention, when the combustion device is also connected with a waste heat recoverer, the heat of the high-temperature flue gas generated in the combustion device is recovered by the waste heat recoverer and is cooled to 320-420 ℃.
In the present invention, preferably, in the step (2), the temperature of the air preheated by the air preheater is 100 to 180 ℃.
In step (2) of the present invention, the source of the ammonia gas includes, but is not limited to, liquid ammonia gasification, ammonia evaporation, urea cracking, etc.
In the present invention, preferably, the NH in the ammonia gas is diluted3The content of (b) is 1 to 5 mol%.
In the present invention, the reaction temperature in the SCR combined reactor is preferably 320 to 420 ℃.
In the present invention, preferably, the SCR combined reactor is filled with a DRC denitration catalyst, preferably a corrugated plate-type DRC denitration catalyst (for example, a corrugated plate-type catalyst DRC35), which has a function of simultaneously decomposing dioxin and catalytically converting an oxynitride, and the dioxin is cracked into CO2、H2O and HCl, nitrogen oxides with NH3Catalytic reduction to N2And H2O。
Since the exhaust gas contains chlorine, a trace amount of dioxin is inevitably generated during combustion. Dioxins are a generic name for a class of polychlorinated oxygen-containing tricyclic aromatic compounds, commonly referred to as polychlorinated dibenzo-p-dioxins (PCDDS) and polychlorinated dibenzo-p-furans (PCDFS). The flue gas containing reducing agent ammonia after being mixed evenly passes through an SCR combined reactor, a multi-bed catalyst is filled in the SCR combined reactor, the catalyst has the functions of simultaneously decomposing dioxin and catalytically converting oxynitride, and the specific reaction comprises the following reaction formulas:
catalytic cracking of dioxin:
PCDDS：
C12HaCl8-aO2+(9+0.5a)O2→(a-4)H2O+12CO2+ (8-a) HCl + Heat of reaction (H)
a is an integer of 0 to 7
PCDFS：
C12HbCl8-bO+(9.5+0.5b)O2→(b-4)H2O+12CO2+ (8-b) HCl + Heat of reaction (I)
b is an integer of 0 to 7
Cracking and converting trace amount of dioxin in flue gas into CO under the action of catalyst2、H2O and HCl, are removed.
Catalytic conversion of nitrogen oxide:
4NO+4NH3+O2→4N2+6H2heat of reaction (J)
6NO+4NH3→5N2+6H2Heat of reaction (K)
The reaction (J) occurs preferentially when there is oxygen in the flue gas, and therefore ammonia consumption is an equivalent relationship to NO.
In addition, there is usually a small amount of NO in the flue gas2，NO2The reactions involved are as follows:
2NO2+4NH3+O2→3N2+6H2heat of reaction (L)
6NO2+8NH3→7N2+12H2Heat of reaction (M)
In the invention, when the SCR combined reactor is connected with the process gas cooler, the heat of the gas reacted by the SCR combined reactor is recovered by the process gas cooler, and the temperature is reduced to 160-220 ℃.
When the process gas cooler is connected with a steam drum, boiler feed water is preheated to 140-180 ℃ by the process gas cooler and then is sent into the steam drum, heat is recovered by a waste heat recoverer to generate medium-pressure steam, and finally the medium-pressure steam is sent out of a boundary area and is merged into a steam pipe network with corresponding pressure of the whole plant.
The positive progress effects of the invention are as follows: the combined treatment system and the process method for the nitrogen-containing waste gas and waste liquid of the coal-to-ethylene glycol provided by the invention have the advantages that the waste gas and waste liquid are subjected to clean treatment, the tail gas is ensured to meet the environmental standard and be discharged after reaching the standard, a steam product is byproduct, the problem that the waste gas and waste liquid generated in the existing coal-to-ethylene glycol production process pollute the environment is solved, and a certain economic value is generated.
Drawings
FIG. 1 is a process flow diagram of a combined treatment system for nitrogen-containing waste gas and waste liquid of an ethylene glycol plant in embodiment 1 of the invention.
Description of reference numerals:
1-a combustion device, 2-a waste heat recoverer, 3-a steam drum, 4-an ammonia injection grid, 5-a gas ammonia pre-mixer, 6-a gas ammonia post-mixer, 7-an SCR combined reactor, 8-a process gas cooler, 9-a quencher, 10-a quench tower, 11-a washing liquid circulating pump, 12-a blower, 13-an air preheater, 14-an ammonia burdening precision control system and 15-a mixing tank.
Detailed Description
The invention is further illustrated by the following examples, which are not intended to limit the scope of the invention.
Example 1
The combined treatment system for nitrogen-containing waste gas and waste liquid of an ethylene glycol plant provided by the embodiment is shown in fig. 1, and comprises: the device comprises a combustion device 1, a mixing device, an SCR combined reactor 7 and a washing device;
the combustion device 1 is used for burning waste gas and waste liquid generated in the production of ethylene glycol,
the mixing device comprises a mixing tank 15 and an ammonia injection grid 4, wherein the mixing tank 15 is used for mixing ammonia gas and air preheated by an air preheater 13 to obtain diluted ammonia gas, and the ammonia injection grid 4 is used for mixing the diluted ammonia gas and outlet gas of the combustion device 1 and introducing the mixed gas into the SCR combined reactor 7;
the SCR combined reactor 7 is used for catalytically cracking dioxin in the intake air into CO2、H2O and HCl, and simultaneously catalytically reducing nitrogen oxides in the inlet gas to N2And H2O；
And a gas outlet of the SCR combined reactor 7 is connected with a washing device and is discharged after passing through the washing device.
Wherein, the waste liquid is atomized by the atomizing nozzle in a steam atomizing mode and then enters the combustion device 1.
The combustion device 1 is also provided with an air inlet for feeding air into the combustion device 1 by means of a blower 12 for incineration.
In this embodiment, this burner 1 specifically is to burn burning furnace, and this burns burning furnace adopts atomizing incineration and many times mixing process, and structural furnace body is inside to adopt the secondary to mix the design for harmful substance can burn the schizolysis completely in furnace.
In this embodiment, a waste heat recovery device 2 is further connected to the downstream of the combustion device 1, and the waste heat recovery device 2 is connected to the combustion device 1 by a direct connection structure, that is, high-temperature flue gas generated in the combustion device 1 directly enters an inlet of the waste heat recovery device 2.
The outlet of the heat exchange medium of the waste heat recoverer 2 is also connected with the steam drum 3 to form a waste heat collecting loop, and the steam drum 3 is a medium-pressure steam drum.
A process gas cooler 8 is connected with the downstream of the SCR combined reactor 7, and the flue gas generated in the SCR combined reactor 7 directly enters the process gas cooler 8.
The process gas cooler 8 is connected with the steam drum 3, the medium-pressure boiler feed water is preheated to 140-180 ℃ by the process gas cooler 8, then enters the steam drum 3, is recovered by the waste heat recoverer 2 to generate medium-pressure steam, and finally is sent out of a boundary area and merged into a steam pipe network with corresponding pressure of the whole plant. And the waste heat recoverer 2 and the steam drum 3 realize heat recovery through natural circulation of boiler feed water.
In this embodiment, a gas ammonia pre-mixer 5 is further disposed between the mixing tank 15 and the ammonia injection grid 4, and a gas ammonia post-mixer 6 is further disposed between the ammonia injection grid 4 and the SCR combined reactor 7.
In this embodiment, an ammonia dosing precision control system 14 is disposed upstream of the mixing tank 15, flue gas detection devices are disposed on outlet pipes of the waste heat recoverer 2 and the process gas cooler 8, and the amount of ammonia gas injected into the ammonia injection grid 4 is precisely controlled by detecting the content of oxynitride in flue gas in the pipes, so as to reduce the amount of ammonia escaping.
In this embodiment, the scrubbing apparatus includes a quencher 9 and a quench tower 10 connected in sequence, and the outlet gas of the SCR combined reactor 7 is cooled by a process gas cooler 8, then passes through the quencher 9 from top to bottom, and then enters the quench tower 10 from the lower portion.
The upper parts of the quencher 9 and the quench tower 10 are provided with washing liquid inlets, respectively.
The quenching tower 10 is also provided with a washing liquid circulating pump 11, washing liquid sprayed from the upper parts of the quenching device 9 and the quenching tower 10 directly enters the bottom of the quenching tower 10, and a small amount of washing liquid is sent out of a battery limit to a downstream sewage treatment device after the washing liquid is pressurized by the washing liquid circulating pump 11; other washing liquid is divided into two parts after heat exchange and cooling, one part is sent back to the quencher 9 to cool the flue gas, and the other part is sent to the top of the quenching tower 10 to be sprayed as the washing liquid.
The upper portion of quench tower 10 is provided with a defogging demister, and a small amount of washing liquid that is smugglied secretly by the flue gas is caught down through the defogging demister on quench tower 10 upper portion. The demister of the embodiment is specifically a wire mesh demister.
The upper part of the demister is also provided with a spraying port through which desalted water is regularly sprayed.
Exhaust gas composition (mol%): 1.1% of CO; CO 22 17.3％；N2O 2.5％；N2 33.2％；NO 1.6％；H24.4 percent of O; MN (methyl nitrite) 31.2%; MF (methyl formate) 124.5 ppm; ML (methylal) 4.4%; ME (methanol) 227.9 ppm; DMC (dimethyl carbonate) 92.6 ppm; DME (dimethyl ether) 2.9%; h2 581.5ppm；CH4 772.5ppm；CH3Cl 1.2％。
The composition of waste liquid (wt%): 3.50% of MN; MF 81.60%; ML 9.59%; ME 5.29%.
Correspondingly, the combined treatment process method in the embodiment comprises the following steps:
(1) burning waste gas and waste liquid generated in the production of ethylene glycol in a combustion device;
waste gas (465 Nm) generated by device for preparing ethylene glycol and dimethyl carbonate by synthesis gas331 ℃, 0.24MPaG) and waste liquid (431.9kg/h, 40 ℃, 0.3MPaG) are sent to an incinerator, wherein the waste liquid is added with low-pressure saturated steam, sprayed into an atomizing nozzle for atomization, mixed with waste gas and incinerated. Meanwhile, air at normal temperature (-10-30 ℃) sent by the air blower 12 is also sent into the waste gas incinerator for incineration reaction. The temperature in the incinerator was 1150 ℃. The blower 12 is installed outdoorsThe air is not heated, and the temperature of the air depends on the outdoor temperature and is usually between-10 and 30 ℃. The normal temperature air sent by the blower 12 plays a role of supporting combustion in the incinerator on one hand, and plays a role of controlling the combustion temperature on the other hand, thereby controlling the reaction process in the incinerator.
The burned hot flue gas (the temperature is about 1150 ℃) directly enters a pipe box of the waste heat recoverer 2 after passing through the inner wall of the incinerator, the heat is recovered by the feed water of the medium-pressure boiler preheated by the process gas cooler 8 and then is discharged out of the waste heat recoverer 2, and the flue gas is cooled to 320-420 ℃.
(2) Mixing ammonia gas and air preheated by an air preheater in a mixing tank to obtain diluted ammonia gas;
the external ammonia gas (from liquid ammonia gasification) and the air (preheated to 180 ℃ by the air preheater 13) sent by the blower 12 are primarily mixed in the mixing tank 15, and the mixed gas in the mixing tank 15 enters the gas ammonia pre-mixer 5 to be further uniformly mixed to form low-concentration gas ammonia with the content of 1.0-5.0 mol%; the low-concentration ammonia gas is sprayed into the flue gas through a plurality of nozzles of an ammonia spraying grid 4; the gas ammonia post-mixer 6 at the downstream of the ammonia injection grid 4 further promotes the mixing of the flue gas and the ammonia, and ensures the uniform distribution of the ammonia concentration in the flue gas, thereby ensuring the Nitrogen Oxide (NO)X) Is fully reduced and ammonia slip is reduced.
The air preheater 13 uses the medium-pressure steam generated by the device as a heat source to preheat the air sent from the blower 12 to about 180 ℃.
(3) Spraying the diluted ammonia gas obtained in the step (2) into the flue gas incinerated in the step (1) through an ammonia spraying grid, and then introducing the flue gas into an SCR combined reactor;
the uniformly mixed flue gas (the temperature is about 370 ℃) containing reducing agent ammonia passes through the SCR combined reactor 7, a four-bed corrugated plate type catalyst DRC35 is filled in the SCR combined reactor 7, the catalyst has the functions of simultaneously decomposing dioxin and catalytically converting oxynitride, and the dioxin is cracked into CO2、H2O and HCl, nitrogen oxides with NH3Catalytic reduction to N2And H2O。
In combined SCR reactors 7The temperature was 408 ℃. NH in SCR combined reactor3The escape rate of (D) is controlled to be 3ppm or less.
The reacted flue gas (about 408 ℃) enters a process gas cooler 8 directly connected with the SCR combined reactor 7, and the temperature is reduced to 160-220 ℃.
The feed water of the medium-pressure boiler is preheated to 140-180 ℃ by a process gas cooler 8, then is sent into a steam drum 3, is subjected to medium-pressure steam generation by a waste heat recoverer 2, and finally is sent out of a boundary area and merged into an external steam pipe network.
(4) The gas reacted by the SCR combined reactor enters a washing device for washing and then is discharged;
the flue gas from the process gas cooler 8 first enters a quencher 9. A strand of circulating washing liquid (32 wt% NaOH aqueous solution) is sprayed into the quenching tower 10 through a washing liquid inlet (spray head) arranged at the middle upper part of the quenching device 9, the sprayed washing liquid is atomized into small liquid drops to form a foam layer, the quenching and humidification of the flue gas are facilitated, and meanwhile, dust in the flue gas is combined with the liquid drops to achieve the aim of dust removal.
Then the flue gas and the washing liquid enter the lower part of a quenching tower 10 through the bottom of the quenching device, gas-liquid separation is realized in the quenching tower 10, meanwhile, washing liquid (32 wt% NaOH aqueous solution) is sprayed into the upper part of the quenching tower 10, the flue gas and the circulating washing liquid are in countercurrent contact in the quenching tower 10, HCl and the like in the flue gas are fully absorbed by the washing liquid, and the clean flue gas (with nitrogen oxide content (with NO) is obtained2Meter) < 80mg/Nm3Oxygen content (dry volume percent): 3% of O2) Is sent into an exhaust funnel from the top of the quenching tower 10 and is exhausted into the atmosphere (meeting the requirements of the emission standard of atmospheric pollutants for thermal power plants GB13223-2011 and the comprehensive emission standard of atmospheric pollutants DB 11/501-2007); a small amount of washing liquid carried by the flue gas is captured by a demister at the upper part of the quenching tower 10; in addition, the upper part of the demister is regularly sprayed with desalted water, so that the liquid level of the quenching tower 10 is supplemented, and the demister is washed. After the washing liquid is pressurized by a washing liquid circulating pump 11, most of the washing liquid is cooled by a circulating liquid water cooler and then is sent to the top of a quenching tower 10 and a nozzle of a quenching device 9 to continuously wash the flue gas, and a small part of the washing liquid (less than or equal to 0.1 m) is3H) is conveyed out of the battery limits to a downstream sewage treatment plant.
The method has the advantages of short flow, low energy consumption, simple and convenient operation, low maintenance cost and obvious environmental protection benefit, and by-products of steam products are produced while the waste gas and the waste liquid are cleaned and treated and the tail gas is ensured to meet the standard of environmental protection.
Example 2
In this embodiment, the combined treatment system for nitrogen-containing waste gas and waste liquid of the ethylene glycol plant provided in embodiment 1 is used for treatment.
Exhaust gas composition (mol%): n is a radical of2 76.33％；CO 14.3％；CO2 4.0％；N2O 0.7％；O2 3.2％；NO 449.4ppm；H2O 0.3ppm；MN 38.2ppm；MF 111.7ppm；ML 49.4ppm；ME 0.75％；DMC 260.5ppm；H2 581.5ppm；CH4 0.7％。
The composition of waste liquid (wt%): 88.6 percent of DMC; MF 0.02%; 0.01% of ML; ME 0.09%; DMO (dimethyl oxalate) 11.28%.
Correspondingly, the combined treatment process method in the embodiment comprises the following steps:
(1) burning waste gas and waste liquid generated in the production of ethylene glycol in a combustion device;
waste gas (2854 Nm) generated by device for preparing ethylene glycol and dimethyl carbonate by using synthesis gas3And/h, -7.1 ℃, 0.2MPaG) and waste liquid (644kg/h, 40 ℃, 0.2MPaG) are sent to an incinerator, wherein the waste liquid is added with low-pressure saturated steam, sprayed into an atomizing nozzle for atomization, mixed with the waste gas and incinerated. Meanwhile, air at normal temperature (-10-30 ℃) sent by the air blower 12 is also sent into the waste gas incinerator for incineration reaction. The temperature in the incinerator was 1150 ℃.
The burned hot flue gas (the temperature is about 1150 ℃) directly enters a pipe box of the waste heat recoverer 2 after passing through the inner wall of the incinerator, the heat is recovered by the feed water of the medium-pressure boiler preheated by the process gas cooler 8 and then is discharged out of the waste heat recoverer 2, and the flue gas is cooled to 320-420 ℃.
(2) Mixing ammonia gas and air preheated by an air preheater in a mixing tank to obtain diluted ammonia gas;
the external ammonia gas (from the gasification of liquid ammonia) and the air (preheated to 180 ℃ by the air preheater 13) sent by the blower 12Then) preliminarily mixing the mixture in a mixing tank 15, and feeding the mixed gas in the mixing tank 15 into a gas ammonia pre-mixer 5 for further uniform mixing to obtain low-concentration gas ammonia with the content of 1.0-5.0 mol%; the low-concentration ammonia gas is sprayed into the flue gas through a plurality of nozzles of an ammonia spraying grid 4; the gas ammonia post-mixer 6 at the downstream of the ammonia injection grid 4 further promotes the mixing of the flue gas and the ammonia, and ensures the uniform distribution of the ammonia concentration in the flue gas, thereby ensuring the Nitrogen Oxide (NO)X) Is fully reduced and ammonia slip is reduced.
The air preheater 13 uses the medium-pressure steam generated by the device as a heat source to preheat the air sent from the blower 12 to about 180 ℃.
(3) Spraying the diluted ammonia gas obtained in the step (2) into the flue gas incinerated in the step (1) through an ammonia spraying grid, and then introducing the flue gas into an SCR combined reactor;
the uniformly mixed flue gas (the temperature is about 370 ℃) containing reducing agent ammonia passes through the SCR combined reactor 7, a four-bed corrugated plate type catalyst DRC35 is filled in the SCR combined reactor 7, the catalyst has the function of catalytically converting nitrogen oxides, and the nitrogen oxides are substituted by NH3Catalytic reduction to N2And H2O。
The temperature in the SCR combined reactor 7 was 402 ℃. NH in SCR combined reactor3The escape rate of (D) is controlled to be 3ppm or less.
And the reacted flue gas (about 402 ℃) enters a process gas cooler 8 directly connected with the SCR combined reactor 7, and the temperature is reduced to 160-220 ℃.
The feed water of the medium-pressure boiler is preheated to 140-180 ℃ by a process gas cooler 8, then is sent into a steam drum 3, is subjected to medium-pressure steam generation by a waste heat recoverer 2, and finally is sent out of a boundary area and merged into an external steam pipe network.
(4) The gas reacted by the SCR combined reactor enters a washing device for washing and then is discharged;
the flue gas from the process gas cooler 8 first enters a quencher 9. A strand of circulating washing liquid (desalted water) is sprayed into the quenching tower 10 through a washing liquid inlet (spray head) arranged at the middle upper part of the quenching device 9, the sprayed washing liquid is atomized into small liquid drops to form a foam layer, the quenching and humidification of flue gas are facilitated, and meanwhile dust in the flue gas is combined with the liquid drops to achieve the aim of dust removal.
Then the flue gas and the washing liquid enter the lower part of a quench tower 10 through the bottom of a quench cooler, gas-liquid separation is realized in the quench tower 10, meanwhile, washing liquid (desalted water) is sprayed into the upper part of the quench tower 10, the flue gas and the circulating washing liquid are in countercurrent contact in the quench tower 10, and escaped NH which does not participate in SCR reaction in the flue gas3The content of Nitrogen Oxide (NO) in the clean flue gas is fully absorbed by the cleaning solution2Meter) < 80mg/Nm3Oxygen content (dry volume percent): 3% of O2) Is sent into an exhaust funnel from the top of the quenching tower 10 and is exhausted into the atmosphere (meeting the requirements of the emission standard of atmospheric pollutants for thermal power plants GB13223-2011 and the comprehensive emission standard of atmospheric pollutants DB 11/501-2007); a small amount of washing liquid carried by the flue gas is captured by a demister at the upper part of the quenching tower 10; in addition, the upper part of the demister is regularly sprayed with desalted water, so that the liquid level of the quenching tower 10 is supplemented, and the demister is washed. After the washing liquid is pressurized by a washing liquid circulating pump 11, most of the washing liquid is cooled by a circulating liquid water cooler and then is sent to the top of a quenching tower 10 and a nozzle of a quenching device 9 to continuously wash the flue gas, and a small part of the washing liquid (less than or equal to 0.1 m) is3H) is conveyed out of the battery limits to a downstream sewage treatment plant.
While specific embodiments of the invention have been described above, it will be appreciated by those skilled in the art that this is by way of example only, and that the scope of the invention is defined by the appended claims. Various changes and modifications to these embodiments may be made by those skilled in the art without departing from the spirit and scope of the invention, and these changes and modifications are within the scope of the invention.
Claims (10)
1. The utility model provides a nitrogen waste gas waste liquid combined treatment system of glycol device which characterized in that, nitrogen waste gas waste liquid combined treatment system of glycol device includes: a combustion device, a mixing device, an SCR combined reactor and a washing device;
the combustion device is used for incinerating waste gas and waste liquid generated in the coal-to-ethylene glycol production process;
the mixing device comprises a mixing tank and an ammonia injection grid, the mixing tank is used for mixing ammonia gas and air preheated by an air preheater to obtain diluted ammonia gas, and the ammonia injection grid is used for mixing the diluted ammonia gas and outlet gas of the combustion device and introducing the mixed gas into the SCR combined reactor;
the SCR combined reactor is used for catalytically cracking dioxin in intake air into CO2、H2O and HCl, and simultaneously catalytically reducing nitrogen oxides in the inlet gas to N2And H2O；
And a gas outlet of the SCR combined reactor is connected with the washing device and is discharged after passing through the washing device.
2. The combined treatment system of the nitrogen-containing waste gas and liquid of the ethylene glycol plant as claimed in claim 1, wherein an air inlet is further provided in the combustion device;
and/or the waste liquid enters the combustion device after being atomized by an atomization device;
and/or the combustion device is an incinerator;
and/or a gas ammonia pre-mixer is arranged between the mixing tank and the ammonia injection grid and is used for further uniformly mixing the gas mixed by the mixing tank;
and/or a gas ammonia post-mixer is also arranged between the ammonia injection grid and the SCR combined reactor and is used for further uniformly mixing the flue gas and the ammonia.
3. The combined treatment system of nitrogen-containing waste gas and liquid of an ethylene glycol plant as claimed in claim 1, wherein the combustion device is further connected with a waste heat recoverer for recovering heat of flue gas generated in the combustion device; preferably, the waste heat recoverer is connected with the combustion device by a direct connection structure.
4. The combined treatment system of nitrogen-containing waste gas and liquid of an ethylene glycol unit as claimed in claim 3, wherein the outlet of the heat exchange medium of the waste heat recoverer is further connected with a steam drum to form a waste heat collecting loop;
and/or the SCR combined reactor is also connected with a process gas cooler, an ammonia batching precise control system is arranged at the upstream of the mixing tank, and flue gas detection devices are respectively arranged on the waste heat recoverer and the outlet pipeline of the process gas cooler.
5. The combined treatment system for the nitrogen-containing waste gas and liquid of the ethylene glycol unit according to claim 4, wherein the SCR combined reactor is further connected with a process gas cooler, the process gas cooler is connected with the steam drum, and the process gas cooler is used for recovering heat of flue gas in the SCR combined reactor and simultaneously is used for preheating boiler feed water entering the steam drum.
6. The combined treatment system for the nitrogen-containing waste gas and liquid of the ethylene glycol unit according to claim 1, wherein the SCR combined reactor is further connected with a process gas cooler for recovering heat of flue gas in the SCR combined reactor; preferably, the process gas cooler and the SCR combined reactor are connected by a direct connection structure.
7. The system of claim 1, wherein the scrubbing unit comprises a chiller and a quench tower connected in series.
8. The combined treatment system for nitrogen-containing waste gas and liquid of an ethylene glycol plant according to claim 7, wherein the upper parts of the chiller and the quench tower are respectively provided with a washing liquid inlet;
and/or the quenching tower is also provided with a washing liquid circulating pump;
and/or a demister is arranged at the upper part of the quenching tower; preferably, the upper part of the demister is further provided with a spraying port.
9. A combined treatment process method for nitrogen-containing waste gas and liquid of an ethylene glycol device is characterized by being carried out by adopting the combined treatment system for nitrogen-containing waste gas and liquid of the ethylene glycol device according to any one of claims 1 to 8, and comprising the following steps of:
(1) burning waste gas and waste liquid generated in the coal-to-ethylene glycol in a combustion device;
(2) mixing ammonia gas and air preheated by an air preheater in a mixing tank to obtain diluted ammonia gas;
(3) spraying the diluted ammonia gas obtained in the step (2) into the flue gas incinerated in the step (1) through an ammonia spraying grid, and then introducing the flue gas into an SCR combined reactor;
(4) the gas reacted by the SCR combined reactor enters a washing device for washing and then is discharged;
wherein, the sequence of the steps (1) and (2) is not limited.
10. The combined treatment process method of nitrogen-containing waste gas and liquid in an ethylene glycol plant as claimed in claim 9, wherein when an air inlet is arranged in the combustion device, air is sent into the combustion device by a blower for incineration, and the temperature of the air is normal temperature;
and/or the waste liquid generated in the coal-to-ethylene glycol is atomized in the form of steam atomization, air atomization or mechanical atomization;
and/or the combustion temperature in the combustion device is 1000-1300 ℃;
and/or when the combustion device is connected with a waste heat recoverer, cooling the flue gas generated in the combustion device to 320-420 ℃ by the waste heat recoverer;
and/or in the step (2), the temperature of the air preheated by the air preheater is 100-180 ℃;
and/or the ammonia gas is from one or more of liquid ammonia gasification, ammonia water evaporation and urea cracking;
and/or, the dilution of NH in ammonia gas3The content of (A) is 1-5 mol%;
and/or the reaction temperature in the SCR combined reactor is 320-420 ℃;
and/or, the SCR combined reactor is filled with a DRC denitration catalyst;
and/or when the SCR combined reactor is connected with a process gas cooler, cooling the gas reacted by the SCR combined reactor to 160-220 ℃ by the process gas cooler;
and/or when the combustion device is connected with a waste heat recoverer, a heat exchange medium outlet of the waste heat recoverer is connected with a steam drum, the SCR combined reactor is connected with a process gas cooler, and when the process gas cooler is connected with the steam drum, boiler feed water is preheated to 140-180 ℃ by the process gas cooler and then is sent into the steam drum.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910407012.9A CN111947167A (en) | 2019-05-16 | 2019-05-16 | Combined treatment system and process method for nitrogen-containing waste gas and waste liquid of ethylene glycol device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910407012.9A CN111947167A (en) | 2019-05-16 | 2019-05-16 | Combined treatment system and process method for nitrogen-containing waste gas and waste liquid of ethylene glycol device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111947167A true CN111947167A (en) | 2020-11-17 |
Family
ID=73335821
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910407012.9A Withdrawn CN111947167A (en) | 2019-05-16 | 2019-05-16 | Combined treatment system and process method for nitrogen-containing waste gas and waste liquid of ethylene glycol device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111947167A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114957008A (en) * | 2021-02-18 | 2022-08-30 | 上海浦景化工技术股份有限公司 | Separation and purification method of byproducts in coal-to-ethylene glycol process |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101634453A (en) * | 2009-08-31 | 2010-01-27 | 北京航天动力研究所 | Quenching process and quenching device of incineration smoke of waste liquid and waste gas containing chlorine |
| WO2011052823A1 (en) * | 2009-10-29 | 2011-05-05 | 광성(주) | Scr system |
| DE102010020277A1 (en) * | 2010-05-11 | 2011-11-17 | Johnson Matthey Catalysts (Germany) Gmbh | Method for reducing nitrogen oxide in flue gas of waste incineration system utilized to produce electricity, involves removing nitrogen using catalytic converter device after selective catalytic reduction process in low temperature region |
| CN107954565A (en) * | 2016-10-17 | 2018-04-24 | 宁波华清环保技术有限公司 | A kind of chemical-industrial emissions total system |
| CN207811301U (en) * | 2017-11-15 | 2018-09-04 | 江苏金牛环保工程设备有限公司 | A kind of high-salt wastewater burning desalting system |
| CN109297037A (en) * | 2018-10-30 | 2019-02-01 | 大连科林能源工程技术开发有限公司 | A kind of environment-friendly type resource utilization system of organic exhaust gas containing chlorine |
| CN109458622A (en) * | 2018-11-14 | 2019-03-12 | 大连科林能源工程技术开发有限公司 | A kind of acrylonitrile salty organic waste liquid and burned waste gas environmental protection and energy saving exhaust system |
-
2019
- 2019-05-16 CN CN201910407012.9A patent/CN111947167A/en not_active Withdrawn
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101634453A (en) * | 2009-08-31 | 2010-01-27 | 北京航天动力研究所 | Quenching process and quenching device of incineration smoke of waste liquid and waste gas containing chlorine |
| WO2011052823A1 (en) * | 2009-10-29 | 2011-05-05 | 광성(주) | Scr system |
| DE102010020277A1 (en) * | 2010-05-11 | 2011-11-17 | Johnson Matthey Catalysts (Germany) Gmbh | Method for reducing nitrogen oxide in flue gas of waste incineration system utilized to produce electricity, involves removing nitrogen using catalytic converter device after selective catalytic reduction process in low temperature region |
| CN107954565A (en) * | 2016-10-17 | 2018-04-24 | 宁波华清环保技术有限公司 | A kind of chemical-industrial emissions total system |
| CN207811301U (en) * | 2017-11-15 | 2018-09-04 | 江苏金牛环保工程设备有限公司 | A kind of high-salt wastewater burning desalting system |
| CN109297037A (en) * | 2018-10-30 | 2019-02-01 | 大连科林能源工程技术开发有限公司 | A kind of environment-friendly type resource utilization system of organic exhaust gas containing chlorine |
| CN109458622A (en) * | 2018-11-14 | 2019-03-12 | 大连科林能源工程技术开发有限公司 | A kind of acrylonitrile salty organic waste liquid and burned waste gas environmental protection and energy saving exhaust system |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114957008A (en) * | 2021-02-18 | 2022-08-30 | 上海浦景化工技术股份有限公司 | Separation and purification method of byproducts in coal-to-ethylene glycol process |
| CN114957008B (en) * | 2021-02-18 | 2024-03-19 | 上海浦景化工技术股份有限公司 | Separation and purification method of byproducts in coal-to-ethylene glycol process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR102098759B1 (en) | Gas denitrification process and equipment | |
| CN203507793U (en) | Device for simultaneously removing sulfur dioxide and nitrogen oxide from coke oven flue gas | |
| CN108636098A (en) | A kind of the minimum discharge purifier and its method of burning city domestic garbage flue gas | |
| CN112460604A (en) | Hazardous waste incineration flue gas treatment system and hazardous waste incineration flue gas treatment method | |
| WO2005028082A1 (en) | A dry flue gas cleaning process and its system for simultaneously desulfurization and denitrating | |
| CN106744722B (en) | A kind of regeneration technology of acetylene cleaning Waste Sulfuric Acid | |
| CN103768903B (en) | A kind of FCC apparatus regenerated flue gas denitrating technique | |
| CN110665352A (en) | Dry desulfurization, denitrification and dust removal device and method for low-sulfur flue gas in cement kiln tail | |
| CN106390741A (en) | H2O2-catalytic-oxidation-based system and method for removing NO, SO2 and Hg0 in flue gas | |
| CN102644922A (en) | Incineration treatment device for nitrogen-containing organic wastes and incineration treatment process | |
| CN210107409U (en) | Hazardous waste burns flue gas clean system | |
| CN108465371A (en) | One kind being based on minimum discharge fume treatment running gear and processing method | |
| CN206986110U (en) | A kind of Denitration in Boiler system using ammonia-contaminated gas as denitrfying agent | |
| CN102309920B (en) | Method for removing NOx and SOx from fluid catalytic cracking (FCC) flue gas | |
| CN110960973A (en) | Industrial flue gas purification process | |
| CN111333290A (en) | Cu-containing industrial sludge hazardous waste recycling treatment system and treatment method thereof | |
| CN113776061A (en) | Hazardous waste incineration flue gas purification and waste heat recovery device and method thereof | |
| CN110425548A (en) | Chemical industry saliferous raffinate incineration system and its burning process | |
| CN106178877A (en) | A kind of coke oven flue waste gas purification waste heat recovery apparatus and technique | |
| CN111947167A (en) | Combined treatment system and process method for nitrogen-containing waste gas and waste liquid of ethylene glycol device | |
| CN211435768U (en) | Flue gas treatment device for semi-dry desulfurization and low-temperature SCR denitration of carbide slag | |
| CN111036039A (en) | Treatment device and treatment method for waste gas in tar treatment process | |
| CN108421383B (en) | Steel pickling waste gas defluorination and denitration device and operation method thereof | |
| CN106853328A (en) | A kind of hydrogen peroxide Efficient utilization method and device for low-temperature flue gas desulphurization denitration | |
| CN106268230A (en) | A kind of waste heat of coke-oven flue gas reclaim and purify system and technique |
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 | ||
| WW01 | Invention patent application withdrawn after publication |
Application publication date: 20201117 |
|
| WW01 | Invention patent application withdrawn after publication |